CA2057231A1 - Method of pretreating lignocellulosic materials prior to alkaline peroxide high yield pulping - Google Patents
Method of pretreating lignocellulosic materials prior to alkaline peroxide high yield pulpingInfo
- Publication number
- CA2057231A1 CA2057231A1 CA 2057231 CA2057231A CA2057231A1 CA 2057231 A1 CA2057231 A1 CA 2057231A1 CA 2057231 CA2057231 CA 2057231 CA 2057231 A CA2057231 A CA 2057231A CA 2057231 A1 CA2057231 A1 CA 2057231A1
- Authority
- CA
- Canada
- Prior art keywords
- chips
- peroxide
- impregnation
- impregnating
- impregnation solution
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
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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
- D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
- D21C9/10—Bleaching ; Apparatus therefor
- D21C9/1026—Other features in bleaching processes
- D21C9/1042—Use of chelating agents
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21B—FIBROUS RAW MATERIALS OR THEIR MECHANICAL TREATMENT
- D21B1/00—Fibrous raw materials or their mechanical treatment
- D21B1/04—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres
- D21B1/12—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres by wet methods, by the use of steam
- D21B1/14—Disintegrating in mills
- D21B1/16—Disintegrating in mills in the presence of chemical agents
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
- D21C9/10—Bleaching ; Apparatus therefor
- D21C9/16—Bleaching ; Apparatus therefor with per compounds
- D21C9/163—Bleaching ; Apparatus therefor with per compounds with peroxides
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- Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- Paper (AREA)
Abstract
ABSTRACT
This invention concerns high yield pulping comprising chemical pretreatments using peroxide in combination with mechanical treatment to produce pulp from chips. More particularly, this invention reduces peroxide decomposition associated with the pretreatment of chips with peroxide prior to refining of the chips by impregnating the chips with a chelant prior to peroxide impregnation. With this invention pulp having desired papermaking properties, particularly a combination of high strength and brightness is obtained with reduced chemical and energy consumption.
This invention concerns high yield pulping comprising chemical pretreatments using peroxide in combination with mechanical treatment to produce pulp from chips. More particularly, this invention reduces peroxide decomposition associated with the pretreatment of chips with peroxide prior to refining of the chips by impregnating the chips with a chelant prior to peroxide impregnation. With this invention pulp having desired papermaking properties, particularly a combination of high strength and brightness is obtained with reduced chemical and energy consumption.
Description
3 :~
METHOD OF PRETREATING LIGNOCELLULOSIC MATERIALS
PRIOR TO ALKALINE PEROXIDE HIGH YIELD PULPING
Pulping processes can be put into either of two broad classifications; high yield pulping and chemical pulping. High yield pulping processes use mechanical destructuring (i.e.
grinding, refining) of the raw material to produce individual fibers or pulp from lignocellulosic materials, usually in chip form, sometimes with mild chemical pretreatment of the chips.
Chemical pulping or low yield processes that primarily use chemical reactions to produce individual fibers from chips. Within the high yield category there are many different combinations of mechanical, chemical, and thermal treatments. Each specific combination of mechanical, chemical and thermal treatments has a different effect on fiber separation, lignin removal, fiber brightness and papermaking strength of paper made from the resulting fibers.
This invention concerns hlgh yield pulping comprising chemical pretreatments using peroxide in combination with mechanical treatment to produce pulp from chips. More particularly, this invention reduces peroxide decomposition associated with the pretreatment of chips with peroxide prior to refining of the chips to produce high yield pulp with peroxide modification of the lignin in the fibers. With this invention pulp having desired papermaking properties, particularly a combination of high strength and brightness is obtained with reduced chemical and energy consumption.
Pulp produced by mechanical refining alone without chemical pretreatment results in extremely high yields (about 95% or higher) but results in fibers containing almost all of the original lignin in essentially a chemically unmodified form and fiber damage/fines generation due to the somewhat indiscriminate mechanical action on the lignocellulosic raw material. Such unmodified lignin imparts relatively low brightness to the fibers, and, due to its hydrophobic nature, the lignin inhibits the development of paper strength through fiber collapse and fiber to fiber bonding (hydrogen bonding). Such fibers are stiffer than partially or 2 ~ 3 1 completely delignified fibers from the same lignocellulosic raw material. Although some high yield pulps containing high amounts of lignin- can be bleached economically to relatively high brightnesses using oxidizing agents such as alkaline peroxide, and/or reducing agents such as sodium hydrosulfite, such post-refining treatments do not increase papermaking strength to levels required for many end uses because much irreversible mechanical damage and fines generation has already been done to the fibers in the refining process. Chemically attacking the lignin before refining prevents much of the mechanical damage and fine generation. Such chemical pretreatment with peroxide prior to refining is improved by the present invention.
The papermaking strength of high yield pulps can be increased by sulfonation of the lignin, particularly when the wood chips are treated with the sulfonation chemicals (usually sodium sulfite with or without sodium hydroxide) prior to mechanical defibration (refining). In some cases, the resulting fibers can also be bleached economically as with alkaline peroxide and/or sodium hydrosulfite to give both improved brightness and papermaking strength. However, the higher levels of sulfonation required for high strength result in pulps which respond less well to bleaching than similar non-sulfonated or low-sulfonated pulps, and therefore such highly sulfonated pulps have high strength but have lower bleached brightnesses and higher bleach chemical demand.
Conversely, low-sulfonation pulps are more bleachable but have lower strength. Moreover, sulfonation processes require the removal and disposal of environmentally objectlonable sulfur compounds from process waste streams. In addition, ~he nee~ for separate sulfonation, refining, and post-refiner bleaching equipment mak~s the capital equipment and operating c03ts for such a system very significant.
An alternative to sulfonation of lignin for increasitlg papermaking strength of hi~h yield fibers is carboxylation and brightening of lignin achieved by th~ combined ~welling and brightening action of alkaline peroxide prior to and/or during 2 ~
defibration. As sulfonation results in lignin containing sulfonate groups, likewise, carboxylation results in lignin with carboxylate groups. ~th the sulfonate and the carboxylate groups are capable of participating in hydrogen bonding which increases the strength of paper made from such high yield pulps (papermaking strength).
Similar to the alkaline high sulfonation treatment of chips prior to refining, alkaline peroxide pretreatment of chips softens the lignocellulosic raw material resulting in easier fiber separation (less energy consumption and less fines generation and fiber fragmentation~ during refining. In addition, refiner brightening with alkaline peroxide can eliminate the need for separate post-refiner bleaching equipment, due to the facts that refiners are excellent mixers of pulp and brightening agents, and the temperature within the refiner (about 100C or higher) causes brightening to occur extremely fast relative to typical post-refiner alkaline peroxide bleaching steps (approximately 50 C to 80 C). The primary drawback to brightening chips within the refiner with alkaline peroxide is peroxide decomposition. Peroxide decomposes to form oxygen (ineffective for lignin-retaining bleaching) and water under the highly alkaline conditions required for papermaking strength development. Peroxide decomposition is hastened by the high temperatures reached in refiners and by metal contaminants, particularly manganese, iron, and copper, which are contained in significant quantities in lignocellulosic raw materials and in lesser quantities in process water. Partial removal or inactivation of such metal contaminants in lignocelluslosic raw material can be effected by introducing chelating agents into the wood chips and then removing the chelant-metal complexes. However, the physical entrapmen~ and chemical attraction of such metals by fiber components within the chips make complete removal of the metals impractical and require additional peroxide protection.
The problems associated with pre-refiner or in-refinex alkaline peroxide treatments are partially avoided by conventional post refiner alkaline peroxide treatments. For exampl~, rather 20~7231 than removing metal contaminan~s from chips, the contaminants have been removed from individual fibers with chelating agents after refining and prior to alkaline peroxide bleaching. Post refininy removal is much more easily achieved because the particle size of the fiber in pulp is much smaller than the size of chips before refining. The smaller size makes the metal contaminants much more accessible to the chelant solution. Consequently, in many cases the individual fibers can be bleached to much higher brightnesses ~ith alkaline peroxide in a post refiner bleaching treatment without significant waste of peroxide bleaching agents due to metal contaminant induced decomposition of peroxide (U.S. Patent No.
4,160,693-Lindahl, et al.). The disadvantage is, that high strength requires high levels of pre-refiner sulfonation and high sulfonation makes post-refiner bleaching difficult.
There have been many attempts to overcome such problems associated with the pre-refiner or in-refiner use of alkaline peroxide in the production of high yield pulps. Control of alkalinity (e.g., see U.S. Patents 3,069,309-Fennell and 4,270,976-Sandstorm, et al., and Canadian Patents 1,078,558 and 1,173,604), control of the temperature (e.g., U.S. Patent 4,187,141-Ahrel), and control of time at high temperature (e.g., U.S. Patent 4,270,976-Sandstorm et al.) have been tried. However, such techniques for reducing peroxide decomposition also reduce the effectiveness of alkaline peroxide in terms of the resulting pulp properties (papermaking strength) while the presence of deleterious metal contaminants still results in inefficient utilization of the peroxide bleaching agent during refinar bleaching.
A common method for circumventing the problem of peroxide decomposition in alkaline peroxide bleaching of chips during refining is to add the bleaching agent directly to the refining zone to minimize the contact time between the chip and alkaline peroxide, and in some cases to allow more intimate contact between metal contaminants and silicate and/or magnesium ion stabilizer flocs (See for example, U.S. Patent Nos. 3,023,140-Textor, 3,069,309-Fennell, 4,022,965 Coheen, et al., 4,270,976-Sandstorm, et al., 4,311,553-Akerlund, et al.; Japanese Patent Application No. 80-72091, and Federal Republic of Germany Patent No. 2818-320). ~dditionally, wood chips have been pretreated by impregnation and/or refining with chelants (U.S. Patents Nos.
3,023,140-Textor, 4,311,553-Akerlund, et al., Japanese Patent Application No. 80-7209, and Federal Republic of Germany Patent No.
2818-320) or with sodium silicate (U.S. Patent Nos. 3,069,309-Fennell, 4,311,553-Akerlund, et al.), or with magnesium salts (U.S.
Patent Nos. 3,023,140-Textor, 3,069,309-Fennell, ~,311,553-Akerlund, et al., and Japanese Patent Application 80-72091) and combinations thereof prior to alkaline peroxide addition into the refiner to reduce peroxide decomposition. U.S. Patent No.
METHOD OF PRETREATING LIGNOCELLULOSIC MATERIALS
PRIOR TO ALKALINE PEROXIDE HIGH YIELD PULPING
Pulping processes can be put into either of two broad classifications; high yield pulping and chemical pulping. High yield pulping processes use mechanical destructuring (i.e.
grinding, refining) of the raw material to produce individual fibers or pulp from lignocellulosic materials, usually in chip form, sometimes with mild chemical pretreatment of the chips.
Chemical pulping or low yield processes that primarily use chemical reactions to produce individual fibers from chips. Within the high yield category there are many different combinations of mechanical, chemical, and thermal treatments. Each specific combination of mechanical, chemical and thermal treatments has a different effect on fiber separation, lignin removal, fiber brightness and papermaking strength of paper made from the resulting fibers.
This invention concerns hlgh yield pulping comprising chemical pretreatments using peroxide in combination with mechanical treatment to produce pulp from chips. More particularly, this invention reduces peroxide decomposition associated with the pretreatment of chips with peroxide prior to refining of the chips to produce high yield pulp with peroxide modification of the lignin in the fibers. With this invention pulp having desired papermaking properties, particularly a combination of high strength and brightness is obtained with reduced chemical and energy consumption.
