Method of pretreating pulp with yield or strength-enhancing additive

Abstract

Chemical pulp is produced from a slurry of comminuted cellulosic fibrous material using a beneficial additive such as AQ, or polysulfide. In the first treatment zone the effective alkali concentration and temperature conditions are such so that substantially no alkali degradation of the cellulose occurs, but so that the material is effectively impregnated with the additive. Then the material is treated with an alkaline cooking liquor, at cooking temperature, to produce a chemical cellulose pulp with higher yield or strength than if the low temperature, low alkali, additive pretreatment was not practiced. Typical alkali and temperature conditions in the first zone are less than 10 g/l expressed as NaOH, and between about 80-130° C., e.g. about 80-110° C. The first zone is preferably a feed system (which may include a separate impregnation vessel) for a continuous digester, while cooking is in a continuous digester.

Description

BACKGROUND AND SUMMARY OF THE INVENTION

Co-pending patent application 09/248,009 now U.S. Pat. No. 6,241,851 filed on Feb. 10, 1999 (the complete disclosure of which is included by reference herein), discloses a method of treating comminuted cellulosic fibrous material with a beneficial additive prior to chemical digestion. This additive is preferably a strength- or yield-enhancing additive, such as athraquinone [AQ] or polysulfide [PS] and their derivatives or equivalents. The present invention comprises a further method and apparatus for effecting the pretreatment of comminuted cellulosic fibrous material, typically wood chips (though the invention is equally applicable to the treatment of other forms of cellulose), to improve the properties [e.g. strength] of the resulting pulp or to improve the effectiveness [e.g. yield] of the pulping process.

It has been discovered that the pretreatment of comminuted cellulosic fibrous material, for example, wood chips, can be more effective if, among other things, the heating and cooking of the chips after pretreatment is essentially isolated from the pretreatment process. That is, a more effective pretreatment can be obtained if the pretreatment process is performed at a cooler temperature, with or, preferably substantially without, the presence of alkali, and the heating of the chips to cooking temperature is performed after the pretreatment (impregnation of the cellulose material) is essentially completed. In one aspect of this invention the additive is added earlier in the treatment process, and the content of cooking chemical, for example, kraft white liquor, is reduced or diverted from this earlier stage of pretreatment and introduced during later stages of pretreatment or in the formal cooking treatment. Thus, according to the present invention, possibly longer, cooler, less alkaline pretreatment is provided so that the cooking additive more effectively treats the chips prior to heating to cooking temperature, that is, to a temperature greater than 140° C.

According to one aspect of the present invention there is provided a method of continuously producing chemical cellulose pulp from a comminuted cellulosic fibrous material slurry, comprising substantially continuously: (a) Impregnating the material with a solution containing yield or strength-enhancing additive at effective alkali and temperature conditions so that substantially no alkali degradation of the cellulose occurs, and so that little or substantially no acid hydrolysis occurs. And, (b) after (a), treating the material with an alkaline cooking liquor, at cooking temperature, to produce a chemical cellulose pulp with higher yield or strength than if (a) were not practiced.

In the method (a) may be practiced so that there also is substantially no dissolution of lignin from the material. At the end of (a), the material has been impregnated with the yield or strength enhancing additive (such as AQ or its derivatives or equivalents) so that the problems associated with conventional higher temperature additive impregnation are avoided. For example specifically with respect to AQ, it is a large molecule and needs a longer time to diffuse into the wood chips, or like cellulose material, than does, for example, alkali, and it needs to be reduced in order to dissolve so that it can diffuse. Therefore sometimes AQ is used in its reduced form (commonly referred to as SAQ). However also typically about 80% of the AQ reacts with dissolved lignin and thus is not capable of performing its intended yield and strength enhancing function, leaving only about 20% of the AQ for performing the desired functions. By utilizing the invention a much higher percentage of the AQ (up to substantially all) that is added actually impregnates the wood chips and performs its yield or strength enhancing function, and the AQ may or may not be added in reduced form. When the AQ successfully impregnates the chips it keeps the hemicellulose from being dissolved during cooking, and thus increases yield, and utilizes other mechanisms to enhance strength. Other materials may also be utilized to facilitate penetration of the chips with the additive, such as the use of a surfactant.

