Production of paper with filler

FIELD: textile, paper.

SUBSTANCE: method includes provision of a thick mixture of suspension, which contains wood mass and a filler. The thick suspension mix is dissolved to form a diluted mix of suspension, in which the filler is available in amount of at least 10 wt % in terms of dry mass of dissolved suspension mix. The thick mix and/or dissolved mix of the suspension are flocculated, using a polymer system of retention/dehydration. The dissolved mixture of suspension is dehydrated on a sieve to form a sheet, and then the sheet is dried. The polymer system of retention/dehydration contains the following: i) a water-soluble branched anion-active polymer and ii) a water-soluble cation-active or amphoteric polymer. The method may be realised on paper-making machines of quick dehydration, such as GAP former.

EFFECT: improved retention of ash with reduction of dehydration.

16 cl, 26 dwg, 46 tbl, 16 ex

 

The present invention relates to a method of manufacturing paper filled with paper pulp containing wood pulp. In particular, the invention includes methods of making paper with a high content of wood filler, such as SC paper (SC-paper or coated paper for gravure printing (for example, LWC).

You know, the paper is produced in a way that includes the occulation diluted pulp mixture by the addition of polymer retention additives and then dehydration flocculosa suspension moving through a sieve (often called net bumagodelatelnoe machine) and then forming a wet sheet, which is then dried. Some polymers tend to form quite large clumps and, although retention and dehydration can be good, unfortunately, the formation and the degree of drying of the resulting sheet may be impaired. It is often difficult to obtain an optimal balance between retention, dehydration, drying and shaping, adding a single polymer additive retention, and therefore common practice to add two separate material sequentially or in some cases simultaneously.

Grade paper with a wood filler, such as SC-paper or coated paper for gravure hour is about done, using soluble dual polymer retention system. Apply the use of two water-soluble polymers that are mixed together in an aqueous solution before it is added to the diluted mixture. Typically, one of the polymers should generally have a higher molecular weight than the other. Both polymer should generally be linear, and water soluble, so far as is reasonably possible. Usually low-molecular weight polymer component should have a high charge density of the cation, such as polienovy, polyethylenimine or DADMAC (polymers diallyldimethylammonium chloride) coagulants. In contrast to low molecular weight polymers of high molecular weight polymer components tend to have a relatively low charge density of the cation. Typically, these macromolecular polymers can be cationic polymers based on acrylamide or, for example, polyvinyl amines have had. A mixture of cationic polymers commonly referred to as a retention system cat/cat.

The total production of paper and cardboard construction, as is well known, used other systems holding. Microgranular system retention, use containing silicon oxide material was found to have been very effective in improving the retention and drainage. EP-A-235893 describes the way is which applied mainly linear cationic polymer to paper pulp to the stage of kneading, to cause occulation, passing flocculating mass through at least one stage of kneading and then deflocculate the introduction of bentonite. In addition to the completely linear cationic polymers may also be used, branched polymers as described in EP-A-202780. This method was successfully commercialized Ciba Specialty Chemicals under the trademark Hydrocol, because it provides increased retention, dewatering and formation.

Examples of other microgranules new systems used in industry paper production, are described in EP-A-0041056 and US 4385961 for colloidal silica; and in WO-A-9405596, and WO-A-9523021 relatively sols based on silicon oxide, used in combination with cationic polymers of acrylamide. US 6358364, US 6361652 and US 6361653 each section describes the use of borosilicate in connection with high-molecular flocculants and/or starch in this sense.

In addition to the inorganic insoluble microgranulation material of organic polymer microgranular material is also known for methods of paper production.

US 5167766 and US 5274055 discuss methods of paper production with improved dewatering and retention when using ionic organic microgranules or microbusiness having average diameter is R less than 750 nm, if cross linked, and less than 60 nm, if not cross linked. Microparticles or microbalance used in combination with high molecular weight organic polymer and/or a polysaccharide. The method can sometimes include alum.

US 20030192664 discloses a method of making paper using Veniaminovich polymers with ionic, organic, cross-linked polymer microbusiness. Optimization of molecular weight, structure and charge provides a system for improved standards of dehydration. The addition of various coagulants, such as polyethylenimine, alum or polyamine, as said above, additionally increases the amount of dehydration of these systems using polymeric microbalance.

