CZ20001011A3 - Pressure drop in wet state in drying membrane with restricting clearness and paper manufacturing process by making use of such membrane - Google Patents

Abstract

The process for producing paper, in particular tissue paper, comprises: the step of fabricating the seed layer and fabricating microporous membranes with a pore size that ensures restricting the flow of air through the embryonic a strip layer which is less than or equal to 20 microns. The microporous membrane shows a through drop wet pressure, which increases as the flow rate increases according to the formula 254OY <0.042X + 0.767, where X is the speed flow in scmmna 80,8 cm2 aY is poklestlaku wet in centimeters of mercury column. The process further comprises a step placement of the embryonic band layer namicroporous membrane and air permeation through the embryonic ribbon layer and microporous membrane, resulting in The germline strip layer removes water. In this procedure followed by removal of the germline sheet layer from the microporous membrane, wherein between the pressure drop at wetness and flow rate apply 2540Y <0.042X + 0.698, especially for a flow rate range of 0.98 to 2.66 scmm to 80.8 cm2. It is particularly suitable for this procedure microporous membrane for use with air a drying paper-making machine with a pore size of less than or equal to 20 microns. This microporous the membrane simultaneously exhibits at a flow rate of 0.12 scmm to 80.8 cm2 the wet pressure drop is less than or equal to 10.16 cmColumn mercury.

Description

The drop in wet pressure in a drying membrane with a restrictive throughput and the papermaking process using this membrane

Area flow

The present invention relates to an apparatus for absorbent germline web materials which are dried through the air to form a cellulosic fibrous structure, and in particular it relates to an apparatus that exhibits energy savings in carrying out the through air drying process.

BACKGROUND OF THE INVENTION

Absorbent sheet materials include cellulosic fibrous structures, absorbent foams, etc. Cellulosic fibrous structures have become a daily necessity. Cellulosic fibrous structures can be found in make-up papers, toilet papers and paper towels.

During the manufacture of cellulosic fibrous structures, a suspension of cellulosic fibers suspended in a liquid carrier is applied to the forming screen to form a seed band. The result is a wet seed layer which can be dried using one known desiccant or a combination of known desiccants, each of which desiccants will affect the properties of the resulting cellulosic fibrous structure. The compositions and processes used to dry the cellulosic fibrous structures also affect the ratio at which the cellulosic fibrous structures can be produced, although not solely by a ratio that is limited only by such means and processes.

An example of one type of desiccant is felt webs. Felt drying belts have long been used to dewater germ cellulosic fibrous webs using the capillary flow of a liquid carrier into a permeable felt medium that is maintained in contact with the germline sheet. However, the dewatering of the cellulosic fibrous web into the felt web or using the felt web results in a total uniformity. Compressing and densifying the embryonic sheet layer of the cellulosic fibrous structure that is dried. The resulting paper is often stiff and does not give a feeling of softness.

Drying using a felt web can be promoted by vacuum or by the action of opposed, opposed pressure rollers. The pressure rollers enhance the effect of mechanically adding the web to the cellulosic fibrous structure. Examples of webbing drying are described in U.S. Patent 4,329,201, issued May 11, 1982 to Bolton, and U.S. Patent 4,888,096, issued December 19, 1989 to Cowan et al.

It is also known in the art to dry cellulosic fibrous structures by vacuum dewatering without the aid of felt webs. Vacuum dewatering of the cellulosic fibrous structure mechanically removes moisture from the cellulosic fibrous structure, which moisture is in the form of a liquid. In addition, when the vacuum is used in combination with a belt of the forming template type, the effect of such vacuum also draws discontinuous regions of the cellulosic fibrous structure into the deflection channels of the drying web and significantly contributes to the occurrence of different amounts of moisture in different regions of the cellulosic fibrous structure. Similarly, it is known in the art to dry a cellulosic fibrous structure by a capillary flow method which is supported by a vacuum that is generated in a porous cylinder having a preferred pore size. Examples of such vacuum-controlled drying processes are disclosed in similarly directed patents, namely, U.S. Patent No. 4,556,450 issued December 3, 1985 to Chuang et al. and U.S. Patent No. 4,973,385 issued to TJ. in the name of Jean et al.

Another drying process that has brought remarkable success is drying the embryonic ribbon layer of the cellulosic fibrous structure through the air. In a typical air-permeable drying process, the dried embryonic ribbon layer is transferred to a perforated air-permeable ribbon. The hot air stream permeates through the cellulosic fibrous structure and then through the air-permeable web or vice versa. The air stream dries the seed layer substantially by evaporation. The regions which are adjacent and partially enter the perforation of the air permeable strip are dried particularly advantageously. The areas adjacent to the hinges in the air permeable belt are dried to a lesser extent by the air flow.

