Classifications

• • D—TEXTILES; PAPER
  • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
  • D21H—PULP COMPOSITIONS; PREPARATION THEREOF NOT COVERED BY SUBCLASSES D21C OR D21D; IMPREGNATING OR COATING OF PAPER; TREATMENT OF FINISHED PAPER NOT COVERED BY CLASS B31 OR SUBCLASS D21G; PAPER NOT OTHERWISE PROVIDED FOR
  • D21H17/00—Non-fibrous material added to the pulp, characterised by its constitution; Paper-impregnating material characterised by its constitution
  • D21H17/20—Macromolecular organic compounds
  • D21H17/21—Macromolecular organic compounds of natural origin; Derivatives thereof
  • D21H17/24—Polysaccharides
  • D21H17/28—Starch
  • D21H17/29—Starch cationic
• • D—TEXTILES; PAPER
  • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
  • D21H—PULP COMPOSITIONS; PREPARATION THEREOF NOT COVERED BY SUBCLASSES D21C OR D21D; IMPREGNATING OR COATING OF PAPER; TREATMENT OF FINISHED PAPER NOT COVERED BY CLASS B31 OR SUBCLASS D21G; PAPER NOT OTHERWISE PROVIDED FOR
  • D21H17/00—Non-fibrous material added to the pulp, characterised by its constitution; Paper-impregnating material characterised by its constitution
  • D21H17/03—Non-macromolecular organic compounds
  • D21H17/05—Non-macromolecular organic compounds containing elements other than carbon and hydrogen only
  • D21H17/14—Carboxylic acids; Derivatives thereof
  • D21H17/15—Polycarboxylic acids, e.g. maleic acid
• • D—TEXTILES; PAPER
  • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
  • D21H—PULP COMPOSITIONS; PREPARATION THEREOF NOT COVERED BY SUBCLASSES D21C OR D21D; IMPREGNATING OR COATING OF PAPER; TREATMENT OF FINISHED PAPER NOT COVERED BY CLASS B31 OR SUBCLASS D21G; PAPER NOT OTHERWISE PROVIDED FOR
  • D21H17/00—Non-fibrous material added to the pulp, characterised by its constitution; Paper-impregnating material characterised by its constitution
  • D21H17/20—Macromolecular organic compounds
  • D21H17/33—Synthetic macromolecular compounds
  • D21H17/34—Synthetic macromolecular compounds obtained by reactions only involving carbon-to-carbon unsaturated bonds
  • D21H17/37—Polymers of unsaturated acids or derivatives thereof, e.g. polyacrylates
  • D21H17/375—Poly(meth)acrylamide
• • D—TEXTILES; PAPER
  • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
  • D21H—PULP COMPOSITIONS; PREPARATION THEREOF NOT COVERED BY SUBCLASSES D21C OR D21D; IMPREGNATING OR COATING OF PAPER; TREATMENT OF FINISHED PAPER NOT COVERED BY CLASS B31 OR SUBCLASS D21G; PAPER NOT OTHERWISE PROVIDED FOR
  • D21H17/00—Non-fibrous material added to the pulp, characterised by its constitution; Paper-impregnating material characterised by its constitution
  • D21H17/20—Macromolecular organic compounds
  • D21H17/33—Synthetic macromolecular compounds
  • D21H17/34—Synthetic macromolecular compounds obtained by reactions only involving carbon-to-carbon unsaturated bonds
  • D21H17/41—Synthetic macromolecular compounds obtained by reactions only involving carbon-to-carbon unsaturated bonds containing ionic groups
  • D21H17/44—Synthetic macromolecular compounds obtained by reactions only involving carbon-to-carbon unsaturated bonds containing ionic groups cationic
  • D21H17/45—Nitrogen-containing groups
  • D21H17/455—Nitrogen-containing groups comprising tertiary amine or being at least partially quaternised
• • D—TEXTILES; PAPER
  • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
  • D21H—PULP COMPOSITIONS; PREPARATION THEREOF NOT COVERED BY SUBCLASSES D21C OR D21D; IMPREGNATING OR COATING OF PAPER; TREATMENT OF FINISHED PAPER NOT COVERED BY CLASS B31 OR SUBCLASS D21G; PAPER NOT OTHERWISE PROVIDED FOR
  • D21H23/00—Processes or apparatus for adding material to the pulp or to the paper
  • D21H23/76—Processes or apparatus for adding material to the pulp or to the paper characterised by choice of auxiliary compounds which are added separately from at least one other compound, e.g. to improve the incorporation of the latter or to obtain an enhanced combined effect
  • D21H23/765—Addition of all compounds to the pulp
• • D—TEXTILES; PAPER
  • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
  • D21H—PULP COMPOSITIONS; PREPARATION THEREOF NOT COVERED BY SUBCLASSES D21C OR D21D; IMPREGNATING OR COATING OF PAPER; TREATMENT OF FINISHED PAPER NOT COVERED BY CLASS B31 OR SUBCLASS D21G; PAPER NOT OTHERWISE PROVIDED FOR
  • D21H21/00—Non-fibrous material added to the pulp, characterised by its function, form or properties; Paper-impregnating or coating material, characterised by its function, form or properties
  • D21H21/06—Paper forming aids
  • D21H21/10—Retention agents or drainage improvers

Definitions

• the present invention relates to a system for making paper to be used as cover sheets for gypsum wallboard, and more particularly refers to a polymer system for use in making such paper and to a novel method for applying the system.
