This invention is concerned with cellulosic fibers exhibiting improved resilient bulking both in the wet and dry states and also with absorbent structures incorporating said cellulosic fibers. More specifically, this invention is concerned with a novel process for producing individualized anfractuous crosslinked cellulosic fibers, where the novelty resides in heating crosslinker treated fibers by entraining them in turbulent superheated steam at particular pressures and temperatures, individualizing said fibers and then curing the fibers while entrained in turbulent superheated steam at elevated temperatures and pressures.

BACKGROUND OF THE INVENTION

Fibers crosslinked in substantially individualized form and various methods of making such fibers have been described in the art. As is known in the art, the term "individualized crosslinked fibers" refers to cellulosic fibers that have primarily intrafiber crosslinked bonds, that is, the crosslinked bonds are primarily between cellulose molecules in a single fiber rather than being between cellulose molecules of separate fibers. Individualized crosslinked fibers are generally regarded as being useful in product applications wherein high bulk, high absorbency or both are desirable. Absorbent structures containing individualized crosslinked fibers generally exhibit an improvement in at least one significant absorbency property relative to conventional uncrosslinked fibers. Structures incorporating these fibers also generally exhibit a high degree of bulk.

As can be seen from U. S. Patent No. 5,137,537 and its disclosure of the prior art, there have been many processes for crosslinking individualized cellulosic fibers and a wide variety of crosslinking agents have been used including formaldehyde and addition products known as n- methylol agents or n-methylolamides. Dialdehyde crosslinking agents have also been used as well as polycarboxylic acids including C ₂ -C ₉ polycarboxylic acids and citric acid in particular. Crosslinking agents are usually used with a coreactant and/or catalyst. The prior art processes, although differing in specific aspects of crosslinking agents, treated cellulosic fibers with a crosslinking agent, allowed sufficient time for the crosslinking agent to penetrate the fibers, and the fibers were then defibrated into an individualized form by a wide variety of techniques including mechanical defibration as well as various fluffing devices. The fibers were dried and cured usually in air at elevated temperatures.

Although the above-referred to processes have resulted in the production of acceptable products for some applications, nevertheless, particularly for the paper industry, a continuing need exists in order to develop crosslinking technology which has the potential of being commercially significant. In particular, it is desired to develop a crosslinking technology which: produces a relatively nit free product at high throughput and low residence time in a reliable low-maintenance system; provides high thermal efficiency and can be conducted in a closed system thereby having no direct atmospheric venting and thus providing obvious advantages with regard to health and safety. The apparatus can be easily controlled, highly reliable and requires only a few moving parts.

SUMMARY OF THE INVENTION

It has now been found that the purposes identified above can be achieved in providing individualized crosslinked resilient bulking fibers, as well as from absorbent structures made from said fibers, by utilizing a process wherein cellulosic fibers which have been subjected to conventional wet processing with a crosslinking agent, are dried and cured while suspended in turbulent superheated steam. The chemical crosslinking agent used to treat the fiber prior to drying and curing is applied in an amount sufficient to produce a standard bulk of at least about 3.4 cc/g when incorporated at a level of 15% by weight into British Handsheets according to Tappi Standards but using a pressing pressure of 15 psig. The fibers are introduced into a pressurized dryer where they are entrained in turbulent superheated steam at a pressure of approximately 10 to 70 psia and at an initial steam temperature in excess of about 140°C, preferably from 200 to 300°C. During drying, the temperature may fall to as low as 150°C, but exit temperatures of 170°C to 220°C are preferred.

The dried fibers may be separated from the superheated steam in a conventional cyclone and the superheated steam conducted back for reuse. The fibers separated in said cyclone pass to a fluffer (which may be omitted, if so desired) and then to a curing tube which is similar to the dryer but differs therefrom in that the fibers which enter have a considerably lower water content i.e. they are preferably 100% dry.

For reasons which are not completely understood, it has been found that the water in the fiber unfavorably affects chemical curing because damaging fiber degradation reactions occur at high temperature in the presence of acid and water. Thus, by separating the drying and curing

stages and carrying out both under pressurized steam, improved results obtained. The temperatures and pressures of the dryer and curing tube are similar e.g. 140 - 350°C and 10-70 psia, but either can be operated at different temperatures and/or pressures.

