GB2393740A

GB2393740A - Jet dried cellulosic fibres and their production

Info

Publication number: GB2393740A
Application number: GB0317212A
Authority: GB
Inventors: Michael David Vrbanac; Ramon Charles Dezutter; Brian Wester; Michael James Yancey
Original assignee: Weyerhaeuser Co
Current assignee: Weyerhaeuser Co
Priority date: 2001-10-30
Filing date: 2002-10-30
Publication date: 2004-04-07
Anticipated expiration: 2022-10-30
Also published as: GB2393502A; GB2393502B; GB0317213D0; GB2393501A; GB2393503A; GB0317214D0; GB2393740B; GB0317215D0; GB0317212D0

Abstract

This invention provides a dried singulated cellulose pulp fiber product as well as an apparatus and a method for forming singulated and dried fibers. In accordance with the process a feed pulp is delivered to a jet drier. The jet drier singulates and dried the feed pulp. The singulated and dried fibers are collected from the jet drier. The feed pulp may be treated with a treatment substance. The jet drier may be maintained at negative pressure. The product fibers may have low knot count, a low fines count, as well improved kink, curl and twist. The apparatus for carrying out the process may include a pretreatment station for supplying the treatment substance, a pulp feed device designed for pulp, a pulp feed device designed for pulp and foam suspensions, and/or a fiber separation station having a vacuum conveyor.

Description

GB 2393740 A continuation (72) cont Brian Wester Michael James Yancey (74)

Agent and/or Address for Service: Barker Brettell 138 Hagley Road, Edgbaston, BIRMINGHAM, B16 9PW, United Kingdom

PROCESS TO PRODUCE DRIED SINGULATED CELLULOSE PULP FIBERS

FIELD OF THE rNVENTION

The present invention relates to a dried singulated cellulose pulp fiber 5 product as well as a process and apparatus for producing dried singulated cellulose pulp fibers, and more particularly, a process and apparatus for producing dried singulated cellulose pulp fibers including the step of using a jet drier to dry the pulp. BACKGROUND OF THE INVENTION

10 Dried singulated cellulose pulp fibers are desirable for many products from absorbent personal articles to a strengthener in concrete. Currently, in the most common process of making singulated fibers, a roll of conventional pulp fibers is hamerrnilled into singulated fibers. This process is energy and time intensive, requiring many steps and pieces of processing equipment. Each piece of processing 15 equipment requires a significant capital expenditure and occupies valuable factory floor space. Further, the current hammerrnilling process often produces fibers with undesirable physical properties, such as low kink, curl, and twist.

This dry singulated pulp will also contain knots of fiber, sometimes referred to as nits or nodules. Knots are fiber clumps that remain strongly adhered to one 20 another as can be seen by placing a small portion of pulp into a clear beaker of water and stirring the water to mix the fibers. Most of the fiber will mix into the

I water as singular fibers, however there will be fiber clumps that are readily visible.

The fiber clumps or knots are undesirable by-products of the hammermilling process. The amount of knots in a pulp that has been hammermilled can be quantified by using a screening system with acoustical energy used as the means to 5 classify the fiber into sizes of knots, accepts and fines. It is desirable to have low knots and fines and high accepts where the accepts are the singulated fibers.

Canadian Patent No. 993618 (Estes, 1976) describes a process for producing a low density fluff pad or batt from individual fibers that have significant kink and interlocking to provide improved batt strength and higher bulk. In accordance with 10 the process, wet pulp is separated into individual fibers during the drying stage.

The process uses fluid jet drying equipment that employ airjets or steamjets for separating the fibers. The fibers are laid on a perforated screen upon exiting from the jet drier. The fibers produced by the process of the Canadian patent, however, have a very high knot content, which as stated above is an undesirable 1 5 characteristic.

SUMMARY OF THE INVENTION

This invention provides a dried singulated cellulose pulp fiber product as well as an apparatus and a method for forming singulated and dried fibers that have a relatively low knot content. In accordance with the process, wet pulp and air are 20 introduced into a jet drier. The pulp is dried in the jet drier to form singulated pulp fibers. The pulp is removed from the jet drier and separated from the air. The process may be used on several types of feed pulp and on treated feed pulp. The product formed by the process has advantageous properties such as a low knot count, a low fines count, as well as improved kink, curl and twist. The apparatus 25 for carrying out the process may include a pretreatment station for supplying a treatment substance, a pulp feed device designed only for pulp, a pulp feed device designed for pulp and foam suspensions of pulp, and/or a fiber separation station having a vacuum conveyor.

In accordance with the process described above, the wet pulp is treated with 30 a treatment substance before drying to reduce the knot content of the pulp fibers.

l -3 The process also includes producing singulated pulp fibers by introducing wet pulp and air into a jet drier through a rotary airlock. The rotary airlock has vanes and a housing, with the end of the vanes being spaced from the housing by a distance sufficient to prevent wet fibers from clogging the airlock. The process includes 5 producing singulated pulp fibers by withdrawing the fibers from said jet drier in an air stream at a velocity sufficient to prevent the fibers from knotting. The process also includes producing singulated pulp fibers by withdrawing the pulp fibers from an outlet from said jet drier under a partial vacuum.

The pulp product includes singulated and jet dried fibers having a knot 10 count equal to or less than 5%, an accepts count equal to or greater than 80%, and a fines count equal to or less than 15%. The pulp product may include singulated and jet dried fibers having a knot count equal to or less than 2%, an accepts count equal to or greater than 77%, and a fines count equal to or less than 21%. The product may be treated with a treatment substance selected from the group consisting of a 15 surfactant and a mineral particulate. The product may be further treated with a crosslinker or a hydrophobic material during jet drying. The product of dried singulated fibers can be incorporated into concrete, an absorbent article, a plastic product, a paper product, or a filter product.

The drying system for the processing of pulp into singulated and dried fibers 20 includes a jet drier, a pulp supply station, an air supply station, an outlet flow conduit and a fiber separation station. The jet drier has a jet conduit, a manifold for air intake into the jet conduit, a pulp intake for delivery of pulp into the jet conduit, and a fiber outlet for removal of singulated and dried fibers, outlet air and fines from the jet conduit. The pulp supply station is coupled to the pulp intake for 25 supplying a feed pulp to the pulp intake. The air supply station is coupled to the manifold for delivering air to the manifold. The outlet flow conduit is coupled to the fiber outlet for the transport of the fibers, outlet air and fines from the jet conduit. The fiber separation station is coupled to the outlet flow conduit for separating the fibers from the outlet air.

-4 In one embodiment, the pulp supply station includes a treatnent supply source for delivering a treatment substance to the pulp. In another embodiment, the pulp supply station includes a pulp feed device coupled to the pulp intake for delivering the feed pulp to the pulp intake while minimizing the amount of air flow 5 through the pulp supply station. The pulp feed device may be a rotary airlock including a rotor housing and a rotor rotatably mounted within the rotor housing, the rotor having rotor vanes for transporting the feed pulp. The rotor vanes and rotor housing are sized so that a gap exists between the rotor vanes and the rotor housing to prevent the feed pulp from jamming the rotary airlock. In a further 10 embodiment, the pulp supply station may further include a foam feeder interposed between the pulp feed device and the pulp intake for mixing a surfactant with pulp and directly injecting foamed pulp mixture into the jet drier.

In a still further embodiment the fiber separation station includes a vacuum conveyor having a screen for passing outlet air and retaining fibers to form a mat of 15 fibers on the screen. The vacuum conveyor may have a first roller, a second roller, a primary fan, a secondary fan, a primary fan vacuum box, and a secondary fan vacuum box. The screen is a continuous loop draped about the first and second rollers so that the screen has an upper portion and a lower portion. The upper portion of the screen has an upper and lower surface. The upper surface of the 20 screen is associated with the outlet flow conduit. The primary fan vacuum box is associated with the lower surface and in flow communication with the primary fan.

The primary fan vacuum box is positioned between the lower and upper portions and directly beneath the outlet flow conduit. The secondary fan vacuum box is associated with the lower surface and in flow communication with the secondary 25 fan. The secondary fan vacuum box is positioned between the lower and upper portions and between the primary fan vacuum box and the second roller. The primary fan provides vacuum to the primary fan vacuum box and the outlet flow conduit. The secondary fan provides vacuum to the secondary fan vacuum box and the upper surface.

The present invention thus provides a dried singulated cellulose pulp fiber product as well as an apparatus and a method that enable forming singulated and dried fibers. The process may take wet pulp directly from a pulp mill and produce a singulated product from the never-dried pulp by using a drying process that 5 singulates the pulp directly. This process forms fibers with greater kink, curl, and twist than hammerrnilled fibers. A further advantage is the ability of the present invention to produce fibers having a low knot and fines content. Another advantage is the treatments that can be performed on the pulp that are difficult or impossible to perform on a roll of dried pulp. Treatments can be done on the never-dried pulp 10 that reduce the amount of knots, increase production rate, andlor form fibers having desirable characteristics.

BRIEF DESCRIPTION OF THE DRAWINGS

The foregoing aspects and many of the attendant advantages of this invention will become more readily appreciated as the same become better 15 understood by reference to the following detailed description, when taken in

conjunction with the accompanying drawings, wherein: FIGURE I is a schematic diagram of a drying system constructed in accordance with the present invention suitable for carrying out the process in the present invention; 20 FIGURE 2 is a schematic view of the drying system of the present invention with a cross section view of a jet drier and a fiber separation station; FIGURE 3 is a cross section view of a pulp feed device of the present invention; FIGURE 4 is an enlarged cross section view of the pulp feed device rotor of 25 the present invention; FIGURE 5 is a side view of a mechanical mixer and the jet drier of the drying system of the present invention; FIGURE 6 is an exploded view of the mechanical mixer of the present invention;

-6 FIGURE 7 is a perspective view of a fiber separation station of the present invention; FIGURE 8 is a bottom perspective view of the fiber separation station of the present invention; 5 FIGURE 9 is an enlarged perspective view of the fiber separation station of the present invention; FIGURE 10 is a schematic diagram of an absorbent article of the present invention; FIGURE I I is a schematic diagram of a concrete or plastic product of the 10 present invention; and FIGURE l2 is a schematic diagram of a paper or filter product of the present invention.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT

The present invention provides for processes and apparatus for the drying, 15 treatment, and singulation of pulp into individual fibers with few knots or nodules.

As used herein the term "dried" in regards to fibers, is a term of art generally indicating a weight percentage of water between 2% and 10%, but may fall above or below this range. As used herein the tenn "air" is not limited to pure air but may include any gas consistent with the present invention. As used herein the term 20 "consistency" means the percentage of solids content of a liquid and solid mixture.

The specific examples set forth below are directed to the drying, treatment, and singulation of cellulose pulp fibers. However, it should be understood that the present invention is also suitable for use in processing other types of natural fibers and/or synthetic fibers.

25 The present invention comprises a drying system having a jet drier designed to dry wet pulp directly from a pulp mill to a singulated fiber product. Referring to FIGURE 1, a drying system 10 constructed in accordance with the present invention includes a jet drier 20, a pulp supply station 40, an air supply station 90, a fiber separation station 100, and a fiber collection station 160.

The pulp supply station 40 is coupled in flow communication with the jet drier 20. The pulp supply station 40 receives supply pulp from a pulp supply source 42 and provides a feed pulp to the jet drier 20 via a pulp feed conduit 44.

The air supply station 90 is coupled in flow communication with the jet drier 20.

5 The air supply station 90 receives supply air from an air supply source 92 and provides feed air via an air feed conduit 94 to the jet drier 20. The jet drier 20 is coupled in flow communication with the fiber separation station 100 via outlet flow conduit 30. The jet drier 20 exhausts outlet air, substantially dried and singulated fibers, and fines to the fiber separation station 100 via outlet flow conduit 30. The 10 fiber separation station 100 is coupled in flow communication with the fiber collection station 160. The fiber separation station 100 separates the outlet air from the fibers, and may also separate a portion of the fines from the fibers. The fibers from the fiber separation station 100 are delivered to the fiber collection station 160.

15 In a preferred embodiment, the apparatus also includes a fines removal station 170 and a noise reduction station 180. The fiber separation station 100 is coupled in flow communication with the fines removal station 170 through fines conduit 172. The fiber separation station 100 provides outlet air and fines to the fines removal station 170 via fines conduit 172. The fines removal station 170 20 removes the fines from the outlet air and recycles the outlet air back to the air supply station 90 via air conduit 182. The noise reduction station 180 is preferably interposed in air conduit 182 to reduce the noise produced by the drying system 10.

Referring to FIGURE 2, the jet drier 20 includes a loop conduit 22, a pulp intake 24, a manifold 26, and a fiber outlet 28. It will be understood that, as used 25 herein, the term "jet drier" means any device which accelerates air into the loop conduit 22, enabling the simultaneous drying and singulation of a substance flowing though the conduit22. The pulp intake24 is coupled to the conduit22 for delivering feed pulp to the conduit 22. The manifold 26 is coupled to the jet drier conduit 22 to deliver feed air via air feed conduit 94 into the conduit 22 through a 30 series of nozzles which are directed to induce a flow within the conduit 22. The

( -8 fiber outlet 28 is coupled to the conduit 22 to supply an outlet for outlet air, fibers, and fines flow out of conduit 22.

The conduit 22 is preferably arranged in a closed loop. The conduit 22 loop can take various shapes such as circular, elongated rectangular, a "D" shape, square, 5 or other similar shape. Without being bound by theory, it is believed that when wet fibers enter the conduit22 loop, a centrifugal separation takes place so that wetter/denser fibers are recirculated along the outer edge of the loop while drierQess-dense fibers move towards the inner part of the loop. Air and dried product exit from a fiber outlet 28 placed along the inner part of the loop. One 10 suitable jet drier 20 for use in the present invention is a Fluid Energy Aljet Model 4 Thermajet, X0870L, manufactured by Fluid Energy Processing Equipment Company. Alternatively, the jet drier conduit 22 may be in a shape other than a closed loop. For example, the conduit 22 could be straight. In this embodiment, the fibers may be recovered at the end of the conduit 22.