• Gypsum wallboard is conventionally fabricated by depositing an aqueous slurry between two paper cover sheets, setting the slurry and drying the finished product.
• paper for utilization as paper cover sheets was prepared by utilizing an acid size, alum and rosin. This sizing system was satisfactory and produced suitable paper for cover sheets. It was subsequently found, however, that when a neutral size material was utilized together with a cationic starch, a paper having greater strength was produced. However, when the system was utilized with waste paper furnish, it was found that contaminated material was deposited on the paper-making machine.
• paper suitable for use in the production of gypsum wallboard is prepared from waste paper furnish and utilizing a neutral size such as an alkenyl succinic anhydride by eliminating a portion or all of the cationic starch conventionally used with such neutral sizes by incorporating into the pulp furnish slurry one or more cationic polymers at particularly selected places of the paper-making apparatus.
• a neutral size such as an alkenyl succinic anhydride
• Waste paper such as waste news, sections, mixed waste or old corrugated paper conventionally contain contaminants such as wax, asphalt, hotmelt glues and adhesives.
• pulp furnish prepared from these materials When pulp furnish prepared from these materials is utilized to form paper, they often deposit at various places of the paper-making machine and cause contamination that must be periodically removed. This results in an added expense to the paper- making process.
• the cationic starch conventionally used together with alkenyl succinic anhydride neutral sizes is quite expensive and a considerable reduction in cost could be achieved if the use of these materials was reduced or discontinued completely.
• alkenyl succinic anhydride neutral size conventionally used for sizing gypsum wallboard paper is disclosed in U.S. Patent No. 3,102,064, which also discloses the use of a cationic starch as a retention aid.
• the general formula of the material is as follows: wherein R is selected from the group consisting of dimethylene and trimethylene radicals, and wherein R' is a hydrophobic group containing more than 5 carbon atoms selected from the group consisting of alkyl, alkenyl, aralkyl and aralkenyl groups.
• Newslined paper is paper that is put on the back face of the gypsum wallboard which is mounted on the inside of the wall in contact with the supporting frame members. Consequently, it need not have the high grade surface required on the facing side of the wallboard.
• Newslined paper is typically comprised of low grade materials which are unsuitable for paper which is applied to the face of the wallboard.
• the low grade constituents are old corrugated container stock which contains many plastics, hotmelt adhesives, wax and other contaminants which may cause bleed-through and are unsuitable for the outer or front face of the wallbaord.
• the newslined is also comprised of sections which are highly coated, thereby creating contamination problems. Newslined can also be inserts cut out of newspapers that are highly coated or printed with rotogravure.
• a substantial cost savings may be accomplished by replacing all or part of the cationic starch.
• the replacement is made by adding a cationic polymer.
• the cationic density of the material relates to a number of reactive groups on a given length of a molecule. The greater the number, the greater is the cationic density and the greater will be the cationic charge on the retention aid molecule, and this will increase what is known as its coagulating effect.
• the preferred cationic polymer a material of low cationic charge density is preferred. This means that the frequency of cationic charges on a molecule is lower and, therefore, it has a lower overall charge density.
• the material used in connection with a high molecular weight molecule creates flocculating conditions, where the cationic charge causes the molecule to be attracted to anionic groups.
• the process does not require a very high charge density in order to accomplish the present purpose, but the process depends more on the length of the molecule, and under these conditions the effect which is achieved is flocculation.