WO-A-9829604 describes how to create a paper by the addition of cationic polymer retention additive to the pulp slurry to form flakes, mechanically destroy clusters and then reaccelerate suspension by adding a solution of water-soluble anionic polymer as a second polymer retention additives. Anionic polymeric retention additive is a branched polymer having a rheological oscillation of the tan Delta of about 0.005 Hz to above 0.7 and/or having a viscosity of deionized SLV at least three times higher values elm the spine salted SLV appropriate polymer, made in the absence of branching agent. The method provides significant improvements in retention, dehydration and formation in comparison with the methods earlier the previous prior art. Highlighted on page 8 that the number of branching agent should not be too high, because the desired improvement in dehydration and in terms of retention will not be achieved.

US 6616806 shows three components of the method of making paper, adding a substantially water-soluble polymer selected from a polysaccharide or a synthetic polymer with internal viscosity at least 4 DL/g, and then deflocculation subsequent addition deflocculation system. Deflocculation system contains containing silicon oxide material and substantially water-soluble polymer. Water-soluble polymer is added before deflocculation system is a water-soluble branched polymer which has an intrinsic viscosity above 4 DL/g and shows the magnitude of flow fluctuations tan Delta of about 0.005 Hz to above 0.7. Dehydration is increased without any significant deterioration of the formation in comparison with other known methods of the previous level of technology.

US 6395134 describes a method of making paper using the three components of the system, the which the pulp suspension flocculated, using water-soluble cationic polymer containing a silicon oxide material and the anionic branched water-soluble polymer formed from ethylene unsaturated monomers having an internal viscosity above 4 DL/g and showing the magnitude of flow fluctuations tangent Delta of about 0.005 Hz to above 0.7. The method provides for more rapid dehydration and better formation than the branched anionic polymer in the absence of colloidal silica. US 6391156 describes a similar method in which, in particular, bentonite is used as a silicon oxide material. This method also provides a more rapid dehydration and better formation than the ways in which the cationic polymer and a branched anionic polymer used in the absence of bentonite.

US 6451902 discloses a method of making paper using water-soluble synthetic cationic polymer to the pulp suspension, in particular, in the flow of the diluted mass, in order to flocculate, accompanying mechanical breakdown. After centresin added water-soluble anionic polymer and cellulosic material to reaccelerate pulp suspension. Accordingly, water-soluble anionic polymer can be a linear polymer. A considerable way which increases the magnitude of dehydration compared with the cationic polymer and bentonite in the absence of anionic polymer.

The previous methods of the prior art provide for improved retention and dehydration and often seek to improve the balance of the retention, dehydration and formation. However, the retention and dehydration increased simultaneously. None of the above previous levels technique does not consider the ways in which the retention, in particular the retention of ash increased, but dehydration maintained at the same level or decreased. Traditional methods of paper production has always attached importance to increasing the retention and dewatering in order to achieve higher performance on bumagodelatelnyh machines as well as to improve at the same time the formation.

However, the introductory part bumagodelatelnyh machines that have extremely fast twin-wire forming section of dehydration, often called a GAP former, has dramatically improved the tile creation and dewatering of paper pulp by mechanical means. Bumagodelatelnye machine type GAP former currently often used for the production of papers for gravure printing, such as SC paper (SC) or lightweight coated paper (LWC). GAP former dehydrate paper suspension quickly enough so that especially for lower densities between 34 and 60 g/ml did not require the additional increase of the degree of dehydration. In some cases, a GAP former provides a high level of initial dehydration. If this is the initial dehydration becomes too high, this may be unfavorable operation located downstream of ratmate and elements of dehydration in a GAP former. This is because the minimum concentration of a suspension of fibers to apply the drying ripple with high forces ratmate to optimize the formation and establishment of a z-oriented sheets.

Description bumagodelatelnoe machine GAP former can be found in "Duoformer CFD - a new development in the field of sheet forming systems" from Schmidt-Rohr, V.; Kohl,B. J.M.Voith GmbH, Heidenheim, Germany Wochenblatt für Papierfabrikation (1992), 120 (11-12), 455-8, 460. This document stated that the initial dehydration with constant pressure in the forming cylinder leads to high retention. Subsequent dehydration pressure pulsations opposite lattice in D-section increases. So Duoformer CFD greatly improved formation can be achieved with improved retention. In the German Supplement "Together-Magazin für Papiertechnik" (Issue 6 (1998), Böck, K.-J.; Moser, J.; published Voith Sulzer Papiertechnik GmbH & Co. KG, Dr. Wolfgang Möhle, Corporate Marketing, Voith Sulzer Papiertechnik GmbH) is stated under "D-section (the section of the blade or blades), which can effectively control the creation of sheets in the z-Orientali. However, is it is important, the fiber is still in the form of suspension in order to enable the mobility of the fibers. Additionally explained that because of the D-section achieved very good results. Stated that, increasing the osushivaniya in D-section, greatly improving the formation.