15 The drying system 20 further includes an outlet flow conduit 30 coupled to the jet drier 20 fiber outlet 28 and associated with the fiber separating station 100.

The outlet flow conduit 30 delivers outlet air, fibers, and fines flow to the fiber separating station 100. The outlet flow conduit may include a first material handling fan 32. The first material handling fan 32 prevents the fibers and fines 20 from settling out of the outlet air if the outlet air slows in the conduit 30. However, the first material handling fan 32 may not be necessary if the outlet flow conduit is of a length which minimizes the effects of drag on the velocity of the outlet air, and/or if the outlet flow conduit is of substantially similar diameter to the fiber outlet 28 of the jet drier 20. The first material handling fan 32 may have an adverse 25 impact on the physical properties of fibers, and so may be excluded from the drying system 10. It is desirable to prevent the fibers and fines from settling out of the outlet air. If fibers and fines settle out of the outlet air, the fibers have an increased tendency to knot.

The pulp supply station 40 may include a first dewatering device 46. The 30 first dewatering device 46 is connected in flow communication with pulp supply 42

-9- and pulp feed conduit 44. The pulp supply source 42 delivers supply pulp directly from the pulping stage of a pulp mill to the first dewatering device 46. The first dewatering device 46 partially dewaters the supply pulp from pulp supply 42 and delivers feed pulp via pulp feed conduit 44 to jet drier 20. The first dewatering 5 device 46 includes, but is not limited to, devices such as a screw press, belt press, continuous centrifuge, batch centrifuge, double roll press, or other similar device.

The supply pulp from pulp supply source 42 will typically have a high fluid content, having a.01-10% consistency, and more typically a 3-10% consistency.

The supply pulp may be bleached pulp, unbleached pulp, mechanical pulp, 10 chemical pulp, a dissolving grade pulp, once dried and reslurried pulp, or any other suitable pulp. In the present invention, much of this fluid may be removed by the first dewatering device 46. Typically, the first dewatering device 46 removes a portion of the fluid from the supply pulp and increases the consistency of the feed pulp to 10-55%, prior to drying the feed pulp by the jet drier 20. Preferably the 15 consistency of the feed pulp is 30 to 50%. The partially dewatered feed pulp is transported to the jet drier 20 via pulp feed conduit 44.

The supply pulp may be a pressed wet web of pulp having a basis weight of a substantial amount to provide sufficient stiffness to feed the web into a shredding device. The basis weight may typically be from 500 to 1500 gem. The wet web 20 supply pulp may be fed into a shredding device such as a rapidly rotating set of rolls containing protruding pins that tear the web into small pieces of pulp, a material handling fan, or other similar device.

The pulp feed conduit 44 may be a pipe, hopper, or other conveyance device. Additionally, the first dewatering device 46 itself may serve as a 25 conveyance device. For example, the first dewatering device 46 may be a screw press which could be used to simultaneously dewater and transport the feed pulp to the jet drier 20. One suitable pulp supply station 40 pulp feed conduit 44 for use in the present invention is a shaftless screw conveyor designed and manufactured by Martin Sprocet and Grear, Inc., Martin Conveyor Division. The shafiless screw 30 conveyor has a shaftless screw which feeds wet pulp at an incline that rises up

( -10 toward the pulp intake 24 of the jet drier 20. The shaftless screw conveyor has a hopper at the lower end of the conveyer for placing supply pulp.

The pulp supply station 40 may include a treatment supply source 48 for incorporating a treatment substance into the feed pulp. The treatment supply 5 source 48 may be coupled in flow communication to the pulp supply source 42, the pulp feed conduit 44, the first dewatering station 46, or anywhere along the pulp supply station 40.

The treatment supply source 48 may deliver the treatment substance with any apparatus known in the art. For instance, treatment supply source 48 may 10 deliver the treatment substance with a conduit, spray system, mixing device, or other device or combination of devices. Where the supply pulp is a pressed wet web of pulp, the treatment substance may be applied to the supply pulp by a spray system, roller coating system, or a combination of spray system and roller coating system. 15 Many treatment substances that may be applied to the feed pulp prior to being dried and singulated by the jet drier 20, are incapable of being incorporated into the traditional process of producing dried singulated fibers. The traditional process is limited in its ability to treat the fibers since they are in a web form. In this web form, treatment of the fibers must be done by running the web through a 20 bath or spraying the web. The present invention is not limited in this way, since treatment substances may be directly delivered to the pulp. For example, the fibers of the supply pulp in the present invention may be suspended within a foam prior to drying by the jet drier 20 or viscous solutions may be mixed with the supply pulp.

Neither one of these treatment choices would be practical with the traditional bath 25 treatment step. The application of treatment substances that are viscous solutions cannot be accomplished with a traditional pulp machine. Additionally, the harsh conditions of hammermilling limit the practicality of the fibers retaining certain compounds that may be used as treatment substances. For example, coating the fibers with mineral particulate, such as clay, would result in low clay retention with 30 hammermilling, but in the present invention retention may be significantly higher

( -11 due to the singulation being accomplished by air rather than mechanical means.

Further, the amount of surfactant used to treat pulp on a traditional pulp machine is limited due to the adverse affect on operations, however, there is no such limitation with the present invention. In traditional pulp machines, the surfactant decreases 5 the strength of the pulp web. If enough strength is lost, the pulp web can no longer be threaded through the traditional pulp machines.

The treatment substance delivered by treatment supply source48 may include, but is not limited to, surfactants, crosslinkers, hydrophobic materials, mineral particulates, superplasticizer, foams, other materials for specific end-use 10 fiber properties, and combinations of treatment substances. The term surfactant includes, but is not limited to oil in water emulsions; surfactants disclosed in U.S. App. No. 08/509,401 to Graef et al.; U.S. Pat. No. 3,554,863 to Hervey et al.; U.S. Pat. No.6, 074,524 to Wu etal.; U.S. Pat. No. 6,159,335 to Owens etal.; and Canadian Pat. No. 947915 to Angel etal.; all of which are expressly incorporated 15 herein by reference. Surfactants impart desirable properties to pulp fibers such as reducing fiber to fiber bonding, improving absorbency or reducing friction of finished webs. Surfactants are used in tissue and towel manufacturing, and are used extensively in the textile industry for numerous enhancements. The classes of surfactants include anionic, cationic, nonionic, or arnpholytic/zwitterionic surface 20 active materials. Examples of anionic surfactants include sodium stearate, sodium oleate, sodium dodecyl sulfate, sodium dodecyl benzene sulfonate, polyether sulfate, phosphate, polyether ester and sulfosuccinate. Examples of cationic surfactants include dodecylamine hydrochloride, hexadecyltrimethyl ammonium bromide, cetyltrimethyl-ammoniun bromide, and cetylpyridiniurn bromide. One 25 class of surfactant is cationic surfactants based on quaternary arnrnonium compounds containing fatty type groups. Examples of non-ionic surfactants include polyethylene oxides, sorbitan esters, polyoxyethylene sorbitan esters, and alkylaryl polyether alcohols. An example of ampholytic or zwitterionic surfactant is dodecyl betaine. Examples of commercial surfactant are EKA Chemicals Inc. l

-12 Berolcell 587K which is a cationic surface active agent and Process Chemicals, LLC Softener CWW which is a cationic surfactant used as a yarn lubricant.

The term crosslinker includes, but is not limited to, polyacrylic acid; glyoxol; crosslinkers disclosed in U.S. App. No. 08/509,401 to Graef et al.; and 5 U.S. App. No. 60/251,999 to Graef et al.; all of which are expressly incorporated herein by reference. The term hydrophobic material includes, but is not limited to, latex, sizing agents used to treat pulp such as alkyl ketone dimer or alkenyl succinic anhydride, waxes, oils, or other chemicals that react with the fiber and render the surface hydrophobic. The term mineral particulate includes, but is not limited to, 10 clay, calcinated clay, calcium carbonate, calcium sulfate, zinc oxide, talc, titanium dioxide, silicas, fly ash, sodium aluminosilicates, or other minerals. The term superplasticizer includes, but is not limited to, linear polymers that contain sulfonic acid groups, modified lignosulfonates, sulfonated melamine-formaldehyde condensates, sulfonated naphthalene-formaldebyde condensates, and 15 polycarboxylate derivatives. An example of a commercial superplasticizers include Boral Materials Technology Boral SP, a sulfonated naphthalene-formaldehyde condensate. The term foam includes, but is not limited to, foaming agents, foamed material, and foams disclosed in U.S. App. No. 09/569,380 to Graef et al., which are expressly incorporated herein by reference.

20 The treatment supply source 48 may also deliver more than one treatment substance, and may deliver treatment substances in any number of steps or stages.

For instance, the treatment substance may include binder molecules and particles, where the binder molecules are first applied to the fibers and then the particles are added to the binder molecule coated fibers thus binding the particles to the fibers 25 (as disclosed in U.S. Pat. No.5, 641,561 to Hansen etal., which is expressly incorporated herein by reference). Other fiber treatment substances and methods I known in the art may be used without departing from the present invention.

In addition to the embodiment described above, the pulp supply station 40 may be adapted so that the water contained in the pulp supply source42 is 30 exchanged for a solvent treatment substance. The term solvent includes, but is not

ill -13 limited to, alcohols, ketones, ethers, alkanes, aromatics, aldehydes, or other classes of organic materials. The solvent used may be recovered at the fiber separation station 100 Additional treatment substances may be added to cause an in situ 5 precipitation. When in situ precipitation is desirable, a first mineral treatment substance is added to the pulp, then a second treatment substance is added to the pulp. The first and second treatment substances react to form a precipitate treatment substance. For example, dissolved calcium hydroxide may be used as the first treatment substance and dissolved sodium bicarbonate may be used as the 10 second treatment substance. The calcium hydroxide and sodium bicarbonate react to precipitate calcium carbonate. Other precipitate treatment substances may be formed for treating the pulp including, but is not limited to, calcium aluminum silicates, calcium aluminum carbonates, calcium alurninuTn phosphates, or other mineral precipitates.

15 The pulp supply station 40 may include a second dewatering device 50. The second dewatering device 50 is inserted in pulp feed conduit44 to be in flow communication with the first dewatering device46. The second dewatering device 50 may include, but is not limited to, devices such as a screw press, belt press, continuous centrifuge, batch centrifuge, double roll press, or other similar 20 device. Like the first dewatering device46, the second dewatering device 50 removes a portion of the fluid so the feed pulp has a consistency of 10-55%, preferably 30-50%, prior to drying the feed pulp by the jet drier 20. The partially dewatered feed pulp is then transported to the jet drier 20 by pulp feed conduit 44.

Altematively, the second dewatering device 50 itself may serve as a conveyance 25 device. For example, a screw press could be used to simultaneously dewater and transport the feed pulp to the jet drier 20.

The second dewatering device 50 further dewaters the treated feed pulp,potentially removing a portion of the treatment substance from the pulp. To recover a portion of the separated treatment substance, a treatment recycle conduit 52 may 30 be connected in flow communication between the second dewatering device 50 first

I -14 dewatering device 46 and/or the treatment supply source 48. The incorporation of treatment substance with the pulp may be accomplished through the agitation supplied by the first and/or second dewatering devices 46 and 50.

Alternatively, the pulp supply station 40 may include a holding tank 5 device 54. The holding tank device 54 may be inserted in recycle conduit 52 to be in flow communication with the second dewatenng device 50. The holding tank device 54 acts as a reservoir to store separated treatment substance from the second dewatering device 50 and disperse the stored separated treatment substance to the first dewatering device 46 and/or to the treatment supply source 48.

10 The pulp supply station 40 may include a second material handling fan S6 inserted in flow communication into pulp feed conduit 44. After dewatering, the feed pulp may be run through the second material handling fan 56 to break apart the larger pieces of feed pulp into pieces of less than 2 inches in nominal diameter, prior to introduction into the jet drier 20. The second material handling fan 56 may

15 be any de-flaking device, including but not limited to, a buster fan, a pin Bluffer, a material handling fan, or a shredder.

The pulp supply station 40 further includes a pulp feed device 60 coupled in flow communication with pulp feed conduit 44 and jet drier 20 pulp intake 24. The pulp feed device 60 is a wet pulp delivery apparatus that can produce a regulated 20 continuously consistent supply of feed pulp at a desired feed rate to the pulp intake 24 of the jet drier 20. The feed pulp has been previously dewatered and in some cases treated. The feed rate of feed pulp is a process variable that has a direct affect on process air temperature, process air pressure, end product fiber appearance, and end product fiber knot count. The pulp feed device 60 is a device 25 that separates atmospheric air from an environment of a higher or lower pressure inside the jet drier 20, and/or separates ambient temperatures from an environment of higher temperatures inside the jet drier 20. The pulp feed device 60 allows a continuous input of feed pulp to pass through to the jet drier 20 with a minimum flow of atmospheric air entering the jet drier 20.

-15 Refernog to FIGURE 3, the pulp feed device 60 may be a rotary air lock 62 having a rotor 64 with rotor vanes 66 rotatably mounted within a rotor housing 68.

One suitable rotary air lock62 for use in the present invention is a modified stainless steel Prater Industries Rotary Air Lock Feeder model number PAV-6C 5 having a rotor housing, and a CLSD,SS,PAV-6 rotor with six rotor vanes.