In the method as described above (a) may be practiced at an alkali concentration between 0-less than 10 g/l expressed as NaOH, and at a temperature of between about 80-130° C., typically less than about 120° C., and preferably about 110° C. or less. The amount of alkali is most desirably substantially zero, but preferably at most less than about 5 g/l expressed as NaOH.

In the method (a) may be practiced in a feed system of a continuous digester and (b) in a continuous digester. Exactly where in the feed system (a) is practiced may be widely variable. For example a chip bin could be located in a wood yard, and the additive could be sprayed or otherwise applied to the wood chips even prior to entry into the chip bin, or while they were entering the chip bin, or while they were in the chip bin. Then the wood chips could be pumped from the wood yard to the digester using primarily or substantially exclusively water as the slurrying medium (with no intentional significant alkali addition) so that the chips would be at desirable low temperature, low alkali, impregnation-facilitating conditions for a significant period of time. In a typical situation impregnation in (a) will take at least about 20 seconds, e.g. between about 2-60 minutes at superatmospheric pressure (which superatmospheric pressure may be provided in any conventional manner including by a level of liquid above the chips, pumping, and/or in a pressure vessel). Alternatively the additive may be introduced after the chip bin and before a pump and/or high pressure feeder, in a separate treatment vessel such as an impregnation vessel, or any other location in the feed system that proves advantageous for any reason.

The invention may also comprise substantially immediately after impregnation in (a) adding between about 35-100% of the alkali used to treat the material, including in (b), to the material. Alternatively the alkali can be added far downstream. Also the method may further comprise (c), between (a) and (b), treating the material in a second zone with a solution containing additive at an effective alkali concentration of about 5-less than 15 g/l expressed as NaOH and greater than in (a), and at a temperature of between about 110-130° C. and higher than in (a)

In the method (a) may be practiced using as the additive at least one of AQ or its derivatives or equivalents, polysulfide or its derivatives or equivalents, or sulfite in the form of sulfur dioxide, NaHSO 3 , or Na 2 SO 3 . A suitable amount of additive may be used; for example if AQ or its derivatives or equivalents are used, typically (a) is practiced with a total additive concentration of between about 0.02-0.5% on wood, typically between about 0.02-0.1% on wood.

Additive may also be added during the digesting process, as is conventional.

According to another aspect of the present invention there may be provided a method of treating comminuted cellulosic fibrous material comprising substantially continuously: (a) Treating a slurry of comminuted cellulosic fibrous material with a first liquid comprising primarily or substantially exclusively water containing a beneficial additive at a maximum effective alkali concentration of less than 10 g/l, and at a first temperature of about 80-130 degrees C., for at least about 20 seconds, e.g. between about 2-60 minutes under superatmospheric pressure. And, (b) after (a), treating the material in the slurry with a second liquid having an initial effective alkali concentration greater than 10 g/l (preferably greater than 15 g/l and most desirably greater than 20 g/l) expressed as NaOH, and at a second temperature greater than 130° C. (e.g. greater than 140° C.), to produce a chemical cellulose pulp.

The method as described above may further comprise (c), between (a) and (b), treating the slurry with a third liquid containing the beneficial additive at a maximum effective alkali concentration greater than the first liquid and less than the second liquid, and at a third temperature, higher than the first temperature and less than 140 degrees C.