It is to be understood that for economic reasons it is preferred to use essentially 100% superheated steam in the pressurized dryer and in the curing tube, but any non- oxygen bearing gas could be used as a diluent such as, for example, nitrogen.

In the embodiments in which steam is separated from the fiber between the dry stage and the cure stage, in order to perform the drying in a time period that would be acceptable in commercial operations and to minimize the time wherein the fiber is in contact with superheated steam, the dryer temperature must be at least 140°C, but as will be recognized by those skilled in the art, such is a poor way of attempting to define fiber temperature. It is not the temperature of the dryer which is important (providing it is initially above 140°C) but the temperature of the fiber, particularly when exiting the dryer. This temperature is difficult to measure, but an exit steam temperature of about 150°C to about 220°C provides satisfactory results.

It is noted that turbulence provided both in the dryer and curing sections provides internal defibration action, thus, promoting and maintaining a high degree of fiber individualization.

Finally, the fiber is separated from the superheated steam in another cyclone and is thereafter optionally refluffed, pressed and baled or conducted directly to any suitable process involving the use thereof. In some applications, it may be considered desirable to wash the fibers after curing to remove unreacted chemical but, in many applications, this will not be necessary.

It should be noted that it is possible to carry out the separate stages of drying and curing in a single piece of apparatus, but for ease of operation and control, a separate dryer and a separate curing tube are preferred. When a single piece of apparatus is used, the drying temperature will usually be somewhat higher than that indicated for the two stage operation and may even be comparable to the temperatures indicated for curing. In some operations, especially where high brightness is desired, three or more stages may be used to facilitate more accurate control over steam quality and temperature.

BRIEF DESCRIPTION OF THE DRAWINGS

Figure 1 is a block diagram of the novel process of this invention.

Figure 2 is a schematic of the novel process of this invention.

DESCRIPTION OF THE PREFERRED EMBODIMENTS

The novel process of this invention can be best understood from the block diagram in Fig. 1 where it is pointed out that wet processing prior to the dryer is conventional technology well known in the art and no novelty is claimed in such technology per se, but only in combination with said curing. Thus, for example, wet processing typically includes formation of a slush fiber, usually at a consistency of about 10-12%, followed by conventional dewatering to a consistency of about 40%, followed by a chemical crosslinking agent treatment step, followed by another conventional dewatering step to bring the consistency back to about 40%, all of these procedures utilizing conventional equipment such as a screw press,

repulping, recycling of water with and without chemicals, and recycling of crosslinking agent, if such is desired.

Although any conventional prior art crosslinking agent can be utilized, including those previously mentioned, particular preference is given to 1,3- dimethylol-4,5-dihydroxyimidazolidione (DMDHEU) catalyzed by magnesium chloride. The amount of DMDHEU which is used is approximately 2 to 6% by weight based on the fiber and the amount of magnesium chloride employed is about from 0.5 to 3% by weight. Use of these materials to treat fibers is known in the art as is evidenced from U. S. Patent No. 3,440,135. The process of the present invention is also well suited to be used with polycarboxylic acid crosslinkers such as citric acid, catalyzed with sodium hypophosphite or monosodium phosphate as well 1,3-dimethyl- 4,5-dihydroxyethyleneurea (DHDMEU) which is also catalyzed with magnesium chloride. Use of the citric acid is described in the previously mentioned U.S. Patent No. 5,137,537.

When the fibers are being impregnated with a crosslinking agent, the impregnated fibers are generally held in an equilibration chest for a sufficient amount of time to allow the crosslinking agent to thoroughly impregnate the fibers. The impregnated fibers are subsequently subjected to conventional dewatering operations and then passed through a conventional shredder and a conventional defibrator. As previously indicated, all these techniques are well known in the art and no novelty per se is claimed in any of them.

The novel process of this invention really begins when cellulosic fibers, usually at a consistency of about 20 to 50 wt.%, are introduced into a dryer, such as a pressurized dryer. As has heretofore been pointed out, the dryer is a pressurized dryer operating with superheated steam at a pressure of approximately 10-70 psia with an

entrance steam temperature in excess of about 140°C and less than 300°C, preferably from 200 to 300°C. The dryer is of the type which provide turbulent flow thereby entraining the fibers in said superheated steam.