Referring to FIGURE 4, the Prater Industries rotor vanes were supplied from the manufacturer with a standard clearance 69 between the leading edge of each vane and the rotor housing68 of less than.010 inches. The rotor with a standard clearance between rotor vanes 66 and housing68 causes the feed pulp to jam 10 between the rotor vanes66 and the housing68. Therefore the Rotary Air Lock Feeder was refitted with a six vane closed end rotor 64 that has reduced diameter.

This reduction in diameter provides more clearance 69 between the vanes 66 and rotor housing 68 so the feed pulp can be run through the pulp feed device 60 without damaging fibers or jamming the pulp feed device 60. Additionally, the 15 vanes 66 were reshaped from having a radial end, to having a flat end perpendicular to the radius of each vane 66. Without being bound by theory, it is believed that the flat ends of the vanes 66 reduced jamming of the pulp feed device 60 by providing an edge to shear fiber clumps of the feed pulp. It was found that if the Prater Industries rotor vanes had.050 inch removed from the centerline radius of each 20 vane 66 having a rounded end, resulting in a.030 inch clearance 69 between the leading edge of each vane 66 and the rotor housing 68, rotor jamming as well air leakage around the rotor64 were minimized. A clearance69 from.010 to.050 inches should be effective for minimizing rotor jamming as well air leakage around the rotor 64.

25 Referring to FIGURES 2, 5, and 6, the pulp feed device 60 may feed pulp to the jet drier 20 via a foam feeder 70. The foam feeder70 may be interposed between the pulp feed device 60 and the pulp intake 24 for mixing a surfactant with pulp and directly injecting foamed pulp mixture into the jet drier 20. The foam feeder 70 is a mechanical mixer that takes pulp feed, adds a surfactant treatment 30 substance and air to the pulp, and mechanically agitates the surfactant to suspend

-16 the pulp fibers in a foam medium. The foam feeder 70 includes a mechanical mixer main body71, a pulp injection port72, a surfactant injection port73, an air injection port74, and a foam outlet conduit75. The mechanical mixer main body 71 may be any suitable mechanical mixer known in the art. The pulp injection 5 port72 is in flow communication between the pulp feed device 60 and the mechanical mixer main body 71. The pulp injection port 72 supplies pulp feed to the mechanical mixer main body71. The surfactant injection port 73 is in flow communication between the treatment supply source 48 and the mechanical mixer main body 71, and is placed in close proximity with the pulp injection port 72. The 10 surfactant injection port 73 supplies surfactant treatment substance to the mechanical mixer main body 71. The air injection port 74 is in flow communication between a pressurized air source 79 and the mechanical mixer main body 71, and is placed in close proximity with the surfactant injection port 73. The air injection port 74 supplies supply air to the mechanical mixer main body 71. The 15 foam outlet conduit 75 is in flow communication between the mechanical mixer main body71 and the jet drier20 pulp intake24. The foam outlet conduit75 discharges the pulp fibers suspended in foam from the mechanical mixer main body 71 and delivers them to the jet drier 20 pulp intake 24. To optimize the flow of the pulp fibers suspended in foam from foam outlet conduit 75, the foam outlet 20 conduit75 diameter, conduit shape, outlet shape, length inserted into the jet drier 20, and/or angle of insertion into the jet drier 20 may be adjusted.

The foam outlet conduit 75 may be sealed to the jet drier 20 pulp intake 24 by a pulp intake seal 76. The pulp intake seal 76 may be supplied with an air leak conduit 77 connected to the pulp intake seal 76 and running from the jet conduit 22 25 to ambient air. The air leak conduit 77 provides a limited path between the jet conduit 22 and ambient air. The conduit may be supplied with a conventional air valve for adjusting the leakage amount. Without being bound in theory, it is believed that the air leak conduit 77 provides a limited pressure relief to the jet conduit 22 and prevents unstable operating conditions within the jet conduit 22.

/ -17 Optionally, the foam feeder 70 includes a treatment injection port 78 in flow communication between the treatment supply source 48 and the mechanical mixer main body 71. The treatment injection port 78 may supply an additional treatment substance to the mechanical mixer main body 71. The treatment injection port 78 5 may be located any where along the mechanical mixer main body 71.

Referring to FIGURE 6, one suitable foam feeder 70 for use in the present invention is a redesigned and modified OAKES mechanical mixer for feeding feed pulp fibers suspended in a foam medium. The foam feeder 70 includes a front stator 80, a rear stator 82, a foaming rotor 84, and a drive shaft 86 driven by a 10 motor 87 (shown in FIGURE 5). The front stator 80 is connected about the pulp injection port 72 and defines a circular plane about the pulp injection port 72. The front stator80 has multiple circular rows of teethed extending perpendicularly from the circular plane of front stator 80. These multiple circular rows of teeth 81 are spaced apart, the spaces fomning channels between the rows of teeth 81. The 15 rear stator 82 is connected about the foam outlet conduit 75 and defines a circular plane about the foam outlet conduit 75. The rear stator 82 has multiple circular rows of teeth 83 extending perpendicularly from the circular plane of rear stator 82.

These multiple circular rows of teeth 83 are spaced apart, the spaces forming channels between the rows of teeth 83. The foaming rotor 84 defines a circular 20 plane and has multiple circular rows of teeth 85 extending perpendicularly from both sides of the foaming rotor 84. One set of the foaming rotor 84 circular rows of teeth 85 fit within the channels formed by the front stator80 circular rows of teeth 81. Likewise the other set of the foaming rotor 84 circular rows of teeth 85 fit within the channels formed by the rear stator 82 rows of teeth 83. This allows the 25 foaming rotor 84 to be rotatably associated with both the front and rear stators 80 and 82. The front and rear stators 80 and 82 are connected together about foaming rotor 84, and the foaming rotor 84 is rotatably associated with both the front and rear stators 80 and 82. The drive shad 86 is connected to the center of the foaming rotor 84 and runs from the foaming rotor 84, through the foam conduit 75, and to 30 motor 87 (shown in FIGURE 5).

-18 Referring now to both FIGURES 5 and 6, As pulp feed is forced from the pulp injection port 72 into front stator 80, the pulp feed contacts the stationary teeth 81 of front stator 80 and the rotating teeth 85 of foaming rotor 84. The pulp is forced out from the pulp injection port 72 along the surface of the front stator 80, 5 around the rotating foaming rotor 84, along the surface of the rear stator 82, and out the foam outlet conduit 75. While the pulp is in contact with the front stator 80, the surfactant treatment substance is forced from the surfactant injection port 73 into contact with the pulp feed front stator teeth 81 and the foaming rotor teeth 85. The supply air is also forced from the air injection port 74 into contact with the pulp 10feed, front stator teeth 81, and the foaming rotor teeth 85. The foaming rotor 84 mixes the pulp feed, surfactant and air together. The mechanical agitation of the foaming rotor 84 causes the pulp feed fibers to be suspended in a foam. The foamed pulp feed may then be fed directly into the jet drier 20 via the foam outlet conduit 75. The consistency of the foamed feed pulp may be 30% or less.

15Referring to FIGURE 6, optionally, drive shaft 86 is connected to the center of the foaming rotor 84 by an auger head 88. The auger head 88 has a generally conical shape, and may have a protrusion 89 from the face of the conical surface of auger head 88. The auger head 88 serves to force the pulp feed from pulp injection port 72 toward the rotating teeth 85 of foaming rotor 84. The protrusion 89 serves 20 to break up the pulp feed and enhance mixing of the pulp feed with the surfactant treatment substance.

The OAKES mechanical mixer was modified by placing the foam outlet conduit 75 at the original inlet of the OAKES mechanical mixer. Without being bound in theory, it has been found that superior mixing is achieved when the pulp 25 injection port 72 has a greater diameter than foam outlet conduit 75. The original outlet of the OAKES mechanical mixer was enlarged to increase flow of feed pulp into pulp injection port 72, and to place the feed pulp in contact with the teeth 85 of rotor 84. The OAKES mechanical mixer, originally came equipped with a nut for connecting the drive shaft 86 to the center of the foaming rotor 84; and this was 30 replaced by the auger head 88 above. Additionally, several rows of teeth (81, 83,

( -19 and 85) were removed from the OAKES mechanical mixer to improve mixing and increase throughput.

Referring again to FIGURE 2, the air supply station 90 may include an air pump 96 and an air heater 98. The air pump 96 receives supply air via the air 5 supply source 92 and is coupled in flow communication with air feed conduit 94.

The air heater 98 is inserted into air feed conduit 94 and in flow communication with air pump 96 and the jet drier 20 manifold 26 via air feed conduit 94.

The air pump 96 may be a positive displacement high volume air pump that delivers the supply air at a positive air pressure and at a fixed volume to the air 10 heater 98. One suitable air pump 96 for use in the present invention is a Roots-

Dresser universal rotary lobe blower system (model number 45 URAI) with inlet silencer type CCF-4 with a paper element, a discharge silencer type Universal SD-4, filtration and electric 15 hp drive motor. The flow rate may be 300 SCFM.

The delivered pressure may be 5 PSIG. The pump speed may be 3176 RPM. The 15 drive motor may run at 1800 RPM. The air pump 96 may have a gauge range of 0 to 15 psig and it may be fitted with a pressure relief valve set at 6 psi". The air heater 98 heats the supply air and delivers the feed air to the manifold 26 of the jet drier 20. The manifold 26 may feed the feed air tangentially into the jet drier 20 conduit 22 loop for the purpose of creating turbulence for fiberizing-and drying the 20 feed pulp inside the jet drier 20.

The air heater 98 may be a flow through type heater that is controlled to regulate the air temperature supplied to the jet drier manifold 26 nozzles that feed the conduit 22. The air heater 98 may be an electric heater, a gas heater or any other form of heater. One suitable air heater 98 for use in the present invention is a 25 Watlow Electric Immersion heater, model number 700-96BD2459 that uses 480 VAC line voltage, and has a pressure rating of 150 psig at 1,050 F. The air heater 98 over temperature protection uses a type K thermocouple and a Watlow series 92 controller. The air heater 98 process temperature regulator uses type J thermocouples and Watlow series965 auto tuning controller. The process air

-20 temperature is a process variable that has a direct affect on end product fiber appearance, end product fiber knot count, and fines content.

Upon exiting the jet drier20, the outlet air, fibers, and fines may be transported along the outlet flow conduit 30 to be recovered by the fiber separation 5 station loo. The fiber separation station loo may be a vacuum conveyorllO slidably associated with outlet flow conduit 30 through a head box 140. The vacuum conveyor 110 includes a screen 112, a first roller 118, a second roller 120, a primary fan vacuum box 122, a primary fan 128, a secondary fan vacuum box 130, and a secondary fan 134.

10 The vacuum conveyorllO screenll2 is a porous conveyor belt device which passes the outlet air and fines through the screen 112 while preventing the flow of fiber through the screen 112. The screen 112 is a continuous loop rotatably coupled to the first rollerll8 and the second rollerl20. The screenll2 thus provides a screen upper portion 113 having a screen upper surface 114 and a screen 15 lower surface 116, and a screen lower portion 117. The outlet flow conduit 30 from the jet drier 20 is slidably associated with the vacuum conveyor 110 by the head box 140 so that the outlet flow conduit 30 is in flow communication with the upper surface 114 of the screen 112. The outlet flow conduit 30 delivers fibers, fines, and outlet air to the upper surface 114. The screen 112 passes the outlet air through the 20 upper surface 114 while retaining fibers on the upper surface 114. A fraction of the fines may be passed through the screen 112. Altematively, the screen 112 may collect the fines by trapping them in the mat of fibers as the mat is fommed in the outlet flow conduit 30 on the moving conveyer screen 112. This trapping of fines may result in a level of fines and opacity that does not require subsequent fines 25 removal at the fines removal station 170. The rotating screen 112 transports the fibers from the outlet flow conduit30 toward the fiber collection station 160, defining an upstream to downstream flow of fibers.

Referring to FIGURES7 and8, the primary fan vacuum boxl22 is a plenum that allows passage of outlet air and fines from the outlet flow conduit 30 30 through the screen to the primary fan 128. Referring to FIGURE 7, the primary fan

-21 vacuum box 122 has an inlet 124 and an outlet 126. The primary fan vacuum box inletl24 is positioned below the screenll2 upper portionll3 and slidably associated with the lower surfacell6 of screenll2 directly under the head box 140, and is thus in flow communication with outlet flow conduit 30 through 5 head box 140 and screen 112. The inlet to the primary fan vacuum box 122 is matched in size to the head box 140 to allow the head box 140 to seal against the primary fan vacuum box 122 conduit opening while allowing the screen 112 to freely pass therebetween without allowing tramp air to affect the vacuum generated by the primary fan 128.

10 Referring to FIGURE2, The vacuum conveyorllO primary fanl28 is coupled in flow communication between the primary fan vacuum box outlet 126 and fines conduit 172. The primary fan 128 pulls the outlet air from the outlet flow conduit 30, through the head box 140, through the screen 112 upper surface 114, through the primary fan vacuum box 122, and to the primary fan 128 for expulsion 15 to fines conduit 172. The primary fan vacuum box 122 allows the primary fan 128 to generate enough vacuum on the jet drier 20 to transport the fiber from the jet drier 20 to the screen 112. The porous conveyor screen 112 retains a portion of the fibers from passing through to the primary fan 128. The porous conveyor screen 112 conveys the fibers away from the outlet flow conduit 30 and toward the 20 second roller 120, by rotating about the first and second rollers 118 and 120. The fibers thus form a mat on the screen upper surface 114.