• the cationic charge density is given herein in terms of mole percent.
• the present invention may be practiced in either one of two embodiments.
• a high molecular weight cationic polymer having a low charge density is introduced into the paper-making process at the discharge of the fan pumps in highly dilute form (for example 0.1% concentration).
• a portion of the cationic starch solution conventionally utilized as a retention aid is eliminated, and only the primary starch or the starch going through the emulsifier for the purpose of providing a cationic charge to retain the neutral size is utilized.
• the retention aid polymer only at the discharge of the fan pumps, contamination of the paper-making apparatus is avoided. Additionally a savings in the cost of the eliminated cationic starch is realized.
• the two polymer system in addition to adding a high molecular weight low charge cationic polymer to the discharges of the fan pumps, the entire cationic starch addition is replaced with a primary solution of the same high molecular weight low charge density cationic polymer applied through the emulsifier, and an additional dilute solution of a low molecular weight, high charged density cationic polymer is applied to the machine chest.
• the use of the second polymer, a low molecular weight high charge density cationic polymer coagulant in the machine chest provides cations to counter the anionic trash present in the slurry.
• a low molecular weight, high charge density cationic coagulant polymer is added to the paper stock in the machine chest, where applicable, at the rate of about 0.15 to 0.45 dry lb. of polymer per ton of paper. This coagulant serves to coagglomerate fine contaminant particles into larger, more readily retained particles at a point where the agglomeration would not cause plating out of the contaminant on the paper machine surfaces.
• the resulting stock called "machine furnish” is then pumped at 3-1/2% oven dry consistency to the fan pump inlets of the forming section of the paper machine where the furnish is divided into 7 separate flows corresponding to their introduction to 7 separate fan pumps.
• a neutral size emulsion comprising an ASA (alkenyl succinic anhydride) size emulsified in either a cationic starch or a cationic polymer solution, is added to the machine furnish in the thick stock down legs just prior to entering the inlet piping to the fan pumps.
• the function of the cationic starch or the cationic polymer is to cause the size to adhere to the anionically-charged cellulose fibers of the machine furnish in order to provide sizing after subsequent heat curing.
• the ASA size is added at rates varying between 2.5 and 5.5 dry lb/ton of paper depending on sizing propensity of the furnish and effectiveness of size retention on the paper machine.
• the flows of machine furnish mixed with size emulsion is diluted to approximately 0.5 to 1.5% consistency with recycled white water from the paper machine, and are then pumped by the fan pumps to the continuously moving forming cylinders of the paper machine.
• a high high molecular weight, low charge density cationic flocculant polymer is pumped at the rate of 0.40 to 1.35 dry lb/ton of paper for use as a retention aid.
• the retention aid is mixed with the dilute machine furnish by means of turbulence created by elbows in the approach piping from the discharges of the fan pumps to the forming cylinders.
• the retention aid serves to improve the retention of cellulose fines and agglomerated contaminant particles which, if poorly retained in the sheet, could become embedded in paper machine surfaces such as carrying and press felts, forming wires and press roll covers.
• the machine furnish is formed on the forming cylinders into separate plies which are joined together on a continuously moving carrying felt.
• the water drained through the wire covers of the cylinders is caused to flow back to the separate fan pumps for dilution of the pulp.
• a seven ply sheet is formed at 23-25% solids consistency and is carried on continuously moving felts through the press section of the paper machine, where the solids content of the sheet is increased to 40-45%.
• the sheet by itself is then passed into the dryer section where it is dried to 1.0-2.5% moisture content on continuously turning drying cylinders loaded to a minimum steam pressure of 25 psig for proper curing of the ASA size.
• the dried sheet of paper after leaving the dryer section, passes through a wet calender stack where water is applied to both faces of the sheet for finish by water addition to the rolls at the calender stack via water boxes attached to the calender stack rolls.
• the sheet of paper then passes through a following dry calender stack where the caliper or thickness uniformity is improved.
• After leaving the dry stack the sheet of paper is wound into a set of paper on a reel. Later the set is slit and wound on a winder into separate rolls for later conversion to gypsum board.
• the liner system When the type of paper produced or the furnish conditions make it necessary, a parallel stock system to the filler stock system, called the liner system is run to provide a two-ply liner on top of the filler stock. Two of the afore-mentioned cylinders are utilized for this purpose.
• the filler portion of the paper as a result, consits of five plies.