Dried heated fiber is separated from the steam in a conventional cyclone, and the steam can be recycled back to the dryer or any other part of the process as desired.

The fiber separated in the cyclone passes into a conventional fluffer (which may be omitted if so desired) and into a curing tube which is of generally the same configuration as the dryer. As mentioned previously, if desired the crosslinked fibers may be washed to remove unreacted chemical crosslinking agent although in many cases the fibers may be used without washing.

A particularly advantageous aspect of utilizing the novel process of this invention is that the formation of nits and knots is considerably reduced as compared to techniques not involving drying and cure while entrained in a stream of turbulent superheated steam. As is known in the art, the formation of nits and knots is a common problem in the preparation of resilient bulking fibers especially when chemical crosslinking is employed.

It has been common practice in the art to employ debonding agents, mechanical defibration such as hammer milling and screening to reduce the nit/knot content of the treated fibers. Such measures tend to be costly and can be deleterious to the fiber and paper quality. The novel process of this invention reduces the amounts and severity of nits and knots formed and thereby provides additional economic benefits.

The novel process of this invention is applicable to dry lap or never-dried wood fibers. Any at least partially chemically digested wood pulp fiber may be used. Bleached high-or low-brightness pulps may be used. We prefer kraft pulps, ideally high brightness kraft softwood pulps, but

either hardwood or softwoods pulped using the kraft, sulfite, soda cook, and modifications of these processes may be used. Throughout this specification and claims, the term "fibers" should understood to comprehend both the relatively high aspect ratio particles typically referred to as fibers as well as the lower aspect ratio particles and fiber debris often referred to as fines.

The process of this invention is not limited to wood pulp fibers but is applicable to fibers such as bagasse, kenaf, abaca, bamboo, sisal, cotton and other individualized non-wood cellulosic fibers.

The cured fibers thus prepared can then be dispersed for use. Preferably, the dispersion step involves contacting the cured fibers with water or preferably with a foamed furnish. These bulking fibers may then be used — alone or in blends — to prepare products that exhibit improved bulking and absorbent properties. The improvement in absorbency relates both to faster rate of absorbency and to increased fluid-holding capacity. The amounts of crosslinked fibers used to prepare the products are readily determinable by those skilled in the art. For instance, filtration and absorbent product applications will often be made 100% from the fibers of the present invention. On the other hand, towel and tissue paper products may be made by blending fibers according to the present invention with a majority of conventional wood pulp fibers. In such applications, crosslinked fibers may be used in an amount of about 30% or less, preferably about 15% by weight of the paper product.

Fig. 2 illustrates the complete process of this invention in that a slush fiber at a consistency of about 10-12% is stored in chest 12 which is conducted to screw press 14 and dewatered so that the consistency is at least 40 wt% solids. Dewatered fiber leaves line 16 and is conducted to repulper 18. Reject water is conducted

through line 20 and may be discharged or used in other places in the plant environment. The crosslinking agent and catalyst are introduced through line 22, while makeup water bearing catalyst and crosslinking agent not previously absorbed is introduced through line 24. The pulp impregnated with crosslinking agent at a consistency of 1-40%, preferably 4-12 wt%, more preferably 6-8 wt%, is conducted through line 26 to equilibration chest 28. Equilibration is an optional step which is normally used to ensure more effective utilization of crosslinking agent by allowing sufficient time for thorough impregnation of the fibers. When equilibration chest 28 is used, it is maintained at relatively low agitation to allow the fiber to become thoroughly impregnated with the crosslinking chemicals. Treated fiber from equilibration chest 28 passes through line 34 and is conducted to screw press 36. Water and chemicals rejected in screw press 36 are recycled through line 38. The fibers from screw press 36 are conducted through line 42 to a shredding conveyer 44 and thence through line 46 to rotary feed valve 48 and a defibrator 49 into pressurized dryer 50.

As can be seen, the pressurized dryer 50 comprises a long tortuous partially steam-jacketed tube 51 having numerous bends 54 formed therein. As disclosed in said US Patent No. 4,244,778, a turbulent flow is created which entrains the fibers and leads to additional fiber individualization and/or fluffing.