The vacuum or negative pressure is defined herein as the null. The null is an internal positive or negative pressure inside the jet drier 20 that is measured in the centrifugal part of the process air stream near the pulp intake 24 and between 25 the pulp intake 24 and the fiber outlet 28 of jet drier 20. The null is a process control variable that has a direct affect on the through put of the jet drier 20 and the knot count of the fibers. The main variables that affect null are as follows: the vacuum generated by the primary fan 128 on the jet drier 20, feed rate of the feed pulp into the jet drier 20, moisture content of the feed pulp, non- uniformity in pulp 30 size and shape, screen 112 speed and mesh size, pulp type and treatment, damper

-22 settings on the primary fan 128, and the temperature of process air fed into the jet drier 20 at the manifold 26. The screen 112 speed is a process control variable that has a direct affect on null. The rate at which the screen 112 transports the fibers from the outlet flow conduit 30 determines the thickness or density of the mat of 5 fibers being formed on the upper surface 114 of screen 112. The density of this mat of fibers constricts the volume of outlet air flowing through the system thus affecting the null. The jet drier20 null is preferably maintained from -I to -5 inches of water.

The primary fan 128 may be a side intake, high temperature, high volume 10 exhaust fan. One suitable primary fan 128 for use in the present invention is a steel high temperature side intake material handling fan with a 10 hp motor with 460 VAC line voltage and may be connected with airtight seals to the primary fan vacuum box 122. An adjustable damper at the exhaust side controls the level of airflow through the primary fan 128 which has a direct affect on the jet drier 20 15 null, and therefore affects the end product fiber appearance and knot count.

Referring to FIGURES 7 and 8, the secondary fan vacuum box 130 is a plenum that allows the secondary fan 134 to pull air through the screen 112 to provide suction on the upper surface 114 of screen 112. Referring to FIGURE 7, the secondary fan vacuum box 130 has an inlet 131 and outlet 132. The secondary 20 vacuum box inlet 131 is slidably associated with the lower surface 116 of the screen 112 and is positioned below the upper portion 113 of screen 112 downstream from the primary fan vacuum box 122. The inlet to the secondary fan vacuum box 130 is positioned just downstream of the terminus of the head box 140. The secondary vacuum box outlet 132 is in flow communication with the secondary 25 fan 134.

It will be understood that although the vacuum conveyorllO has been described as having primary and secondary fans 128 and 134, a single fan device with dampers may serve as both the primary and secondary fans 128 and 134 without departing from the present invention. The fan vacuum boxes 122 and 130

( -23 may have a honeycomb shaped bame to distribute the intake of fresh air through the mat of fibers on the screen upper portion 113.

Referring to FIGURE 2, the vacuum conveyor 110 secondary fan 134 is coupled in flow communication between the secondary fan vacuum box outlet 132 5 and fines conduit 172. The secondary fan 134 provides a vacuum which pulls on the mat of fibers being conveyed on the upper surface 114. The secondary fan 134 pulls air through the screen 112, through the secondary fan vacuum box 130, and to the secondary fan 134 for expulsion to fines conduit 172. The porous conveyor screen 112 prevents the fibers from passing through to the secondary fan 134. The 10 secondary fan 134 retains the mat of fibers on the screen 112 while the screen 112 is in motion and aids in the extraction and transport of the mat of fibers by creating a vacuum that is strong enough to prevent the primary fan 128 from pulling fibers back into the head box 140. Without the secondary vacuums 134 to hold the mat of fibers intact, the vacuum created by the primary fan 128 in the head box 140 may 15 pull the mat of fibers back into the head box 140. Without the secondary vacuum 134 the result could be an inconsistent mat density inside the head box 140 causing a fluctuation in null resulting in non-uniform mat of fibers, inconsistent fiber separation in the end product, and, eventually, process shut down due to a plugging of the head box 140 with excess fiber.

20 The secondary fan 134 may be a side intake low velocity exhaust fan. One suitable secondary fan 134 for use in the present invention is a fan manufactured by Buffalo with a '/. hp motor with 110 VAC line voltage. It has variable speeds and may be connected with airtight seals to the secondary fan vacuum box 130.

Referring to FIGURES 7 and 8, the vacuum conveyor 110 includes a 25 support structure 135. The support structure 135 provides a surface to support the moving screen 112. The support structure 135 is shown extending between and supporting the first roller 118 and the second roller 120, along the same plane as that of the screen lower surface 116. The openings of the vacuum boxes are located in the support surface 135. It will be understood that, although shown as a single

-24 object, the support structure 135 may comprise many separate support structures unassociated with one another.

The vacuum conveyor 110 may optionally include a screen vacuum 137.

The screen vacuum 137 removes any residual fibers from the screen 112 before the 5 screen 112 receives new fibers from outlet flow conduit 30. The screen vacuum 137 may be located anywhere along screen 112 aRer the fiber mat has been removed. In one embodiment, the screen vacuum 137 is a vacuum manifold slidably associated with the upper surface 114 of screen 112, upstream of the head box 140. One suitable screen vacuum 137 for use in the present invention is a Sears 10 Shop Vacuum and an unmodified vacuum attachment. Alternatively, the primary fan 128 may be used as the vacuum source for the screen vacuum 137. In another embodiment, an air supply device may be positioned on the opposite side of screen 112 from the screen vacuum 137 to force air through the screen 112 and into the screen vacuum 137.

15 The vacuum conveyor 110 may optionally include a separation device 138.

The vacuum conveyor 110 separator device may be a thin physical barrier running across and slidably associated with the upper surface 114 of the screen 112 above the downstream end of the secondary vacuum box 130. The separation device 138 serves to loosen the collected mat of fibers from the upper surface 114 of the 20 screen 112 so that the fibers may easily be removed from the screen 112, for instance by gravity, at the vacuum conveyor 110 terminal end adjacent roller 120.

The separator device 138 may also separate the entangled mat of fibers from the screen 112 and re-lay the mat on the screen 112 without changing the physical properties of the mat of fibers. The fibers may then be collected at the fiber 25 collection station 160 into a bulk mass which can be compressed into a bale for shipping to a customer. One suitable separation device 138 for use in the present invention is a blade made from Teflon sheet 0.030 inches thick by 2 inches wide placed at a 45 degree angle across the screen 112 at the downstream end of the secondary fan vacuum box 130 and secured at both ends of the separation 30 device 138 to the support structure 135.

-25 Alternatively, the separation device 138 may be a gas blowing device operatively associated with the screen 112, and located beneath the screen 112 downstream from the secondary vacuum box 130. The gas blowing separation device 138 would force gas up through screen 112 to separate the mat of fibers 5 from the screen.

The fiber separation station 100 includes a head box 140 coupled to the end of the outlet flow conduit 30, for slidably associating outlet flow conduit 30 with screen 112. The head box 140 is an apparatus where the separation of entrained fibers and outlet air occurs. In one embodiment, the head box 140 has a vacuum 10 tight seal against upper surface 114 of the screen 112 where the outlet air and fines are removed. The fibers are trapped on the moving screen 112 and the outlet air and fines pass through the mat of fiber and through the screen 112.

Referring to FIGURE 9, the head box 140 includes a head box shell 142, an out feed roller 145 and a dynanuc lip seal 146. The head box shell 142 is in flow 15 communication between the outlet flow conduit 30 and the upper surface 114 of the screen 112. The head box 140 out feed roller 145 is positioned at the downstream end of head box shell 142 (also referred to as the outlet side of the head box shell 142). The head box 140 out feed roller 145 is rotatably and movably coupled to the head box shell 142, and rollably associated with the upper surface 114 of the 20 screen 112. The dynamic lip seal 146 is positioned above the out feed roller 145 at the downstream end of box shell 142. The dynamic lip seal 146 is hingedly coupled to the head box shell 142, and slidably associated with the out feed roller 145.

The head box 140 may be composed of a low friction material, wherever moving parts are in contact. For instance, the head box shell 142 may be composed 25 of Teflon where the head box shell 142 contacts the screen 112. Additionally, the head box shell 142 may be composed of Teflon where the head box shell 142 contacts the out feed roller 145.

The head box shell 142 preferably includes vertically oriented slots 143.

The axles of the out feed roller 145 are positioned in the slots 143. The slots 143

( -26 allow the out feed roller 145 to move in an up and down manner to adjust for the varying thickness of the fiber mat on screen 112.

The out feed roller 145 is positioned at the downstream end of head box 140 to provide a force for pulling the fibers along the screen 112 and out of the head 5 box 140. The out feed roller 145 may otherwise be a belt or rotor, or other similar device. The out feed roller 145 may be powered by any conventional source. The bottom surface of the out feed roller 145 provides an additional force for pulling the fibers along the screen 112and out of the outlet flow conduit 30. The out feed roller 145 may be made from Teflon coated steel.

10 The dynamic lip seal 146 allows the head box 140 to maintain a vacuum tight seal against upper surface 114 of the screen 112. The dynamic lip seal 146 seals the out feed roller 145 to the head box shell 142. This design allows the out feed roller 145 to rotate and travel vertically to compensate for non-uniform mat of fiber thickness at the out feed of the head box 140, without drawing tramp air from 15 around the out feed roller 145. The dynamic lip seal may be made from an inflexible piece 147 joined to a flexible piece 149 by a pivot portion 148. The pivot potion 148 is rotatably coupled to the head box shell 142. The inflexible piece 147 moves up and down in response to the motion of out feed roller 145. The flexible piece 149 allows the inflexible portion to move, while maintaining a vacuum seal 20 against the head box shell 142. The inflexible piece 147 and the flexible piece 149 may be formed of Teflon having differing thickness.

Optionally, the head box 140 further may include a pair of drive wheels 150 for driving the out feed roller 145. The drive wheels 150 are rotatably coupled to the upstream end of head box shell 142, in driving communication with the out feed 25 roller 145, and also in mechanical communication with the screen 112. The drive wheels 150 rotate in response to the movement of screen 112 and transfer that movement to the out feed roller 145 to rotate the out feed roller 145. The drive wheels 150 drive the out feed roller 145 with the use of a coupling device 151. The coupling device 151 may be a chain coupling or any other device capable of 30 mechanically associating the drive wheels 150 and out feed roller 145 to turn in

-27 unison. It is preferred that the drive wheels 150 be coupled to the out feed roller 145 at a 1: I ratio, to enable the surface of out feed roller 145 to rotate at the same rate as screen 112.

The head box 140 may also include a height adjustment structure 154. The S height adjustment structure 154 is connected to the head box shell 142 and to the support structure 135. The height adjustment structure 154 enables space between the head box shell 142 and screen 112 to be adjusted. The height adjustment structure 154 includes a frame 155, an adjustment nut 156, and an adjustment bolt 157. The frame lSS is connected to the head box shell 142. The adjustment 10 bolt 157 is connected to the support structure 135. The adjustment nut 156 is adjustably connected to the adjustment bolt 157 and is also connected to the frame ISS. As the adjustment nut 156 is adjusted along the adjustment bolt 157, the adjustment nut 156 acts on the frame 155 to increase or decrease the space between I the head box shell 142 and screen 112.

15 Alternatively the fiber separation station 100 may be a cyclone, bag house, or other similar device for removing fines and fiber together from outlet air. The fiber separation station 100 may then recycle the separated outlet air back to the air supply station90. In this embodiment, the fines removal station 170 may be located upstream along conduit 30, to remove the fines from the fibers prior to the 20 fibers being recovered at the fiber separation station 100.

Referring again to FIGURE 2, the drying system 10 fines removal station 170 receives outlet air and fines from the fiber separation station 100. The fines removal station 170 is coupled in flow communication with the fines conduit 172 and the air conduit IX2. The fines removal station receives fines and 25 outlet air from fines conduit 172, removes at least a portion of the fines, and discharges the outlet air to the air conduit 182. The fines removal station 170 may then recycle the outlet air back to the air supply station 90. The fines removal station 170 may be a cyclone, bag house, or other similar device.

Alternatively, the fines removal station 170 is coupled to the outlet flow 30 conduit 30 between the jet drier 20 and the fiber separation station 100. The fines

( -28 removal station 170 in this embodiment may include a cyclone smilar to that used as a dust collector for sawdust in wood shops. The fines removal station 170 receives outlet air, fines, and fibers from the jet drier; removes at least a portion of the fines; and sends the fiber coming from the jet drier 20 to the fiber separation 5 station 100. The fines removal station 170 of this embodiment may further include a second cyclone, bag house, or other similar device located at the primary and secondary fan 128 and 134 outlets. This second cyclone may also receive the filtered fines exhaust from the first cyclone.

The drying system 10 noise reduction station 180 is inserted into air 10 conduit 182 and in flow communication with the fines removal station 170 via air conduit 182. The noise reduction station 180 provides a reduction in the noise produced by the drying system 10. The noise reduction station 180 receives outlet air from the fines removal station 170 via air conduit 182, absorbs kinetic energy from the outlet air, and discharges the outlet air via air conduit 182. The discharged 15 outlet air may be vented to the atmosphere or recycled to the air supply station 90.

Alternatively the noise reduction station 180 is directly coupled to the primary and secondary fans 128 and 134. The noise reduction station 180 may be a cyclone ducted to the exhaust from the primary fan 128. The exhaust from the primary fan 128 is discharged into the input side of the cyclone and the cyclone 20 outlet ports are independently vented to atmosphere. The exhaust from the secondary fan 134 may be vented to the cyclone or to the cyclone outlet ports.

Additionally, the fines removal station 170 may also serve as a noise reduction station. The drying system 10 described above forms singulated and dried fibers.

25 The process takes wet pulp directly from a pulp mill and produces a singulated product from the never-dried pulp by using a drying process that singulates the pulp directly. This avoids the intermediate steps of the pulp drier, handling of the pulp reels and rolls, and hammermilling in a traditional process. The drying system 10 produces fibers having a low knot and fines content. These fibers also have 30 physical characteristics such as kink, curl, and twist that are more pronounced than

( -29 fibers processed by harnmermilling. The drying system I O also produces fibers that have been treated with a treatment substance. The treatments that can be performed on the pulp may be difficult or impossible to perform on a roll of dried pulp.

Treatments can be done on the pulp that reduce the amount of knots, increase 5 production rate, and/or form fibers having desirable characteristics.