In this field, air-permeable strips have been improved several times and are used for air-permeable drying. Air-permeable belt with

For example, it can be fabricated to have a large permeable or open area, which is at least forty percent. Alternatively, such a belt may have limited air permeability. The limited air permeability can be achieved by applying a resin composition for sealing the joints between the spun yarns in the belt. The desiccant web may be impregnated with metal particles to increase its thermal conductivity and reduce its radiation, or alternatively there is the possibility of making the web of light-sensitive resin in the form of a continuous web. The desiccant web may be particularly adapted to provide air at a high temperature of up to 815 ° C (1500 ° F). Examples of such air permeable drying technology are found in U.S. Patent Re. No. 28,459, reissued on July 1, 1975 in the name of Cole et al .; U.S. Pat. No. 4,172,910, issued October 30, 1979 to Rotar, and U.S. Pat. No. 4,251,928, issued February 24, 1981 to Rotar et al .; commonly assigned U.S. Patent 4,528,239 issued July 9, 1985 to Trokhan, which is incorporated herein by reference; and U.S. Patent 4,921,750, issued May 1, 1990 to Todd. Several attempts have been made in the art to regulate the dried profile of the cellulosic fibrous structure while it is still in the embryonic sheet layer to be dried. In such experiments, either a drying belt or an infrared dryer can be used in combination with a Yankee lid. Examples of profiled drying are shown in U.S. Patent 4,583,302 issued April 22, 1986 to Smith and U.S. Patent 4,942,675 issued June 24, 1990 to Sundovist.

Although the prior art is particularly concerned with air-permeable drying, it does not address the problems that need to be encountered when drying a cellulosic fibrous structure with several regions. For example, a first region of cellulosic fibrous structure having less absolute moisture, density, or basis weight than the second region will exhibit greater air permeability than the second region. This relatively greater air permeability occurs because less absolute humidity, density and basis weight represent a proportionally less airflow resistance passing through such an area.

This problem reappears after relocation of the dried cellulosic fibrous structure with several regions on the Yankee dryer drum. On the Yankee desiccant drum, separate, separated regions of the cellulosic fibrous structure are in close contact with the periphery of the heated drum and hot air from the lid is introduced to the surface of the cellulosic fibrous structure that is opposite to the heated drum. However, it is typical that for the closest touch, · fe ················· > ······························································

-4 with the Yankee Dryer Drum occurs in an area of high density or basis weight. After removal of some moisture from the cellulosic fibrous structure, regions of greater density or greater basis weight do not achieve such a degree of drying as regions of lower density or less basis weight. Preferred drying of the less dense areas is due to the convective heat transfer from the air stream in the lid of the Yankee drying drum. In this context, the production ratio of the cellulosic fibrous structure must be slowed down to compensate for the drying of more moisture in areas of greater density or basis weight. In order to completely dry the area of greater density and basis weight of the cellulosic fibrous structure and to prevent burning or smoldering of already dried areas of low density or basis weight due to the effect of hot air from the lid, there is a need to lower the air temperature from the Yankee lid. on the other hand, the simultaneous extension of the residence time of the cellulosic fibrous structure in the Yankee lid, thereby slowing the resulting production ratio.

A further drawback of the prior art approaches (with the exception of those that use mechanical compression, as is the case with felt webs) is that each of them relies on supporting the dried cellulosic fibrous structure. The air flow passes through the cellulosic fibrous structure and then through the carrier web or, alternatively, it first passes through the drying belt and then through the cellulosic fibrous structure. Differences in resistance to air permeability through the web or through the cellulosic fibrous structure multiply the differences in moisture distribution in the cellulosic fibrous structure and / or create differences in the occurrence of moisture where no moisture previously existed.

One prior art improvement that addresses this problem is shown in U.S. Pat. No. 5,274,930, issued January 4, 1994 to Ensign et al. and which describes the drying of cellulosic fibrous structures by means of a membrane having a limited pore size in combination with the drying by permeable air, the patent being incorporated herein by reference. This patent discloses a device that utilizes a microporous drying membrane that has greater resistance to permeability than joints between the fibers of the cellulosic fibrous structure. Under these circumstances, the microporous membrane forms a restrictor orifice during permeable air drying which uniformly or at least more uniformly affects the moisture distribution in the drying process.

· * * «« «« «« «« «« «« «« «« «« «« «« «« · · ··· · · · ·

Some other improvements in this art that focus on desiccant problems are shown in the same subject-matter US patents, namely, U.S. Patent 5,543,107 issued August 1, 1995 to Ensign et al .; U.S. Patent 5,584,126 issued December 19, 1996 to Ensign et al .; and U.S. Patent 5,584,128, issued December 17, 1996 to Ensign, the disclosures of which are incorporated herein by reference. The '126 and' 128 patents of Ensign et al. disclose a multi-zone aperture limiting device for permeable air drying of cehilos fiber structures. However, the '126,' 128 and '930 patents of Ensign et al. do not mention anything about minimizing the pressure drop across the microporous desiccant membrane when it encounters a liquid flow or a two-phase flow. The magnitude of the pressure drop over the meniscus fluid in the capillary is important. As the pressure in the diaphragm decreases at a given flow rate, the power demand required to drive the fan or fans that suck air through the device decreases. Reducing fan performance is an important source of energy savings. By balancing the power and dropping the pressure, it is possible to suck in an additional stream of air passing through the cellulosic structure, thereby improving the drying ratio. The improved drying ratio allows for increased paper machine performance.