Pulp produced by mechanical refining alone without chemical pretreatment results in extremely high yields (about 95% or higher) but results in fibers containing almost all of the original lignin in essentially a chemically unmodified form and fiber damage/fines generation due to the somewhat indiscriminate mechanical action on the lignocellulosic raw material. Such unmodified lignin imparts relatively low brightness to the fibers, and, due to its hydrophobic nature, the lignin inhibits the development of paper strength through fiber collapse and fiber to fiber bonding (hydrogen bonding). Such fibers are stiffer than partially or 2 ~ 3 1 completely delignified fibers from the same lignocellulosic raw material. Although some high yield pulps containing high amounts of lignin- can be bleached economically to relatively high brightnesses using oxidizing agents such as alkaline peroxide, and/or reducing agents such as sodium hydrosulfite, such post-refining treatments do not increase papermaking strength to levels required for many end uses because much irreversible mechanical damage and fines generation has already been done to the fibers in the refining process. Chemically attacking the lignin before refining prevents much of the mechanical damage and fine generation. Such chemical pretreatment with peroxide prior to refining is improved by the present invention.
The papermaking strength of high yield pulps can be increased by sulfonation of the lignin, particularly when the wood chips are treated with the sulfonation chemicals (usually sodium sulfite with or without sodium hydroxide) prior to mechanical defibration (refining). In some cases, the resulting fibers can also be bleached economically as with alkaline peroxide and/or sodium hydrosulfite to give both improved brightness and papermaking strength. However, the higher levels of sulfonation required for high strength result in pulps which respond less well to bleaching than similar non-sulfonated or low-sulfonated pulps, and therefore such highly sulfonated pulps have high strength but have lower bleached brightnesses and higher bleach chemical demand.
Conversely, low-sulfonation pulps are more bleachable but have lower strength. Moreover, sulfonation processes require the removal and disposal of environmentally objectlonable sulfur compounds from process waste streams. In addition, ~he nee~ for separate sulfonation, refining, and post-refiner bleaching equipment mak~s the capital equipment and operating c03ts for such a system very significant.
An alternative to sulfonation of lignin for increasitlg papermaking strength of hi~h yield fibers is carboxylation and brightening of lignin achieved by th~ combined ~welling and brightening action of alkaline peroxide prior to and/or during 2 ~
defibration. As sulfonation results in lignin containing sulfonate groups, likewise, carboxylation results in lignin with carboxylate groups. ~th the sulfonate and the carboxylate groups are capable of participating in hydrogen bonding which increases the strength of paper made from such high yield pulps (papermaking strength).
Similar to the alkaline high sulfonation treatment of chips prior to refining, alkaline peroxide pretreatment of chips softens the lignocellulosic raw material resulting in easier fiber separation (less energy consumption and less fines generation and fiber fragmentation~ during refining. In addition, refiner brightening with alkaline peroxide can eliminate the need for separate post-refiner bleaching equipment, due to the facts that refiners are excellent mixers of pulp and brightening agents, and the temperature within the refiner (about 100C or higher) causes brightening to occur extremely fast relative to typical post-refiner alkaline peroxide bleaching steps (approximately 50 C to 80 C). The primary drawback to brightening chips within the refiner with alkaline peroxide is peroxide decomposition. Peroxide decomposes to form oxygen (ineffective for lignin-retaining bleaching) and water under the highly alkaline conditions required for papermaking strength development. Peroxide decomposition is hastened by the high temperatures reached in refiners and by metal contaminants, particularly manganese, iron, and copper, which are contained in significant quantities in lignocellulosic raw materials and in lesser quantities in process water. Partial removal or inactivation of such metal contaminants in lignocelluslosic raw material can be effected by introducing chelating agents into the wood chips and then removing the chelant-metal complexes. However, the physical entrapmen~ and chemical attraction of such metals by fiber components within the chips make complete removal of the metals impractical and require additional peroxide protection.
The problems associated with pre-refiner or in-refinex alkaline peroxide treatments are partially avoided by conventional post refiner alkaline peroxide treatments. For exampl~, rather 20~7231 than removing metal contaminan~s from chips, the contaminants have been removed from individual fibers with chelating agents after refining and prior to alkaline peroxide bleaching. Post refininy removal is much more easily achieved because the particle size of the fiber in pulp is much smaller than the size of chips before refining. The smaller size makes the metal contaminants much more accessible to the chelant solution. Consequently, in many cases the individual fibers can be bleached to much higher brightnesses ~ith alkaline peroxide in a post refiner bleaching treatment without significant waste of peroxide bleaching agents due to metal contaminant induced decomposition of peroxide (U.S. Patent No.
4,160,693-Lindahl, et al.). The disadvantage is, that high strength requires high levels of pre-refiner sulfonation and high sulfonation makes post-refiner bleaching difficult.
There have been many attempts to overcome such problems associated with the pre-refiner or in-refiner use of alkaline peroxide in the production of high yield pulps. Control of alkalinity (e.g., see U.S. Patents 3,069,309-Fennell and 4,270,976-Sandstorm, et al., and Canadian Patents 1,078,558 and 1,173,604), control of the temperature (e.g., U.S. Patent 4,187,141-Ahrel), and control of time at high temperature (e.g., U.S. Patent 4,270,976-Sandstorm et al.) have been tried. However, such techniques for reducing peroxide decomposition also reduce the effectiveness of alkaline peroxide in terms of the resulting pulp properties (papermaking strength) while the presence of deleterious metal contaminants still results in inefficient utilization of the peroxide bleaching agent during refinar bleaching.
A common method for circumventing the problem of peroxide decomposition in alkaline peroxide bleaching of chips during refining is to add the bleaching agent directly to the refining zone to minimize the contact time between the chip and alkaline peroxide, and in some cases to allow more intimate contact between metal contaminants and silicate and/or magnesium ion stabilizer flocs (See for example, U.S. Patent Nos. 3,023,140-Textor, 3,069,309-Fennell, 4,022,965 Coheen, et al., 4,270,976-Sandstorm, et al., 4,311,553-Akerlund, et al.; Japanese Patent Application No. 80-72091, and Federal Republic of Germany Patent No. 2818-320). ~dditionally, wood chips have been pretreated by impregnation and/or refining with chelants (U.S. Patents Nos.
3,023,140-Textor, 4,311,553-Akerlund, et al., Japanese Patent Application No. 80-7209, and Federal Republic of Germany Patent No.
2818-320) or with sodium silicate (U.S. Patent Nos. 3,069,309-Fennell, 4,311,553-Akerlund, et al.), or with magnesium salts (U.S.
Patent Nos. 3,023,140-Textor, 3,069,309-Fennell, ~,311,553-Akerlund, et al., and Japanese Patent Application 80-72091) and combinations thereof prior to alkaline peroxide addition into the refiner to reduce peroxide decomposition. U.S. Patent No.
4,270,076-Sandstorm, et al., is the only case in which brightness comparable to post refiner alkaline peroxide bleaching was obtained but it utilized lower alkalinity as the means of reducing the peroxide decomposition rate which sacrificed good papermaking strength development.
The present invention is based in part upon the hypothesis that with processes employing alkaline peroxide addition directly into the refiner, the majority of the defibration occurs before the alkali and peroxide can react with the wood fibers, thereby reducing the potential for papermaking strength development imparted with requiring more energy for refining and increasing the generation of fines, all of which could be avoided if alkaline peroxide could be inserted into and stabilized within the chip and allowed to react with the chip prior to defibration.
Impregnation of chips with alkaline peroxide prior to refining has also been practiced (U.S. Patent~ 4,187,141-Ahrel, and 4,270,976-Sandstorm, et al., and Canadian Patents 1,078,558, and 1,173,604). In most cases, the brightnes~ obtained was comparable to that obtainable with post refiner alkaline peroxide bleaching.
However, with such processes, metal contaminants are not removed or deactivated; rather, peroxide decomposition is reduced by lower alkalinity (U.S. Patent Nos. 4,270,976-Sandstorm, et al., Canadian Patent 1,078,558, and 1,173,604) or by minimizing refining ~723~.
temperature (U.S. Patent No. 4,187,141-Ahrel). However, the lowering of the alkalinity or temperature causes less papermaking strength to be developed than with high sulfonation methods.
Lowering of the temperature below 100 C is difficult to accomplish practically. At higher alkalinity, strengths comparable to those of post refiner bleached, sulfonated high yield pulps were obtained but at the expense of lower brightness due to increased peroxide decomposition (Canadian Patent No. 1,078,558).
Additional examples of prior art teachings of treating pulp (rater than chips) with peroxide demonstrate the continuing tendency in the art to avoid treating chips with peroxide because of the decomposition problem. U.S. Patent No. 4,787,959 is another example of a high yield pulping process that avoids peroxide treatment of chips by treating pulp rather than chips with peroxide using a first alkaline cooking stage to fiberize the chips prior to a second cooking with peroxide. By the time the peroxide is added in this process the "lignin-cellulose" material exists as more or less discr0te fibers because the cellular structure has been fractured. Thus, the problem of peroxide stability within the cells of chips or wood particles does not exist.
Thus in many recent prior art patents such as, U.S. Patents 4,787,959, 4,734,161 and 4,732,650 the material being treated is pulp made up of small fibers, so the problem of stability of peroxide within the essentially unbroken cellular structure of wood particles existing prior to the refininq does not exist.
Alkaline peroxide stabilizers like water soluble alkaline sodium silicate and magnesium sulfate are often utilized in the peroxide bleaching of high yield pulps to further reduce peroxide decomposition caused by metal contaminants. The silicate-magnesium combination forms a floc in alkaline peroxide solutions and this floc attracts and absorbs the metal ions thereby reducing the ability of such ions to decompose peroxide. Magnesium ions also reduce peroxide decomposition by electronically deactivating the metal ions, thereby reducing the potential of the metal ions to decompose peroxide.
2~723~
Recently, it was discovered that flocs or precipitates formed by silicates and/or magnesium in alkaline peroxide solutions cannot readily pe~etrate into the wood chip structures prior to refining due to the physical size of the flocs relative to the pore size of the wood chips. The discovery was based upon the observation that such stabilizers effectively stabilize peroxide against decomposition when pulp is being bleached with peroxide but are not as effective when the same fibers are still in chip form rather than pulp. It was postulated that the difference in stabilizer effectiveness when treating pulp fibers versus wood chips is due to the relatively small molecules of alkali and peroxide entering the cellular structure of the chip while the stabilizer floc if impeded from penetrating into the cells to counteract decomposition induced by metal contaminants within the cellular structure. The alkaline peroxide in the chips, upon entering the cellular structure and becoming separated from the stabilizing floc, rapidly decomposes thereby reducing the amount of peroxide available for bleaching during refining. In addition, the pressure buildup within the chip due to the evolution of oxygen gas during peroxide decomposition forces alkaline peroxide solution back ollt of the chip resulting in insufficient peroxide retention in the chip as it enters the refining zone. Furthermore, irreversible alkaline yellowing of the pulp occurs if there is insufficient residual peroxide remaining with the pulp after refining.
U.S. Patent 4,849,053 to Gentile, et al. and the references cited during the prosecution of that patent are the most pertinent prior art, over which the present invention constitutes an improvement. The Gentile, et al. patent describes and claims a highly successful method for producing wood pulp from chips using pre-treatment with stabilizers and alkaline peroxide prior to mechanical fiberization (refining~ to increase the brightness of the resulting fibers and papermaking strength achievable with the fibers. This sequential pre-treatment of the wood chips prior to refining results in the "in-situ" formation within the chips of a peroxide-stabilizing floc or sol.
2~723~
The alkaline peroxide impregnated chips with the "in-situ"
formed stabilizing floc within the cellular structure are refined in one ~r more stage(s) under atmospheric pressure or superatmospheric pressure and the corresponding saturated steam temperature. (The refining pressure is usually associated with steam added to or generated within the re~ining device.) The resulting pulp is dewatered and washed to remove bleaching and stabilizing chemicals and dissolved wood substances to result in a non-sulfonated pulp having a unique combination of properties including high yield, superior brightness and papermaking strength, and low fines content. Recyclable alkaline peroxide is obtained from the dewatering of the pulp after refining and preferably before acidification~ The alkaline peroxide obtained from the post refiner dewatering step can be reused as makeup in the impregnation step in which peroxide is added to the chips.