Another embodiment of the present invention may be a method of treating comminuted cellulosic fibrous material consisting of or comprising: (a) treating (e.g. pretreating) a slurry of comminuted cellulosic fibrous material with a liquid containing a beneficial additive at a first alkali content (e.g. from 0-less than 10 g/l) at a first temperature; (b) after (a), treating the slurry with a second liquid containing a beneficial additive at a second effective alkali content [greater than zero, and preferably at least 10% greater than the first effective alkali content] at a second temperature higher than the first temperature; and (c) after (b), treating [possibly, although not necessarily, after displacement of substantially all of the additive therefrom] the slurry with a third liquid having an effective alkali content (i.e. concentration) greater than the first and second effective alkali contents and a temperature greater than the first and second temperatures and greater than 130° C. (e.g. greater than 140° C.) to produce a chemical cellulose pulp.

As described above, the beneficial additive used in steps (a) and (b) may be AQ (most desirably SAQ), polysulfide, sulfur, surfactants, and combinations thereof. The first alkali content, expressed as “effective alkali” (EA) as NaOH, is preferably less than 10 g/l, and may be less than about 5 g/l, or the first liquid may contain no alkali at all. For example, the first liquid may be mill water, steam condensate, or washer filtrate containing little or no alkali content. The first temperature of treatment (a) is preferably a relatively cool temperature, that is, a temperature less than 130° C., preferably less than about 120° C., for example, the first temperature may range from about 90 to 110° C., or be even lower.

Procedure (a) may be performed using the methods and apparatuses described in U.S. Pat. Nos. 5,476,572; 5,622,598; and 5,632,025, that is the system marketed under the trademark LO-LEVEL® feed system by Andritz-Ahlstrom Inc. of Glens Falls, N.Y. The LO-LEVEL® feed system, that is a system employing a chip pump and not using a horizontal “steaming vessel”, is particularly suited for treatment according to the present invention since this system allows for the feeding and treatment of chips at lower temperatures than can be handled by conventional feed systems. Other conventional equipment and processes may also be used to perform the present invention, for example, those not including a chip pump and including a horizontal steaming vessel.

The second liquid of step (b) preferably contains at least some alkali, for example, the second liquid contains less than 15 g/l EA, typically about 5 to 10 g/l EA. This alkali content may be supplied by kraft white, green, or black liquor, or from combinations of white, green, or black liquor and water or washer filtrate. The second temperature is also preferably less than 140° C., for example, less than about 120° C., and is typically between about 110 and 130° C. The procedure (b) is typically performed in the upper part of continuous digester, for example, a Kamyr® continuous digester as also sold by Andritz-Ahistrom Inc. of Glens Falls, N.Y.

Procedure (c), the formal pulping process, may be any form of chemical pulping process, but is preferably one or more of the processes described in U.S. Pat. Nos. 5,489,363; 5,536,366; 5,547,012; 5,575,890; 5,620,562; 5,662,775 and others. The processes and apparatuses described in these patents are marketed under the name LO-SOLIDS® Pulping by Andritz-Ahlstrom.

According to another aspect of the present invention there is provided a method of continuously producing chemical cellulose pulp from a comminuted cellulosic fibrous material slurry, comprising continuously: (a) In a first treatment zone treating the material with a solution containing yield or strength-enhancing additive at effective alkali and temperature conditions so that substantially no alkali degradation of the cellulose occurs (and so that the material and additive flow in contact with each other for a period of time). (b) After (a), treating the material in a second zone with a solution containing additive at an effective alkali concentration of about 5-less than 15 g/l expressed as NaOH, and at a temperature of between about 110-130° C. and higher than in (a). And (c) after (b) (and possibly, but not necessarily desirably, after removing substantially all of the additive from contact with the material), treating the material with an alkaline cooking liquor, at cooking temperature, to produce a chemical cellulose pulp with higher (e.g. at least 2% higher) yield or strength than if (a) and (b) were not practiced.

In the method preferably (a) is practiced in a feed system of a continuous digester, (b) is practiced in a top zone of the continuous digester, and (c) is practiced in the continuous digester below the top zone. Also, preferably (a) is practiced at an alkali concentration between 0-less than 10 g/l expressed as NaOH, and less than in (b), and at a temperature of between about 80-110° C. At least 50% of the additive may be introduced in (a), or about 40% may be introduced in (a) and 60% of the additive introduced elsewhere, for primary use in (b). In an embodiment wherein the additive is AQ or its derivative or equivalents, and wherein (a) and (b) are practiced with a total additive concentration of between about 0.05-0.15% on pulp.