The dried fiber exits through line 55 into cyclone 60 wherein steam can be recycled through line 61. Fiber which is separated in cyclone 60 passes through line 62 to the curing section 65 via rotary valve 63 and fluffer 64 (optional) . Curing section 65 is substantially identical to dryer 50, except that the materials used should be capable of withstanding the higher temperatures often involved in the practice of the present invention. As

before, flow through the curing tube provides turbulence and entrains the fiber in superheated steam.

The fiber is then led via line 66 into cyclone 67 wherein the fiber is separated from the superheated steam. The fiber exiting through rotary valve 68 and line 69 is thereafter optionally washed, refluffed, pressed and/or baled or conducted directly to further processing operations.

Superheaters 52 are, in both drying and curing sections, used to boost temperatures to bring the incoming fiber up to operating temperatures quickly.

Although a screw press is depicted for dewatering, it is considered obvious that other equipment can be used which performs a similar function such as a twin roll or belt press. Similarly, where we have indicated a shredding conveyor, a simple screw conveyor, belt conveyor or similar apparatus can be used. In some cases, it may be advantageous to use an inclined wire or other dewatering equipment, such as a centrifuge, to impart a two- dimensional structure to the dewatered fiber.

The following examples will now illustrate the best mode contemplated for carrying out the invention.

In the examples which follow, the process described in Fig. 2 was used with combinations of various pulps with various crosslinking agents as indicated. The temperature of the superheated steam in the dryer when the fiber entered through line 46 was about 250°C and it dropped to about 190°C when the fiber exited through line 55. The temperature of the superheated steam in the curing tube was about 350°C when the fiber entered through line 62 and it dropped to about 200°C when it exited through line 66. The dryer operated at a pressure of about 20-25 psia and the curing tube pressure was about 20-25 psia. Had lower dryer temperatures been used, it would have been desirable to use higher temperatures for the superheated steam in the curing

section. In some cases, the higher curing temperature would have been detrimental to fiber quality.

In each of the examples, 15 wt.% of the fiber produced was blended with 85 wt.% of a control furnish and pressed into British handsheets according to Tappi standard methods except that a pressing pressure of 15 psig was used. Bulk, breaking length and brightness were measured and compared to handsheets made from said control furnish. Throughout this specification and claims, the term "standard bulk" should be understood to comprehend the bulk of a handsheet formed as described in this paragraph.

The typical control furnish and the properties of handsheets made therefrom is listed below:

CONTROL FURNISH Compositions 50 wt.% Previously-dried Softwood Kraft 50 wt.% Never-dried Northern Hardwood Kraft

Properties (All measured at 400 Canadian Standard Freeness (CSF)

Bulk B. L. ^l Brite ² cc/g km %

2.4 4.4 85.6

¹ Breaking length

² % Brightness as determined by a G. E. brightness meter

EXAMPLES 1-3 These examples will illustrate the novel process of this invention when citric acid catalyzed by sodium hypophosphite is used as a crosslinking agent.

EXAMPLE 1

Never-dried hardwood Kraft fibers were treated with a solution of citric acid and sodium hypophosphite in accordance with the process described in Fig. 2 to produce fiber having 4.1 wt% citric acid and 1.4 wt% sodium hypophosphite in/on the fiber based on dry weight of the fiber. Handsheets obtained by blending 15 wt.% of the fiber had the properties listed below:

Bulk B. L. Brite cc/g km %

3.3 3.8 77.2

EXAMPLE 2

Dry lap softwood Kraft fibers were treated with a solution of citric acid and sodium hypophosphite in accordance with the process described in Figure 2 to produce fiber having 5.0 wt% citric acid and 3.9 wt% sodium hypophosphite in/on the fiber based on the dry weight of the fiber. Handsheets obtained by blending 15 wt.% of the fiber had the properties listed below:

Bulk B. L. Brite cc/g km %

3.5 3.4 81.2

EXAMPLE 3

Never-dried softwood Kraft fibers were treated with a solution of citric acid and sodium hypophosphite in accordance with the process described in Figure 2 to produce fiber having 4.9 wt% citric acid and 1.3 wt% sodium hypophosphite in/on the fiber based on the dry weight of the fiber. Handsheets obtained by blending 15 wt.% of the fiber had the properties listed below:

Bulk B. L. Brite cc/g km %

3.6 3.4 77.0

EXAMPLES 4-9 These examples will illustrate the novel process of this invention when l,3-dimethyl-4,5- dihydroxyimidazolidione (DMDHEU) catalyzed by magnesium chloride is used as a crosslinking agent.