In industry publication from J.M.Voith GmbH ("Triple Star" - The state of the art and most efficient production line in the world for woodfree coated papers; Kotitsche, G., Merzeder, K.-D. and Tiefengruber, M. from Sappi Gratkorn GmbH; Voith trade publication p316e, 6.98 4000, page 7, column 2, paragraph 3, figure 8), stated that "the flow rate of the liquid to be dehydrated in the section of the foil forming device should be as high as possible. Thus is achieved a uniform and soft formation."

The above principles are still valid also for the new generation GAP formers. In industry publication Voith R e 4000 2002-06 "Duoformer TQv" declared that the curvature of the suction box and load forming blades, also known as D-section, are a prerequisite for excellent formation. The box has two compartments for osushivaniya and management structure of the sheet in the z-orientation. Further stated that in combination with the quality of paper pulp, were found two main parameter affecting the formation, regardless of the sort: the making of blades and reverse flow of water in the forming block. High flow rate formiruya the camping pads improves the formation in any situation, loaded emerging blade or not. This is caused by the effect that the forming blades work best when the suspension is sufficiently liquid to allow movement of the fiber.

Another example again emphasizes the importance of a managed initial dehydration in GAP formers, for example, developed and designed in accordance with WO-2004018768. Trade publication Metso EN_03 (12/2004) States that BelBaie V GAP former gives "the best formation due to the soft start osushivaniya and boot blades (page 1). Additional information can be found in the "Bel Baie V upgrade" (Swietlik, Frank; Irwin, Jeff; Jaakkola, Jyrki. Metso Paper USA, Norcross, GA, USA. Preprint - Annual Meeting, Pulp and Paper Technical Association of Canada, 90th, Montreal, QC, Canada, Jan. 27-29, 2004 (2004), Book AA109-A112. Publisher: Pulp and Paper Technical Association of Canada, Montreal, Que)."

Comparative situation also applies to the hybrid molding machines in which the sheet is formed on a conventional Fourdrinier the tablet, and then the main grid with reclaimed elements applied in the same manner. General description this former hybrid can be found in "Sheet forming with Duoformer D and pressing with shoe presses of the Flexonip type for manufacturing of linerboard and testliner, corrugating medium and folding boxboard" (Grossmann, U.; J.M.Voith GmbH, Heidenheim, Germany. Wochenblatt fur Papierfabrikation (1993), 121 (19), 775-6, 778, 780-2). Control dehydration is extremely important to create a worksheet and quality of the final product.

It is clear that simply increasing dehydration in mn the instances will not provide an optimized solution quality paper. On the contrary, it would be desirable to provide a controllable dehydration.

Although the increase osushivaniya section of the blade can be achieved by increasing the speed of the mixing pump, which will carry more water in the zone of formation, adjusting elements of dehydration, reducing polyparaphenylene solid particles and/or reducing the initial dehydration on the forming drum, however, it would be desirable to provide chemicals that optimize the quality of the paper. In particular it would be desirable to provide chemical retention system, which will reduce the rate of dehydration, but will increase retention. In particular it would be desirable to optimize the creation of the sheet, combined with adequate holding the ash to achieve the desired amount of filler in addition to optimizing the distribution of cereals in size. It would be especially desirable to achieve this, in addition to the production of smaller/small units for improved formation. In addition, it would be desirable to provide a method which provides increased retention of ash, and preferably forming, and maintaining or preferably reducing dehydration for grade paper with a wood filler.

According to the present invention we provide a method POPs the project for a paper filler, includes the steps of providing a thick mixture of pulp suspension which contains wood pulp and a filler dilution mass of thick suspension to form a diluted mixture of a suspension, in which the filler is present in the diluted mixture slurry in the amount of at least 10 wt.% in terms of the dry mass of the diluted mixture suspension,

deposition of thick flakes mixture of suspension and/or diluted mixtures using polymer retention system/dehydration

dehydration diluted mixture of the suspension on the grid to form a sheet and then drying the sheet,

in which polymer retention system/dehydration includes

i) a water-soluble branched anionic polymer and

ii) a water-soluble cationic or amphoteric polymer.