The apparatus used in practice of the present invention is primarily conventional apparatus, except, for some aspects, for the additive additions to the feed system, and to the top zone of a continuous digester, and the potential recirculation of additive withdrawn from the top zone (including a screen at a transition between the top zone and the cooking zone of the continuous digester) and introduction to the feed system.

According to another aspect of the present invention there is provided a cellulose slurry treatment system comprising: An upright continuous digester having an inlet adjacent the top and an outlet adjacent the bottom thereof. A feed system for the digester including a slurry pump. A yield or strength-enhancing additive conduit for introducing yield or strength-enhancing additive into the slurry before the slurry pump. A top treatment zone of the digester, and a screen assembly adjacent the bottom of the top treatment zone, and a cooking zone below the screen assembly. The screen assembly providing a temperature transition within the digester. Means for introducing or re-circulating liquids into the digester so as to establish upward flow of liquid in the digester above the screen. And means for introducing yield or strength-enhancing additive into the top zone and/or feed system of the digester.

In the system, the means for introducing additive into the feed system may comprise conventional conduits, nozzles, venturis, or other conventional structures capable of introducing a liquid into a flowing liquid or slurry. The means for introducing liquid into the digester to ensure upward flow immediately adjacent the screen assembly (which preferably comprises the second screen in the digester going from the top to the bottom) comprises any conventional structure that will accomplish that purpose, including re-circulation conduits with central pipes connected to pumps, etc. The invention also preferably comprises means for re-circulating additive withdrawn from the top zone of the digester to the additive introduction means associated with the feed system. Such re-circulation means may comprise conventional conduits, and/or pumps, valves, or like fluid structures for that purpose, and may also include separation equipment for separating the additive from some of the liquid with which it is re-circulated. The preferred additives are those described in co-pending application Ser. No. 09/248,009.

It is the primary object of the present invention to provide for the effective treatment of comminuted cellulosic fibrous material so as to increase the strength, yield, and/or other advantageous properties of the pulp or the treatment process. This and other objects of the invention will become clear from an inspection of the detailed description of the invention and from the appended claims.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a schematic representation of exemplary apparatus for practicing the method according to the present invention, and comprising an exemplary system according to the present invention.

DETAILED DESCRIPTION OF THE DRAWINGS

FIG. 1 illustrates one preferred embodiment of the present invention. FIG. 1 illustrates a comminuted cellulosic fibrous material treatment system 10 consisting essentially of or comprising a continuous digester 11 and a continuous digester feed system 12 . Feed system 12 may be a LO-LEVEL® feed system as sold by Andritz-Ahlstrom, but any conventional feed system for introducing, steaming, and slurrying comminuted cellulosic fibrous material may be used; and/or one or more separate impregnation vessels may be used; and/or unconventional systems, such as those including equipment and/or a chip bin in the wood yard with pumping to the digester. Also in some circumstances a plurality of impregnation ponds may be used, with slurry pumped from a particular pond once impregnation with additive is complete (or will complete during pumping).

Comminuted cellulosic fibrous material, for example, in the form of softwood chips 13 , are introduced to an isolation device 14 which forwards the chips to steam treatment in a vessel 14 , which is preferably a vessel as described in U.S. Pat. Nos. 5,500,083; 5,617,975; 5,628,873; 4,958,741; and 5,700,355, and marketed by Andritz-Ahlstrom under the trademark DIAMONDBACK®, though other types of steaming vessels may be used. From vessel 14 the chips pass through a metering device 15 to a conduit 16 , which is preferably a Chip tube provided by Andritz-Ahlstrom. Slurry liquid is introduced to the chips in conduit 16 by way of a conduit 17 so that a level of liquid is maintained in conduit 16 . The slurry of chips and liquid is fed to the inlet of chip pump 18 which pressurizes and feeds the slurry to the inlet of high-pressure transfer device 20 via a conduit 19 .