The two or three stage impregnation and pulping process of Gentile et al. tU.S. Patent 4,849,063) is designed to stabilize alkaline peroxide so it can effectively and economically develop pulp strength and brightness by the time the pulp exists the mechanical pulping stage (refiner). This method, while eminently successful on most species of wood chips, does not produce the maximum stabilization of alkaline peroxide. For example, with wood chips from such softwoods as eastern black spruce, eastern balsam fir, lodgepole pine/white spruce (50/50% mix), and hardwoods such as aspen, the peroxide is not stabilized as completely as possible in the normal fashion, some peroxide decomposition occurs and maximum brightness is not achieved as economically as possible with the practice of the present invention.
SUMMARY OF INVENTION
The present invention is based upon the discovery that the key to the realization of successful peroxide stabilizat~on and brightening utili~ation lies in (1) substantial reduction of metallic ions content in the chips, such as iron, copper, and (in particular) manganese content in the chips (these metals catalyze peroxide decomposition) prior to impregnation of chips with peroxide and (2) the maintenance of high level of magnesium in the chips with the alkaline peroxide prior to and preferably during refining.
The present invention provides an alkaline peroxide process for the production of high yield pulps from wood chips having a reduced manganese concentration prior to peroxide impregnation and increased magnesium concentration prior to or simultaneously with alkaline peroxide impregnation, followed by refining to produce a pulp of high brightne~s and pulp streng~h with a minimum of peroxide consumption.
Other aspects of this invention are as follows:
In a high yield pulping process comprising impregnating chips with- an alkaline peroxide solution containing stabllizers for peroxide followed by mechanical defibration, wherein the improvement comprises:
pretreatinq the wood chips prior to peroxide impregnation, said pretreatment comprising;
(a) impregnating the chips wlth an impregnation solution consisting essentially o~ a chelating agent for metallic ions; and, (b) expressing from ~he chips chelating agents and metallic ions.
A high yield alkaline peroxide pulping proceR~ for wood chips comprising:
(a) impregnating the wood chips with a first impregnation solution consisting essentially of a chelating agent for metallic ions;
(b~ expressing, at least 25~ of said first impregnation solution containing metallic ions from within the chips;
tc) removing expressed impregnation solution from contact with the chips;
(d) impregnating the chips with a second impregnating solution containing magnesium salts at a concentration of from 0.5%
grams per liter to 20 grams per liter to result in from 0.05% to 2~ by weight magnesium in the chips calculated as MgSOI.7H2O and based upon the oven dried weight of the wood chlps;
~ e) impregnating the chips with a third peroxide and having a pH from 9 to 13; and, (f) mechanically defiberizing the chips to produce pulp.
A high yield alkaline peroxide pulping process for wood chips comprising:
(a) impregnating the wood chips with a first impregnation solution containing a chelating agent for metallic ions without containing significant quantities of magnesium ions;
(b) expressing said first impregnation solution containing metallic ions from within the chips;
(c) removing expressed impregnation solution from contact with the chips;
(d) impregnating the chips wit:h a second impregnating solution containin~ peroxide and a stabilizer for peroxide and having a pH from 9 to 13 and containing magnesium salts at a concentration of from 0.5% grams per liter to 20 gram3 per liter to result in from O . 05% to 2% by weight magnesium in the chips calculated as MgSO~.7H2O and based upon the oven dried weight of the wood chips; and (e) mechanically defiberizing the chips ~o produce pulp.
DETAILED DESCRIPTION OF THE INVENTION AND PREFERRED EMBODIMENTS
This invention is di~ected toward the removal of metallic ions such as manganese from lignocellulosic material in chip~ form prior to treatment with alkaline peroxide and to the utilization of high levels of magnesium (Mg) withln the chips while in contact with alkaline peroxide. The present invention is particularly useful 9a for pulp~ from wood species naturally high in metallic ions such as eastern black spruce, eastern balsam fir, lodgepole pine/white spruce mixtures and aspen.
The present process i~ charactarized by at least a two stage and preferably three or more stage impregnation process of chips prior to refining. In the first stage, wood chips, which preferably have been purged of entrapped air, are impregnated with a chelating agent such as die~hylenetriaminepantaacetic acid (DTPA), ethylene diaminetetraacetic acid (EDTA), hydroxyethyle~hylenediamine triacetic acid (HEEDTA), and nitrilo~riacetic acid (NTA), sodium tripolyphosphate (STPP), and phosphonic acid derivative or other similar compounds known in the 9b ~7~3~
art for such functionality or a combination of such chelating agents. The concentration of the chelating agent in the impregnati~g solution should be preferably from 0.1 gram/liter to 20 grams/liter (expressed as 100% chelating agent in the solution) to give preferably 0.01% to 2% chelant based on the dry weight of the chips with from 0.05% to 0.5% being particularly preferred.
The temperature of the first impregnation step is preferably between 15 C and 80C. The pH is preferrably between 4 and 12 with between 8 to 11 being particularly preferred. Adjustments to the solution pH can be made with any suitable acid or alkaline substance which does not react with pero~ide, cause darkening of the chips, or cause any of the components of the impregnation solu~ion to be precipitated or to lose chelating ability such as sulfuric acid or sodium hydroxide.
Before, or as part of the first impregnating step, the chips are preferably squeezed to expel liquid and any remaining air and then allowed to expand in contact with the impregnation solution.
The quantity of solution absorbed in an impregnation step is influenced by the impregnation device (primarily the degree of squeezing of the chips~ and the particular material being impregnated. The level of chemical addition into the chips is primarily controlled by the concentration of the particular chemical in the impregnating solution and the quantity of solution absorbed. The concentration of chelant and quantity of solution absorbed is preferably adjusted to give a chemical addition of 0.01% to 2% based cn the dry weight of lignocellulosic material being treated. The first impregnation solution is expressed either prior to or as the initial part of the second impregnation step.
Metallic ions are removed from the chips with the expressed first impregnation solution which removal is enhanced by the presence of the chelating agents. Preferably a-t least about 25% of the first impregnation solution is expressed from the chips with from about 33~ to about 50% being particularly preferred. The effectiveness of the first impregnation step to remove metallic ions is enhanced by providing some reten$ion time between impregnation and expressing the impregnation solution from the chips. This enhanced effectiveness is observed with a retention time of one half hour although ~everal hours is more effective. Since the first impregnation stage is primarily for the purpose of removing metallic ions from the chips, the first impregnation solution should consist esstentially of a chelating agent because it is expressed from the chips. The presence of substantial quantities of peroxide ( e.g. above 1%) or stabilizers in the first impregnation solution would be wasteful of such chemicals since they would be removed from the chips when the first impregnation solutions is expressed from the chips. Metallic stabilizers, particularly magnesium should be avoided in the first stage because they interfere with the primary purpose of the chelating agent.
The second impregnation step can be a conventional alkaline peroxide impregnation stage with stabilizers and chelating agents.
Preferably the second impregnation stage is with an aqueous solution of solub1e magnesium salts (e.g., epsom salt - MgSO4.7H2O~.
The epsom salt addition level i5 0.05% to 2% based on oven dried (o.d.) wood expressed as MgSO4.7H2O. This can be readily accomplished with an impregnation solution containing 0.5 grams per liter to 20 grams per liter. The purpose of this second step is to allow the soluble magnesium salts to penetrate the chip interstices. The temperature o~ the second impregnation step is preferably between 15 C and ~0 C, and the pH is maintained below 10 to keep the magnesium in a soluble form. Adjustment to the solution p~ is preferably made in the same manner as described for the first impregnation solution. Optionally, the second impregnation solution can contain alkalin~ peroxide with silicate stabilizers.
The third impregnation solution is an aqueous alkaline peroxide solution which contains peroxide stabilizers such as silicates. Preferably the third impregnation solution contains magnesium and silicate stabilizers. Silicates are preferably in a concentration range of 1 gram per liter to 5~ grams per liter to yield between 0.1% to 5% by weight of silicates (calculated as 2~7~31L
SiO2) based upon the dry weight of the chips. Magnesium based on weight of Mg in salt, is preferably in a concentration of from 0.01 grams per ~iter to 2 grams per liter to result after impregnation in from 0.001% to 0.2% by weight Mg based upon the dry weight of the chips. The third impregnation solution contains preferably hydrogen peroxide although any other peroxygen compound suitable for lignin brightening may be used. The peroxygen compound is preferably in the concentration range of between 5% and 100 grams per liter (calculated and expressed as hydrogen peroxide) to give additional lavels of preferably between 0.5~ and 10% of the dry weight of chips expressed as hydrogen peroxide. In addition, an alkaline substance (preferably sodium hydroxide) is added to the third impregnation solution to give a solution pH preferably in the range between 9 and 13 with between 10 and 12.5 being most preferred.
The most preferred impregnation sequence is the three stage sequence previously described and presented in greater detail in the axamples. However, it should be understood that the invention is not limited to the generally described three stage sequence.
A two-stage impregnation sequence in which the first impregnation stage is practiced as previously described and the second impregnation (Mg compounds) solution is combined with the third impregnation solution (alkaline peroxide and peroxide stabilizers such as silicates) and used as the impregnation solution in the second staye, preferably at a pH from 9 to 13 can also be employed.
It is importan~ that the entire chip become uniformly impregnated with any reactant solutions. Best results are achieved when a squeezing ratio (e~ual to mass of liquid squeezed from the chips per unit mass of dry chips) of unity or slightly higher is achieved. This requires a compression ratio of about 4:1, and results in the chips being squeezed from about 33% solid to about 50% solids. ~n other words, about 50% of the liquid present in the chips entering the compression device is squeezed out and replaced by "new" liquid in the impregna~ion expansion which follows.
2~7~3~L
The invention is not limited to the concentration and addition level ranges previously described for stabilizers and chelating agents, 3ince differences in metal contamination levels of lignocellulosic raw materials or process water could justify stabilizer or chelating agent usages outside of the specified preferred ranges.
Optionally, the chemically treated chips can be allowed to react with or without the application of heat, prior to entering the refining stage by retaining the impregnated chips for some finite time in any suitable vessel. A retention time of 5 minutes to 60 minutes is particularly suitable. Each impregnation is preferrably followed by a short drainage period and additional time for diffusion and/or reaction to occur within the chips. The amount of diffusion/reaction time required depends on the type of wood processed.
Refinin~ of Chemically Im~reqnated Chi~s (Def bration) The chemically treated chips are mechanically refined in a suitable defibration apparatus in one cr more stages in accordance with conventional processes and equipment. The steam pressure and corresponding temperature during refining are optional and can b~
at atmospheric and/or superatmospheric pressure, depending on the species being pulped and the desired pulp properties. Atmospheric pressure refining is preferred.
After refining, it is preferred that the pulp remain alkaline so that the silicate and other pH-sensitive materials can be removed prior to washing and neutralization. This prevents silicate deposition which can impair final pulp properties.
Post-Refininq_~teps:
After refining, the pulp may be allowed to continue bleaching as long as is practical prior to expelling the impregnation solutions. The amount of peroxide used in the impregnation steps is preferably preselected to result in some residual peroxide remaining after refining in order to maintain high brightness.
2~7~3~
Preferably the refined pulp is concentrated, e.g., by compressing or thickening, to remove residual impregnation solution containing potentiall~ recyclable alkaline peroxide, then diluted with water, washed and acidified preferably with sulfur dioxide, sodium bisulfite, sulfurous acid, or sulfuric acid, to a pH between 5.5 and 6Ø In particular, washing prior to acidification is preferred for removal of alkali soluble wood components and silicate. The residual peroxide extracted from the pulp after refining can be recycled as a source of peroxide in one of the impregnation solutions particularly if the process is practiced continuously or in sequential batches. The washed pulp is preferably screened and cleaned by conventional means to result in a pulp suitable for the production of paper products.