A restricting membrane of the permeable air desiccant device according to the '107 patent of Ensign et al. it has one zone or a plurality of zones with either negative or positive pressure to promote flow in each direction.

Applicants have unexpectedly found a method for treating a microporous desiccant membrane that is used in prior art devices. This method of treating a known microporous desiccant membrane reduces the pressure drop in a steady flow of liquid or biphasic flow, or alternatively increases the liquid flow or biphasic flow of a steady pressure drop. In addition, it has unexpectedly been found that the present invention can be additionally incorporated into the prior art microporous desiccant dryer without the need for substantial redesign.

The apparatus of the present invention is useful for making paper. The paper may be dried through the air. If air permeability drying is to be carried out, the procedures described in U.S. Pat. No. 4,191,609 issued March 4, 1980 to Trokhan and U.S. Pat. No. 4,528,239 may be used for such permeability air drying. the contents of both patents are incorporated herein by reference. 4 444444 4 4 4444 444 * 444 4444 * 4 *

4,444 4,444

444 444 44 444 44 44

-6in the form of reference. If conventional drying is to be carried out, such conventional drying is carried out according to the same subject-matter U.S. Patent No. 5,629,052, issued May 13, 1997 to Trokhan et al., The contents of which are incorporated herein by reference.

SUMMARY OF THE INVENTION

The present invention relates to a microporous membrane. The microporous membrane can be used in a papermaking device for air-permeable drying and, in addition, can create a restricting orifice for the air-permeable flow. The microporous membrane may exhibit a wet pressure drop across the membrane, wherein the wet pressure drop value is less than or equal to 10.16 cm (i.e., 4 inches) of mercury at a flow rate of about 1.12 scmm (i.e., 40 scfin) to 80.8 cm ² (ie 0.087 square feet). With an increase in flow rate from about 1.68 to about 2.24 scmm (i.e., from about 60 to about 80 scfin) to

80.8 cm ² (i.e. 0.087 square feet), the wet flak drop reaches a value that is less than or equal to 12.7 cm (i.e., 5.0 inches) and 15.24 he (i.e. 0 inches) columns of mercury.

The relationship between flow rate and flak drop is given by the general formula which states that the wet flak drop in inches of mercury column is less than or equal to 0.048 times the flow rate in scfin to 0.087 square feet + 2.215.

Another aspect of the present invention relates to papermaking using a microporous membrane. The paper is made by making the seed layer and using microporous membranes having a predetermined pore size. Pore size is a limiting factor of airflow permeability through the embryonic band structure. The pore size is preferably less than or equal to 20 microns. The microporous membrane also exhibits a continuous wet pressure drop. The wet drop in the wet increases as the flow rate through the membrane increases.

The embryonic band structure is placed on the microporous membrane. Air permeates through the germ structure and microporous membrane, where air encounters a drop in wet flak due to permeation at a predetermined flow rate through the germline sheet and microporous medium. Flow Rate and Falling Drop in • 0 • · · 0 0 0 0 0 0 0 0 «0 00000 0 0 0 0 · 0 0 · 0 0 0»

000 »00 00 000» 0 0 0

-7wets create a relationship that can be generally expressed by the formula:

Y0.048X +2.215 in which Y is the wet pressure drop in inches of mercury and X is the flow velocity in scfin to 0.087 square feet, calculated as follows:

2540 Y <0.042X + 0.767 where X is the flow rate in scmm to 80.8 cm ² and Y is the wet pressure drop in centimeters of mercury column. This general formula applies to a range of flow rates of from about 35 to about 95 scfin (i.e., from about 0.98 to about 2.66 scmm) per 0.087 square feet (ie.

80.8 cm ^2, and more preferably for a range of flow rates of from about 40 to about 80 scfin (ie, from about 1.12 to about 2.24 scmm) per 0.087 square inch (ie, 80.8 cm ² ).

BRIEF DESCRIPTION OF THE DRAWINGS.

The present invention will now be described with reference to the drawings, in which:

Giant. 1 is a side cross-sectional view of a microporous membrane of the present invention that is incorporated on a permeate roller with an increase in thickness for clarity.

Giant. 2 is a plan view of a portion of a microporous membrane according to the present invention showing different layers.

Giant. 3 is a schematic view of a device that is useful for testing the invention.

Ohr. 4 is a graph of the relationship between flow rate and wet pressure drop.

DETAILED DESCRIPTION OF THE INVENTION

Referring to Fig. 1, the present invention includes a permeable air dryer 20 with limited permeability in combination with a microporous membrane 40. The apparatus 20 and membrane 40 may be fabricated according to the aforementioned U.S. Patents 5,274,930; 5,543,107; 5,584,126; 5,584,128; and U.S. Patent Application Serial No. 08 / 878,794, filed June 16, 1997 under the name of Ensign et al., the contents of which are incorporated herein by reference. The device 20 comprises a permeate cylinder 30. The microporous membrane 40 may describe the circumference of the permeate cylinder 32.

