Patent Description:
The present innovations generally address pulp processing, and more particularly, include HIGH ALPHA AND HIGH INTRINSIC VICOSITY PULP PRODUCTION APPARATUSES, METHODS AND SYSTEMS.

The use of pre-hydrolysis kraft process ("PHKP") associated to cold caustic extraction ("CCE") has been described previously, such as <CIT> and <CIT>. Both patents are hereby incorporated by reference as if set forth fully herein. A schematic description of such a method is given as a block diagram in <FIG>.

The association of cooking process and CCE process has been described and presents useful industrial application for production of high purity pulps (alpha cellulose content from <NUM>% to <NUM>%). One aspect of the art is the management of CCE filtrate as an alkali source, avoiding or at least minimizing the precipitation of hemicelluloses, and has been successfully used in industrial installation.

Resulting pulp is washed, bleached and dried in appropriate manner to result in commercial product especially suitable to manufacture of cellulose acetate (tri-acetate and di-acetate).

Such process produces Elemental Chlorine Free (ECF) bleached pulp with typical IV of <NUM>/l at high brightness level (above <NUM> %ISO) that can be extended up to <NUM>/l at normal market pulp brightness (<NUM>% to <NUM>%ISO).

Cooking process may be conducted in batch or continuous installations. State of art installations are batch with most of current production of high purity pulp.

Batch cooking plants implement PHKP in a very effective way, producing high quality product through long times (year or more) without necessity to stop for cleaning or convert to KP production.

Continuous cooking PHKP has been historically tried in single vessel installations producing pulp of acceptable quality, but with fouling problems leading to short campaign times and the need to run KP campaigns or stop the unit for cleaning (typically measure in a few weeks' time).

Recently PHKP has been re-introduced in continuous cooking by means of a <NUM> vessel system separating the PH phase from KP phase. This system seems to have a better performance but still suffers from some fouling problems.

In such system most of the purification work is done in the PHKP cooking <NUM>, with a typical removal of more than <NUM>% of the hemicellulose present in the wood. Typically such cooking process will deliver pulp with alpha cellulose content in the range of <NUM>-<NUM>%.

Pulp from cooking will typically have Kappa Number ("KN") in the range <NUM> to <NUM> and IV in the range <NUM> - <NUM> depending on raw material and cooking conditions (P factor (PF) typically ><NUM>, H factor (HF) typically <<NUM>, alkali charge typically <NUM> - <NUM> % Effective Alkali as NaOH on oven dry (OD) wood basis).

After cooking, pulp is washed and cleaned to remove debris <NUM>, uncooked material and other rejects, following to the CCE stage <NUM>.

The subsequent CCE stage will boost purity level up to <NUM>% in alpha cellulose by application of alkali charge in the range of <NUM> - <NUM> NaOH/kg OD pulp and temperatures up to 50oC.

As mentioned before CCE acts by solubilizing the low molecular weight substances present in the pulp fiber. With such action not only hemicellulose and degraded cellulose molecules are removed from the fibers, but also some degraded lignin is removed, resulting in a KN drop of up to <NUM> units.

After CCE stage, pulp is washed <NUM> to remove residual caustic content and also lignin, hemicellulose and low degree of polymerization ("dp") cellulose in CCE process. The filtrate from this process is referred to as CCE filtrate or CCE liquor, and is recycled to cooking process. Excess filtrate can be exported for other areas (e.g., evaporation plant, hemicellulose recovery plant, lignin recovery plant, other pulp production line, etc.).

In bleaching plant <NUM> pulp residual lignin is chemically removed and brightness is increased in a multi stage setup with typically <NUM> to <NUM> stages. The bleached pulp may then be subjected to further screening and/or sand removal <NUM>; dewatering, pressing and/or drying <NUM>; and finishing in rolls or bales <NUM> to result in commercial product especially suitable to manufacture of cellulose acetate (tri-acetate and di-acetate).

An ECF process may include Chlorine Dioxide (D) stage, Alkaline Extraction (E) stage, Oxygen (O2) stage and Peroxide (P) stage.

D-P being an instance of <NUM> stage sequence and D-E-D-E-D being an instance of <NUM>-stage sequence, where E may or may not be reinforced by O2 or Peroxide. Other chemicals like Per Acetic Acid (PAA) or enzymes may be used.