Suddenly, this method is equal to or greater retention of the ash relative to the full retention manifested in equal or higher level of ash on weight basis, without increasing dehydration. In some cases, full retention increased. In addition, in many cases, dehydration reduced. The method also provides enhancements formation. This reduction or support at the same level as free hydrated enables you to optimize the creation of the sheet, especially by the tea bumagodelatelnyh machines rapid dehydration. In a preferred form, we also find that the full dosage of the polymer is reduced when they are made of paper with a wood filler, especially paper SC in comparison with the previous methods of the prior art. We also find that the method enables the formation of small flakes, which leads to improved formation, pore size, suitability for printing as well as good ability to resist treatment in the press section bumagodelatelnoe machine.

Such improvement may not have been provided above the previous prior art, for example WO-A-9829604 that uses a cationic polymer and a branched anionic polymer, leading to increased and dewatering and retention. Without being limited by theory, we believe that in the present invention, the anionic branched polymer and/or cationic polymer or otherwise interact with the pulp suspension containing wood fiber and at least 10 wt.% filler, leading to the separation factor of dehydration on the degree of retention or to the specific retention of the ashes. This separation dehydration and full retention or retention of ash may be referred to as the effect of separation.

This decoupling of the dewatering and retention of ash especially field is but for manufacturing grade securities with a wood filler, such as paper for gravure printing, such as SC paper (SC paper) and coated wood-free coated paper (LWC).

In the manufacture of extremely full paper the present method provides a means to enable more preferably the filler in paper. Thus, in the preferred form of this invention, where the retention of ash increased relatively complete retention, the relative level of retention of the fibers will tend to decrease. This has the advantage that allows paper sheets to contain higher levels of filler and a reduced level of fiber. This causes a significant commercial advantage as the fiber is more expensive than the filler.

Preferably the water-soluble cationic or amphoteric polymer is a natural polymer or a synthetic polymer, which has an internal viscosity of at least 1.5 DL/g Suitable natural polymers include polysaccharides, which carry a cationic charge usually after modifications or alternatives are amphoteric property, and they are cationic and anionic charges. Typical natural polymers include cationic starch, amphoteric starch, chitin, chitosan, etc. Preferably cationic or amphoteric polymer is sinteticheskimi preferably a synthetic polymer formed from ethylene unsaturated cationic monomer or mixture of monomers, including at least one cationic monomer, and, if amphoteric, at least one cationic monomer and at least one anionic monomer. When the polymer is amphoteric, it is preferred, because it carries more cationic groups than anionic groups, so that the amphoteric polymer is predominantly cationic. In General, cationic polymers are preferred. Particularly preferred cationic or amphoteric polymers have an internal viscosity of at least 3 DL/g is Usually internal viscosity can be at least 4 DL/g and often it can be up to 20 or 30 DL/g, but preferably will be between 4 and 10 DL/g

The internal viscosity of the polymers can be determined by preparation of an aqueous polymer solution (0.5-1% m/m), based on the active content of the polymer. 2 g of this 0.5-1% polymer solution was diluted to 100 ml in a volumetric flask with 50 ml of 2M solution of sodium chloride, buffered to pH 7.0 (using 1.56 g of sodium dihydrophosphate and 32.26 g of disodium hydrogen phosphate per liter of deionized water), all diluted to 100 ml with deionized water. The internal viscosity of the polymers was measured using a viscometer with a suspended level Room 1 at 25°C in 1M buffered saline. The value of the intrinsic viscosity is determined according to the method,unless otherwise stated.

The polymer can be prepared by polymerization of water-soluble monomer or water soluble monomer mixture. Dissolved in water, we mean that the water-soluble monomer or water soluble mixture of the monomer has a solubility in water of at least 5 g in 100 ml of water and 25°C. the Polymer can be conveniently prepared by any suitable polymerization method.