Fc fc fc fc fcfc fcfc fcfcfcfc fcfc fcfc fcfcfcfc fcfc fcfc

A carrier member 28, such as an air-drying belt or a pressure felt web, surrounds the permeable roller 32 from the supply roller 34 to the discharge roller 36, forming an arc defining a portion of the circle. This portion of the ring may be divided into a number of zones having differently differentiated differential flake relative to the atmospheric flake. Alternatively, the apparatus 20 may comprise a split vacuum slot, flat or arcuate plates, or an endlessly circulating belt. The device 20 removes moisture from the seed layer 21.

As confirmed by reference to FIG. 2, the microporous drying membrane of the present invention comprises a number of layers 41-46. The microporous membrane 40 of the present invention may have a first layer 41 that is closest to the seed layer 21 and is in contact with the seed layer 21. It is preferred that the first sheet 41 is woven, and more preferably it is woven with Dutch twill or BMT ZZ weave.

Below or below the first layer 41 may be one or a plurality of additional layers 42-46. The lower layers 42-46 provide support for the layers 41-45 and serve to stretch the fatigue deflection. The layers 41-46 may have an increased pore size to remove water passing through the underlying layers 42-46. At least one layer 41, and more specifically the pores on the surface that is in contact with the seed layer 21, have, as will be described in more detail below. Alternatively, all and all of the layers 41-46 that form the membrane 40 of the present invention can be treated to have a low surface energy, which will be explained below. Although Fig. 2 shows six layers, it will be apparent to one skilled in the art that any acceptable number of layers can be utilized in the membrane 40.

Each of the layers 41-46 has two opposite surfaces, a first surface and a second surface. These first and second surfaces are in fluid communication through the permeable pores.

The membrane 40 of the present invention has a pore size of less than 20 microns. The membrane 40 further exhibits a moisture pressure drop at 1.12 scmm (i.e. 40 scfin) per 80cm ² (0.087 square feet) of less than 10.16 cm (i.e. 4.0 inches), preferably less than 8.89 cm (i.e. 3.5 inches) and more preferably less than 7.62 cm (i.e. 3.0 inches) of mercury. The diaphragm 40 further exhibits a drop in moisture flux at 1.68 scmm (i.e., 60 scfin) to 80.8 cm ² (i.e., 0.087 square feet) of less than 12.7 cm (i.e., 5.0 inches), preferably less than 11 inches. 43 cm (i.e., 4.5 inches) and even more preferably less than 10.16 cm (i.e., 4.0 inches) of mercury. The membrane 40 further exhibits a drop in moisture flux pn of 2.24 scmm (i.e. 80 scfin).

··· · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · ···

-9 to 80 cm ² (i.e., 0.087 square feet) less than 15.24 cm (6.0 inches), preferably less than 13.97 cm (i.e. 5.5 inches) and even more preferably less than 12.7 cm ( i.e., 5.0 inches) of mercury. These characteristics of the membrane 40 according to the present invention are shown in the "Table"

Table 1

Flow ratio (scmm / 80.8 square centimeters) (scfin / 0.087 square feet) 1.12 (40) 1.68 (60) 2.24 (80) Maximum wet pressure drop (cm mercury) (inches of mercury) 10.2 (4.0) 12.7 (5.0) 15.2 (6.0) Advantageous wet pressure drop (cm mercury) (inches of mercury) 8.9 (3.5) 11.4 (4.5) 14.0 (5.5) More favorable wet pressure drop (cm mercury) (inches of mercury) 7.6 (3,0) 10.2 ^ (4>) 12.7 (5.9)

As used herein, "scfm" refers to the flow rate of a standard cubic footprint (i.e., 0.0283 m ³ ) of air at 20.1 ° C (ie, 70 ° F) and a pressure of 76.0 cm (ie, 29.92) of mercury. columns.

Referring to Fig. 4, the relationship between flow velocity and wet pressure drop can be approximately determined as a linear relationship over a flow velocity of from 1.12 to

2.24 scmm (i.e., from 40 to 80 scfin) per 80.8 cm ² (i.e., 0.087 square feet) and for certain values can be approximately determined by a linear relationship from flow rates in the range from 0.98 to 2.66 scmm (i.e., from 35 to 95 scfin) per 80.8 cm ² (i.e., 0.087 square feet).

In particular, the relationship between pressure drop and flow velocity is given by the formula:

2540 YS0.042X +0.767 and more preferably: 2540 Y 0,0 0.042X + 0.698 wherein X is the flow rate in scmm to 80.8 cm ² and Y is the wet pressure drop in centimeters of mercury.

YS0.048X +2.215 and more preferably: Y < 0.048X + 2.015 wherein X is the scfin flow rate to 0.087 square feet and Y is the wet pressure drop in mercury inches.

The drying performance of the example membrane 40 of the present invention was compared to the drying performance of the uncoated membrane 40. In order to create stricter conditions.

0000 • »0

0 000

0 0 0 · · 0 0 0 0

0 0 0

0 0 0 · 0 0

0 0 0

0 00

In the case of the first layer 41 of the membrane 40 according to the present invention, a finer pore size was used than the first layer 41 of the uncoated membrane 40. In particular, the membrane 40 according to the present invention was a membrane 40 having a 200 x 400 Dutch twill weave coated KRYTOX DF, mentioned earlier in connection with the first layer 41.