EXAMPLES
In the following examples wood chips from eas~ern black spruce, eastern balsam fir, lodgepole pine/white spruce 50/50 mixture (all softwoods) and/or aspen (hardwood), are treated by both the process of the present invention and that of Gentile, et al., U.S. Patent 4/849,058 and a comparison of the results tabulated. The proc~ss of U.S. Patent 4,849,058 was chosen for comparison because it represents the what is believed to be the best of the prior art processes for stabilizing alkaline peroxide in chips prior to high yield mechanical pulping. In the examples, all parts are by weight unless specified otherwise.
EXAMPLES A ( CONTROL ) AND
Screened eastern black spruce chips (2000 grams o.d. of wood at a solid content of 49%) were steamed for 15 minutes. The hot chips (solid content 40%) were placed into a Sprout-Bauer Ll-12 laboratory impregnator and compressed to a solids content of 60-70%. The impregnator was then closed, filled with 55 liters of impregnation liquor and the chips released (allowed to expand) into the liquorO The impregna~ed chips were removed from the 2~7~.31 impregnator and drained for 5 minutes to remove all excess liquor.
The same procedure was repeated for all three impregnation stages.
In Exampl~ A, the preferred three-stage impregnation process of U.S. Patent 4,849,058 was employed. In Example 1, the 3 impregnation steps were conducted according to the process of the present invention.
Table 1 lists the impregnation conditions, the amount ~nd type of chemicals added, and the test results comparing the process of the present invention (Example lj with the control (Example A).
The amounts of chemicals applied during impregnation were determined as follows:
Ca = (0.1) (PUR)(CL), where Ca = amount of chemical applied in % by weight of oven dried (o.d.) wood CL = concentration of chemicals in liquor in grams/liter PUR = amount of li~uor picked up during impregnation in liters divided by oven dried (o.d.) weight of wood in kilograms (kg) The magnesium salt used in these examples was Epsom salt (MgSO4-7H20)- The reported amounts of pentasodium salt of diethylenetriamine-pentaacetic-acid (DTPA) are based on a solution with 40.2% active ingredient. Trisodium salt of hydroxy-ethyl-ethylene-diamine-triacetate (HEEDTA) was a 41.3% solution. Also, the concentrations for silicate are calculated using a 37.6%
solution with a SiOz/Na20 ratio of 3.22.
After impregnation chips were refined in a Sprout-Bauer 12-lCP laboratory refiner under atmospheric pressure. After refining residual peroxide and caustic were determined by titration. The pulp was dewatered, washed and the pH adjusted to 6.0 with dilute H2S04. "Brightness" is defined as ISO brightness in percent units which is determined by using the sample preparation procedure given in the Technical Association of the Pulp and Paper Industry (TAPPI) Official Test Method T218 om-83. The brightness of the sample was measured using a Technibrite Micro TB-IC meter.
2 3 ~
Hydrogen peroxide usage or consumption (expressed as a weight percent of the dry weight of the chips) is based on the quantity of peroxide applied to the wood chips minus the quantity of residual peroxide in the pulp after refining. The percentage peroxide consumed is calculated as being equal to the quantity of peroxide consumed times 100 divided by the dry weight of the chips.
The quantity of peroxide in a solution was determined by iodometric titration using starch as an end point indicator (Vogel, Quantative Inorganic Analysis, Wiley & Sons, 1961, p. 363).
The magnesium and manganese concentration in the original wood chips and after impregnation was determined by atomic absorption spectroscopy.
As shown, the process of the present invention led to an increase in manganese removal and magnesium retention, which in turn gave a 2% brightness increase and a 47% reduction in peroxide consumption, thus demonstrating the increased peroxide s~ability under the process of the present invention.
2 3 3 7 ~ 3 .L
TABLE I
Process conditions, added chemical amounts, test results of 3-stage alkaline peroxide process of present invention vs control 3-stage process.
.
EXAMPLE NO. A (CONTROL) #1 TYPE WOOD: EASTERN EASTERN
1. 1st Impregnation a. process conditions pH 7.0 11.0 b. chemicals added CL CA CL CA
DTPA 1.35 0.22 2.5 0.39 HEEDTA 1.35 0.22 2.5 0.39 MgSO4.7H203.35 0.53 - -2. 2nd Impregnation a. process conditions pH 10.8 9.5 b. chemicals added DTPA 1.25 0.19 - -HEEDTA 1.25 0.19 Silicate 12.5 1.9 MgSO4.7HzO - - 3.35 0.53 3. 3rd Impregnation a. process conditions pH 11.6 11.2 b. chemicals added MgSO .7H O 4.5 0.54 3.35 0.48 Sili4 te 216.5 2.13 26.65 3.81 NaOH 31.7 4.09 27.20 3.89 HzO2 33'5 4.32 27.20 3.89 4. Total Chemicals Added DPTA 0.41 0.39 HEEDTA 0.41 0.39 MgSO .7H O 1.07 1.01 Silic~ate 2 4.03 3.81 NaOH 4.09 3.89 H~Oz 4.32 3.89 2 ~ 3 1 5. Te~t Results CA CA
ISO brightness (%) 74.1 76.1 H2o2 c0nsumed (%) 3.74 2.73 NaOH consumed (%) 3-35 3.18 PUR 3rd stage (1/kg) 1.29 1.43 Mn in chip3 3rd stage (ppm) 10.3 8.4 Mg in chips 3rd stage (ppm) 364 1050 Mn content original chipB (ppm) 37-5 37-5 Mg content original chip~ (ppm) 73-5 73-5 COMPARISON
Control: 74.1% brightnesa 3.74% H202 consumption 10.3 ppm Mn in 3rd atage chips 364 ppm Mg in 3rd stage chips Invention: 76.1% brightneqs 2.73% H22 con~umption 8.4 ppm Mn in 3rd stage chip~
1050 ppm Mg in 3rd stage chipa Improvement: 2.0 greater brightneas units 27% decrease in H2O2 conaumption 1.9 ppm lesa Mn in 3rd ~tage chips 686 ppm more Mg in 3rd ~tage chip~
~723~
EXAMPLES B (CONTROL) AND 2 Two kilograms of screened eastern Canadian balsam fir chips with a sol-ids content of 56.2~ were impregnated and refined as in control Example A. The pH of the first stage liquor was adjusted to 7~0 and the 2nd stage liquor pH was 10.7. This experiment is designated as comparative Example B.
A three impregnation step sequence of the present invention was made on an identical batch eastern Canadian balsam fir chips as used in Example B. The general impregnation and refining conditions were the same as for Example 1 above. Table 2 lists the process conditions, chemical types and amounts added, and the comparative test resul-ts for both examples. This experiment is designated as Example 2.
As with Examples A and 1, the greater manganese removal from the chips and greater magnesium addition to the chips prior to refining gave improved brightness (1.5 ISO brightness units) and reduced (27~) peroxide consumption compared to the control.
~9 20~7231 TABLE II
Process conditions, added chemical amounts, test results of 3-stage alkaline peroxide process of present invention vs. control 3-stage process.
-EXAMPLE NO. B (CONTROL) #2 ~ASTERN EASTEPN
TYPE WOOD: ~ALSAM FIR BALSAM FIR
1. 1st Impregnation a. proces3 condition3 pH 7.0 11.0 b. chemicals added CL CA CL CA
DTPA 1.70 0.24 3.35 0.49 HEEDTA 1.70 0.24 3.35 0.49 ~S04 .7H204.45 0.64 - _ 2. 2nd Impregnation a. proces3 conditions pH 10.7 9.5 b. chemicals added DTPA 1.90 0.27 - -HEEDTA 1.90 0.27 Silicate 18.85 2.71 MgSO4O7HzO - - 5.0 0.65 3. 3rd Impregnation a. proces~ conditions pH 11.3 11.0 b. chemicals added MgSO .7H O 6.5 0.63 5.55 0.61 Silic~ate 225.95 2.52 44.5 4.9 NaOH 50.0 4.9 41.20 4.5 HzOz 55.0 3.3 45.22 4.9 4. Tctal Chemical~ Added DPTA 0.51 0.49 HEEDTA 0.51 0.49 MgSO .7H O 1.27 1.26 Silicgate 2 5.23 4.90 NaOH 4-9 4-5 HzO2 5.3 4.9 2~7~3~
5. Test Results CA CA
ISO brightness (%) 74.2 75.7 Hzo consumed (~) 5.03 3.65 NaO~ consumed (~) 3.68 2~88 PU~ 3rd stage (1/kg) 0.97 1.1 Mn in chips 3rd stage (ppm) 31.5 29.1 Mg in chips 3rd stage (ppm) 430 722 Mn content original chips (ppm) 162.7 162.7 Mg content original chips (ppm) 110.1 110.1 C ARISo Control: 74.2~ brightnes~ WITH 5.03~ H22 congumption 31.53% ppm Mn in 3rd stage chip3 430 ppm Mg in 3rd stage chip~
Invention: 75.7% brightnes3 with 3.65% H202 con3umptiion 29.1% ppm Mn in 3rd 3tage chips 722 ppm Mg in 3rd 3tage chips Improvement. 1.5 greater brightness units 27~ leY~ H22 con~umption 2.43 ppm les~ Mn in 3rd stage chips 292 ppm more Mg in 3rd ~tage chips 2~2~
EXAMPLES C (CONTROL) AND 3 Screened aspen (populus tremuloides) chips at a solid content of 58.2% were impregnated and refined using the general procedures described in Example A. The pH of the first stage liquor was adjusted to 7.0 and the 2nd stage liquor had a pH of 10.7. This is designated Example C. An identical aspen chip charge was impregnated and refined by the general procedures of Example 1 above using the sequence of this invention. The specific additions used and results obtained are shown in Table III.
Although the original aspen chips had a low manganese content resulting in a low 3rd stage manganese level in the chips in both Examples C and 3, the third stage chips of Example 3 retained much more magnesium. As a result, brightness was improved by 1.2% while peroxide consumption was reduced by about 18% vs. the control.
2 ~ ~
TABLE III
The process conditions, added chemical amounts, test results of 3-stage alkaline peroxide process of present invention vs. control 3-stage process.
EXAMPLE NO. C (CONTROL) #3 1. 1st Impregnation a. process condition3 pH 7.0 11.1 b. chemicals added CL CA CL CA
DTPA 1.450.24 2.6 0.37 HEEDTA 1.450.24 2.65 0.37 MgSO4.7H20 3.6 0.59 2.65 2. 2nd Impregnation a. proces~ conditions pH 10.7 9.5 b. chemicals added DTPA 1.550.25 HEEDTA 1.550.25 Silicate 15.4 2.53 - -MgSO4.7H2O - 3 55 3. 3rd Impregnation a. process conditions pH 11.6 11.8 b. chemicals added MqSO .7H O 4.15 0.62 4.15 0.63 Silicate 2 16.65 2.50 33.3 5.02 NaOH 37.5 5.63 38.8 5.86 H2O2 23.4 4.41 29.2 4.41 4. Total Chemicals Added DPTA 0.49 0.37 MgSO .7H O 1.21 1.18 Silic4ate 2 5-03 5.02 NaOE~ 5.63 5.86 , H22 4.41 4.41 2,~7~:
5. Test Results CA CA
ISO brightne~s (%) 78.9 80.1 HzO~ consumed ~%) 3.54 2.92 NaOH consumed (%) 4.57 4.15 PUR 3rd stage (l/ky)~ 1.5 1.5 Mn in chips 3rd stage (ppm) 2.9 5.2 Mg in chips 3rd stage (ppm) 471 746 Mn content original chips (ppm) 9-3 9-3 Mg content original chips (ppm) 137 137 COMPARISON
Control: 78.9% brightness 3.54% H Oz consumption 441 ppm ~g in 3rd stage chips Invention: 80.1% brightness 2.92% H Oz consumption 746 ppm ~g in 3rd staga chips Improvement: Process: 1.2 greater brightness units 18~ less in H O2 consumption 293 ppm more ~g in 3rd atage chips * See def inition of PUR in Examples A and B .