It is preferred that the dried and singulated fibers produced in drying system 10 have a knot count equal to or less than 5%, more preferably equal to or less than 2%, more preferably equal to or less than 1.6%, and most preferably equal to or less than.73%. Where the fibers have been treated with a treatment substance 10 selected from the group consisting of surfactant, crosslinker, or hydrophobic material; the fibers have a knot count equal to or less than 5%, and preferably equal to or less than 2%. Where the fibers have been treated with a treatment substance I selected from the group consisting of mineral particulate, surfactant, crosslinker, or hydrophobic material; the fibers have a knot count equal to or less than 5%, 15 preferably equal to or less than 2%; and more preferably equal to or less than 1.6%.

It is preferred that the dried and singulated fibers produced in drying system 10 have a fines count equal to or less than 21%, more preferably equal to or less than 15%, and most preferably equal to or less than 14%. Where the fibers have been treated with a treatment substance selected from the group consisting of 20 surfactant, crosslinker, or hydrophobic material; the fibers have a fines count equal to or less than 21%, preferably equal to or less than 15%, and more preferably equal to or less than 14%. Where the fibers have been treated with a treatment substance selected from the group consisting of mineral particulate, surfactant, crosslinker, or hydrophobic material; the fibers have a fines count equal to or less than 21%.

25 It is preferred that the dried and singulated fibers produced in drying system 10 have low knot counts, high accepts counts, and low fines counts. Where the fibers have been treated with a treatment substance selected from the group consisting of surfactant, crosslinker, or hydrophobic material; the fibers have a knots count equal to or less than 5%, an accepts count equal to or greater than 80%, 30 and a fines count equal to or less than 15%; preferably a knots count equal to or less

-30 than 5%, an accepts count equal to or greater than 80%, and a fines count equal to or less than 14%; more preferably a knots count equal to or less than 5%, an accepts count equal to or greater than 85%, and a fines count equal to or less than 15%; and most preferably a knots count equal to or less than 2%, an accepts count equal to or 5 greater than 80%, and a fines count equal to or less than 15%. Where the fibers have been treated with a treatment substance selected from the group consisting of mineral particulate, surfactant, crosslinker, or hydrophobic material; the fibers have a knots count equal to or less than 2%, an accepts count equal to or greater than 77%, and a fines count equal to or less than 21%; and preferably a knots count 10 equal to or less than 1.6%, an accepts count equal to or greater than 77%, and a fines count equal to or less than 21 %.

The dried and singulated fibers produced in drying system 10 may be used in any number of end products including but not limited to absorbent articles, concrete products, plastic products, filter product, and paper products. Referring to 15 FIGUREIO, the absorbent article210 includes a pervious top portion212, an impervious bottom portion214, and an absorbent layer216 located between the pervious top portion 212 and the impervious bottom portion 214. The absorbent layer 216 includes singulated and dried fibers 218. It will be understood that the term absorbent article, as used herein, includes but is not limited to diapem, 20 tampons, sanitary napkins, incontinence guards, and bandages.

Referring to FIGURE 11, the concrete product220 includes a concrete matrix 226 having singulated and dried fibers 228 incorporated therein. It will be understood that the term concrete products, as used herein, includes but is not limited to cement, concrete, mortars, precast material, high strength cement 25 products, extruded cement products, gypsum products, and any other cemeticious material. It will be understood that while FIGURE 11 has been illustrated as a concrete product 220, FIGURE 11 may also show a plastic product 220 including a plastic matrix 226 having singulated and dried fibers 228 incorporated therein. It will be understood that the term plastic products, as used herein, includes but is not 30 limited to plastics and rubbers.

-31 Referring to FIGURE 12, the paper product 230 includes a paper sheet 236 having singulated and dried fibers 238 incorporated therein. It will be understood that the term paper products, as used herein, includes but is not limited to paper and paperboard. It will be understood that while FIGURE 12 has been illustrated as a 5 paper product 230, FIGURE 12 may also show a filter product 230 having singulated and dried fibers 238 incorporated therein.

EXAMPLES

In the processing of pulp into dry singulated fibers used in the examples below, several process conditions were evaluated. The effects of variations in the 10 jet drier temperature, feed rate, treatment application, types of pulp, feed rate, and pre-drying dewatering methods were all explored in the Examples below.

Urrless otherwise noted, the apparatus used for the Examples below is as follows: pulp was dried and singulated into fibers using a Fluid Energy Abet Model 4 Thermajet, X0870L jet drier. No modifications were made to the Model 4 15 Thermajet. The pulp was fed to the jet drier in several different apparatuses. For large runs a shaftless screw conveyor manufactured by Martin Sprocet and Grear, Inc., Martin Conveyor Division was used. It had a hopper at the lower end of the conveyer for placing the wet pulp, and conveyed the wet pulp up an incline that rose up towards the pulp feed device on the jet drier. For runs of low quantities of 20 pulp, a Weyerhaeuser designed and manufactured conveyor with hopper type feeder for feeding wet pulp was used. For feeding fibers suspended in a foam medium a Weyerhaeuser redesigned and modified CAKES mechanical mixer was used to directly inject foamed pulp into the jet drier.

In Examples 1-9, the feed pulp used was a pressed wet web of pulp having a 25 basis weight of a substantial amount to provide sufficient stiffness to feed the web into a shredding device. The wet web was produced on a pilot paperrnachine that had a spray system attached to it to allow treatment of the wet web prior to pressing. A basis weight of 500 to 1500 gem was found to work adequately. The web was fed into the shredding device through a rotating and reversible roller nip

( -32 and into a rapidly rotating set of rolls containing protruding pins that tore the web into small pieces of pulp.

The feed pulp was delivered to the jet drier using a stainless steel Prater Industries Rotary Air Lock Feeder model number PAV-6C having a rotor housing, 5 and a CLSD,SS,PAV-6 rotor with six rotor vanes. The refitted rotor was a custom modified six vane closed end rotor that was reduced in diameter to give more clearance between the vane and rotor housing so wet pulp could be run through the feeder without damaging fibers or jamming the rotor.

The feed air was delivered to the jet drier with a Roots-Dresser universal 10 rotary lobe blower air pump with silencer and filtration. The model number was 45 URAI. The flow rate was 300 SCFM. The delivered pressure was 5 PSIG. The pump speed was 3176 RPM. The drive motor was an electric Lincoln 15 hp that was running at 1800 RPM. The air pump had an inlet silencer type CCF-4 with a paper element and a discharge silencer type Universal SD-4. The assembly had a 15 gauge range of O to 15 psig and it was fitted with a pressure relief valve set at 6 psi".

The feed air was heated with a Watlow Electric Immersion air heater, model number 700-96BD2459. The air heater used 480 VAC line voltage, and had a pressure rating of 150 psig at 1,050 F. The over temperature protection used a 20 type K thermocouple and a Watlow series 92 controller. The process temperature regulator used type J thermocouples and Watlow series 965 auto tuning controller.

A material handling fan (MHF) was placed in the ducting between the jet drier and the vacuum conveyer. The MHF was used in Examples 1-8, but was not used in Examples 9-24.

25 The outlet air, fibers and fines were delivered to a custom designed vacuum conveyor via a head box sealed to the conveyor screen. A Sears Shop Vacuum with an unmodified vacuum attachment was used for the screen vacuum. The primary fan was a steel high temperature side intake material handling fan with airtight seals to the primary fan vacuum box. The primary fan had a 10 hp motor 30 with 460 VAC line voltage. An adjustable damper at the exhaust side controlled

( -33 the level of airflow through the fan which had a direct effect on the jet drier null, which created a vacuum of -I to -5 inches of water. The exhaust from the primary fan discharged into a cyclone that currently serves the purpose of noise reduction.

The secondary fan was manufactured by Buffalo and had a I/. hp motor with 110 5 VAC line voltage. The secondary fan had variable speeds and was connected with airtight seals to the secondary fan vacuum box. The secondary fan discharged to the exhaust side of the cyclone. The separation device was made from Teflon sheet 0.030 inches thick by 2 inches wide placed at a 45 degree angle across the conveyor screen at the down stream end of the secondary fan vacuum box.

10 In the exar,nples below, "sonic knots" were tested by the following method for classifying dry fluffed pulp into three fractions based on screen mesh size. The first fraction is the knots and is defined as that material that is captured by a No. 12 mesh screen. The second fraction is the accepts or the singulated fibers and is defined as that material that passes through a No. 12 mesh screen but is captured by 15 a No. 60 mesh screen. The third fraction is of the fines and is defined as that material that passes through a No. 12 and through a No. 60 mesh screen. The separation is accomplished by sound waves generated by a speaker that are imposed upon a pre-weighed sample of fluff pulp placed on a No. 5 mesh screen that is near the top of a separation column where the speaker sits at the very top. After a set 20 period of time, each fraction is removed from the separation column and weighed to obtain the weight fraction of knots, accepts/singulated fiber and fines.

EXAMPLE I

Singulated dried Douglas fir fiber and treated dried Southern pine fiber was produced by making wet rolls of pulp on a pilot papermachine and hand feeding the 25 wet rolls into the shredding device and drier system described above. Some untreated (as is) bleached Southern pine and Douglas fir rolls were dried.

Additional Southern pine rolls were treated then dried. The treatments on the separate runs of the Southern pine feed pulp were as follows: 1. Citric acid; 2. Gyloxol; 3. Clay; 4. Hydrophobic latex and fly ash; 5. Hydrophobic latex, fly ash 30 and superplasticizer; 6. Glyoxol, hydrophobic latex, fly ash, and superplasticizer;

-34 7. Glyoxol, hydrophobic latex, fly ash, methyl cellulose, and superplasticizer. The feed rate of the pulp was 25-11 I g/min OD (oven dried). The solids content was approximately 28% in the rolls prior to drying. The outlet temperature of the drier ranged from 1 80 C to 200 C. The inlet temperature was varied to attain the outlet 5 temperature. Table I summarizes these runs and treatments. The clay and fly ash treated pulp appeared to fiberize the best. The pulp with methylcellulose was difficult to run and fiberize. The other runs appeared to fiberize similar to untreated pulp. Sonic knots were not measured on these samples.

Table 1: Fiber treatment.

Run Citric Glyoxal Latex Clay Fly Ash Methyl Super- Outlet Feed # Acid Cross- C A Cellulose plasticizer temp. Rate Cross- Linker (L) ( L) (F) (MC) (SP) ( C) G/MIN Linkn (XLG) _ OD l 200/180 73.9 2 -.' = 200/180 63.4

4 200 113.3

5 200 69.1

6 200 98.8

7 200 95.6

-8 _= _ = 21)0 24.8

10 200 81 0

Oa 200/180 52.5 Ob 180 24.8 EXAMPLE 2

Unbleached and untreated singulated dried fiber was produced by making wet rolls of unbleached Douglas fir (DF) pulp on a pilot papermachine and hand feeding the wet rolls into the shredding device and drier system described above.

I S The dried fiber was collected and tested for sonic knots which were 5% at one feed rate (in rpm of the feed roller motor into the shredder) and 15% at a higher feed

-35 rate. The outlet temperature was maintained at 180 C for both runs. The fines content was about 11% at the lower feed rate and 12% at the higher feed rate. The accepts were 83% at the lower feed rate and 74% at the higher feed rate. Table 2 summarizes the data.

5 Table 2: Varying feed rate effects on untreated roll samples.

Run - Knots Accepts Fines Feed Outlet # (id) Speed Temp. 11 OF 14.73 74. 13 11.13 300 180

12 OF 5.07 83.07 11.87 250 180

EXAMPLE 3

Bleached and untreated singulated dried fiber samples were produced by 10 making wet rolls of bleached Douglas fir pulp on a pilot papermachine and hand feeding the wet rolls into the shredding device and drier system described above.

The dried fiber was collected and tested to determine the effect of outlet temperature and feed rate on sonic knots and also the effect on fiber strength as measured by wet zero span tensile strength (ZST). The tab% gives a value to 15 establish the lower and upper limits of the error range for the ZST results. There was no statistically significant change in fiber strength. It was found that a higher feed rate produced a higher amount of knots and a higher outlet temperature produced more knots. Table 3 shows the results.

Table 3: Jet drier runs showing effect of temperature and feed rate on knots 20 and ZST.

Run # ZST t86% Knots Accepts Fines Shredder Outlet Feed Rate Index (%) (%) (%) Speed Temp. (g OD/ (Nm/g) ( C) min) Control 108 10.6 13 106 5.7 20. 53 66.87 12.60 300 160 70

14 103 1.4 19.87 65.60 14.53 300 170 70

1Sa 105 4.9 25.00 63.67 11.33 300 180 70

-36 Run # j ZST t86% Knots Accepts Fmes Shredder Outlet Feed Rate Index (%) (%) (o/o) Speed Temp. (g OD/ I (Nm/g) I ( C) mm) 15b 1 101 4. 9 47.33 41.27 11.40 500 180 116 15c j 95 2.8 6.40 78.33 15.27 125 180 29 16 103 3 5 26.53 60.87 12.60 300 190 70

17 99 4.9 41.93 47.20 10.87 300 200 70

EXAMPLE 4

Beached and untreated singulated dried Douglas fir fiber samples were produced by slushing wet lap and de-watering it by using a centrifuge and then 5 hand feeding the pulp on a belt conveyer into the drier system described above.

The dried fiber was collected and tested to determine the effect of various wet pulp preparation methods. The wet pulp preparation methods included centrifuged, centrifuged and pin-fluffed, and centrifuged and wetted. Sonics knot levels were tested and the results are shown in Table 4 where it can be concluded that just 10 centrifuging provides the lowest sonic knots at 14.2%.

Table 4: Jet drier runs showing effect of pulp preparation on sonic knots.