Both membranes were tested for layer compaction over different time periods of germ structure residence on these membranes. The test was carried out under conditions of a constant wet pressure drop of 10.3 cm (i.e. 4.3 inches) of mercury. At a residence time of 50 milliseconds, the density increased by two percentage points. By extending the residence time to 150 milliseconds, the density increased by seven percent rolls. By extending the residence period to 250 milliseconds, the density increased by nine percentage points. These results are shown in "Table Π":

Table Π

Duration of stay Increase density to uncoated (milliseconds) membrane (percentage points) 50 2 150 7 250 9

It can be seen that the invention advantageously improves drying over a period of residence.

Referring to FIG. 2 it can further be noted that achieving a relatively low wet pressure drop is ensured as follows. The first surface, which is oriented towards the high pressure or to the side from which the air or water jet passes, should have low surface energy in accordance with the present invention (will be explained below). Also, the pores between the first and second surfaces, especially those pores that create a restricting orifice on the flow path, should also have a surface with low surface energy, which will be discussed further below.

Low surface energy can be achieved by coating the surface. The coating is applied after joining and sintering the layers 41-46 as a unit to prevent the detrimental effects of the manufacturing operation on the coating or to prevent the detrimental effects of the coating on the manufacturing operation.

• 0 ·

In accordance with the present invention, the diaphragm 40 is coated to reduce the pressure drop during the passage of liquid or biphasic flow. In particular, the coating reduces the surface energy of the membrane 40 as a result of which the membrane becomes more hydrophobic. Any coating that reduces the surface energy of the microporous membrane 40 is acceptable for the purposes of the present invention, although coating of the first layer 41 of the microporous membrane 40 seems to be a particularly effective method of reducing surface energy. It appears advantageous to reduce the surface energy to less than 46 dynes per cm ( centimeter), more preferably less than 36 dynes per cm and most preferably less than 26 dynes per cm.

Surface energy refers to the amount of work required to increase the surface area of a liquid on a rigid surface. In the case of rigid surfaces, the cosine of the liquid-to-surface contact angle is a monotonous function of the surface tension of the liquid. The closer the contact angle approaches zero, the wolf's surface is wet. If the contact angle equals zero, the solid surface is perfectly wet. If the contact angle approaches 180 °, then the surface approaches a condition where the surface cannot be wetted. It will be appreciated that neither the zero angle nor the 180 ° contact angle is associated with the water that can be used in the liquid suspension of the present invention. As used herein, the term surface energy refers to the critical surface tension of a solid surface and can be empirically determined by extrapolating the relationship between the surface tension of the liquid and its contact angle on the surface of interest. In this sense, the surface energy of the solid surface is indirectly measured with respect to the surface tension of the fluid present on the solid surface. Further details regarding surface energy can be found in "Adv. Chem. Ser. "No. 43 (1964) by W. A. Zisman and in" Physical Chemistry of Surfaces "Fifth Edition (1990) by Arthur W. Adamson, both of which are incorporated herein by reference.

Surface energy is measured using low surface tension solutions (for example, a mixture of 2-propane with water or methanol with water). In particular conditions of the present invention, the surface energy can be measured by applying a calibrated dyn pen to the surface of the membrane 40 based on assessment. The contact area should be at least 2.54 cm (i.e. one inch) long to ensure proper reading. The surface is tested at 21.1 ° C ± 2 ° C (ie 70 ° F ± 5 ° F). Applicable pen pens are marketed by the Control-Cure Company of Chicago, Illinois.

Alternatively, there is the possibility of using a goniometer when correcting the surface topography results of the layers 41-46. In general, the coarser the surface, the apparent contact angle is less than the actual contact angle. If the surface is porous, as is the case with the layers 41-46 of the present invention, then the apparent contact angle is greater than the actual contact angle due to the increased surface in contact with the liquid-air.

Non-limiting and illustrative examples of suitable coatings that are useful for reducing surface energy include both liquids and dry film lubricants. Useful dry film lubricants include fluorotelomers such as "KRYTOX DF" manufactured by "DuPont Corporation" in Wilmington, Delaware. The dry film lubricant may be dispersed in fluorinated solvents from the Freon family, which includes 1,1-dichloro-1-fluoroethane or 1,1,2-trichloro-1,2,2-trifluoroethane or isopropyl alcohol, etc. KRYTOX DF "Is preferably heat cured to melt the" KRYTOX DF "grease. Vulcanizing at 316 ° C (ie 600 ° F) for 30 minutes appears to be acceptable to the membrane 40 of the present invention.

Alternatively, the coating material may comprise other particles to promote low surface energy that are dispersed in the liquid carrier. Particularly useful particles include graphite or molybdenum disulphite powder.