Total Chlorine Free (TCF) bleaching will be typically <NUM> or <NUM> stages with <NUM>, Ozone (O3) and P stages. PAA and enzymes may be also used.

TCF bleaching in general is less selective leading to lower bleached pulp viscosity.

Pulp bleaching is not a perfectly selective process and cellulose IV will be typically reduced by at least <NUM>/l, and more typically <NUM>-<NUM>/l, resulting in lower final product viscosity, lower overall process yield (conversion of wood to final goods) and sometimes lower pulp purity (as alpha-cellulose) due to cellulose degradation.

Document <CIT> discloses method and system for pulp processing using cold caustic extraction with alkaline filtrate reuse.

The HIGH ALPHA AND HIGH INTRINSIC VICOSITY PULP PRODUCTION APPARATUSES, METHODS AND SYSTEMS (hereinafter "High-A High-IV Pulp Production") disclosed herein in various embodiments provide for pulp processing used in connection with Kraft Processes ("KP") and Pre Hydrolysis Kraft Processes ("PHKP"), embodiments employing a Cold Caustic Extraction ("CCE") stage and/or appropriate washing and bleaching stages, resulting in pulp with high Intrinsic Viscosity ("IV") and high purity, such as may be as determined by alpha cellulose content, and adequate brightness for use downstream in applications such as high tensile regenerated cellulose and ether applications, or other applications employing high IV pulp with significant purity (e.g., alpha cellulose > <NUM>%).

The invention is defined by the annexed set of claims.

The accompanying appendices and/or drawings illustrate various non-limiting, example, innovative aspects in accordance with the present descriptions:.

The HIGH ALPHA AND HIGH INTRINSIC VICOSITY PULP PRODUCTION APPARATUSES, METHODS AND SYSTEMS (hereinafter "High-A High-IV Pulp Production") disclosed herein in various embodiments address optimization of process conditions from the combined cooking and CCE stages resulting in high IV bleached pulp (e.g., ><NUM>/g, alpha cellulose content ><NUM>% and pulp brightness ><NUM>%ISO). The optimized conditions go beyond the original described conditions in previous art, but do not require changes in main equipment.

Embodiments of High-A High-IV Pulp Production may also be applied to continuous cooking processes, bringing potential process benefits regarding process simplification and reduced equipment scaling potential.

Embodiments of High-A High-IV Pulp Production may include the redistribution of purification work done in cooking and CCE stages, shifting most of the purification effect to the CCE stage (e.g., <NUM>% or more of hemicellulose reduction; in some implementations, <NUM>% or more), while reducing the cooking process hemicellulose reduction effect.

This change in purification strategy, combined with described modifications in cooking process and adequate, i.e., selective bleaching conditions results in high viscosity pulp with dissolving grade purity and brightness, suitable for specialty applications such as cellulose ethers and high strength regenerated cellulose.

CCE filtrate can be partially or completely recycled to the cooking plant without any treatment as applied in previous art <CIT>, which is incorporated in its entirety herein by reference.

Pulp produced from cooking will typically have viscosity above <NUM>/g at a bleachable KN (below <NUM> for hardwood pulp) and purity above <NUM> % in alpha cellulose.

In the subsequent CCE stage, pulp purity is increased up to <NUM>% alpha cellulose content. For some applications in which mercerized cellulose content is irrelevant, alpha cellulose purity may be increased up to <NUM>%.

KN will drop significantly (typically <NUM>-<NUM> units) and once most of low dp cellulose and hemicellulose products are removed a significant increase in average pulp dp is seen, bringing IV above about <NUM>/g level.

In some implementations, a subsequent high selectivity bleaching sequence with <NUM> or <NUM> stages (D-P or D-EP-D) will bring brightness to a commercial level (e.g., <NUM>%-<NUM>% ISO; in some implementations <NUM>%-<NUM>% ISO) at final IV level above <NUM>/g.

See comparison of previous art results with current results on table <NUM>.

Such viscosity and purity levels are not currently available from Hardwood KP or PHKP, being only obtained by Sulphite cooking of Softwood or by the use of cotton linter.

The CCE filtrate will have high hemicellulose content and also significant lignin content, being a potential candidate for hemicellulose and lignin recovery process. Independently of such recovery processes, the CCE Filtrate can be recycled to the cooking plant without other treatment than temperature and alkalinity adjustments as the main alkali source for the cooking process (e.g., more than <NUM>% of total EA charge applied on BD wood).