• the liner system is run utilizing paper stock from clean, cut-up rolls of paper. The liner so formed alleviates the press roll deposition problem and allows continued operation of the paper machine. Without this modification, the press rolls would soon be covered with sticky contaminant causing picking of the sheet and eventual sheet breaks.
• Paper was produced without the addition of any cationic polymer after the fan pumps and had the composition shown below in Table I.
• the cationic starch solution was pumped through the emulsifier with the ASA size, and was mixed with additional starch solution after the emulsifier.
• the dilute ASA size emulsion was then pumped to the thick stock lines to the fan pump inlets. Under these process conditions and with the resulting contaminated condition of the furnish a total of 12.5 lb/ton of cationic starch and 5.0 lb/ton of ASA size were required to provide adequate paper sizing, and the liner system had to be run utilizing cut up clean rolls of the same approximate fiber composition as run in the filler stock.
• Paper was prepared by the use of one cationic polymer retention aid applied immediately after the fan pumps and had the composition shown in Table II below.
• the cationic starch solution added to the ASA-starch emulsion after the emulsifier was shut off and was replaced with clarified process water.
• a high molecular weight, low charge density cationic polymer was added at the rate of 0.5 dry lb/ton paper to the discharge of the fan pumps pumping dilute machine furnish to the forming cylinders.
• the results of this mode of paper manufacture were that cationic starch usage, was decreased by 9.0 lb/ton or 72% of the usage of Example 2 above.
• the neutral sizing rate was reduced by 0.5 lb/ton or 10% of Example 2's usage and use of the liner system with its attendant electrical power consumption was eliminated.
• the paper machine press rolls remained clean with no assistance from the liner system.
• Example 4 illustrates the preparation of a two polymer system using newslined paper according to a further embodiment of the invention.
• Paper produced with the two cationic polymers had the composition illustrated in Table III below.
• Table III below.
• 0.25 dry lb/ton of a low molecular weight, high charge density cationic coagulant polymer was added to the filler system machine chest.
• the primary purpose of the coagulant addition was to trap anionic trash which consumed a disproportionate share of the cationic size emulsion and reduced the efficiency of sizing. It was discovered that its effect on coagulating furnish contaminant particles was beneficial.
• a pregelled powdered or flaked cationic potato starch was wetted out with fresh water in a hopper-type eductor and was discharged into an agitated mixing tank where full solubility of the the starch was achieved over 30-60 minutes, and the starch solution concentration was adjusted to 3%.
• the completed batch of starch solution was transferred to the holding tank and was pumped at a rate of 3.5 to 4.0 dry lb/ton of paper through a turbine pump size emulsifier, where it served as the size emulsifying medium.
• An oily ASA (alkenyl succinic anhydride) sizing agent was added at a rate of 3.5 to 5.0 lb/ton of paper to the starch solution just prior to the emulsifier. After emulsification, the solids content of the emulsion was 6.0% including starch solids.
• the thick-size starch emulsion flowed to the inlet of an eductor where the emulsion was diluted with clarified water at a rate sufficient to lower the solids content of the emulsion to 0.35% solids.
• the dilute emulsion was then metered through orifices and was then injected into the thick paper machine stock slurry just prior to its entry into the suction of the fan pumps. Subsequently, the thick stock was mixed and diluted with white water drainings from the forming cylinders in the fan pumps.
• the high molecular weight low charge density cationic emulsion polymer designated hereinas polymer "A", consisting of 28-31% polymer solids, 40-43% water and 23-26% hydrocarbon oil was inverted to a 1-3% solids aqueous solution in agitated mixing and holding tanks.
• the polymer solids consisted of a copolymerization product of acrylamide monomer and cationic trimethyl ammonium chloride methacrylate where the cationic charge density of 7.5 mol percent was provided by quaternary amide groups attached to the polymer.
• the mean average molecular weight of the polymer was 2,000,000. Wetting out of the polymer was accomplished in hopper-type eductors with fresh water.
• the moderately dilute aqueous polymer solution was pumped through a rotameter and thence to a mixing eductor with a variable speed, non- pulsing type constant displacement gear pump. Mill clarified water was used as the motivating fluid in the eductor to raise the dilute polymer line pressure to approximately 60 psig pressure and to lower the polymer solids concentration to approximately 0.1% solids.
• the dilute polymer was metered at the rate of 0.40 to 1.35 dry lb/ ton into the dilute paper machine stock slurry just before the forming cylinders at the discharges of the forming cylinder fan pumps.