Alternatively, the coating material may be a fluid. A suitable liquid coating material is a potydimethylsiloxane fluid, such as a one percent solution with the trade name "GE Silicones DF 581" supplied by "The General Electric Corporation" of Fairfield, Connecticut. The polydimethylsiloxane fluid may be dispersed in isopropyl alcohol or hexane. It has also been found that 2-hexyl-1-hexanol is also a suitable carrier for the purposes of the present invention. After being applied to the membrane 40, the polydimethylsiloxane is heat treated to increase its cross-linking molecular weight and to evaporate said carrier. It has been found that a one hour heat treatment at 260 ° C (ie 500T) is acceptable for the purposes of the present invention.

Coating materials, films, or liquids can be sprayed, printed, applied by brush or roller onto the membrane 40. Alternatively, there is the possibility of immersing the membrane 40 in the coating material. A relatively uniform sheet is preferred. The dry film coating material is preferably applied at relatively low concentrations such as 0.5 to 2.0 weight percent

-13procenta. It is believed that it is important to avoid clogging the small pores of the 41-46 microporous membrane layers 40. Solutions containing silicone coatings may be applied at concentrations of from about 0.5 to about 10 weight percent, and preferably from about 1 to about 2 weight percent. .

Optionally, organically modified ceramic materials known as ormocets may be used to reduce the surface energy of membrane 40. Ormocers can be made according to the procedure disclosed in U.S. Patent No. 5,508,095, issued April 16, 1996 to Allum et al., Which is incorporated herein by reference. For the purpose of reducing the surface energy of the membrane 40, it will be apparent that various dry foil lubricants, various fluid coatings, various ormocers, and combinations thereof may be used.

If the coatings are used to enhance the hydrophobic grease by a microporous drying membrane, then it seems important that the coatings do not clog the fine pores of the layers 41-46, and especially the first layer 41 of the membrane 40. The layers 41-46, especially the first layer 41, must have such pores whose dimensions in any direction are less than or equal to 20 microns, or even less than or equal to 10 microns. The pore size is prescribed by SAE ARP 901, the contents of which are incorporated herein by reference. The pore size of the layers 41-46 may gradually increase from the first layer 41 to the last plate 46, the last plate 40 being located furthest from the first plate 41. The dry film coatings and fluid coatings mentioned are successfully used without causing clogging of the layer pores 41 and to 46. A coating that largely clogs the pores of membrane 40 is not acceptable. For example, a coating whose thickness and / or concentration is too large is not acceptable.

In addition to coating the surface of one or more of the membrane layers 41-46 for the purpose of reducing the surface energy described above, it is optionally possible to fabricate the membrane from a material that has low surface energy per se. Although the above patents cite stainless steel as a usable material for layers 41-46, there is also the possibility of impregnating or making layers 41-46, especially the first layer 41, using low surface energy materials such as tetrafluoroethylene, which is commonly available on the market available under the trade name "TEFLON" and manufactured by "DuPont Corporation" in Wilmington, Delaware, or using extruded low surface energy plastics such as potyesters or polypropylenes. It will be clear that even the materials they have

By itself, a low surface energy can be coated as described above to achieve an even lower surface energy level.

In yet another alternative embodiment, the device 20 may only require a through air drying zone and may omit the capillary drying zone. It is believed that such a device is also useful in combination with the present invention.

In another embodiment, one of the intermediate layers 42-45 may have the smallest flow pores. In this embodiment, there will be such an intermediate layer (one of the layers 42 45). In this embodiment, it is important that the intermediate layer 42-45, which has the greatest flow resistance, have a low surface energy, the efficiency of which has been explained above. It will be appreciated that, as in the previously described embodiments, it is desirable to position the low surface energy surface on the high pressure side (i.e., the side facing upstream) and within the pore stopper of such a layer 41-45.

The reference to Fig. 3 is related to the following pressure drop measurement method. A sample of membrane 40 having a suitable size is fabricated to form a circular portion of membrane 40 having a diameter of 10.2 cm (i.e., 4 inches) that can be subjected to flow testing. Simultaneously, a test fixture 50 is made. The length of the test fixture tube 50 is 17.8 cm (i.e. seven inches) and the fixture has a nominal diameter of 5.1 cm (i.e., 2 bats). The tube is connected to a reducer 50 which is 40.6 cm (16 inches) long and has a nominal internal diameter of 5.1 cm (2 inches). The internal diameter of the reducer 60 tapers at a cutting angle of 7 degrees over a length of 40.6 cm (16 inches) to a nominal internal diameter of 10.2 cm (4 inches).

A sample of membrane 40 is placed on that portion of the test fixture having an internal diameter of 10.2 cm (i.e., 4 inches). The position of the diaphragm 40 is oriented so that the first layer 41 faces the high-pressure airflow side (upstream). The test fixture 50 is symmetrical about the membrane sample 40.

Further away from the downstream diaphragm sample 40, the test fixture 50 narrows again along the length of the reducer at a cutting edge angle of 7 degrees from an internal nominal diameter of 10.2 cm (i.e. 4 inches) to an internal nominal diameter of 5.1 cm (i.e. 2 inches). . A tube is also attached to the reducer 60. This tube is also 17.8 cm (7 inches) long, straight, and has an internal nominal diameter of 5.1 cm (2 inches).