Examples of process conditions to achieve the desired viscosity and purity levels are described in the following exemplary statements.

In implementations, the raw material can be hardwood, softwood or non-wood source.

Cooking method may be PHKP, with KP being considered as a particular case of PHKP were P factor is <NUM> (Zero).

Cooking equipment may be batch cook or continuous.

<FIG> shows an example of logic flow for high-A high-IV pulp production in one embodiment from raw material to finished product.

<FIG> presents detailed cooking process parameters, i.e., the cooking recipe, for high-A high-IV pulp production in one embodiment. In one embodiment, actual conditions in one or more steps may slightly deviate from the ones presented due to implementation particularities (e.g. batch or continuous digester, or different strainer set arrangement on continuous digesters) or due to other accessory processes limitations (e.g. steam supply or evaporation plant). Detailed procedures of each step in the cooking recipe are disclosed further. Some steps may have alternative procedures disclosed, but not represented in the recipe flowsheet for simplification.

In some implementations, a PHKP cooking process <NUM> may include wood chips being fed into the digester <NUM> and heated <NUM> to, e.g., <NUM> -<NUM> (e.g., in one implementation to <NUM>-<NUM>) with, e.g., direct steam injection or similar method and kept at such temperature for time enough <NUM> to reach a P factor from <NUM> to <NUM> (e.g., in one implementation, from <NUM> to <NUM>). In this condition air removal is at acceptable levels and a mild pre hydrolysis will take place (no pre hydrolysis for the particular case of <NUM> P factor).

In one implementation, the acid aqueous phase containing hemicellulose, cellulose and lignin degradation products, referred as hydrolysate, may be extracted or displaced from the digester. This stream can be recycled to the chip feeding and/or chip heating step as a form of heating or chip transport media. In one implementation, the hydrolysate can be purified and its key valuable molecules, such as acetic acid, furfural and sugar monomers and oligomers, separated as an additional revenue stream, or can be neutralized with any alkaline stream and sent to the evaporation plant.

A next step, in one implementation, includes the addition of a white liquor pad <NUM>, e.g., to avoid hemicellulose and lignin precipitation. In one implementation, the white liquor pad amount will correspond to <NUM>-<NUM>% of the BD wood weight.

A next step, in one implementation, includes the addition of a high volume of CCE filtrate <NUM> for wood chip alkali impregnation, e.g., corresponding from <NUM> to <NUM>% of total alkali requirement for cooking.

This filtrate may have a typical concentration of, e.g., <NUM> to <NUM> Effective Alkali (EA) / l, with EA expressed as NaOH (e.g., in one implementation, <NUM>-<NUM> EA/l). This filtrate may have its concentration increased by addition of white liquor.

In some implementations, CCE filtrate will be pre heated to, e.g., <NUM>-<NUM> (e.g., in one implementation, to <NUM>-<NUM>).

Sufficient impregnation time can be achieved, by leaving the digester static or circulating the liquor through the digester in the case of batch digesters, or having a sufficient retention time at the impregnation zone in continuous digesters.

A next step, in some implementations, includes heating of chips to reach the desired cooking temperature, e.g., in the range of <NUM>-<NUM> (e.g., in one implementation to <NUM>-<NUM>). Heating can be provided, for example, by the addition of hot black liquor that will displace the spent CCE filtrate and/or by forced circulation of the digester liquor to an external heat exchanger, or another form of external heating.

With implementations including the addition of hot black liquor <NUM>, concentration of, e.g., <NUM>-<NUM> EA/l (e.g., in one implementation <NUM>-<NUM> EA/l) may be employed in some implementations and can be adjusted by addition of fresh white liquor or CCE filtrate. Black liquor temperature may be, e.g., <NUM>-<NUM> (e.g., in one implementation, <NUM>-<NUM>). The addition of hot black liquor may be sufficient to reach the cooking temperature target, or a few degrees (e.g., not more than <NUM>) lower. If the latter, in one implementation, the liquor inside the digester can be circulated to an external form of heating to reach its desired temperature.

Once target temperature is reached it may be kept <NUM> until a desired H-factor is reached. An H-Factor target may be set, in one implementation, to result in bleachable pulp of suitable KN (e.g., for hardwood KN may be from <NUM> - <NUM> (e.g., in one implementation, from <NUM>-<NUM>)).