EXAMPLE 4

Never-dried softwood Kraft fibers were treated with a solution of DMDHEU and magnesium chloride in accordance with the procedure of Fig. 2 to produce fiber having 3.0. wt% DMDHEU and 0.3 wt% magnesium chloride in/on the fiber based on the dry weight of the fiber. Handsheets obtained by blending 15 wt.% of the fiber had the properties listed below:

Bulk B. L. Brite cc/g km %

4.3 3.2 80.8

EXAMPLE 5

Never-dried softwood Kraft fibers were treated with a solution of DMDHEU and magnesium chloride in accordance with the procedure of Fig. 2 to produce fiber having 3.0 wt% DMDHEU and 0.3 wt% magnesium chloride in/on the fiber based on the dry weight of the fiber. Handsheets obtained by blending 15 wt.% of the fiber had the properties listed below:

Bulk B. L. Brite cc/g km %

4.1 3.1 82.8

EXAMPLES 6-11 Examples 6-11 illustrate the novel process of this invention when citric acid catalyzed with sodium monophosphate is used as the crosslinking agent.

EXAMPLE 6

Previously dried softwood Kraft fibers were treated with a solution of citric acid and sodium monophosphate in accordance with the process described in Fig. 2 to produce fiber having 5.0 wt% citric acid and 3.9 wt% sodium monophosphate in/on the fiber based on dry weight of the fiber. Handsheets obtained by blending 15 wt.% of the fiber had the properties listed below:

Bulk B. L. Brite cc/g km %

3.5 3.4 81.2

EXAMPLE 7

Never-dried softwood Kraft fibers were treated with a solution of citric acid and sodium monophosphate in accordance with the process described in Fig. 2 to produce fiber having 6.8 wt% citric acid and 5.1 wt% sodium monophosphate in/on the fiber based on dry weight of the fiber. Handsheets obtained by blending 15 wt.% of the fiber had the properties listed below:

Bulk B. L. Brite cc/g km %

3.4 3.2 82.0

EXAMPLE 8

Never-dried softwood Kraft fibers were treated with a solution of citric acid and sodium monophosphate in accordance with the process described in Fig. 2 to produce fiber having 3.7 wt% citric acid and 3.4 wt% sodium monophosphate in/on the fiber based on dry weight of the fiber. Handsheets obtained by blending 15 wt.% of the fiber had the properties listed below:

Bulk B. L. Brite cc/g km %

3.4 3.1 82.0

EXAMPLE 9

Secondary fibers were treated with a solution of citric acid and sodium monophosphate in accordance with the process described in Fig. 2 to produce fiber having 4.1 wt% citric acid and 3.0 wt% sodium monophosphate in/on the fiber based on dry weight of the fiber. Handsheets obtained by blending 15 wt.% of the fiber had the properties listed below:

Bulk B. L. Brite cc/g km %

3.0 3.5 80.4

EXAMPLE 10

Never-dried softwood Kraft fibers were treated with a solution of citric acid and sodium monophosphate in accordance with the process described in Fig. 2 to produce fiber having 5.7 wt% citric acid and 1.2 wt% sodium monophosphate in/on the fiber based on dry weight of the fiber. Handsheets obtained by blending 15 wt.% of the fiber had the properties listed below:

Bulk B. L. Brite cc/g km %

4.0 3.0 83.1

EXAMPLE 11

The process of Example 10 was repeated with the exception that the fiber was not cured in turbulent superheated steam. In this example, the fiber exiting the cyclone from the pressurized dryer was mechanically fluffed, made into a handsheet and cured by passing 190°C air through the sheet for 40 seconds. The handsheets had the properties listed below:

Bulk B. L. Brite cc/g km %

4.3 3.1 82.1

As can be seen a lower brightness value was obtained as compared to Example 10.