-15Air flow of 22.4 scmm (ie eight hundred scfin) per 0.093 m ³ (cubic foot) permeates through membrane 40, which is approximately 1.96 scmm (ie 70 scfin) per 80.8 cm ² for the sample just described. (i.e., 0.087 square feet). The air flow temperature is maintained at 23.9 ° C ± 1 ° C (ie 75 ° F ± 2 ° F). The static pressure from one side of the membrane to the other is measured by a pressure gauge, a pair of pressure transducers, or other useful means known in the art. This static pressure reflects the dry pressure drop for the membrane 40 tested.

For the purpose of measuring the wet pressure drop, the same sample as described above and the modified test fixture 50 are used. This modification of the test fixture 50 consists in adding a spray nozzle 55 which is positioned upstream of the sample of membrane 40 in the direction of flow. The spray nozzle 55 is a perfectly conical spray nozzle 55 with the type designation &quot; 1/4 TTG &quot; manufactured by &quot; Spraying Systems &quot; in Cincinnati, Ohio and having a 0.51 mm (0.020 inch) passage and 100 mesh mesh or its equivalent. The nozzle 55 is placed at a distance of 12.7 cm (5 inches) in front of the membrane sample 40. The nozzle 55 sprays 0.2271 / m (i.e. 0.06 gpm) of water at 275.8 kPa (i.e. 40 psi) at a perfect conical angle of 58 degrees. Water is sprayed at a temperature of approximately 22.2 ° C ± 1 ° C (ie 72 ° F ± 2 ° F). The above spraying completely covers the membrane 40 sample and causes an increase in pressure drop across membrane 40. The wet pressure drop is measured at different flow speeds.

Referring to Fig. 1, the apparatus 20 of the present invention may be used in combination with a paper making web that provides a cellulosic fibrous structure having several regions of different density and / or areal density. The papermaking belt and cellulosic fibrous web are manufactured according to the same U.S. patents, including U.S. Pat. No. 4,191,609, issued March 4, 1980 to Trokhan; U.S. Patent 4,514,345 issued April 30, 1985 to Johnson et al .; U.S. Patent 4,528,230, issued July 9, 1985 to Trokhan; U.S. Patent 4,528,565, issued July 16, 1985 to Trokhan; No. 5,245,025, issued September 14, 1993 to Trokhan et al .; U.S. Patent 5,275,700 issued January 4, 1994 to Trokhan; No. 5,328,565, issued July 12, 1994 to Rash et al .; U.S. Patent 5,334,289, issued Aug. 2, 1994 to Trokhan et al .; U.S. Patent 5,364,504, issued November 15, 1995 to Smurkoski et al .; No. 5,527,428, issued June 18, 1996, to U.S. Pat

I · 4 · 4 4 to β

-16 the name Trokhan et al .; U.S. Patent 5,554,467, issued September 18, 1996 to Trokhan et al .; and U.S. Patent 5,628,879, issued May 13, 1997 to Ayers et al.

In another embodiment, the paper making web may be a felt web, often referred to in the prior art as a press web, and described in U.S. Patent 5,556,509, issued September 17, 1996 in the name of Trokhan and PCT application WO 96/00812, which was published on January 11, 1996, by the name of Trokhan et al., and therefore the contents of the aforementioned patent and application are incorporated herein by reference.

In addition, the paper that is dried on the microporous membrane 40 of the present invention may have several regions of different basis weight as described in the same U.S. patents, namely, U.S. Patent 5,534,326, issued July 9, 2006.

1996 in the name of Trokhan et al. and U.S. Patent 5,503,715 issued April 2, 1996 to Trokhan et al., the contents of which are incorporated herein by reference, or European Patent Application WO 96/35018 published November 7, 1996, by Kamps et al. Paper dried on the microporous membrane of the present invention can also be made using other paper making webs. In this case, the highly probable use of belts is described in European Patent Application WO 97/24487 published July 10, 1997, by the author named Kaufinan et al. and European Patent Application 0 677 612 A2 published October 10, 1995, by Wendt et al. Similarly, there is the possibility of using other papermaking technologies in combination with papermaking hardware and machinery and paper made with the benefit of the microporous membrane 40 of the present invention. Potentially useful technologies include those contained in US patents, namely, U.S. Patent 5,411,636 issued May 2, 1995 to Hermans et al .; No. 5,601,871, issued February 11

1997 in the name of Krzysik et al .; U.S. Patent 5,607,551 issued March 4, 1997 to Farrington Jr. et al .; and European Patent Application 0 617 164 published September 28, 1994, by Hyland et al.

The germline sheet layer may be completely dried on the membrane 40 of the present invention. Alternatively, there is the possibility of drying the embryonic sheet layer on a Yankee dryer drum as is conventional in the art. Alternatively, the final drying of the cellulosic fibrous web may be performed without the use of a Yankee drying drum.