Preferably a water-soluble polymer is cationic and is formed from one or more ethylene unsaturated cationic monomers randomly with one or more nonionic monomers mentioned here. Cationic monomers include dialkylaminoalkyl (meth) acrylates, dialkylaminoalkyl (meth) acrylamide, including their salts accession acids and Quaternary ammonium salts, diallyldimethylammonium chloride. Preferred cationic monomers include methylchloride Quaternary ammonium salts dimethylaminoethylacrylate and dimethylaminoethylmethacrylate. Suitable nonionic monomers include unsaturated nonionic monomers such as acrylamide, methacrylamide, hydroxyethylacrylate, N-vinyl pyrrolidone. Particularly preferred polymer includes a copolymer of acrylamide with methylchloride Quaternary ammonium salts dimethylaminoethylacrylate.

When the polymer is and what fotonnym, it is possible to prepare at least one cationic monomer and at least one anionic monomer and optionally at least one nonionic monomer. Cationic monomers and optional nonionic monomers set out above in respect of cationic polymers. Suitable anionic monomers include acrylic acid, methacrylic acid, maleic acid, crotonic acid, taconova acid, vinylsulfonate, arylsulfonate, 2-acrylamide-2-methylpropanesulfonate and their salts.

The polymers can be linear, because they were prepared substantially in the absence of the agent branching or crosslinking. Alternative polymers can be branched or crosslinked, for example as in EP-A-202780.

Optionally, the polymer can be prepared by polymerization of the opposite phase of the emulsion, optionally followed by dehydration under reduced pressure and temperature, often referred to as azeotropic dehydration to form a dispersion of polymer particles in oil. Alternative polymer may be provided in the form of beads polymerization of the opposite phase of the suspension, or as a powder polymerization of an aqueous solution, followed by crushing, drying and then grinding. The polymers can be produced by the AK beads by suspension polymerization or emulsion water-in-oil or dispersion polymerization emulsion water-in-oil for example, according to the method described in EP-A-150933, EP-A-102760 or EP-A-126528.

Particularly preferably, the cationic polymer and formed of at least 10 wt.% cationic monomer or monomers. Even more preferred polymers, including at least 20 or 30 wt.% cationic Monomeric units. It may be desirable to use cationic polymers having a very high degree of nationali, for example more than 50% up to 80 or even 100% of cationic monomer units. Particularly preferably, when the second cationic polymer occulant selected from the group consisting of cationic polyacrylamides, polymers of diallyldimethylammonium chloride, such as diallyldimethylammonium chloride, dialkylaminoalkyl (meth)-acrylate (or their salts) and dialkylaminoalkyl (meth)-acrylamide (or their salts). Other suitable polymers include polyvinylidene, and modified by Manicho polyacrylamides. Particularly preferred polymers include between 20 and 60 wt.% dimethylaminoethylacrylate and/or methacrylate and between 40 and 80 wt.% acrylamide.

Dose of water-soluble cationic or amphoteric polymer should be an effective amount, and should generally be at least 20 g and usually at least 50 g per ton of dry cellulosic suspension. The dose may be up to one and two pounds per ton, but should usually be within the range of 100 or 150 g / tonne to 800 g / tonne. Usually more effective results are achieved when the dose of water-soluble cationic or amphoteric polymer is at least 200 g / tonne, usually at least 250 g / tonne and often at least 300 g / tonne.

Cationic or amphoteric polymer may be added in a dense mass of a suspension or in a diluted mixture of the suspension. Preferably cationic or amphoteric polymer is added to dilute the mixture of the suspension, for example, before a single stage or stage mechanical degradation, such as a mixing pump or centresin. Preferably, the polymer is added after at least one stage of mechanical destruction.

Particularly effective results are found when water-soluble cationic or amphoteric polymer is used in conjunction with cationic coagulant. Cationic coagulant may be an inorganic material such as alum, polyaluminium, the trihydrate of aluminum chloride and alamoflorida. However, it is preferable that the cationic coagulant is an organic polymer.

Cationic coagulant is optionally water-soluble polymer, which may, for example, be a relatively low polymer molecules of the nuclear biological chemical (NBC mass relatively high camionnette. For example, the polymer may be homopolymers any suitable ethylene unsaturated cationic monomer, polymerizing to provide internal polymer viscosity to 3 DL/g Internal viscosity will generally be at least 0.1 DL/g, and often within the range from 0.2 or 0.5 DL/g to 1 or 2 DL/g of the Polyvinyl chloride of diallyldimethylammonium (DADMAC) are preferred. Other cationic coagulants include polyethylenimine, polyamideimides and polydicyandiamide.