2~
~7~3~
EXAMPLES D - N and 4-7 A lodgepole pine/white spruce (50/50%) chips mixture was subjected to both the 3-stage process of the present invention and that of the control process used in Example A. The same general impregnation and refining conditions were employed as in the previous examples along with comparable chemical applications while the specific conditions are given in Table IV. Table IV compares the brightness values, chemical compositions and Mn and Mg content for identical chip charges and both examples D, E, F, G (control) examples with 4, 5, 6 and 7, respectively (process of invention).
In all cases, brightness is higher and peroxide consumption lower for examples 4, 5, 6, and 7. Also, chips impregnated in example 4, 5, 6 and 7 always have a lower Mn content and a higher Mg content after the 3rd impregnation stage, thus leading to greater peroxide efficiency in pulp brightening.
Brightness gains attributable to the process of invention range from 1.8 to 6.2% ISO, while peroxide consumption is reduced by from 13 to 28% compared to the control.
25' 2 ~ 3 ~
TABLE IV
~omparati~e test results of 3-stage alkaline peroxide process of the present invention vs control 3-stage processO
.
EXAMPLE NO. D 4 E 5 F 6 G 7 ISO Brightness 74.2 76.0 67.771.766.472.6 72.0 74.8 PUR (l/kg) 0.850.910.70 0.75 0.83 0.95 1.03 1.3 H2O2 Consumed (%) 2.782.002.53 2.19 3.102.43 2.20 1.78 NaOH Consumed (%) 2.201.8~1.82 2.27 1.81 2.07 1.76 2.24 Mn Content in 3rd Stage (ppm) 12.78.6 20.8 12.124.8 7.1 12.14.7 Mg Content in 3rd Stage Ippm~ 377 885 515 697 462 795296 855 Mn Content in (ppm) 83.283.2 62.8 62.872.0 72.0 67.7 67.7 Mg Content in Original Wood (ppm) 112 112 103 103 122 122 104104 _ _ 2~231 Thus, as substantiated by the examples for both hardwoods and softwoods, the 3-stage preferred process of the present invitation increased ~rightness and decreased H202 consumption compared to the best prior art process for high yield peroxide pretreated pulp ~U.S. Patent 4,849,058) .
The concept and practice of the present invention leads to two major advantages over other alkaline peroxide chip treatment processes. These are:
1. More efficient removal of heavy metal ions [(particularly) manganese (Mn)], which catalyze peroxide decompositions;
2. Maintenance of a higher concentration of magnesium ions in the chips so they can protect the peroxide from decomposition prior to, during, and following the refining process.
The best mode presently contemplated for practicing the invention is with a three stage impregnation process as examplified in Example 1 with chemical selection, concentration of impregnation solutions and chemical quantities impregnated into the chips in the ranges demonstrated in Examples 1 throuyh 7.
The present invention, described in its hroadest concept is an improvement to peroxide treatments of wood chips prior to refining in which the concentration of metal ions within the cellular structure of the chips is reduced in a first impregnation step as shown in examples 1 through 7 and followed by alkaline peroxide impregnation with stabilizers for peroxide including magnesium ions and then mechanical pulping (refining).
The present invention is based in part upon the hypothesis that with processes employing alkaline peroxide addition directly into the refiner, the majority of the defibration occurs before the alkali and peroxide can react with the wood fibers, thereby reducing the potential for papermaking strength development imparted with requiring more energy for refining and increasing the generation of fines, all of which could be avoided if alkaline peroxide could be inserted into and stabilized within the chip and allowed to react with the chip prior to defibration.
Impregnation of chips with alkaline peroxide prior to refining has also been practiced (U.S. Patent~ 4,187,141-Ahrel, and 4,270,976-Sandstorm, et al., and Canadian Patents 1,078,558, and 1,173,604). In most cases, the brightnes~ obtained was comparable to that obtainable with post refiner alkaline peroxide bleaching.
However, with such processes, metal contaminants are not removed or deactivated; rather, peroxide decomposition is reduced by lower alkalinity (U.S. Patent Nos. 4,270,976-Sandstorm, et al., Canadian Patent 1,078,558, and 1,173,604) or by minimizing refining ~723~.
temperature (U.S. Patent No. 4,187,141-Ahrel). However, the lowering of the alkalinity or temperature causes less papermaking strength to be developed than with high sulfonation methods.
Lowering of the temperature below 100 C is difficult to accomplish practically. At higher alkalinity, strengths comparable to those of post refiner bleached, sulfonated high yield pulps were obtained but at the expense of lower brightness due to increased peroxide decomposition (Canadian Patent No. 1,078,558).
Additional examples of prior art teachings of treating pulp (rater than chips) with peroxide demonstrate the continuing tendency in the art to avoid treating chips with peroxide because of the decomposition problem. U.S. Patent No. 4,787,959 is another example of a high yield pulping process that avoids peroxide treatment of chips by treating pulp rather than chips with peroxide using a first alkaline cooking stage to fiberize the chips prior to a second cooking with peroxide. By the time the peroxide is added in this process the "lignin-cellulose" material exists as more or less discr0te fibers because the cellular structure has been fractured. Thus, the problem of peroxide stability within the cells of chips or wood particles does not exist.
Thus in many recent prior art patents such as, U.S. Patents 4,787,959, 4,734,161 and 4,732,650 the material being treated is pulp made up of small fibers, so the problem of stability of peroxide within the essentially unbroken cellular structure of wood particles existing prior to the refininq does not exist.
Alkaline peroxide stabilizers like water soluble alkaline sodium silicate and magnesium sulfate are often utilized in the peroxide bleaching of high yield pulps to further reduce peroxide decomposition caused by metal contaminants. The silicate-magnesium combination forms a floc in alkaline peroxide solutions and this floc attracts and absorbs the metal ions thereby reducing the ability of such ions to decompose peroxide. Magnesium ions also reduce peroxide decomposition by electronically deactivating the metal ions, thereby reducing the potential of the metal ions to decompose peroxide.
2~723~
Recently, it was discovered that flocs or precipitates formed by silicates and/or magnesium in alkaline peroxide solutions cannot readily pe~etrate into the wood chip structures prior to refining due to the physical size of the flocs relative to the pore size of the wood chips. The discovery was based upon the observation that such stabilizers effectively stabilize peroxide against decomposition when pulp is being bleached with peroxide but are not as effective when the same fibers are still in chip form rather than pulp. It was postulated that the difference in stabilizer effectiveness when treating pulp fibers versus wood chips is due to the relatively small molecules of alkali and peroxide entering the cellular structure of the chip while the stabilizer floc if impeded from penetrating into the cells to counteract decomposition induced by metal contaminants within the cellular structure. The alkaline peroxide in the chips, upon entering the cellular structure and becoming separated from the stabilizing floc, rapidly decomposes thereby reducing the amount of peroxide available for bleaching during refining. In addition, the pressure buildup within the chip due to the evolution of oxygen gas during peroxide decomposition forces alkaline peroxide solution back ollt of the chip resulting in insufficient peroxide retention in the chip as it enters the refining zone. Furthermore, irreversible alkaline yellowing of the pulp occurs if there is insufficient residual peroxide remaining with the pulp after refining.
U.S. Patent 4,849,053 to Gentile, et al. and the references cited during the prosecution of that patent are the most pertinent prior art, over which the present invention constitutes an improvement. The Gentile, et al. patent describes and claims a highly successful method for producing wood pulp from chips using pre-treatment with stabilizers and alkaline peroxide prior to mechanical fiberization (refining~ to increase the brightness of the resulting fibers and papermaking strength achievable with the fibers. This sequential pre-treatment of the wood chips prior to refining results in the "in-situ" formation within the chips of a peroxide-stabilizing floc or sol.
2~723~
The alkaline peroxide impregnated chips with the "in-situ"
formed stabilizing floc within the cellular structure are refined in one ~r more stage(s) under atmospheric pressure or superatmospheric pressure and the corresponding saturated steam temperature. (The refining pressure is usually associated with steam added to or generated within the re~ining device.) The resulting pulp is dewatered and washed to remove bleaching and stabilizing chemicals and dissolved wood substances to result in a non-sulfonated pulp having a unique combination of properties including high yield, superior brightness and papermaking strength, and low fines content. Recyclable alkaline peroxide is obtained from the dewatering of the pulp after refining and preferably before acidification~ The alkaline peroxide obtained from the post refiner dewatering step can be reused as makeup in the impregnation step in which peroxide is added to the chips.
The two or three stage impregnation and pulping process of Gentile et al. tU.S. Patent 4,849,063) is designed to stabilize alkaline peroxide so it can effectively and economically develop pulp strength and brightness by the time the pulp exists the mechanical pulping stage (refiner). This method, while eminently successful on most species of wood chips, does not produce the maximum stabilization of alkaline peroxide. For example, with wood chips from such softwoods as eastern black spruce, eastern balsam fir, lodgepole pine/white spruce (50/50% mix), and hardwoods such as aspen, the peroxide is not stabilized as completely as possible in the normal fashion, some peroxide decomposition occurs and maximum brightness is not achieved as economically as possible with the practice of the present invention.
SUMMARY OF INVENTION
The present invention is based upon the discovery that the key to the realization of successful peroxide stabilizat~on and brightening utili~ation lies in (1) substantial reduction of metallic ions content in the chips, such as iron, copper, and (in particular) manganese content in the chips (these metals catalyze peroxide decomposition) prior to impregnation of chips with peroxide and (2) the maintenance of high level of magnesium in the chips with the alkaline peroxide prior to and preferably during refining.
The present invention provides an alkaline peroxide process for the production of high yield pulps from wood chips having a reduced manganese concentration prior to peroxide impregnation and increased magnesium concentration prior to or simultaneously with alkaline peroxide impregnation, followed by refining to produce a pulp of high brightne~s and pulp streng~h with a minimum of peroxide consumption.
Other aspects of this invention are as follows:
In a high yield pulping process comprising impregnating chips with- an alkaline peroxide solution containing stabllizers for peroxide followed by mechanical defibration, wherein the improvement comprises:
pretreatinq the wood chips prior to peroxide impregnation, said pretreatment comprising;
(a) impregnating the chips wlth an impregnation solution consisting essentially o~ a chelating agent for metallic ions; and, (b) expressing from ~he chips chelating agents and metallic ions.
A high yield alkaline peroxide pulping proceR~ for wood chips comprising:
(a) impregnating the wood chips with a first impregnation solution consisting essentially of a chelating agent for metallic ions;
(b~ expressing, at least 25~ of said first impregnation solution containing metallic ions from within the chips;
tc) removing expressed impregnation solution from contact with the chips;
(d) impregnating the chips with a second impregnating solution containing magnesium salts at a concentration of from 0.5%
grams per liter to 20 grams per liter to result in from 0.05% to 2~ by weight magnesium in the chips calculated as MgSOI.7H2O and based upon the oven dried weight of the wood chlps;
~ e) impregnating the chips with a third peroxide and having a pH from 9 to 13; and, (f) mechanically defiberizing the chips to produce pulp.
A high yield alkaline peroxide pulping process for wood chips comprising:
(a) impregnating the wood chips with a first impregnation solution containing a chelating agent for metallic ions without containing significant quantities of magnesium ions;
(b) expressing said first impregnation solution containing metallic ions from within the chips;
(c) removing expressed impregnation solution from contact with the chips;
(d) impregnating the chips wit:h a second impregnating solution containin~ peroxide and a stabilizer for peroxide and having a pH from 9 to 13 and containing magnesium salts at a concentration of from 0.5% grams per liter to 20 gram3 per liter to result in from O . 05% to 2% by weight magnesium in the chips calculated as MgSO~.7H2O and based upon the oven dried weight of the wood chips; and (e) mechanically defiberizing the chips ~o produce pulp.