·· 00 000 ···· · 00000 0 · 0

000 000 000 000 0

0 00 0 000 · • 0 · ··· ·· ··· ·· 0 ·

The Cehilose fiber structure may be shortened in a manner known in the art. For shortening purposes, a Yankee dryer drum or other roller suitable for creping with the aid of a prior art wiper blade may be used. Creping can be performed according to the same U.S. Patent 4,919,756, issued April 24, 1992 to Sawdai, the contents of which are incorporated herein by reference. Alternatively, or additionally, the truncation may be performed based on the effect of vermicil microconcentration according to the guidance contained in the same U.S. Patent 4,440,597, issued April 3, 1984 to Wells et al., The disclosure of which is incorporated herein by reference.

PV 2000-1011

Claims (4)

PATENT CLAIMS A microporous membrane for use with an air-drying papermaking machine, characterized in that said membrane has a pore size of less than or equal to 20 microns, said microporous membrane exhibiting such a through-flow wet pressure drop at a flow rate of 1.12 scmm ( ie 40 scfin) to 80.8 square centimeters (i.e. 0.087 square feet), which is less than or equal to 10.16 cm (i.e. 4.0 inches) of mercury column, and that said decrease in the vacuum is preferably lower or equal to 8.89 cm (i.e., 3.5 inches) of mercury column, and that said drop in the vacuum is even more preferably less than or equal to 7.62 (i.e., 3.0 inches) of mercury column. 2. A microporous membrane for use with an air-drying papermaking apparatus, wherein said membrane has a pore size of less than or equal to 20 microns, said microporous membrane exhibiting such a through-flow wet pressure drop at a flow rate of 2.24 scmm ( i.e., 80 scfin) to 80.8 square centimeters (i.e. 0.087 square feet), which is less than or equal to 15.24 cm (i.e. 6.0 inches) of mercury column, and that said decrease in the vacuum is preferably less than or equal to equals 13.97 cm (i.e., 5.5 in.) of the mercury column and that said decrease in the vacuum is even more preferably less than or equal to 12.7 (i.e., 5.0 in) of the mercury column. 3. A microporous membrane for use with an air-drying papermaking machine, wherein said microporous membrane has a pore size of less than or equal to 20 microns and has a through-flow of wet suction, wherein said wet-vacuum drop increases with increasing flow rate, there is a relationship between said wetting of the vacuum and the flow rate, which is generally expressed by the formula: Y £ 0.048X +2.215 in which X is the flow rate in scfin to 0.087 square feet and Y is the wet decrease in tacos in inches of mercury column, or v is expressed by the formula: 2540 Y <0.042X + 0.767 · · · · ······· · 0 0 0 0 0 ···· · · 0 0 0 0 0 «· • · 00 0 · * ·· 000 000 0 Wherein X is the flow velocity in scmm to 80.8 cm ² and Y is the wet hook drop in centimeters of the mercury column, and that there is an advantageous relationship between the wet pressure drop and said flow rate, which is generally expressed by the formula: Y0,048X +2,015 where X is the flow rate in scfin to 0.087 square feet and Y is the wet pressure drop in inches of mercury column, or recalculated by the formula: 2540 Y <0.042X +0.698 in which X is the flow rate in scmm to 80.8 cm ² and Y is the wet pressure drop in centimeters of the mercury column, and that said pressure drop, to which the formula generally applies, applies to the range flow rates of from about 35 to about 95 scfin (i.e., from about 0.98 to about 2.66 scmm) per 0.087 square feet (i.e., 80.8 square centimeters). 4. A tissue manufacturing process, comprising the steps of: forming a seed layer; forming a microporous membrane, said microporous membrane having a pore size that provides restrictive airflow permeability through said germline sheet, said membrane having a pore size of less than or equal to 20 microns and exhibiting a continuous wet pressure drop, wherein said wet pressure drop increases with increasing flow rate, wherein there is a relationship between said wet pressure drop and said flow rate, which is generally expressed by the formula: Y0,048X +2,215 where X is the flow rate in scfin to 0.087 square feet and Y is the wet pressure drop in inches of mercury column, or v is expressed by the formula: 2540 Y <0.042X + 0.767 wherein X is the flow rate in scmm to 80.8 cm ² and Y is the wet pressure drop in centimeters of mercury; placing said germline sheet on said microporous membrane; permeation of air through said germline sheet and said microporous membrane, wherein said microporous membrane provides restrictive permeability to - 20 air flow through said germline sheet, thereby removing water from said germline sheet; and removing said germline sheet from said microporous membrane; and that preferably there is a relationship between said wet pressure drop and said flow rate, which is generally expressed by the formula: Y £ 0.048X +2.015 wherein X is the flow rate in scfin to 0.087 square feet and Y is the wet pressure drop in inches of mercury column, or recalculated by the formula: 2540 Y < 0.042X +0.698 wherein X is the flow rate in scmm to 80.8 cm ² and Y is the wet pressure drop in centimeters of mercury column, and that said formula more preferably applies to a range of flow rates of about 35 to about 95 scfin (i.e., from about 0.98 to about 2.66 scmm) per 0.087 square feet (i.e., 80.8 square centimeters) and that said formula most preferably applies to a flow rate range of from about 40 to about 80 scfin (i.e., from about 1.12 to about 2.24 scmm) per 0.087 square feet (i.e. 80.8 square centimeters).