The device 20 is typically a High-pressure Feeder as sold by Andritz-Ahistrom. The device 20 further pressurizes the slurry to a pressure of between about 5 and 15 bar and propels the slurry via conduit 21 to the top of the continuous digester 11 . Excess liquor contained in the slurry is removed from the slurry at the inlet of the digester 11 by a separating device 22 , typically a conventional Top Separator, and the excess liquid is removed and returned to feed system 12 via conduit 23 and pump 24 . The pressurized slurry provided by pump 24 and conduit 25 provides the motive force for propelling the slurry from feeder 20 to digester 11 .

Feed system 12 also typically includes conventional devices such as In-line drainer 26 , Level Tank 27 , and Make-up Liquor Pump 28 . Cooking liquor, for example, kraft white liquor (WL) is typically provided to the Level Tank 27 as is conventional.

Digester 11 typically includes a plurality of annular screen assemblies 31 , 32 , 33 , 34 and 35 . Though five such screen assemblies are schematically illustrated in FIG. 1 , the present invention may be effected in a digester with any number of screens, from two to five, or even more. Each screen assembly 31 - 35 typically includes an extraction with a recirculation conduit, 36 through 40 ; a pump, 41 through 45 ; and a heat exchanger, 46 through 50 . Essentially fully-treated pulp is discharged via conduit 51 from the bottom of the digester 11 .

According to the present invention, cooking additive 60 , for example AQ, polysulfide, etc. is introduced to the feed system 12 via one or more conduits 61 , 62 , or 63 . Alkali containing liquor for example, kraft white, green, or black liquor or washer filtrate is introduced to feed system 12 via conduit 64 , or significant alkali introduction (i.e. 10 g/l or more, or 5 g/l or more) can be delayed until later (i.e. no significant alkali addition in the feed system at all, except perhaps to lubricate the feeder 20 or like equipment). Typically the sources of alkali provides an effective alkali concentration [AG] of less than 10 g/l as NaOH, preferably less than about 5 g/l as NaOH. In one embodiment of this invention, the liquid introduced to conduit 64 contains little or no alkali, for example, the liquid introduced may be water, condensate, hot black liquor, or weak black liquor.

According to the present invention, the temperature in feed system 12 is preferably kept below 130° C., that is, preferably between about 80 and 130° C., and most desirably less than about 120° C., or even less than about 110° C., and the alkali content is low enough so that little or no alkali degradation of the cellulose occurs, and substantially no dissolution of lignin, during the treatment with the additive, such as AQ. Penetrants, such as surfactants, may also be introduced with the additive to enhance the treatment of the additive or the penetration or the alkali into the chips. Though the LO-LEVEL® Feed system is suited to low temperature treatment of this kind, this treatment may also be effected in a conventional feed system by reducing the temperature in the feed system, for example, reducing the pressure in the horizontal steaming vessel and/or using a cooling heat exchanger to cool the liquor in and around the feed system to prevent liquor flash evaporation, or other equipment may be utilized.

Desirably after this pretreatment at low temperature and little or no alkali, the material is cooked with conventional alkali cooking liquor (e.g. the kraft, sulfite, or other alkali processes), to produce chemical pulp. Treatment with a cook level of alkali (e.g. initially over 30 g/l expressed as NaOH) may be substantially immediately after the additive-impregnation, or those may be intermediate steps or treatments. One such intermediate treatment is seen in FIG. 1 .