DETAILED DESCRIPTION OF THE INVENTION AND PREFERRED EMBODIMENTS
This invention is di~ected toward the removal of metallic ions such as manganese from lignocellulosic material in chip~ form prior to treatment with alkaline peroxide and to the utilization of high levels of magnesium (Mg) withln the chips while in contact with alkaline peroxide. The present invention is particularly useful 9a for pulp~ from wood species naturally high in metallic ions such as eastern black spruce, eastern balsam fir, lodgepole pine/white spruce mixtures and aspen.
The present process i~ charactarized by at least a two stage and preferably three or more stage impregnation process of chips prior to refining. In the first stage, wood chips, which preferably have been purged of entrapped air, are impregnated with a chelating agent such as die~hylenetriaminepantaacetic acid (DTPA), ethylene diaminetetraacetic acid (EDTA), hydroxyethyle~hylenediamine triacetic acid (HEEDTA), and nitrilo~riacetic acid (NTA), sodium tripolyphosphate (STPP), and phosphonic acid derivative or other similar compounds known in the 9b ~7~3~
art for such functionality or a combination of such chelating agents. The concentration of the chelating agent in the impregnati~g solution should be preferably from 0.1 gram/liter to 20 grams/liter (expressed as 100% chelating agent in the solution) to give preferably 0.01% to 2% chelant based on the dry weight of the chips with from 0.05% to 0.5% being particularly preferred.
The temperature of the first impregnation step is preferably between 15 C and 80C. The pH is preferrably between 4 and 12 with between 8 to 11 being particularly preferred. Adjustments to the solution pH can be made with any suitable acid or alkaline substance which does not react with pero~ide, cause darkening of the chips, or cause any of the components of the impregnation solu~ion to be precipitated or to lose chelating ability such as sulfuric acid or sodium hydroxide.
Before, or as part of the first impregnating step, the chips are preferably squeezed to expel liquid and any remaining air and then allowed to expand in contact with the impregnation solution.
The quantity of solution absorbed in an impregnation step is influenced by the impregnation device (primarily the degree of squeezing of the chips~ and the particular material being impregnated. The level of chemical addition into the chips is primarily controlled by the concentration of the particular chemical in the impregnating solution and the quantity of solution absorbed. The concentration of chelant and quantity of solution absorbed is preferably adjusted to give a chemical addition of 0.01% to 2% based cn the dry weight of lignocellulosic material being treated. The first impregnation solution is expressed either prior to or as the initial part of the second impregnation step.
Metallic ions are removed from the chips with the expressed first impregnation solution which removal is enhanced by the presence of the chelating agents. Preferably a-t least about 25% of the first impregnation solution is expressed from the chips with from about 33~ to about 50% being particularly preferred. The effectiveness of the first impregnation step to remove metallic ions is enhanced by providing some reten$ion time between impregnation and expressing the impregnation solution from the chips. This enhanced effectiveness is observed with a retention time of one half hour although ~everal hours is more effective. Since the first impregnation stage is primarily for the purpose of removing metallic ions from the chips, the first impregnation solution should consist esstentially of a chelating agent because it is expressed from the chips. The presence of substantial quantities of peroxide ( e.g. above 1%) or stabilizers in the first impregnation solution would be wasteful of such chemicals since they would be removed from the chips when the first impregnation solutions is expressed from the chips. Metallic stabilizers, particularly magnesium should be avoided in the first stage because they interfere with the primary purpose of the chelating agent.
The second impregnation step can be a conventional alkaline peroxide impregnation stage with stabilizers and chelating agents.
Preferably the second impregnation stage is with an aqueous solution of solub1e magnesium salts (e.g., epsom salt - MgSO4.7H2O~.
The epsom salt addition level i5 0.05% to 2% based on oven dried (o.d.) wood expressed as MgSO4.7H2O. This can be readily accomplished with an impregnation solution containing 0.5 grams per liter to 20 grams per liter. The purpose of this second step is to allow the soluble magnesium salts to penetrate the chip interstices. The temperature o~ the second impregnation step is preferably between 15 C and ~0 C, and the pH is maintained below 10 to keep the magnesium in a soluble form. Adjustment to the solution p~ is preferably made in the same manner as described for the first impregnation solution. Optionally, the second impregnation solution can contain alkalin~ peroxide with silicate stabilizers.
The third impregnation solution is an aqueous alkaline peroxide solution which contains peroxide stabilizers such as silicates. Preferably the third impregnation solution contains magnesium and silicate stabilizers. Silicates are preferably in a concentration range of 1 gram per liter to 5~ grams per liter to yield between 0.1% to 5% by weight of silicates (calculated as 2~7~31L
SiO2) based upon the dry weight of the chips. Magnesium based on weight of Mg in salt, is preferably in a concentration of from 0.01 grams per ~iter to 2 grams per liter to result after impregnation in from 0.001% to 0.2% by weight Mg based upon the dry weight of the chips. The third impregnation solution contains preferably hydrogen peroxide although any other peroxygen compound suitable for lignin brightening may be used. The peroxygen compound is preferably in the concentration range of between 5% and 100 grams per liter (calculated and expressed as hydrogen peroxide) to give additional lavels of preferably between 0.5~ and 10% of the dry weight of chips expressed as hydrogen peroxide. In addition, an alkaline substance (preferably sodium hydroxide) is added to the third impregnation solution to give a solution pH preferably in the range between 9 and 13 with between 10 and 12.5 being most preferred.
The most preferred impregnation sequence is the three stage sequence previously described and presented in greater detail in the axamples. However, it should be understood that the invention is not limited to the generally described three stage sequence.
A two-stage impregnation sequence in which the first impregnation stage is practiced as previously described and the second impregnation (Mg compounds) solution is combined with the third impregnation solution (alkaline peroxide and peroxide stabilizers such as silicates) and used as the impregnation solution in the second staye, preferably at a pH from 9 to 13 can also be employed.
It is importan~ that the entire chip become uniformly impregnated with any reactant solutions. Best results are achieved when a squeezing ratio (e~ual to mass of liquid squeezed from the chips per unit mass of dry chips) of unity or slightly higher is achieved. This requires a compression ratio of about 4:1, and results in the chips being squeezed from about 33% solid to about 50% solids. ~n other words, about 50% of the liquid present in the chips entering the compression device is squeezed out and replaced by "new" liquid in the impregna~ion expansion which follows.
2~7~3~L
The invention is not limited to the concentration and addition level ranges previously described for stabilizers and chelating agents, 3ince differences in metal contamination levels of lignocellulosic raw materials or process water could justify stabilizer or chelating agent usages outside of the specified preferred ranges.
Optionally, the chemically treated chips can be allowed to react with or without the application of heat, prior to entering the refining stage by retaining the impregnated chips for some finite time in any suitable vessel. A retention time of 5 minutes to 60 minutes is particularly suitable. Each impregnation is preferrably followed by a short drainage period and additional time for diffusion and/or reaction to occur within the chips. The amount of diffusion/reaction time required depends on the type of wood processed.
Refinin~ of Chemically Im~reqnated Chi~s (Def bration) The chemically treated chips are mechanically refined in a suitable defibration apparatus in one cr more stages in accordance with conventional processes and equipment. The steam pressure and corresponding temperature during refining are optional and can b~
at atmospheric and/or superatmospheric pressure, depending on the species being pulped and the desired pulp properties. Atmospheric pressure refining is preferred.
After refining, it is preferred that the pulp remain alkaline so that the silicate and other pH-sensitive materials can be removed prior to washing and neutralization. This prevents silicate deposition which can impair final pulp properties.
Post-Refininq_~teps:
After refining, the pulp may be allowed to continue bleaching as long as is practical prior to expelling the impregnation solutions. The amount of peroxide used in the impregnation steps is preferably preselected to result in some residual peroxide remaining after refining in order to maintain high brightness.
2~7~3~
Preferably the refined pulp is concentrated, e.g., by compressing or thickening, to remove residual impregnation solution containing potentiall~ recyclable alkaline peroxide, then diluted with water, washed and acidified preferably with sulfur dioxide, sodium bisulfite, sulfurous acid, or sulfuric acid, to a pH between 5.5 and 6Ø In particular, washing prior to acidification is preferred for removal of alkali soluble wood components and silicate. The residual peroxide extracted from the pulp after refining can be recycled as a source of peroxide in one of the impregnation solutions particularly if the process is practiced continuously or in sequential batches. The washed pulp is preferably screened and cleaned by conventional means to result in a pulp suitable for the production of paper products.
EXAMPLES
In the following examples wood chips from eas~ern black spruce, eastern balsam fir, lodgepole pine/white spruce 50/50 mixture (all softwoods) and/or aspen (hardwood), are treated by both the process of the present invention and that of Gentile, et al., U.S. Patent 4/849,058 and a comparison of the results tabulated. The proc~ss of U.S. Patent 4,849,058 was chosen for comparison because it represents the what is believed to be the best of the prior art processes for stabilizing alkaline peroxide in chips prior to high yield mechanical pulping. In the examples, all parts are by weight unless specified otherwise.
EXAMPLES A ( CONTROL ) AND
Screened eastern black spruce chips (2000 grams o.d. of wood at a solid content of 49%) were steamed for 15 minutes. The hot chips (solid content 40%) were placed into a Sprout-Bauer Ll-12 laboratory impregnator and compressed to a solids content of 60-70%. The impregnator was then closed, filled with 55 liters of impregnation liquor and the chips released (allowed to expand) into the liquorO The impregna~ed chips were removed from the 2~7~.31 impregnator and drained for 5 minutes to remove all excess liquor.
The same procedure was repeated for all three impregnation stages.
In Exampl~ A, the preferred three-stage impregnation process of U.S. Patent 4,849,058 was employed. In Example 1, the 3 impregnation steps were conducted according to the process of the present invention.
Table 1 lists the impregnation conditions, the amount ~nd type of chemicals added, and the test results comparing the process of the present invention (Example lj with the control (Example A).
The amounts of chemicals applied during impregnation were determined as follows:
Ca = (0.1) (PUR)(CL), where Ca = amount of chemical applied in % by weight of oven dried (o.d.) wood CL = concentration of chemicals in liquor in grams/liter PUR = amount of li~uor picked up during impregnation in liters divided by oven dried (o.d.) weight of wood in kilograms (kg) The magnesium salt used in these examples was Epsom salt (MgSO4-7H20)- The reported amounts of pentasodium salt of diethylenetriamine-pentaacetic-acid (DTPA) are based on a solution with 40.2% active ingredient. Trisodium salt of hydroxy-ethyl-ethylene-diamine-triacetate (HEEDTA) was a 41.3% solution. Also, the concentrations for silicate are calculated using a 37.6%
solution with a SiOz/Na20 ratio of 3.22.
After impregnation chips were refined in a Sprout-Bauer 12-lCP laboratory refiner under atmospheric pressure. After refining residual peroxide and caustic were determined by titration. The pulp was dewatered, washed and the pH adjusted to 6.0 with dilute H2S04. "Brightness" is defined as ISO brightness in percent units which is determined by using the sample preparation procedure given in the Technical Association of the Pulp and Paper Industry (TAPPI) Official Test Method T218 om-83. The brightness of the sample was measured using a Technibrite Micro TB-IC meter.
2 3 ~
Hydrogen peroxide usage or consumption (expressed as a weight percent of the dry weight of the chips) is based on the quantity of peroxide applied to the wood chips minus the quantity of residual peroxide in the pulp after refining. The percentage peroxide consumed is calculated as being equal to the quantity of peroxide consumed times 100 divided by the dry weight of the chips.
The quantity of peroxide in a solution was determined by iodometric titration using starch as an end point indicator (Vogel, Quantative Inorganic Analysis, Wiley & Sons, 1961, p. 363).
The magnesium and manganese concentration in the original wood chips and after impregnation was determined by atomic absorption spectroscopy.
As shown, the process of the present invention led to an increase in manganese removal and magnesium retention, which in turn gave a 2% brightness increase and a 47% reduction in peroxide consumption, thus demonstrating the increased peroxide s~ability under the process of the present invention.