Run # Sample Preparation Knots Accepts Fines Inlet Temp.

(%) (%) (%) C)

18 Centrifuge & Fluffed 17.9 69.5 12.7 220 19 Centrifuged 14.2 71.4 14. 4 220 20 Centrifuged & Wetted 16.7 70.7 12.6 220 EXAMPLE 5

15 Fly ash treated and untreated bleached singulated dried Douglas fir fiber samples were produced by slushing wet lap and de-watering it by using a centrifuge and then hand feeding the pulp on a belt conveyer into the drier system described above. The fly ash containing pulp was made by adding 20% by weight fly ash with high molecular weight anionic retention aid to the slush pulp prior to 20 centrifuging. The dried fiber was collected and tested to determine the effect of

( -37 inlet temperature and fly ashon sonic knots. The results are shown in Table 5 where it can be seen that fly ash treatment dramatically reduces knots from a high of 20 % to a low of 1% by weight. Also it can be seen for these runs that increased inlet temperature and outlet temperature slightly reduced knots.

5 Table 5: Singulated Douglas fir pulp with and without fly ash.

Run Sample Fly Ash Knots Accepts FinesInlet Outlet # Preparation Id/ If/ If/ /.)Tem T(eocm)p.

Centrifuged, 21 a fluffed 20.40 66.73 12.87260 160 2 1 b Centrifuged 1 4. 1 3 74.40 11.47260 1 80 21 c fluffed 16.13 72.93 10.93300 180 22a Centrifuged, FA 20% I 07 80.00 18.93260 180 22b fluffed FA 20% I. 27 79.00 19.73230 180 EXAMPLE 6

Singulated dried fiber was produced from never dried unbleached pulp taken 10 from a double roll press in a commercial mill after deflaking. The pulp was run as collected from the mill and no treatments were done on it. The results are provided in Table 6 which shows that the knots ranged from 0.75 to 2.37 percent. Increasing outlet temperature by decreasing feed rate resulted in a slight decrease in knots.

Increasing inlet temperature by increasing feed rate increased knots slightly.

15 Washing, centrifuging and fluffing increased knots slightly. Reheating the pulp appeared to have no effect. The "kappa" number is a measure of the amount of lignin remaining in the pulp post pulping, and is quantified by the Tappi Standard Test Methods test number T-236.

Table 6: Untreated centrifuged Douglas fir unbleached samples from 20 double roll press. Effect of kappa #, pulp temperature and sample preparation.

-38 Run # Pulp Sample Kappa # Knots Accepts Fines Inlet Outlet PreparTemp. Temp. ation ( C) ( C) 23a DF As-is 25 230 150 23b DF As-is 25 0. 90 83.92 15.18 240 150 23c DF As-is 25 1.36 85.95 12.70 250 155 23d DF Asis 25 1.27 83.60 15.13 260 160 23e DF As-is 25 1.80 76.33 21.87 300 220 23f DF As-is 25 I.49 80.98 17.53 260 160 23g DF 25 1.29 81.04 17 67 260 180 23h DF As-is 25 0.75 84.10 15.15 300 180 24a DF As-is 25 I. 16 82.41 16.43 260 160 heated PP 24b DF As-is 25 1.97 81.89 16.13 260 180 pulp 25a DF As-is 12 2.37 79.21 18.42 260 160 25b DF As-is 12 1.82 82. 19 15.99 260 180 25c DF As-is 12 2.31 80.75 16.95 300 180 26a DF Washed, 25 2.60 82.93 14.47 260 160 Centrifuged fluffed 26b DF Washed, 25 1. 87 82.80 15.33 260 180 l C=ofl6'e4ie EXAMPLE 7

Bleached and untreated singulated dried fiber samples were produced by making wet rolls of bleached Douglas fir pulp on a pilot paperrnachine and hand 5 feeding the wet rolls into the shredding device and drier system described above.

The knots for this system were high at 34% indicating that feeding pulp directly is better than forming a wet web and shredding the web during feed.

EXAMPLE 8

Bleached and untreated singulated dried fiber samples were produced by 10 pin-fluffing never-dried Southern pine and feeding the pulp by placing it into a

( -39 foam feed system where water and surfactant are injected and mixed with the wet pulp providing a Plowable mix that can be fed into the jet drier system. The knots were less than 2% but the fines amount has gone up to almost 20% compared to previous runs.

5 EXAMPLE 9

An unbleached and untreated singulated dried fiber sample was produced by running the pulp as obtained from a mill in the drying system described above without the material handling fan between the drier and the vacuum conveyer.

Compared to previous runs, the knots increased slightly from 1.8% to 3.5% for the 10 same temperatures.

EXAMPLE 10

15 Compared to previous runs, the knots increased slightly from 1.3% to 2. 6% for the same temperatures. A bleached control sample had a slight increase in knots from 20.4 to 21.9%.

EXAMPLE 1 1

A bleached dissolving grade fiber was dried using the drying system 20 described above. The pulp had about 10% knots. The moisture was less than 2% which is typically too low. Dissolving tests showed that the fiber performed about the same as typical commercial grade pulp.

EXAMPLE 12

Bleached singulated fiber was produced with the drying system described 25 above to compare the effect of de-watering process on knots. Screwpressed pulp was compared to centrifuged pulp and centrifuged control wet lap pulp. The results are in Table 12 which shows that centrifuging provides a lower amount of knots.

Table 12: Runs to determine difference between screw-pressed, centrifuged wet lap, and centrifuged slush. Two levels of spring pressure were used on the 30 press.

l o- Run Sample Spring Average Knots Accepts Fines Inlet Outlet # Preparation Pmssure K=ots, Temp Temp Screwpressed 32a bleasCIhuesdh DF Him 19.3 61.5 19.3 260 0 Screwpressed 32b bleaSclbuesh DF Hi 3h 25. 7 61.1 13 3 280 130 Screwpressed bleached DF 59 14 5 32c slush High Z5.69. 110 200 Screwpressed 32e bleached DF Low 27.957.7 14.3 280 Screwpressed 32f bleasClhuesdh DF Low 22.3 13.366.7 20.0 260 180 33a ceC tn. tfru led 20.161.7 18.1 260 180 wedap 33b CeCn trnitfru g'ed 16.665.5 17. 9 270 200 _ wetlap 33c CeCn trnitfru l'ed 26.359.1 14.5 280 180 _ wetlap 33d Cont,rol, 21. I 21.365.1 13.6 280 200 wetlap 34a CenStiruf heed 20. 864.0 15.2 180 34b Centnfilged = = 15.6 68.0 16.4 200 34c Cenclfilged 14. 6 67.9 17.5 280 180 34d CenstirufSuhged 17.6 19.2 67.5 13.3 280 200

EXAMPLE Crosslinked bleached singulated fiber was produced with the drying system

described above to determine the ability of the drier to run crosslinked treated pulp.

As with other grades of pulp, a low amount of knots is desirable with crosslinked 5 pulp. Two runs were done at different temperatures as shown in Table 13.

Polyacrylic acid (PAA XL) was added to the pulp at approximately 5% by weight on pulp. Post curing was done to complete the reaction. The data shows that the higher temperature in the jet drier lowered sonic knots slightly and lowered wet knots also. Post cure time increased wet knots and may have increased sonic knots.

10 The level of sonic knots is considerably higher than untreated pulp indicating that the polyacrylic acid treat nent increases knots. Rewetting the crosslinked pulp and drying in an oven showed that the pulp did not bond to itself indicating crosslinking of the pulp.

Table 13: Five percent polyacrylic acid treated pulp.

Run Sample Post Cure Sonic Wet Knots Accepts Fines Inlet Outlet # Preparation Time Knots (a/. Temp. Temp (min) Rejects) ( C) TIC) bleached never 35e dried w/ PAA 0 35.00 0.0 48.33 16 67 286 200 bleached never dried w/ PAA 2 32.07 15.35 56 87 I 1.07 286!0 bleached never dried w/ PAA 3.5 28.93 16.02 58.6 12.47 286 200 bleached never dried w/ PAA 5 23.30 18.24 62.13 14.07 286 200 bleached never 35b dried w/ PAA O 28.07 0.26 55.00 16.93 296 1 _ bleached never 14 48 dried w/ PAA 2 24.00 63.00 13.00 296210 bleached never 3.5 20.40 9.57 65.33 14. 27 296 210

-42 Run Sample Post Cure Sonc Wet Knots Accepts Fines Inlet Outlet # Preparation Time Knots (% Temp. Temp.

(rein) Rejects) ( C) ( C) XL bleached never dned w/ PAA 5 24.67 11.28 63. 60 11.73 296 210 XL _

EXAMPLE 14

Clay and fly ash treated bleached singulated fiber was produced with the drying system described above to determine the effect on sonic knots. The clay and 5 fly ash was added at 0%, 1%, and 10% by weight. The samples with 10% mineral have less knots. The fly ash containing fibers had lower knots than the clay containing fibers at the same dosage. The samples with 1% mineral do not appear much different than the control. Table 14 provides a summary of the data.

Table 14: Runs to determine effect of clay and fly ash on knots.

Run # Sample Preparation Mineral Knots Accepts Fines Inlet Outlet % Temm. Temp Control, wet lap centrifuged 35 As is O 1913 65.50 15.07 2 180 Control, wet lap 39 centrifuged 1 23.87 63.87 12.27 270 I 80 With Clay Control, wet lap 40 centrifuged 10 10.07 71.27 18.67 270 180 With Clay Control, wet lap 41 centrifuged 1 15.93 68.00 16.07 270 I 80 With Fly Ash Control, wet lap 42 centrifuged 10 4.00 69.20 26.80 270 180 With Fly Ash

-43 EXAMPLE 15

* Singulated fiber was produced using the drying system described above from bleached Douglas fir pulp. The pulp was prepared by centrifuging and then running the pulp through the drier system cold to break apart the wet chunks of pulp 5 and then feeding the broken apart pulp through the drier system hot as normal. The purpose is to determine the efficiency of the drier system to prepare pulp for singulation. The effect of outlet temperature on singulation was also tested. Outlet temperature is changed by changing feed rate. At the same outlet temperature, the cold then hot run through the drier reduced knots by half. Increasing outlet 10 temperature reduces knots significantly. The results are shown in Table 15.

Table 15: Jet drier runs to determine the effect of running fiber through the drier system with no heat and then rurniing the same fiber through the system hot. I Run # | Sample Preparation Sonic Accepts Fines Inlet Outlet Conveyer Knots Temp. Temp. Speed ( C) ( C) I)

Control, wet lap 6ged(t vice 20.13 6493 1493 26 170 40 L hot) _ -

Control, wet lap 46b centrifuged (twice 7.87 76.80 15.33 260 197 3.0 through - cold then hot) Control, wet lap 46 centrifuged (twice i.53 76 73 14.73 260 +20 2.25 Control, wet lap 47 centrifuged (once 1 4.53 70. 67 14.80 260 198 3.5 through - hot only) 15 EXAMPLE 16

Singulated fiber was produced using the drying system described above from unbleached Douglas fir pulp. The pulp was prepared by centrifuging it in a batch centrifuge. Sonic knots ranged from 2% to 5% over a several hour period

-4 indicating good system stability. The results are shown in Table 16, where "run ave" is the mean average of all six (46a-46f) runs.

Table 16: Jet drier runs to determine system stability.

Run Time Sonuc Accepts Fines Inlet Outlet # mto run Temp. Temp.

Knots ( C) ( C) 48 Run eve 4.5 84.3 11.2 260 160 48a (1 hour) 5 83 12 260 160 48b (2 hour) 4 85 260 160 48c (3 hour) 6 84 10 260 160 48d (4 hour) 2 87 260 160 48e (5 hour) 5 84 260 160 48f (6 hour) 5 83 12 260 160 s EXAMPLE 17

Singulated fiber was produced using the drying system described above from bleached and unbleached Douglas fir and bleached Southern pine pulp. The pulp was prepared by centrifuging it in a batch centrifuge. A material handling fan 10 was used to break apart the pulp prior to drying it. Steam heat was used to prepare selected pulps. Different outlet temperatures were also run. The results are shown in Table 17. Steam heating the pulp prior to drying reduced knots. A higher outlet temperature reduces knots. Unbleached pulp had the lowest amount of knots.

Table 17: Runs to compare bleached and unbleached Douglas fir and 15 bleached Southern pine singulated fibers, as well as steam treatment.

Run Pulp Sample Preparation Kappa Sonic Accepts Fines Inict Outlet # Knots Temp. Temp. _ ( C) ( C)

Neverned, bleached, 50a SP slushed, centrifuged, 0 14.80 69.73 15.47 260 160 material handling fan _ Never-dned, bleached, 50c SP slushed, centrifuged, 0 5.13 73.07 21.80 250 200 material handling fan,

-45 Run Pulp Sample Preparabon Kappa Sonc Accepts Fines Inlet Outlet # Knots Temp. Temp.

( C) ( C)

steam heat Neverried, bleached, 50d SP slushed, centn fuged, 0 4.00 75. 80 20.20 260 220 material handhng fan, steam heat Neverdried, 51a Uunbleached, 25 2 60 85.67 11.73 260 160 DF centrifuged, material handling fan 52 B- Control, wet lap 0 16.20 70.73 13.07 260 160 DF centnfuged BControl, wet lap, 52a DF centrifuged, steam heat 0 13 13 75.67 11.20 230 130 52b B- Control, wet lap, 0 8.40 75.33 16.27 250 200 DF centrifuged, steam heat B- Control, wet lap, 52c DF centnfuged, steam heat 0 10.53 77.27 12.20 260 220 EXAMPLE 18

Singulated fiber was produced using the drying system described above from bleached Douglas fir and bleached Southem pine pulp. The pulp was 5 prepared by centrifuging it in a batch centrifuge. A material handling fan was used to break apart the pulp prior to drying it. Passing the pulp through the jet drier system with the heat off was done on selected samples. The results are shown in Table 18. Sonic hoots ranged from 1.87 to 10.07. Running the pulp through the system with the heat off prior to drying the pulp reduced knots.