In FIG. 1 , after pretreatment in the feed system 12 , the pretreated slurry is transferred via conduit 21 to the digester 11 for further pretreatment (at the top of digester 11 , e.g. in zone 29 ) and for formal cooking (in the middle of the digester 11 , below the vicinity of screen 32 ). After passing through separator 22 the chip slurry preferably still at a temperature less than about 120° C. passes downwardly as schematically shown by arrows 65 , until screen 31 is reached. At screen 31 some of the liquid in the slurry is removed from the slurry. Some of the removed slurry may be removed via conduit 66 , and used or treated elsewhere, and/or some of the liquid may be removed and circulated via conduit 36 back to the vicinity of screen 31 . The re-circulated liquor is pumped by pump 41 and may or may not be heated or cooled by heat exchanger 46 . The liquid in conduit 66 typically contains at least some additive. This additive may be returned to feed system 12 , for example, by introducing it to conduit 67 . The liquid in conduit 66 may be cooled by the heat exchanger 68 . Cooking chemical, additive, dilution liquid, or a combination thereof may be added to circulation 36 via conduit 69 .

The slurry of material passes screen 31 and then encounters screen 32 . According to the present invention, removal of liquid from screen 31 preferably causes a countercurrent flow of liquid relative to the flow of chips between screens 31 and 32 schematically shown by arrows 70 . At screen 32 , additional liquid is removed and re-circulated via pump 42 , conduit 37 and heat exchanger 47 , with or without heating. Again, additive, dilution, cooking liquor, and/or combinations thereof, may be introduced to circulation 37 via conduit 71 . Heat may be introduced to circulation 47 so that the slurry temperature increases to a temperature greater than 120° C. while passing screen 32 . In one mode of operation, the flow of liquid above screen 32 is upward and the flow of liquid below screen 32 is downward so that a temperature separation is established in the vicinity of screen 32 .

In the zone 29 , the slurry includes additive (e.g. AQ), and if there is a proper alkali addition is at a second alkali concentration (e.g. about 5-less than 15 g/l and greater than the first alkali concentration in the feed system 12 ), and at a second temperature (e.g. about 110-130° C.) which is greater than in the first temperature in the feed system 12 . In the zone 29 a small amount of alkali degradation may take place, but effective treatment with additive also takes place.

After passing the screen 32 , the slurry is typically heated to formal cooking temperature, that is, to a temperature greater than 140° C., and the formal cooking process commences. Some of the additive may pass into the cooking process, but alternatively the additive may be partially or substantially completely (e.g. more than 90%) removed prior to the cooking process commencing, e.g. being displaced in conduit 80 .

According to the present invention, pretreatment additive is introduced to feed system 12 , and the chips are treated with additive prior to introducing the chip slurry to digester 11 . This treatment is preferably performed at a temperature less than 120° C. In the case of AQ, the additive concentration is typically less than 0.20% on pulp and is typically between about 0.02 and 0.5% on pulp. About 50% of the AQ may be introduced via conduit 61 and about 25% introduced to conduits 69 and 71 . Also, all the AQ, that is substantially 100%, may be introduced to feed system 12 (or otherwise before significant alkali addition), and little or no AQ introduced to digester 11 . In another embodiment about 40% of the AQ is introduced to feed system 12 and about 60% is introduced to the digester 11 .

Less than 50% of the total alkali introduced to system 10 may be introduced to feed system 12 . This may be less than about 40% or even about 30%. In one embodiment, no alkali is introduced to the feed system 12 , that is, during treatment in the feed system 12 , the chips may essentially only be exposed to the additive and primarily water (whether fresh, in the form of filtrate, etc.).

The treatment time in the feed system 12 , the top zone 29 of the digester 11 , and in the cooking zone (below 32 ) in the digester 11 , may be varied depending upon the particular material being treated, and other factors. With typical softwood, the treatment time with additive in the feed system 12 (that is under conditions so that substantially no alkali degradation of the cellulose occurs) is about 2-60 minutes, whereas—if used—treatment in the zone 29 (at alkali and temperature conditions slightly higher than in the feed system 12 ) has a treatment time of about 20-60 minutes, and the cook time is conventional, e.g. about 1-3 hours.