2 3 3 7 ~ 3 .L
TABLE I
Process conditions, added chemical amounts, test results of 3-stage alkaline peroxide process of present invention vs control 3-stage process.
.
EXAMPLE NO. A (CONTROL) #1 TYPE WOOD: EASTERN EASTERN
1. 1st Impregnation a. process conditions pH 7.0 11.0 b. chemicals added CL CA CL CA
DTPA 1.35 0.22 2.5 0.39 HEEDTA 1.35 0.22 2.5 0.39 MgSO4.7H203.35 0.53 - -2. 2nd Impregnation a. process conditions pH 10.8 9.5 b. chemicals added DTPA 1.25 0.19 - -HEEDTA 1.25 0.19 Silicate 12.5 1.9 MgSO4.7HzO - - 3.35 0.53 3. 3rd Impregnation a. process conditions pH 11.6 11.2 b. chemicals added MgSO .7H O 4.5 0.54 3.35 0.48 Sili4 te 216.5 2.13 26.65 3.81 NaOH 31.7 4.09 27.20 3.89 HzO2 33'5 4.32 27.20 3.89 4. Total Chemicals Added DPTA 0.41 0.39 HEEDTA 0.41 0.39 MgSO .7H O 1.07 1.01 Silic~ate 2 4.03 3.81 NaOH 4.09 3.89 H~Oz 4.32 3.89 2 ~ 3 1 5. Te~t Results CA CA
ISO brightness (%) 74.1 76.1 H2o2 c0nsumed (%) 3.74 2.73 NaOH consumed (%) 3-35 3.18 PUR 3rd stage (1/kg) 1.29 1.43 Mn in chip3 3rd stage (ppm) 10.3 8.4 Mg in chips 3rd stage (ppm) 364 1050 Mn content original chipB (ppm) 37-5 37-5 Mg content original chip~ (ppm) 73-5 73-5 COMPARISON
Control: 74.1% brightnesa 3.74% H202 consumption 10.3 ppm Mn in 3rd atage chips 364 ppm Mg in 3rd stage chips Invention: 76.1% brightneqs 2.73% H22 con~umption 8.4 ppm Mn in 3rd stage chip~
1050 ppm Mg in 3rd stage chipa Improvement: 2.0 greater brightneas units 27% decrease in H2O2 conaumption 1.9 ppm lesa Mn in 3rd ~tage chips 686 ppm more Mg in 3rd ~tage chip~
~723~
EXAMPLES B (CONTROL) AND 2 Two kilograms of screened eastern Canadian balsam fir chips with a sol-ids content of 56.2~ were impregnated and refined as in control Example A. The pH of the first stage liquor was adjusted to 7~0 and the 2nd stage liquor pH was 10.7. This experiment is designated as comparative Example B.
A three impregnation step sequence of the present invention was made on an identical batch eastern Canadian balsam fir chips as used in Example B. The general impregnation and refining conditions were the same as for Example 1 above. Table 2 lists the process conditions, chemical types and amounts added, and the comparative test resul-ts for both examples. This experiment is designated as Example 2.
As with Examples A and 1, the greater manganese removal from the chips and greater magnesium addition to the chips prior to refining gave improved brightness (1.5 ISO brightness units) and reduced (27~) peroxide consumption compared to the control.
~9 20~7231 TABLE II
Process conditions, added chemical amounts, test results of 3-stage alkaline peroxide process of present invention vs. control 3-stage process.
-EXAMPLE NO. B (CONTROL) #2 ~ASTERN EASTEPN
TYPE WOOD: ~ALSAM FIR BALSAM FIR
1. 1st Impregnation a. proces3 condition3 pH 7.0 11.0 b. chemicals added CL CA CL CA
DTPA 1.70 0.24 3.35 0.49 HEEDTA 1.70 0.24 3.35 0.49 ~S04 .7H204.45 0.64 - _ 2. 2nd Impregnation a. proces3 conditions pH 10.7 9.5 b. chemicals added DTPA 1.90 0.27 - -HEEDTA 1.90 0.27 Silicate 18.85 2.71 MgSO4O7HzO - - 5.0 0.65 3. 3rd Impregnation a. proces~ conditions pH 11.3 11.0 b. chemicals added MgSO .7H O 6.5 0.63 5.55 0.61 Silic~ate 225.95 2.52 44.5 4.9 NaOH 50.0 4.9 41.20 4.5 HzOz 55.0 3.3 45.22 4.9 4. Tctal Chemical~ Added DPTA 0.51 0.49 HEEDTA 0.51 0.49 MgSO .7H O 1.27 1.26 Silicgate 2 5.23 4.90 NaOH 4-9 4-5 HzO2 5.3 4.9 2~7~3~
5. Test Results CA CA
ISO brightness (%) 74.2 75.7 Hzo consumed (~) 5.03 3.65 NaO~ consumed (~) 3.68 2~88 PU~ 3rd stage (1/kg) 0.97 1.1 Mn in chips 3rd stage (ppm) 31.5 29.1 Mg in chips 3rd stage (ppm) 430 722 Mn content original chips (ppm) 162.7 162.7 Mg content original chips (ppm) 110.1 110.1 C ARISo Control: 74.2~ brightnes~ WITH 5.03~ H22 congumption 31.53% ppm Mn in 3rd stage chip3 430 ppm Mg in 3rd stage chip~
Invention: 75.7% brightnes3 with 3.65% H202 con3umptiion 29.1% ppm Mn in 3rd 3tage chips 722 ppm Mg in 3rd 3tage chips Improvement. 1.5 greater brightness units 27~ leY~ H22 con~umption 2.43 ppm les~ Mn in 3rd stage chips 292 ppm more Mg in 3rd ~tage chips 2~2~
EXAMPLES C (CONTROL) AND 3 Screened aspen (populus tremuloides) chips at a solid content of 58.2% were impregnated and refined using the general procedures described in Example A. The pH of the first stage liquor was adjusted to 7.0 and the 2nd stage liquor had a pH of 10.7. This is designated Example C. An identical aspen chip charge was impregnated and refined by the general procedures of Example 1 above using the sequence of this invention. The specific additions used and results obtained are shown in Table III.
Although the original aspen chips had a low manganese content resulting in a low 3rd stage manganese level in the chips in both Examples C and 3, the third stage chips of Example 3 retained much more magnesium. As a result, brightness was improved by 1.2% while peroxide consumption was reduced by about 18% vs. the control.
2 ~ ~
TABLE III
The process conditions, added chemical amounts, test results of 3-stage alkaline peroxide process of present invention vs. control 3-stage process.
EXAMPLE NO. C (CONTROL) #3 1. 1st Impregnation a. process condition3 pH 7.0 11.1 b. chemicals added CL CA CL CA
DTPA 1.450.24 2.6 0.37 HEEDTA 1.450.24 2.65 0.37 MgSO4.7H20 3.6 0.59 2.65 2. 2nd Impregnation a. proces~ conditions pH 10.7 9.5 b. chemicals added DTPA 1.550.25 HEEDTA 1.550.25 Silicate 15.4 2.53 - -MgSO4.7H2O - 3 55 3. 3rd Impregnation a. process conditions pH 11.6 11.8 b. chemicals added MqSO .7H O 4.15 0.62 4.15 0.63 Silicate 2 16.65 2.50 33.3 5.02 NaOH 37.5 5.63 38.8 5.86 H2O2 23.4 4.41 29.2 4.41 4. Total Chemicals Added DPTA 0.49 0.37 MgSO .7H O 1.21 1.18 Silic4ate 2 5-03 5.02 NaOE~ 5.63 5.86 , H22 4.41 4.41 2,~7~:
5. Test Results CA CA
ISO brightne~s (%) 78.9 80.1 HzO~ consumed ~%) 3.54 2.92 NaOH consumed (%) 4.57 4.15 PUR 3rd stage (l/ky)~ 1.5 1.5 Mn in chips 3rd stage (ppm) 2.9 5.2 Mg in chips 3rd stage (ppm) 471 746 Mn content original chips (ppm) 9-3 9-3 Mg content original chips (ppm) 137 137 COMPARISON
Control: 78.9% brightness 3.54% H Oz consumption 441 ppm ~g in 3rd stage chips Invention: 80.1% brightness 2.92% H Oz consumption 746 ppm ~g in 3rd staga chips Improvement: Process: 1.2 greater brightness units 18~ less in H O2 consumption 293 ppm more ~g in 3rd atage chips * See def inition of PUR in Examples A and B .
2~
~7~3~
EXAMPLES D - N and 4-7 A lodgepole pine/white spruce (50/50%) chips mixture was subjected to both the 3-stage process of the present invention and that of the control process used in Example A. The same general impregnation and refining conditions were employed as in the previous examples along with comparable chemical applications while the specific conditions are given in Table IV. Table IV compares the brightness values, chemical compositions and Mn and Mg content for identical chip charges and both examples D, E, F, G (control) examples with 4, 5, 6 and 7, respectively (process of invention).
In all cases, brightness is higher and peroxide consumption lower for examples 4, 5, 6, and 7. Also, chips impregnated in example 4, 5, 6 and 7 always have a lower Mn content and a higher Mg content after the 3rd impregnation stage, thus leading to greater peroxide efficiency in pulp brightening.
Brightness gains attributable to the process of invention range from 1.8 to 6.2% ISO, while peroxide consumption is reduced by from 13 to 28% compared to the control.
25' 2 ~ 3 ~
TABLE IV
~omparati~e test results of 3-stage alkaline peroxide process of the present invention vs control 3-stage processO
.
EXAMPLE NO. D 4 E 5 F 6 G 7 ISO Brightness 74.2 76.0 67.771.766.472.6 72.0 74.8 PUR (l/kg) 0.850.910.70 0.75 0.83 0.95 1.03 1.3 H2O2 Consumed (%) 2.782.002.53 2.19 3.102.43 2.20 1.78 NaOH Consumed (%) 2.201.8~1.82 2.27 1.81 2.07 1.76 2.24 Mn Content in 3rd Stage (ppm) 12.78.6 20.8 12.124.8 7.1 12.14.7 Mg Content in 3rd Stage Ippm~ 377 885 515 697 462 795296 855 Mn Content in (ppm) 83.283.2 62.8 62.872.0 72.0 67.7 67.7 Mg Content in Original Wood (ppm) 112 112 103 103 122 122 104104 _ _ 2~231 Thus, as substantiated by the examples for both hardwoods and softwoods, the 3-stage preferred process of the present invitation increased ~rightness and decreased H202 consumption compared to the best prior art process for high yield peroxide pretreated pulp ~U.S. Patent 4,849,058) .
The concept and practice of the present invention leads to two major advantages over other alkaline peroxide chip treatment processes. These are:
1. More efficient removal of heavy metal ions [(particularly) manganese (Mn)], which catalyze peroxide decompositions;
2. Maintenance of a higher concentration of magnesium ions in the chips so they can protect the peroxide from decomposition prior to, during, and following the refining process.
The best mode presently contemplated for practicing the invention is with a three stage impregnation process as examplified in Example 1 with chemical selection, concentration of impregnation solutions and chemical quantities impregnated into the chips in the ranges demonstrated in Examples 1 throuyh 7.
The present invention, described in its hroadest concept is an improvement to peroxide treatments of wood chips prior to refining in which the concentration of metal ions within the cellular structure of the chips is reduced in a first impregnation step as shown in examples 1 through 7 and followed by alkaline peroxide impregnation with stabilizers for peroxide including magnesium ions and then mechanical pulping (refining).
Claims (7)
1. In a high yield pulping process comprising impregnating chips with an alkaline peroxide solution containing stabilizers for peroxide followed by mechanical defibration, wherein the improvement comprises:
pretreating the wood chips prior to peroxide impregnation, said pretreatment comprising;
(a) impregnating the chips with an impregnation solution consisting essentially of a chelating agent for metallic ions; and, (b) expressing from the chips chelating agents and metallic ions.
pretreating the wood chips prior to peroxide impregnation, said pretreatment comprising;
(a) impregnating the chips with an impregnation solution consisting essentially of a chelating agent for metallic ions; and, (b) expressing from the chips chelating agents and metallic ions.