10 Table 18: Bleached Douglas fir and Southem pine with no treatment but with selected defiberization.

Run Pulp Sample Preparation Sonic Accepts Fines Inlet Outlet Null # Knots Temp. Temp.

_ ( C) ( C)

Never dried, bleached, -3.5 53a B-SP slushed, centrifuged, 1.87 79.93 18. 20 250 185 4 0 material handling fan

-46 Run Pulp Sample Preparation Sonic Accepts Fines Inlet Outlet Null # Knots Temp. Temp.

( C) ( C)

= = Run twice - cold/hot = Never-dried, bleached, slushed, centatuged, 53a2 B-SP material handling fan 10.07 72.60 17.3 250 177 -3.5 Hot only 53a2 sub sample -1 9.87 75.33 14.8 53a2 sub sample -2 6.87 74.87 18.2 = _ 53a2 sub sample -3 9.33 73.47 17.2 Never-dried, bleached, slushed, centrifuged 53b B-SP material handling fan 9.40 72.40 18.2 250 171 -3.5 Hot only Control, wet lap B- bleached, centrifuged, 54a DF material handling fan 3.00 82.20 14.80 250 -5 Run twice - cold/hot Control, wet lap, B- bleached, centrifuged, -3 5 54a2 DF material handling fan 5.87 80. 73 13.40 250 177 4 0 Run twice - cold/hot Control, wet lap, B- bleached, centrifuged, 54b DF material handling fan 9.80 77.67 12.53 250 171 -3.5 . Hot only EXAMPLE 19

Singulated fiber was produced using the drying system described above from bleached Douglas fir treated with 0. 1% sodium dodecyl sulfate. The pulp was 5 prepared by centrifuging it in a batch centrifuge aRer treatment. Passing the pulp through the jet drier system with the heat off was done on the samples. The results are shown in Table 19. Sonic knots ranged from 0.73 to 2.27% indicating that surfactant treatment significantly reduces sonic knots.

Table 19: Runs on bleached Douglas fir pulp treated with 0.1% sodium 10 dodecyl sulfate.

1i -47 Run Sample Preparabon Amount Sonc AcceptsFincs Inlet Outlet # (kg) Knots Temp. Temp. _ ( C) ( C)

Control, wet lap bleached, slushed in 1 07 84 4014.53 0.1 % solution of SDS, 3 separate.

55 centrifuged only btaegshin[ gr 0.73 83.80 15.47 250 180 Run twice cold then 0.73 84.00 15 27 hot _ Control, wet lap bleached, slushed, 1. 33 85.00 13.67 centrifuged, material 3 separate 56 handling fan btaegshn[ gr 2.27 83.93 13.80 240 170 Run twice - cold then 0.87 85. 07 14.07 hot Control, wet lap bleached, slushed in 1 00 83 13 15.87 0.1 % solution of SDS, 3 separate.

57 centrifuged only bags for I.00 83.67 15.33 240 170 Run twice - cold then testing 1.00 83.93 15.07 hot _ EXAMPLE 20

Singulated fiber was produced using the drying system described above 5 from bleached Southern pine (B-SP) with and without latex treatment and from unbleached and bleached Douglas fir (U-DF and B-DF, respectively) pulp. The bleached Southern pine pulp was prepared by centrifuging slushed pulp, running it through a material handling fan, and then running it through the jet drier with the heat off prior to drying it. The unbleached Douglas fir was only centrifuged after 10 slushing. The latex treated bleached Southern pine pulps were prepared by passing the pulps through the jet drier system with the heat off aRer treatment and centrifuging. The bleached Douglas fir control pulp was only centrifuged after slushing. The results are shown in Table 20. Sonic knots are low on the bleached Southern pine indicating the mechanical treatments reduce knots. The unbleached 15 Douglas fir pulp had the lowest knots indicating that it fiberizes well in this system.

The latex treated pulps also had low knots showing that the latex may reduce knots

j or may not affect their production. The control bleached Douglas fir had low knots indicating an improvement in the drier system. The latex treated pulps were hydrophobic. Table 20: Singulated Southern pine and Douglas fir pulps run through the 5 drier with no heat.

Run # Pulp Sample Preparation Sonic Accepts Fines Inlet Outlet Knob; Temp. ( C) Bleached, neverdried, slushed, centrifuged, I.07 81.07 17.87 58 B- SP material handling fan 1.67 79.40 18.93 240 167- 170 Run twice - cold then 3.67 78.53 17.80 hot centrifuged only 59 U-DF 0.80 85.73 13. 47 240 167-170

Run hot only 60 B-SP Latex #1 1.27 88.20 10.53 240 160-165 Run twice cold and hot Latex #2 61 B-SP 1.60 84.00 14.40 240 160-

Run twice - cold and hot Latex #3 62 B-SP 1.33 84.60 14.07 240 160-

Run twice - cold and hot _ Latex #4 63 B-SP 1.07 84.93 14.00 240 160-165

Run twice - cold and hot Control, wet lap 64 B-DF bleached, slushed, 2. 20 83.67 14.13 240 167-170 centrifuged only EXAMPLE 21

Singulated fiber was produced using the drying system described above 10 from bleached Douglas fir pulp. The pulps were prepared by centrifuging only, centrifuging and running through a material handling fan, centrifuging and running through the drier with the heat off before drying or adding chemical surfactant prior to centrifuging. The results are in Table 21. Pulp that had been centrifuged or centrifuged and run in the material handling fan were about equal in sonic knots at

15%. Running centrifuged pulp through the system with no heat reduced knots to about 10%. The surfactant treatment reduced knots to about 3%. These results were duplicated in follow-up runs. Conveyer speed was 7 ft/min, null was -3.5 to 4 inches water.

5 Table21: Singulated bleached Douglas fir pulp comparing mechanical fiberization pulp preparation to Berol 587k chemical surfactant.

Run Sample Preparation Sonic Accepts Fines Inlet Outlet Feed # Knots Temp Temp. Rate _. ( C) ( C)

Control, wet lap bleached, slushed, centnfige4 material 65 handhng fan 15. 33 71.47 13.20 260 180 150 Hot only Control, wet lap bleached, 66 slushed, centnfi,ged only, 9.93 76.13 13.93 260 180 150 Cold then Hot Control. wet lap bleache4 slushed centnfiaged with I % 67 surfactant 2.88 85 80 11. 32 260 180 150 Hot only Control, wet lap bleache4 68 slushed, centnfl,ged only, 15.62 72.03 12.35 260 180 150 _ Hot only EXAMPLE 22

to Singulated fiber was produced using the drying system described above from bleached Douglas fir pulp and Southern pine pulp with and without polyacrylic acid crosslinker, surfactant, and clay treatments. The pulps were prepared by centrifuging only or centrifuging and running through a material handling fan (MHF) prior to drying. The results are in Table 22. The Douglas fir 15 control had 9% knots. The Southern pine with surfactant had 2% knots confirming the benefit of surfactant. The polyacrylic acid only treatment increased knots to 15%. Adding surfactant or clay to the polyacrylic acid treated pulp reduced knots below 2% demonstrating the benefit of surfactant and clay to reduce knots. The

I i ( -50 inlet temperature was 240 C and outlet temperature was 165 C. Null was -3.5 inches of water and conveyer speed was 6.0 ft/min.

Table 22: Singulated bleached Douglas fir control and Southern pine pulp with and without polyacrylic acid, surfactant, and clay treatments.

Run Pulp Sample Preparation Clay Knots Accepts Fmes OD Feed # Rate _ (g/min) B Control, wet lap centrifuged 75 O 9.00 79.47 11.53 71.02

DF Hot only Bleached, neverried, 76 B-SP slushed, centrifuged, MHF, 0 2. 07 84.93 13.00 83.15 with 1% surfactant Bleached, never-dried, 77 B- SP slushed, centrifuged, MHF, 0 14.87 65.80 19.33 92.63 wl 20% PAA on fiber _ Bleached, never deed, slushed cer fuged, M, 78 B-SP wl 200io PAA on fiber and 0 I.60 85.40 13.00 89.71 _ with 1% surFactant Bleached, never deed, 79 B-SP slushed, centrifuged, MHF, 10 1.20 77.80 21.00 88.07 w/ 20% PAA on fiber Bleached, never-dried, 80 B-SP slushed, centrifuged, MHF, 20 1.80 76.67 21.53 86.91 _ w/ 20% PAA on fiber EXAMPLE 23

Singulated fiber was produced using the drying system described above from two different bleached Douglas fir pulps with selected amounts of Berol 587k 10 surfactant on one of the pulps. One batch of pulp was treated with soluble iron.

The pulps were prepared by centrifuging only. The results are in Table 23. The surfactant works best at the 1% dosage level. The iron reduced knots sigruficantly but also increased fines to a high level. Feed rate may have had an influence on the surfactant results. Higher feed rates appear to increase knots. The inlet temperature 15 was 240 C and outlet was 160 C. The conveyer speed was 6 ft/min and null was 3.5 inches water.

( Table 23: Run to determine minimum amount of surfactant needed to reduce knot content below 2% using the bleached KKT from Kamloops.

Run Pulp Sample Preparation Sonic Accepts fines OD Feed # Surfactant Rate Knots (g/min) Control, slushed, 85 DBF#2 centrifuged only 0 4.20 82.07 13. 73 75.80 Hot only Slushed, centrifuged, w/ surfactant, 86 DBF#2 centrifuged 0.1 4.13 81.00 14.87 108.32 Hot only Slushed, centrifuged, w/ surfactant, 87 DBF#2 centrifuged 0.5 3.73 84.33 11.93 90. 51 Hot only _ Slushed, centrifuged, B- w/ surfactant, 88 DF#2 centrifuged 1.0 2.00 86.27 11.73 73.25 Hot only Wet lap centrifuged 89 B-DF (bleached) with 0.056/O 0 1.93 65.27 32.80 71.90 Fe3+ Control, wet lap bleached, slushed, 90 B-DF centrifuged - end of run O 5. 00 80.67 14.33 71.56 sample Hot only 5 EXAMPLE 24

Singulated fiber was produced using the drying system described above from bleached Douglas fir pulp that had been de-watered using a screwpress. The results are in Table 24. The amount of knots is sufficiently low compared to previous runs to show that screwpress de- watering is an acceptable option to I O remove excess water prior to drying pulp with the jet drier system.

J -52 Table 24: Singulated bleached Douglas fir prepared from pulp dewatered through a screwpress.

Run Sample Preparation Sonic Accepts Fines Inlet Outlet Null # Knots T(mc) p T(.mc)p Control, wet lap bleached, 91 slushed; cenuifuged, 3.20 85. 87 10.93 240 189-190 -3.5 Cold then Hot Never dried, Screw pressed 92 (HC > 30?, material 3.87 82.33 13.80 240 169-171 -345.oo Hot only _ l While the preferred embodiment of the invention has been illustrated and 5 described, it will be appreciated that various changes can be made therein without departing from the spirit and scope of the invention.

Claims

( CLAIMS

The embodiments of the invention in which an exclusive property or privilege is claimed are

defined as follows: 1. A pulp product comprising: smgulated and Jet dried fibers, said product having a knot count equal to or less than 5%, an accepts count equal to or greater than 80%, and a fines count equal to or less than 15%
2. The product of Claim 1, wherein the knot count is equal to or less than 2%.
3. The product of Claim 1, wherein the accepts count is equal to or greater than 85%.
4. The product of Claim 1, wherem the fines count equal to or less than 14%.
5. The product of Claim 1, wherein the product is treated with a treatment substance selected from the group consisting of surfactants and mineral particulates during jet drying.
6. The product of Claim 5, further treated with a crosslinker during jet drying.
7. The product of Claim 5, further treated with a hydrophobic material during jet drying.
8 A pulp product comprising: singulated and jet dried fibers, said product having a knot count equal to or less than 2%, an accepts count equal to or greater than 77%, and a fines count equal to or less than 21%.
9. The product of Claim 8, wherein the knot count is equal to or less than 1.6%.
10. The product of Claim 8, treated with a treatment substance selected from the group consisting of a surfactant and a mineral particulate.
The product of Claim 10, wherein the treatment substance is clay.
12. The product of Claim 10, wherein the treatment substance is fly ash.

(
13. The product of Claim 10, further treated with a crosslinker during jet drying.
14 The product of Claim 10, further treated with a hydrophobic material during jet drying
15 he product of Claim I or Claim 8 admixed with concrete products.
16. The product of Claim I or Claim 8 incorporated into an absorbent article.
17. The product of Claim I or Claim 8 incorporated into a plastic product.
18. The product of Claim I or Claim 8 incorporated into a paper product.
19. The product of Claim I or Claim 8 incorporated into a filter product.
20. A pulp product substantially as described herein and with reference to Figures 10 to 12.
21. A process for producing singulated pulp fibers comprising: ntroducmg a wet pulp and air into a jet drier; drying said pulp in said jet drier to form singulated pulp fibers; removing said pulp from said jet drier and separating said pulp fibers from said air; and treating said wet pulp with a treatment substance before drying said wet pulp to reduce the knot content of said pulp fibers.
22. The process of Claim 21, wherein said treatment substance Is mixed with said wet pulp before introducing said wet pulp into said drier.
23. The process of Claim 21, wherem said wet pulp is at least partially dewatered prior to introducing said pulp into said drier.
24. The process of Claim 21, wherein said treatment substance is selected from the group consisting of a surfactant and a mineral particulate.
25. The process of Claim 24, wherein said treatment substance and said wet pulp are mechamcally mixed to form a foam suspension of said pulp prior to introducing said pulp into said drier.
26. The process of Claim 24, wherein said treatment substance is a surfactant.
27. The process of Claim 21, wherem said wet pulp is further treated with a substance selected from the group consisting of a crosshnker and a hydrophobic material.
28. The process of Claim 21, wherein the knot count of said pulp fibers Is less than 5%.
29. The process of Claim 28, wherein the knot count of said pulp fibers is less than 2%.
30. The process of Claim 28, wherein the knot count of said pulp fibers is less than 1.6%.
31. The process of Claim 28, wherein the knot count of said fibers is less than 0.73%.
32. The process of Claim 21, wherein said wet pulp is further treated with a substance selected from the group consisting of crosslinker and hydrophobic material, and wherein said fibers have a knot count less than 5%.
33. The process of Claim 32, wherein said fibers have a knot count less than 2%.
34. The process of Claim 21, wherein said treatment substance is a mineral particulate and the wet pulp is further treated with a substance selected from the group consisting of a crosshnker and hydrophobic material, and wherem said fibers have a knot count less than 5%.
35. The process of Claim 34, wherein the fibers have a knot count less than 2%.
36. The process of Claim 34, wherein the fibers have a knot count less than 1.6%.
37. The process of Claim 34, wherein the fibers have a fines count less than or equal to 21 %.