Low molecular weight highly cationic polymer can for instance be additional polymer formed by the condensation of amines with other suitable di - or trifunctional varieties. For example, the polymer may be formed by the interaction of one or more amines selected from dimethylamine, trimethylamine and ethylene diamine, etc., and epichlohydrin, epichlorohydrin is preferred. Other suitable cationic coagulation polymers include low molecular weight polyvinylidene charge high density. Polyvinylene can be prepared by polymerization of vinylacetate to form polyvinylacetate with subsequent hydrolysis, leading to polyvinylene. In General, cationic coagulants show the charge density of the cation of at least 2 and usually less than the least 3 mEq/g and can be up to 4 or 5 mEq/g or higher.

Especially preferred that the cationic coagulant is a synthetic polymer of intrinsic viscosity at least 1 or 2 DL/g is often up to 3 DL/g or higher and shows the charge density of the cation is greater than 3 mEq/g, preferably homopolymer of DADMAC. DAD can be prepared by polymerization of an aqueous solution of DADMAC monomer using redox initiators, to provide an aqueous solution of the polymer. Alternative aqueous solution of DADMAC monomer may be suspended in liquids, immiscible with water, using a suspension agents, such as surfactants or stabilizers, and polymerisation to form polymer beads DADMAC.

Particularly preferred cationic coagulant is a relatively high-molecular homopolymer DADMAC, which shows the internal viscosity of at least 2 DL/g, Such a polymer can be manufactured by preparing an aqueous solution containing DADMAC monomer, a radical initiator, or a mixture, which is a radical initiators and/or between 0.1 and 5%, based on the monomer and optional chelating agent. Heat this mixture of monomer at a temperature below 60°C in order to polimerizuet monomer to homopolymer with a level conversion between 80 and 99%. Then post-processing this is the first homopolymer heating bilateral temperature between 60 and 120°C. Usually this DADMAC polymer can be prepared in accordance with the description given in PCT/EP 2006/067244.

An effective amount of the dose of cationic coagulant will typically be at least 20 g and usually at least 50 g per ton of dry cellulosic suspension. The dose may be up to one or two pounds per ton, but should usually be within the range of 100 or 150 g / tonne to 800 g / tonne. Usually more effective results are achieved when the dose of water-soluble cationic or amphoteric polymer is at least 200 g / tonne, usually at least 250 g / tonne and often at least 300 g / tonne.

Water-soluble cationic or amphoteric polymer and cationic coagulant can be added sequentially or simultaneously. Cationic coagulant may be added in a dense mass or in the diluted mixture. In some circumstances it may be useful to add a cationic coagulant in a mixing VAT or solvent Chan or alternatively in one or more element thick mixture. Cationic coagulant can be added to water-soluble cationic or amphoteric polymer or alternatively it can be added after the water-soluble cationic or amphoteric polymer. Preferably, however, in rastvorimy cationic or amphoteric polymer and cationic coagulant is added to the pulp slurry as a mixture. This mixture may be referred to as retention system cat/cat.

In General, water-soluble cationic or amphoteric polymer should have a higher molecular weight (and internal viscosity)than the cationic coagulant.

The amount of the mixture cat/cat should normally be as stated above for each of these two components. In General we find that dosage only one cationic or amphoteric polymer or a mixture of cat/cat below in comparison with a system that doesn't include branched anionic polymer.

Water-soluble branched anionic polymer may be any suitable water-soluble polymer that has at least some degree of branching or structure, provided that the structuring is not so excessive as to cause insolubility of the polymer.

Preferably the water-soluble branched anionic polymer has

(a) intrinsic viscosity higher than 1.5 DL/g and/or the viscosity Brookfield (viscosity UL) of the above salt solution of approximately 2.0 MPa·s and

(b) rheological variations of tan Delta from 0.005 Hz to above 0.7 and/or

(c) the coefficient of viscosity of deionized SLV, which is at least three times the coefficient of viscosity salt SLV corresponding neravetla the second polymer, made in the absence of branching agent.

Anionic branched polymer formed from a water soluble monomer mixture containing at least one anionic or potentially anionic ethylene unsaturated monomer and a small amount of a branching agent, for example as described in WO-A-9829604. In General, the polymer must be formed from a mixture of 5-100 wt.% anionic water-soluble monomer and from 0 to 95 wt.% nonionic water-soluble monomer.