Associated with each of the screens assemblies 33 - 35 there also may be extraction conduits 81 - 83 , which can be sent to flash tanks and chemical recovery, or simply for extracting liquid having relatively high levels of dissolved organic material during LO-SOLIDS®) cooking processes. Instead of a single vessel system, multiple vessel systems (including an impregnation vessel) may be used with significant alkali addition (except to keep equipment free running) only at the end of, or after, the impregnation vessel.

In the above disclosure all specific ranges within each broad range are also specifically disclosed herein. For example, and example only, an EA of less than 10 g/l means 0-1 g/l, 0.2-5 g/l, 3-8 g/l, and all other narrower ranges within the broad range.

While the invention has been shown and described in what is conceived to be the most practical and preferred embodiment thereof it will be apparent to those of ordinary skill in the art that many modifications may be made thereof within the scope of the invention, which scope is to be accorded the broadest interpretation of the appended claims so as to encompass all equivalent processes and systems.

Claims

1. A method of continuously producing chemical cellulose pulp from a comminuted cellulosic fibrous material slurry, comprising substantially continuously:(a) impregnating the material with an anthraquinone (AQ) solution comprising an AQ additive in the substantial absence of alkali to achieve an effective alkali condition of substantially zero, and at a temperature condition so that substantially no alkali degradation of the cellulose occurs, and so that little or substantially no acid hydrolysis occurs; and (b) after (a), treating the material with an alkaline cooking liquor, at cooking temperature, to produce a chemical cellulose pulp with higher yield or strength than if (a) were not practiced.

2. A method as recited in claim 1 wherein (a) is practiced in a feed system of a continuous digester, and (b) is practiced in the continuous digester.

3. A method as recited in claim 1 wherein (a) is practiced at a temperature of between about 80-30° C.

4. A method as recited in claim 3 wherein (a) is practiced for a time of between about 20 seconds-60 minutes under superatmospheric conditions.

5. A method as recited in claim 1 wherein at least 50% of the additive used is introduced in (a), and wherein the additive is SAQ.

6. A method as recited in claim 1, wherein (a) is practiced with a total AQ additive addition in aqueous solution of between about 0.02-0.5% on wood.

7. A method as recited in claim 1 wherein (a) is practiced at a temperature of less than about 120° C.

8. A method as recited in claim 1 wherein (a) is practiced to enhance yield at least one percent.

9. A method as recited in claim 1 wherein (a) is practiced at a temperature of less than about 110° C.

10. A method as recited in claim 1 wherein (a) is practiced so that there is substantially no dissolution of lignin from the material.

11. A method as recited in claim 1 further comprising: substantially immediately after impregnation in (a) adding between about 35-100% of the alkali used to treat the material, including in (b), to the material.

12. A method as recited in claim 1, further comprising (c), between (a) and (b), treating the material in a second zone with an AQ solution containing an AQ additive at an effective alkali concentration of about 5 to less than 15 g/l expressed as NaOH and greater than in (a), and at a temperature of between about 110-130° C. and higher than in (a).

13. A method of treating comminuted cellulosic fibrous material comprising continuously:(a) treating a slurry of comminuted cellulosic fibrous material with a first liquid comprising primarily or substantially exclusively water containing an anthraquinone (AQ) additive at an effective alkali concentration of substantially zero, and at a first temperature of about 80-130 degrees C., for about 20 seconds-60 minutes under superatmospheric pressure; and (b) after (a), treating the material in the slurry with a second liquid having an initial effective alkali concentration greater than 10 g/l expressed as NaOH, and at a second temperature greater than 130° C., to produce a chemical cellulose pulp.

14. A method as recited in claim 13, further comprising (c), between (a) and (b), treating the slurry with a third liquid containing the AQ additive at a maximum effective alkali concentration greater than the first liquid and less than the second liquid, and at a third temperature, higher than the first temperature and less than 130 degrees C.

15. A method as recited In claim 14, further comprising adding further AQ additive In association with (c).

16. A method as recited in claim 13 wherein (a) is practiced in a feed system of a continuous digester, and (b) is practiced in a continuous digester.