(
38. The process of Claim 21, wherein said treatment substance is a surfactant and the wet pulp is further treated with a substance selected from the group consisting of a crosslinker and hydrophobic material, and wherein said fibers have a knot count less than 5%.
39 The process of Claim 38, wherein the fibers have a knot count less than 2%.
40 The process of Claim 38, wherein the fibers have a knot count less than 1.6%.
The process of Claim 38, wherein the fibers have a fines count less than or equal to 21 %.
42. The process of Claim 38, wherein the fibers have a fines count less than or equal to 15%.
43. The process of Claim 38, wherein the fibers have a fines count less than or equal to 14%.
44. The process of Claim 21, wherein the treatment substance is a surfactant and the wet pulp is further treated with a substance selected from the group consisting of crosslinkers and hydrophobic material, and wherein the fibers have a fines count less than or equal to 21 %.
45. The process of Claim 44, wherein the fibers have a fines count less than or equal to 15%.
46. The process of Claim 45, wherein the fibers have a fines count less than or equal to 14%.
47. The process of Claim 21, wherein the treatment substance is a mmeral particulate and the wet pulp Is further treated with a substance selected from the group consisting of a crosslinker and a hydrophobic material, and wherein the fibers have a fines count less than or equal to 21 %.
48. The process of Claim 21, wherein the treatment substance is a surfactant and the wet pulp is further treated with a substance selected from the group consisting of a crosslinker and a hydrophobic material, and wherein the knots count is less than or equal to 5%, the accepts are greater than or equal to 80%, and the fines are less than or equal to 15%.
49 The process of Claim 48, wherein the knots are less than or equal to 5%, the accepts are greater than or equal to 80%, and the fines are less than or equal to 14%.
50. The process of Claim 48, wherein the knots are less than or equal to 5%, the accepts are greater than or equal to 85%, and the fines less than or equal to 15%.
51. The process of Claim 48, wherem the knots are less than or equal to 2%, the accepts are greater than or equal to 80%, and the fines are less than or equal to 15%.
52 The process of Claim 21, wherein said wet pulp has a consistency of from 0.01% to 10% before mtroducton into saidJet drier
53. The process of Claim 52, wherein said wet pulp has a consistency of from 3% to 10% before introduction with said drier.
54. The process of Claim 21, wherem said singulated pulp is dried to a moisture content of less than 2 percent to 10 percent by weight.
55. A process for producing singulated pulp fibers comprising: ntroducmg wet pulp and air into a jet drier through a rotary airlock, said rotary airlock having vanes and a housing, the end of said vanes being spaced from said housing by a distance sufficient to prevent wet fibers from clogging said airlock.
56. The process of Claim 55, wherem said gap between said vane end and said housing is In the range of.010 to.050 Inches.
57. The process of Claim 55, wherein said vanes shear fiber clumps as they enter said housing to prevent clogging said airlock.
58. A process for producing singulated pulp fibers comprising: introducing a wet pulp and air into ajet drier; drymg said wet pulp m said Jet drier to form singulated pulp fibers;

withdrawing said fibers from said Jet drier m an air stream at a velocity sufficient to prevent said fibers from knotting; and separating said pulp fibers from said air stream.
59. The process of Clalm SB, wherem said pulp fibers are withdrawn from said drier through a conduit, said conduit being sized and said air stream being maintained at a velocity sufficient to maintain fibers suspended m said air stream m said conduct.
60. A process for producing slogulated pulp fibers comprising: mtroduclng wet pulp and air into aJet drier; drying said wet pulp m said jet drier to form singulated pulp fibers; and wthdrawmg said pulp fibers from an outlet from said jet drier under a partial vacuum.
61. The process of Claim 60, wherein said vacuum is applied to a plenum, the process further composing: positioning a head box at the outlet; positioning a movable screen between said plenum and said head box on which said pulp fibers and deposited, said head box and said plenum being in sealing contact with said screen; and moving said screen past said head box to remove pulp fibers from said head box.
62. The process of Claim 61, wherem said fibers emerge from said head box at an outlet side as said screen Is moved, the process further comprising: posltlomng a second plenum under said screen adjacent said outlet side; and drawing a partial vacuum in said second plenum to hold said fibers on said screen as they emerge from said head box.
63. Singulated pulp fibers produced by the process of Claim 21.
64. A drying system for the processing of pulp into singulated and dried fibers composing: a Jet drier with a Jet conduit, a pulp intake for delivery of pulp into the Jet conduit, a manifold for air intake into the jet conduit, and a fiber outlet for removal of singulated and dried fibers, outlet air and fines from the Jet conduit;

l a pulp supply station coupled to the pulp mtake for supplying a feed pulp to the pulp intake, the pulp supply station including a treatment supply source for delivering a treatment substance to the pulp; an air supply station coupled to the manifold for delivering air to the manifold; an outlet flow conduit coupled to the fiber outlet for the removal of the fibers, outlet air, and fines from the Jet conduit; and a fiber separation station coupled to the outlet flow conduit for separating the fibers from the outlet air.
65 The drying system of Claim 64, wherein the pulp supply station further includes a first de-

waterng device and a second dewatering device in flow communication with the first de-watering device; the first de-watering device receiving a pulp supply having a liquid content, removing a portion of the liquid content, and sending a de-watered supply pulp to the second de-watering device; the treatment supply source dehvenng the treatment substance to the de-watered supply pulp prior to entry into the second dewatering device; and the second de-watering device removing additional liquid content from the treated and de-watered supply pulp and sending a treated feed pulp to the jet drier pulp intake.
66. The drying system of Claim 65, wherein the pulp supply station further includes a treatment recycle conduit m flow communication between the first de-watering device and the second de-watering device; and wherein the treatment recycle conduit delivers at least a portion of the additional liquid content from the second de.-watering device to the first de-watering device
67. The drying system of Claim 66, wherein the pulp supply station further includes a holding tank device inserted in recycle conduit; and wherein the holding tank device stores at least a portion of the additional liquid content from the second de-watering device and disperses the additional liquid content to the first dewatermg device.
68. The drying system of Claim 65, wherein the pulp supply station further includes a treatment recycle conduit in flow commumcation between the first de-watering device and the treatment supply source; and wherein the treatment recycle conduit delivers at least a portion of the additional liquid content from the second de-watering device to the treatment supply source.
69. The drymg system of Claim 68, wherem the pulp supply station further includes a holding tank device inserted m recycle conduit; and wherem the holding tank device stores at least a portion of the additional hquid content from the second de-watenng device and disperses the additional liquid content to the treatment supply source.
70. A drying system for the processing of pulp into singulated and dried fibers comprising: a jet drier with a Jet conduit, a manifold for air intake into the jet conduit, a pulp intake for delivery of pulp mto the Jet conduit, and a fiber outlet for removal of sngulated and dried fibers, outlet air, and fines from the Jet conduit; a pulp supply station coupled to the pulp mtake for supplying a feed pulp to the pulp intake; an air supply station coupled to the manifold for delivering air to the manifold; an outlet flow conduit coupled to the fiber outlet for the transport of the fibers, outlet air, and fines from the jet conduit; a fiber separation station coupled to the outlet flow conduit for separating the fibers from the outlet air, and the pulp supply station including a pulp feed device coupled to the pulp intake for delivering the feed pulp to the pulp intake while minimizing the amount of air flow through the pulp supply station, the pulp feed device bemg a rotary airlock including a rotor housing and a rotor rotatably mounted within the rotor housing, the rotor having rotor vanes for transporting the feed pulp, wherein the rotor vanes and rotor housing are sized so that a gap exists between the rotor vanes and the rotor housing to prevent the feed pulp from jammmg the rotary airlock.
71. The drying system of Claim 70, wherein said gap between said rotor vanes and said housing is in the range of.O10 to.050 inches.
72. A dry sing system for the processing of pulp into singulated and dried fibers comprising: a jet drier with a jet conduit, a manifold for air intake into the jet conduit, a pulp intake for delivery of pulp into the jet conduit, and a fiber outlet for removal of singulated and dried fibers, outlet air and fines from the jet conduit; a pulp supply station coupled to the pulp intake for supplying a feed pulp to the pulp intake, the pulp supply station includes a pulp feed device coupled to the pulp intake for delivering the feed pulp to the pulp Intake while minimizing the amount of air flow through the pulp supply station;

( an air supply station coupled to the manifold for dehvering air to the manifold; an outlet flow conduit coupled to the fiber outlet for the transport of the fibers, outlet air, and fines from the jet conduit; a fiber separation station coupled to the outlet flow conduit for separating the fibers from the outlet air; and the pulp supply station further comprising a foam feeder interposed between the pulp feed device and the pulp mtake for mixing a surfactant with pulp and directly injecting foamed pulp mixture into the Jet drier.
73. A drying system for the processing of pulp into singulated and dried fibers comprising: a jet drier with a jet conduit, a manifold for air intake into the jet conduit, a pulp intake for I dehvery of pulp into the jet conduit, and a fiber outlet for removal of smgulated and dried fibers, outlet air and fines from theet conduit; a pulp supply station coupled to the pulp intake for supplying a feed pulp to the pulp intake; an au supply station coupled to the manifold for delivering air to the mamfold; an outlet flow conduit coupled to the fiber outlet for the transport of the fibers, outlet air, and fines from the jet conduit; and a fiber separation station coupled to the outlet flow conduit for separating the fibers from the outlet air; the fiber separation station including a vacuum conveyor having a screen for passing outlet air and retaining fibers to form a mat of fibers on the screen; a first roller, a second roller, a primary fan, a secondary fan, a primary fan vacuum box, and a secondary fan vacuum box; said screen bemg a continuous loop draped about the first and second rollers so that the screen has an upper portion and a lower portion; the upper portion of the screen having an upper and lower surface; the upper surface of the screen being associated with the outlet flow conduit; the primary fan vacuum box being associated with the lower surface and in flow communication with the primary fan; the primary fan vacuum box being positioned between the lower and upper portions and directly beneath the outlet flow conduit; the secondary fan vacuum box bemg associated with the lower surface and in flow communication with the secondary fan; the secondary fan vacuum box being positioned between the lower and upper portions and between the primary fan vacuum box and the second roller; the primary fan providing vacuum to the primary fan vacuum box and the outlet flow conduit; the secondary fan provdmg vacuum to the secondary fan vacuum box and the upper surface.
74. The drymg system of Claim 73, wherem the fiber separation station further includes a screen vacuum for removing excess fiber from the screen prior to the screen recevmg fibers from the outlet flow conduit, the screen vacuum being associated with the upper surface between the outlet flow conduit and the first roller.
75. The drying system of Claim 73, wherein the fiber separation station further includes a separation device, wherein the secondary fan vacuum box has a vertical wall facing the second roller, the separation device being associated with the upper screen directly above the vertical wall so that the mat of fibers may pass over the separation device to release the mat of fibers from the screen as well as from the vacuum of the secondary fan.
76. The drymg system of Claim 73, wherein the fiber separation station further includes an out feed roller, the out feed roller being associated with the upper surface of the screen between the outlet flow conduit and the second roller so that the out feed roller may contact the mat of fibers and pull the mat of fibers from the outlet flow conduit.
77. The drying system of Claim 73, wherein the fiber separation station further includes a head box with a head box shell, an out feed roller and a dynamic lip seal; the head box shell being a conduit having an mlet and an outlet for the passage outlet air, fibers and fines from the outlet flow conduit to the upper surface; the head box shell bemg positioned between the upper surface and the outlet flow conduit and being coupled to the outlet flow conduit and associated with the upper surface; the out feed roller bemg movably coupled to the side of the outlet of the head box shell facing the second roller so that the out feed roller may move vertically to adjust for varying mat of fiber thickness; the dynamic hp seal being movably coupled to the side of the outlet of the head box shell facing the second roller so that the dynamic lip seal may move vertically to adjust for varying mat of fiber thickness while maintaining a vacuum seal with the upper surface.
78. The drymg system of Claim 77, wherein the head box further includes a pair of drive wheels and a couphng device, the drive wheels bemg rotatably coupled to the side of the outlet of the head box shell facmg the first roller and is associated with the upper surface so that the motion of the upper surface results in the drive wheels rotating, the coupling device bemg coupled to the drive wheels and the out feed roller so that the rotation of the drive wheels acts on the coupling device which in turn acts on the out feed

l roller.
79. A process for producing sngulated pulp fibers substantially as described herein.
80. A drymg system for the processing of pulp Into singulated and dried fibers substantially as described herein and with reference to Figures I to 9.

81 Sngulated pulp fibers substantially as described herein.