Usually water-soluble monomers have a solubility in water of at least 5 g/100 cm3. The anionic monomer is preferably selected from the group consisting of acrylic acid, methacrylic acid, maleic acid, crotonic acid, basis of itaconic acid, 2-acrylamide-2-methylpropanesulphoacid, arylsulfonate and vinylsulfonate and their salts of alkali metal or ammonium. The nonionic monomer is preferably selected from the group consisting of acrylamide, methacrylamide, N-vinylpyrrolidone and hydroxyethylacrylate. Particularly preferred branched polymer contains sodium acrylate with a branching agent or acrylamide, sodium acrylate and branching agent.

The branching agent can be any chemical material which causes branching reaction through carboxyl or other side groups(such as epoxide, silane, polyvalent metal or formaldehyde). Preferably the branching agent is polyethylene unsaturated monomer included in the monomer mixture from which the formed polymer. The amount of branching agent must necessarily vary according to the characteristics of the branching agent. Thus, using polyethyleneimine acrylic branching agents, such as methylene-bis-acrylamide, the molar amount is usually below 30 mole frequent. per million and preferably below 20 frequent. per million Generally it is below 10 frequent. per million and most preferably below 5 frequent. on million the Optimum amount of branching agent is from about 0.5 to 3 or 3.5 molar frequent. at 3.8 million or even frequent. per million, but in some cases it may be desirable to use a 7 or 10 frequent. in million

Preferably the branching agent soluble in water. Typically, this can be a bifunctional material, such as methylene (bis) acrylamide, or it may be trifunctionally, tetrafunctional or a crosslinking agent of higher functionality, for example the chloride of tetraalkylammonium. Generally because of allyl monomer tends to have a lower constants of polymerization, they are polymerized with less readiness, and thus is common practice, the use of plastic nanosys is the R allylic branching agents, such as chloride of tetraalkylammonium to use higher levels, for example 5 to 30 or even 35 molar frequent. at 38 million or even frequent. per million and even up to 70 or 100 frequent. in million

Also, it may be desirable to enable the regulator to the degree of polymerization of the chains in the monomer mixture. Where the regulator polymerization degree is enabled, it can be used in amounts of at least 2 frequent. per million by weight, and may also be included in an amount up to 200 frequent. per million by weight. Usually the number of control degrees of polymerization can be in the range of 10-50 frequent. per million by weight. Control degree of polymerization may be any suitable chemical, such as sodium phosphate, 2-mercaptoethanol, malic acid or thioglycolate acid. Preferably, however, unioncounty branched polymer prepared in the absence of added control degree of polymerization.

Anionic branched polymer is generally in the form of emulsion, water-in-oil or dispersion. Typically, the polymers made by the polymerization of opposite phase emulsion to form a reverse phase emulsion. This product usually has at least a particle size of 95 wt.% below 10 microns and preferably at least 90 wt.% below 2 μm, for example substantially above 100 nm and particularly substantially in the range of 50 nm to 1 μm. The polymers can be prepared by conventional methods of polymerization opposite phase emulsion or microemulsion.

Tan Delta at value 0.005 Hz obtained using a rheometer with controlled indignation in the form of vibrations to 1.5 wt.% an aqueous solution of the polymer in deionized water after treatment in the drum for two hours. In the course of this work were used Carrimed CSR 100 is equipped with 6 cm, with the cone angle 1°58' and the value of the truncation 58 μm (link 5664). Used sample volume of approximately 2-3 cm3. The temperature was controlled to about 20.0°C±0.1°C using a Peltier module. The angle of deviation of 5×10-4the radian is applied during the sweep frequency from 0.005 Hz to 1 Hz in 12 stages on a logarithmic basis. G' and G" dimension is registered and used to calculate the tangent Delta (G'/G") values. The value of tan Delta is the ratio of the modulus (viscous) losses G" to the module (elastic) accumulation G' within the system.

At low frequencies (0.005 Hz) it is believed that the rate of deformation of the sample is sufficiently slow to allow linear or branched confusing chains to unravel. Mesh or custom made systems have a constant tangle of chains and show low values of tan Delta over a wide frequency range. Therefore, in order to characterize the properties of p is limera in the aquatic environment, there is a low frequency (for example, 0.005 Hz)measurements.