An extra alkali charge (<NUM>-<NUM>%), either in the form of CCE filtrate or pure white liquor, may be added at one or multiple intermediate H-factors, e.g., to avoid the residual alkali concentration inside the digester reaching a low level that will promote lignin and hemicellulose precipitation trough the cooking phase.

A next step, in one implementation, includes the cooking liquor displacement with cold wash liquor <NUM>, containing some residual alkali, e.g., higher than <NUM> gEA/l, such as to avoid lignin and hemicellulose precipitation.

In some implementations, the wash liquor may have its alkalinity increased, e.g., by the use of white liquor or CCE filtrate. Wash liquor temperature may be adjusted to a level such that the pulp discharge from the cooking vessel will be below boiling conditions.

A next step, in one implementation, includes pulp discharge from the cooking vessel <NUM>, e.g., to an atmospheric discharge tank, atmospheric washing equipment (e.g. atmospheric diffuser), pressurized washing equipment (e.g. pressure diffuser), and/or the like.

A next step, in one implementation, includes washing of the pulp. In one implementation, the pulp may also be screened <NUM>. Screening may be performed before or after washing of pulp, or after CCE stage.

A next step, in one implementation, includes the addition of cold fresh alkali <NUM>, e.g., in the form of NaOH or White Liquor or a combination of both to perform the Cold Caustic Extraction (CCE) process.

For example, white liquor with a concentration from, e.g., <NUM>-<NUM> EA/l (e.g., in one implementation from <NUM>-<NUM> gEA/l) and sulfidity of, e.g., <NUM>-<NUM>% (e.g., in one implementation from <NUM>-<NUM>%) may be used after being cooled, so as to adjust CCE stage to operate at temperature from, e.g., <NUM> -<NUM> (e.g., in one implementation from <NUM> - <NUM>) at a pulp mass consistency of, e.g., <NUM> to <NUM>% in fiber weight (e.g., in one implementation from <NUM> - <NUM> %) and an alkali concentration in the pulp slurry of, e.g., <NUM> - <NUM> EA/l (e.g., in one implementation from <NUM> - <NUM> EA/l). Pulp slurry concentration may be adjusted by the addition of a dilution liquid, e.g., in one implementation, filtrate from a washing stage after the CCE.

Retention time in CCE stages can, in various implementations, be from a few minutes to several hours. For example, in one implementation, the time span may be in the range of <NUM> to <NUM> minutes.

A next step, in one implementation, includes counter current washing of CCE pulp <NUM>, e.g., in <NUM> or more washing stages (e.g., in one implementation from <NUM> to <NUM> stages), such as to recover CCE filtrate and minimize alkali and organic dissolved solid loss to subsequent bleaching processes.

Washing can be done with any kind of washing equipment (e.g., press, wash press, pressurized filters, vacuum filters, pressurized and atmospheric diffusers, and/or the like).

Various washing media may be used, e.g., pure water, condensate from evaporation plant, and/or other suitable washing liquor (e.g., EOP filtrate, P filtrate, and/or the like). Washing media temperature may depend, for example, on washing machine specifics, overall process mass, heat balance, and/or the like, and may be in the range of <NUM>-<NUM>, but not restricted to that range.

A next step, in one implementation, includes bleaching the pulp <NUM>, e.g., in a high selective bleaching sequence in order to minimize viscosity loss.

For Hardwood pulp, a <NUM>-stage ECF sequence may be employed to reach final brightness of <NUM>-<NUM>% ISO, whereas a <NUM>-stage ECF sequence may be used for brightness level <NUM>-<NUM> %ISO.

The bleaching sequence may include the use of viscosity preservers such as magnesium salts, chelating agents, and/or the like for the control of transition metals.

Next steps, in some implementations, may further include additional screening and/or sand removal <NUM>; dewatering, pressing and drying <NUM>; and finishing the resulting pulp in rolls, bales, and/or the like <NUM>.

Further embodiments of High-A High-IV Pulp Production are demonstrated in the following examples. In some instances, the examples are based on principles presented in <FIG> and as well as the recipes presented in <FIG>. Deviation and particulars are described in each example.