2. The process of claim 1 wherein:
(a) the chelating agent in the pretreatment impregnation solution is selected from the group consisting of diethylenetriaminepentaacetic acid (DTPA), ethylene diaminetetraacetic acid (EDTA), hydroxyethylethylenediamine triacetic acid (HEEDTA), and nitrilotriacetic acid (NTA), sodium tripolyphosphate (STPP), and phosphonic acid derivatives; and is at a concentration of chelating agent of from 0.1 gram per liter to 20 grams per liter;
(b) the pretreatment impregnation results in from 0.01%
to 2% chelant in the chips based upon the dry weight of the chips;
and, (c) at least 25% of the pretreatment impregnation solution is expressed from the chips prior to impregnating the chips with alkaline peroxide.
(a) the chelating agent in the pretreatment impregnation solution is selected from the group consisting of diethylenetriaminepentaacetic acid (DTPA), ethylene diaminetetraacetic acid (EDTA), hydroxyethylethylenediamine triacetic acid (HEEDTA), and nitrilotriacetic acid (NTA), sodium tripolyphosphate (STPP), and phosphonic acid derivatives; and is at a concentration of chelating agent of from 0.1 gram per liter to 20 grams per liter;
(b) the pretreatment impregnation results in from 0.01%
to 2% chelant in the chips based upon the dry weight of the chips;
and, (c) at least 25% of the pretreatment impregnation solution is expressed from the chips prior to impregnating the chips with alkaline peroxide.
3. The process of claim 1 further comprising a retention time of at least 30 minutes after the impregnated chips of step (a) and prior to the expression of step b.
4. A high yield alkaline peroxide pulping process for wood chips comprising:
(a) impregnating the wood chips with a first impregnation solution consisting essentially of a chelating agent for metallic ions;
(b) expressing, at least 25% of said first impregnation solution containing metallic ions from within the chips;
(c) removing expressed impregnation solution from contact with the chips;
(d) impregnating the chips with a second impregnating solution containing magnesium salts at a concentration of from 0.5%
grams per liter to 20 grams per liter to result in from 0.05% to 2% by weight magnesium in the chips calculated as MgSO4.7H2O and based upon the oven dried weight of the wood chips;
(e) impregnating the chips with a third peroxide and having a pH from 9 to 13; and, (f) mechanically defiberizing the chips to produce pulp.
(a) impregnating the wood chips with a first impregnation solution consisting essentially of a chelating agent for metallic ions;
(b) expressing, at least 25% of said first impregnation solution containing metallic ions from within the chips;
(c) removing expressed impregnation solution from contact with the chips;
(d) impregnating the chips with a second impregnating solution containing magnesium salts at a concentration of from 0.5%
grams per liter to 20 grams per liter to result in from 0.05% to 2% by weight magnesium in the chips calculated as MgSO4.7H2O and based upon the oven dried weight of the wood chips;
(e) impregnating the chips with a third peroxide and having a pH from 9 to 13; and, (f) mechanically defiberizing the chips to produce pulp.
5. The process of claim 4 where steps (d) and (e) are combined into a single second impregnation step with a second impregnation solution containing peroxide and a stabilizer for peroxide and having a pH from 9 to 13 and magnesium salts at a concentration of from 0.5% grams per liter to 20 grams per liter to result in from 0.05% to 2% by weight magnesium in the chips calculated as MgSO4.7H2O and based upon the oven dried weight of the wood chips.
6. The process of claim 4 wherein:
(a) the chelating agent in the first impregnation solution is selected from the group consisting of diethylenetriaminepentaacetic acid (DTPA), ethylene diaminetetraacetic acid (EDTA), hydroxyethylethylenediamine triacetic acid (HEEDTA), and nitrilotriacetic acid (NTA), sodium tripolyphosphate (STPP), and phosphonic acid derivatives; and is at a concentration of chelating agent of from 0.1 gram per liter to 20 grams per liter;
(b) the first impregnation results in from 0.01% to 2%
chelant in the chips based upon the dry weight of the chips; and, (c) at least 25% of the first impregnation solution is expressed from the chips prior to impregnating the chips with alkaline peroxide.
(a) the chelating agent in the first impregnation solution is selected from the group consisting of diethylenetriaminepentaacetic acid (DTPA), ethylene diaminetetraacetic acid (EDTA), hydroxyethylethylenediamine triacetic acid (HEEDTA), and nitrilotriacetic acid (NTA), sodium tripolyphosphate (STPP), and phosphonic acid derivatives; and is at a concentration of chelating agent of from 0.1 gram per liter to 20 grams per liter;
(b) the first impregnation results in from 0.01% to 2%
chelant in the chips based upon the dry weight of the chips; and, (c) at least 25% of the first impregnation solution is expressed from the chips prior to impregnating the chips with alkaline peroxide.
7. A high yield alkaline peroxide pulping process for wood chips comprising:
(a) impregnating the wood chips with a first impregnation solution containing a chelating agent for metallic ions without containing significant quantities of magnssium ions;
(b) expressing said first impregnation solution containing metallic ions from within the chips;
(c) removing expressed impregnation solution from contact with the chips;
(d) impregnating the chips with a second impregnating solution containing peroxide and a stabilizer for peroxide and having a pH from 9 to 13 and containing magnesium salts at a concentration of from 0.5% grams per liter to 20 grams pex liter to result in from 0.05% to 2% by weight magnesium in the chips calculated as MgSO4.7H2O and based upon the oven dried weight of the wood chips; and (e) mechanically defiberizing the chips to produce pulp.
(a) impregnating the wood chips with a first impregnation solution containing a chelating agent for metallic ions without containing significant quantities of magnssium ions;
(b) expressing said first impregnation solution containing metallic ions from within the chips;
(c) removing expressed impregnation solution from contact with the chips;
(d) impregnating the chips with a second impregnating solution containing peroxide and a stabilizer for peroxide and having a pH from 9 to 13 and containing magnesium salts at a concentration of from 0.5% grams per liter to 20 grams pex liter to result in from 0.05% to 2% by weight magnesium in the chips calculated as MgSO4.7H2O and based upon the oven dried weight of the wood chips; and (e) mechanically defiberizing the chips to produce pulp.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US63824491A | 1991-01-07 | 1991-01-07 | |
| US07/638,244 | 1991-01-07 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2057231A1 true CA2057231A1 (en) | 1992-07-08 |
Family
ID=24559219
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA 2057231 Abandoned CA2057231A1 (en) | 1991-01-07 | 1991-12-06 | Method of pretreating lignocellulosic materials prior to alkaline peroxide high yield pulping |
Country Status (9)
| Country | Link |
|---|---|
| EP (1) | EP0494519A1 (en) |
| AU (1) | AU660435B2 (en) |
| BR (1) | BR9105643A (en) |
| CA (1) | CA2057231A1 (en) |
| FI (1) | FI920048A (en) |
| MX (1) | MX9102773A (en) |
| NO (1) | NO920082L (en) |
| NZ (1) | NZ240910A (en) |
| PT (1) | PT99980A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7001484B2 (en) | 2000-05-04 | 2006-02-21 | University Of New Brunswick | Peroxide bleaching of wood pulp using stabilizers and sodium hydrosulfide reducing agent |
Families Citing this family (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SE520874E (en) | 2001-11-30 | 2013-01-15 | Stfi Packforsk Ab | Removal of inorganic elements from wood chips before cooking to pulp |
| US7384502B2 (en) * | 2002-12-24 | 2008-06-10 | Nippon Paper Industries Co., Ltd. | Process for impregnating, refining, and bleaching wood chips having low bleachability to prepare mechanical pulps having high brightness |
| US8268122B2 (en) | 2005-12-02 | 2012-09-18 | Akzo Nobel N.V. | Process of producing high-yield pulp |
| DE102007022754A1 (en) * | 2007-05-11 | 2008-11-13 | Voith Patent Gmbh | Method for reducing the heavy metal content of lignocellulosic raw material |
| EP2438235A1 (en) * | 2009-06-02 | 2012-04-11 | Akzo Nobel Chemicals International B.V. | Process for producing mechanical pulp |
| CN101748634B (en) * | 2009-12-16 | 2011-09-14 | 陕西科技大学 | Improved APMP pulping method |
| EP2348154A1 (en) * | 2010-01-22 | 2011-07-27 | Andritz AG | Method for manufacturing wooden material |
| CN102242512A (en) * | 2011-04-30 | 2011-11-16 | 李刚荣 | Environmentally-friendly paper making and pulping technique and system with high yield |
| US20130126109A1 (en) * | 2011-11-17 | 2013-05-23 | Buckman Laboratories International, Inc. | Silicate Free Refiner Bleaching |
| CN103757955B (en) * | 2014-01-06 | 2016-08-24 | 南京林业大学 | A kind of APMP technique of improving improves the new method of pulp strength |
| EP2949812A1 (en) * | 2014-05-27 | 2015-12-02 | Jokiel & Ullmann Consulting GbR | Mixture for preparing an impregnation liquor for the impregnation of papers and nonwoven hybrid fabrics |
| SE542430C2 (en) * | 2017-09-19 | 2020-04-28 | Domsjoe Fabriker Ab | Removal of inorganic elements from wood chips |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3251731A (en) * | 1963-02-11 | 1966-05-17 | Andrew J Gard | Bleaching of wood pulp with a sequestering agent and hydrogen peroxide |
| SE454186C (en) * | 1985-03-13 | 1989-09-25 | Eka Nobel Ab | SET FOR PREPARATION OF CHEMICAL MECHANICAL |
| AU605745B2 (en) * | 1985-09-20 | 1991-01-24 | Kimberly-Clark Worldwide, Inc. | Method of preparing pulp with stabilizers and peroxide prior to mechanical refining |
| US4849053A (en) * | 1985-09-20 | 1989-07-18 | Scott Paper Company | Method for producing pulp using pre-treatment with stabilizers and defibration |
| US4960399A (en) * | 1988-07-14 | 1990-10-02 | Lyon Richard A | Diver's utility console |
-
1991
- 1991-12-06 CA CA 2057231 patent/CA2057231A1/en not_active Abandoned
- 1991-12-09 NZ NZ24091091A patent/NZ240910A/en unknown
- 1991-12-11 AU AU89609/91A patent/AU660435B2/en not_active Expired - Fee Related
- 1991-12-13 EP EP91311614A patent/EP0494519A1/en not_active Withdrawn
- 1991-12-23 MX MX9102773A patent/MX9102773A/en unknown
- 1991-12-30 BR BR919105643A patent/BR9105643A/en unknown
-
1992
- 1992-01-03 FI FI920048A patent/FI920048A/en not_active Application Discontinuation
- 1992-01-06 PT PT9998092A patent/PT99980A/en not_active Application Discontinuation
- 1992-01-06 NO NO92920082A patent/NO920082L/en unknown
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7001484B2 (en) | 2000-05-04 | 2006-02-21 | University Of New Brunswick | Peroxide bleaching of wood pulp using stabilizers and sodium hydrosulfide reducing agent |
Also Published As
| Publication number | Publication date |
|---|---|
| NZ240910A (en) | 1992-10-28 |
| BR9105643A (en) | 1992-09-29 |
| AU8960991A (en) | 1992-07-09 |
| FI920048A (en) | 1992-07-08 |
| FI920048A0 (en) | 1992-01-03 |
| EP0494519A1 (en) | 1992-07-15 |
| MX9102773A (en) | 1992-07-01 |
| PT99980A (en) | 1993-01-29 |
| AU660435B2 (en) | 1995-06-29 |
| NO920082D0 (en) | 1992-01-06 |
| NO920082L (en) | 1992-07-08 |
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