• the metering was accomplished through orifices, and introduction of the polymer into the dilute machine stock slurry was done through inlet quills set into the fan pumps discharge piping.
• the dilute polymer was mixed with the dilute machine stock slurry in the turbulence that occurs after each bend in the piping before the machine stock reaches the forming cylinders.
• the dilute machine stock slurry was then formed by drainage through the forming cylinder wires into plies which were co-joined onto a carrying felt.
• the joined plies were transferred as a web onto another carrying felt, and the web was then pressed between press rolls and contacted by several hot dryer rolls in a dryer section to remove all but the last 2-5% of the moisture from the web.
• the sheet was run between steel rolls to provide smoothness and uniform thickness.
• the paper was wound on a reel and was later slit and rewound on a reel into rolls that were shipped to the market or to the converting stage for making gypsum board.
• the following example illustrates the preparation and use of the additional materials for the two polymer system.
• a cationic quaternary amine polymer designated herein as polymer "B"
• polymer B of very high charge density of 100 mol percent and a low mean average molecular weight of approximately 200,000 was added at the rate of 0.15-0.45 dry lb/ton of paper to the machine chest dilute at 10% of the as-received concentration.
• This polymer was added to the machine chest and utilized to neutralize colloidal anionic furnish components that would have consumed disproportionate amounts of cationically charged size.
• the polymer served to coagulate dispersed contaminant particles in the machine chest. If such coagulation were to have occurred on the paper machine proper, substantial deposits of contaminants would have been prone to occur on the paper machine components such as the top press rolls, cylinder wires and press felts.
• Emulsion polymer termed "A" in Example 6 related to the one polymer system, was adjusted to a 0.18% solids content solution directly by wetting the polymer with fresh water in a hopper eductor followed by strong agitation in a mix tank.
• the dilute polymer was transferred to a holding tank and was then pumped through a variable speed gear pump to a turbine pump size emulsifier at a rate of 0.10-0.15 dry lb/ton of paper where it served as the size emulsifier medium.
• An oily ASA (alkenyl succinic anhydride) sizing agent was added to the polymer solution at a rate of 2.5-5.0 lb/ton just prior to the emulsifier. After emulsification the solids content of the emulsion was 6.2% including polymer solids.
• the thick size-polymer emulsion flowed to the inlet of an eductor where the emulsion was mixed with a volume of clarified process water equal in volume to 30 times the volume of the emulsion, thus providing a dilute emulsion of 0.19% solids concentration.
• This dilute emulsion under approximately 60 psig pressure was metered to the thick stock slurry lines ahead of the forming cylinder fan pumps through orifices.
• the dilute emulsion was added to the thick stock slurry through injection quills set into the thick stock slurry lines.
• the thick stock slurry was diluted with recycled white water drainage from the forming cylinders and then was pumped to the forming cylinders as dilute machine stock slurry.
• a pregelled powdered or flaked cationic potato starch was wetted out with fresh water in a hopper type eductor and was discharged into an agitated mixing tank where full solubilization of the starch was permitted to occur over 30-60 minutes, and the starch solution concentration was adjusted to 3%.
• the completed batch of starch solution was transferred to the holding tank and was pumped with a centrifugal pump to a turbine pump emulsifier at a rate of 2.5-5.0 lb/ton.
• ASA size as previously discussed was added at a rate of 4.5 to 5.5 lb/ton to the starch solution before emulsification in the starch solution as emulsifying medium.
• the size emulsion concentration leaving the emulsifier was 6%.
• the size emulsion was mixed with a continuous flow of more starch solution equal to a rate of 6 to 11.5 dry lb/ton of starch in an eductor to provide a dilute emulsion solids concentration of 4%.
• the dilute size emulsion was then metered to separate forming cylinders through separate rotameters for each forming cylinder.
• the starch-size emulsion then flowed to injection quills in the thick stock lines to the fan pump suctions where it was added to the thick stock.
• the sheet of paper was then formed as described above.
• the retention aid polymer added to the discharge of the fan pumps according to the invention is a copolymerization product of acrylamide monomer and cationic trimethyl ammonium chloride methacrylate.
• the material has a cationic charge density of 7.5 mol percent. Materials having a mean average molecular weight of from 2,000,000 to 4,000,000 may be utilized.
• the structure of the polymer is as follows:
• Betz 1260 or 1264 which are copolymers of a quaternary amine and acrylamide with a mean average molecular weight of 5 x 10 6 .