Kraft process for high Intrinsic Viscosity high Purity pulp in one embodiment, using a single vessel steam phase continuous digester where main alkali source is untreated CCE filtrate.

In this case the sequence shown in <FIG> is implemented in a single vessel continuous digester as described, in one embodiment, in <FIG>. The cooking recipe follows closely the one presented in <FIG>.

The downstream process comprises washing, screening, CCE treatment, CCE washing and ECF bleaching as previously described.

Wood Chips (<NUM>) are processed via chip feeding system and transferred (<NUM>) to Digester vessel. In various implementations, the chip feeding system may comprise, e.g., chip silo with chip pumping system to feed the digester, chip silo with High Pressure Feeder to feed the digester, direct digester feeding with a metering and pressure locking device, and/or the like.

In digester top the chips may be heated up with Steam (<NUM>) to desired temperature and retention time to achieve a given P factor. Chip level and/or liquor level may be controlled to establish defined specified retention time. Digester Pressure may be controlled to achieve the desired temperature without boiling.

A set of strainers may be located in a second digester section, such as to establish a circulation loop. Liquor may be extracted from digester, receive white liquor charge (<NUM>) and returned to digester via central pipe (<NUM>) above the said set of strainers. This circulation flow may be employed to facilitate white liquor pad effect.

A second set of strainers may be located in a third digester section, such as to establish a circulation loop. Liquor may be extracted from digester (<NUM>), receive a CCE filtrate charge (<NUM>) and returned to digester via central pipe (<NUM>) above the said set of strainers. This circulation flow may be employed to facilitate CCE filtrate distribution and impregnation process. Retention time may be selected to facilitate impregnation.

In one implementation, this circulation loop may include extraction capability (<NUM>) to facilitate digester liquor level control.

A third set of strainers may be located in a fourth digester section to establish a circulation loop. Liquor may be extracted from digester, receive a CCE filtrate charge (<NUM>) and/or white liquor charge (<NUM>), may be heated up with steam (<NUM>) and returned to digester via central pipe (<NUM>) above the said set of strainers. This circulation flow may be employed to facilitate alkali distribution and heat up process. Retention time may be selected to facilitate cooking time to desired H factor.

In one implementation, residual alkali may be adjusted in this step to facilitate kappa number control.

A fourth set of strainers may be located in a fifth digester section, such as to establish the main digester extraction flow. The extraction pipes (<NUM>) may be directed to heat recovery system, liquor filtration, and/or the like and then sent to evaporation plant.

Cold wash filtrate (<NUM>) may be introduced to digester bottom, such as to allow washing and/or cooling before the pulp discharge (<NUM>).

Retention time in this section may be selected to facilitate pulp cooling and to provide a washing effect as well.

In one implementation, white liquor (<NUM>) and/or CCE filtrate (<NUM>) may be used to correct the wash filtrate alkalinity.

In one implementation, pulp may be discharged from digester (<NUM>) at a selected temperature, below boiling point, to the subsequent process step (e.g., blow tank, pressure diffuser, and/or the like).

Kraft process for high Intrinsic Viscosity high Purity pulp in one embodiment using a single vessel hydraulic phase continuous digester were main alkali source is untreated CCE filtrate.

Principle diagram shown in one embodiment in <FIG>.

Similar to principles described in connection with example <NUM> above, except that digester is hydraulically filled, employing one additional set of strainers in First digester section in order to establish a circulation loop. Liquor may be extracted from digester, heated and returned to digester via central pipe above the said set of strainers (<NUM>). This circulation flow may be employed to facilitate heat up to desired temperature. An extraction line may be employed to facilitate digester pressure control (<NUM>, <NUM>, <NUM>).

After the modified First digester section, the process may resume through remaining sections as described in example <NUM>.

Kraft process for high Intrinsic Viscosity high Purity pulp in one embodiment, using a two vessel steam phase continuous digester were main alkali source is untreated CCE filtrate.

Similar to principles described in connection with example <NUM> above, except that a second vessel for pre hydrolysis may be introduced between chip feeding system and Digester. In some implementations, such vessel can be steam/liquor phase, hydraulically pressurized, and/or the like.

In one implementation, chips may be heated up to specified pre hydrolysis temperature, such as by direct steam injection in case of steam/liquor phase vessel <NUM>, or by means of indirect heating by the establishment of a liquor circulating loop (strainer, circulation pump and heat exchanger) in the top of said vessel.