• the polymer has a cationic charge density of 20 mol percent.
• the amine provides the cationicity.
• 1260 is a dry material and 1264 is an emulsion polymer of 30% active polymer solids content.
• Hercules Reten 210 which is an acrylamide/quaternary ammonium salt monomer copolymerization product which has a molecular weight in the range of 9-10 x 10 6 , a cationic charge density 7.5 Mol percent, and is supplied as a dry powder.
• the cationic polymer coagulant is a cationic quaternary amine polymer of 200,000 mean average moleculer weight and 100 Mol percent charge density. It is supplied at low solids in solution under the trademark Nalco 7625, and supplied by Nalco Chemical Co., Oak Brook, Illinois.
• a Dow coagulant under the trademark Polymeric PC Copolymer formed of acrylamide and cationic monomer 50/50 by weight, can be used.
• the cationic monomer is a quaternary methyl ammonium chloride salt with the monomer part cyclic in structure.
• the cationic charge density is 7 mol percent, the range of molecular weight is 1.0-1.5 x 10 6 . It is supplied as an 8% aqueous solution.
• Still another coagulant which may be used is sold under the trademark Quaker 3015 and has a basic structure of polyamino/amide with a molecular weight range of from 200,000-300,000 and a cationic charge density of 50 mol percent. It is supplied as a liquid solution containing 38X solids.
• the gypsum board paper produced above utilizing the two-polymer system processes was subjected to a number of quality control tests to make sure that it met minimum standards required for proper conversion to wallboard.
• Table IV below provides test data obtained by testing wallboard produced by using the paper produced by the methods described above.
• tests of both manila and newslined gypsum board paper met the indicated standards per test.
• the sizing or water resistance of both papers as indicated by the saturations and cobb water resistance tests was good. Sheet strength in terms of ply bond and tensile strength were also good.
• the manila paper tested above was made up of 2 plies of a flyleaf liner stock applied to 5 plies of a filler stock consisting of box plant kraft cuttings and waste news.
• the newslined paper was made up of 7 plies of a blend of old corrugated container stock and waste stock.
• the gypsum board papers described above were converted into gypsum board on a conventional board line where stucco slurry was spread onto the inside face of the manila where the flyleaf topliner was face down. a forming roll or forming plate on a continuously moving forming belt.
• the board when fully set was cut into 8 foot lengths, inverted and conveyed to a drying kiln where it was dried by forced convection drying. The board after leaving the drying kiln was inspected and tested, and then made into bundles and shipped.
• Gypsum board produced as discussed above must meet a variety of quality tests in order to reach the market.
• the covering papers must bond well to the gypsum board core, and the board must possess adequate transverse strengths.
• the dry bond test is conducted by first drying the finished board for one hour at 110°F in a forced convection oven, and then subjecting the board to a force sufficient to break the bond between the paper and the board core.
• the applied force or weight at failure is the measure of bond strength.
• the bond failure is designated as the percentage of the tested board surface that becomes exposed or has no fiber covering after the bond has been broken. In reference to Table IV it is apparent that both manila and newslined paper bonded well to the gypsum core because the bond strengths fall within the desired range and the bond failure test shows zero bond failure for both papers.
• Transverse strength tests were conducted by first conditioning the finished board for 16 hours in a 70°F and 50% relative humidity environment, and then applying a downward force in the center of the specimen supported at its opposing outer edges. The face positioned downward is the face which is tested. Force applied at failure is the measurement of transverse strength.
• the method of the present invention offers several advantages over prior art methods utilizing a neutral size for making paper suitable for gypsum wallboard.
• a high molecular weight low charge density retention aid polymer is added immediately after the fan pumps instead of at a prior position. This results in the prevention of the deposition of contaminants on the cylinder wires, press and carrying felts and for press rolls of the paper-making machine. Additionally, it permits a reduction in the use of a cationic starch retention aid, a material which is considerably more expensive on a total use basis than the polymers utilized.
• a high molecular low charge density polymer of the same type is added immediately after the fan pumps, obtaining the benefits described with regard to the one-polymer method.

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• 1985
  • 1985-11-12 EP EP85308223A patent/EP0186956A3/de not_active Withdrawn
  • 1985-12-09 AU AU51015/85A patent/AU5101585A/en not_active Abandoned
  • 1985-12-23 GB GB08531595A patent/GB2169323B/en not_active Expired
  • 1985-12-25 JP JP29960085A patent/JPS61160493A/ja active Pending

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