In one implementation, chip transfer for digester <NUM> may be achieved by pressurization with steam and/or compressed air in the top of such steam/liquor phase vessel and/or by use of a pressurization pump in chip feeding system, such as in the case of a hydraulically filled vessel.

In another implementation, chip pumping may be used for chip transference between pre hydrolysis vessel and digester.

Such vessel may employ a retention time set so as to reach a desired P factor.

After transfer to digester, the process may proceed as described in example <NUM>, with the possible optimization of doing the white liquor pad addition in the transfer loop between both said vessels (pre hydrolysis and digester, <NUM> and <NUM>) using this circulation loop as a replacement from sections <NUM> and <NUM>.

Kraft process for high Intrinsic Viscosity high Purity pulp in one embodiment using a batch digester system where main alkali source is untreated CCE filtrate.

In one implementation, a first step the cooking vessel (digester) includes filling with wood chips <NUM>. In one implementation, a small amount of steam may be added to facilitate chip packing and start the heating process.

In one implementation, a second step may include, with the cooking vessel full of chips and closed, heating up to specified temperature and pressure <NUM>.

In one implementation, a third step may include maintaining specified conditions (e.g., of temperature and pressure) until target P factor is reached <NUM>.

In one implementation, a fourth step may include introducing white liquor pad to the cooking vessel <NUM>.

In one implementation, a fifth step may include introducing a specified amount of pre heated CCE filtrate in the cooking vessel and waiting for a specified degree of impregnation to be achieved <NUM>.

In one implementation, a sixth step may include heating up the vessel to cooking temperature <NUM>. For example, that may be achieved by circulating the liquor present in the vessel through an external heater, by displacing the liquor present in the vessel with hot black liquor of controlled alkalinity, and/or the like. In one implementation, in this stage extra alkali charge from fresh white liquor or from CCE filtrate can be introduced, such as via circulation, displacement, and/or the like.

In one implementation, a seventh step may include keeping specified conditions until target H factor is reached <NUM>.

In one implementation, an eighth step may include displacing the liquor present in the vessel <NUM>, e.g., with cooled wash liquor so as to cool down the product to below boiling point at discharge condition.

Claim 1:
A method for high intrinsic viscosity pulp production, comprising:
pre-hydrolyzing raw material in a digester via steam heating, the raw material comprising hardwood chips, including performing pre-hydrolysis kraft process cooking of the hardwood chips in the digester via steam heating to obtain a pre-hydrolysis condition comprising a P factor from <NUM> to <NUM>;
adding a white liquor pad to the cooked hardwood chips, wherein the white liquor pad comprises <NUM>% to <NUM>% of a weight of the hardwood chips;
pre-heating a non-purified cold caustic extraction filtrate having a filtrate concentration of between <NUM> gEA/l and <NUM> EA/l to a filtrate temperature of between <NUM> and <NUM>
adding non-purified cold caustic extraction filtrate to produce alkali impregnated cooked hardwood chips;
heating the alkali impregnated cooked hardwood chips to reach a target temperature between <NUM> and <NUM> and holding for a cooking time to reach a target H-factor corresponding to a kappa number between <NUM> and <NUM> and produce pulp;
displacing cooking liquor with a cold wash liquor comprising residual alkali at concentration higher than <NUM> gEA/l until the pulp is below boiling conditions;
discharging the pulp from the digester to at least one of an atmospheric discharge tank, atmospheric washing equipment, and pressurized washing equipment;
washing the pulp;
screening the pulp;
adding cold fresh alkali, comprising NaOH, white liquor, or both, to the pulp for cold caustic extraction to operate at an extraction temperature of between <NUM> and <NUM> for an extraction time of between <NUM> and <NUM> minutes;
performing counter current washing of the pulp at a washing temperature of between <NUM> and <NUM> to recover the cold caustic extraction filtrate; and
bleaching the pulp in a high selective bleaching sequence comprising a three stage ECF sequence to yield a final pulp having intrinsic viscosity > <NUM>/g, alpha cellulose content > <NUM>%, and brightness of between <NUM>% and <NUM>% ISO, wherein the bleaching includes at least one of a magnesium salt and a chelating agent;
dewatering the pulp;
pressing the pulp;
drying the pulp; and
forming the pulp into rolls or bales.