Anionic branched polymers should have a value of tan Delta at 0.005 Hz of above 0.7. Preferred anionic branched polymers have a value of tan Delta of 0.8 at 0.005 Hz. The value of tan Delta can be at least 2 DL/g, for example at least 4 DL/g, especially at least 5 or 6 DL/g, it May be desirable to provide polymers of much higher molecular weight, which show intrinsic viscosity of up to 16 or 18 DL/g however, The most preferred polymers have an intrinsic viscosity in the range of 7-12 DL/g, especially 8-10 DL/g

Preferred branched anionic polymer can also be characterized in relation to the corresponding polymer made under the same conditions of polymerization, but in the absence of branching agent (i.e., "non-branched polymer"). Unbranched polymer generally has an intrinsic viscosity of at least 6 DL/g and preferably at least 8 DL/g this is Often 16-30 DL/g, the Amount of branching agent is usually such that the internal viscosity is reduced by 10-70%, or sometimes up to 90%, the initial value (expressed in DL/g) for an unbranched polymer mentioned above.

The viscosity Brookfield (viscosity UL) salt solution polymerizable preparation of 0.1 wt.% an aqueous solution of the active polymer in 1M aqueous solution of NaCI at 25°C, using a Brookfield viscometer, fitted with UL adapter to 6 revolutions per minute. Thus, the powdered polymer or polymer of opposite phase must be first dissolved in deionized water to form a concentrated solution, and this concentrated solution is diluted with 1M aqueous NaCl. The viscosity of the salt solution is usually higher than 2.0 MPa·s and is often at least 2.2 and preferably at least 2.5 MPa·S. In many cases it is not more than 5 MPa·s, and the magnitude of 3-4 are usually preferred. They all measured at 60 revolutions per minute.

Viscosity coefficients of the SLV used to characterize the anionic branched polymer, determined by using a glass viscometer with a suspended level at 25°C. the viscometer was chosen to be appropriate according to the viscosity of the solution. The coefficient of viscosity η-ηaboutaboutwhere η and ηaboutare the results of the viscosity of aqueous solutions of the polymer and the blank solution, respectively. It may also be referred to as the relative viscosity. The coefficient of viscosity of deionized solution SLV is the coefficient obtained for 0.05% aqueous solution of the polymer prepared in deionized water. The coefficient of viscosity of the salt solution SLV is the coefficient obtained for a 0.5% aqueous solution of the polymer, prepared in 1M sodium chloride.

The coefficient of viscosity of deionized solution SLV is preferably at least 3 and, in General, at least 4, for example up to 7, 8 or higher. Best results are obtained when it is above 5. Preferably it is higher than the coefficient of viscosity of deionized solution for SLV unbranched polymer, i.e. a polymer made under the same conditions of polymerization, but in the absence of branching agent (and therefore have a higher internal viscosity). If the coefficient of viscosity of deionized solution SLV is not higher than the coefficient of viscosity of deionized solution SLV unbranched polymer, preferably it is at least 50% and usually at least 75% of the coefficient of viscosity of deionized solution SLV unbranched polymer. The coefficient of viscosity of the salt solution SLV usually below 1. The coefficient of viscosity of deionized solution SLV often at least five times and preferably at least eight times the coefficient of viscosity of the salt solution SLV.

Water-soluble branched anionic polymer may consequently be added to the pulp suspension at a dose of at least 10 g / tonne, calculated on the dry weight. The number can be as much as 2000 or 3000 g / tonne or above. Preferably the dose of bude is between 100 g / tonne and 1000 g / tonne, more preferably between 150 g / tonne and 750 g / tonne. More preferably still, the dose often needs to be between 200 and 500 grams per ton. All doses are based on weight of active polymer on the dry weight of the pulp suspension.

Water-soluble branched anionic polymer may consequently be added at any convenient point in the method, such as a dilute mixture of the suspension stock or alternatively in a mass of thick suspension. In some cases it may be desirable to add anionic branched polymer in a mixing VAT, the solvent Chan or perhaps one, or more, are components of the mixture.

Preferably, however, the anionic branched polymer to be added to the diluted mixture slurry. The exact point on the addition may be before one of the stages of shift. Typically, these phase shift include the stage of mixing, pumping and cleaning or other stages, which include mechanical degradation of cereal. Optional phase shift is selected from one or more of the mixing pumps or centresin. This alternative anionic polymer can be added after one or more mixing pump, but before centresin, or in some cases after centresin.

Phase splitting can be considered as stages in a mechanical what about cleavage, preferably acting on flocculating suspension in such manner as the destruction of the flakes. All system components retention/dehydration can be added to the phase shift, although preferably at least the last component of the system retention/dehydration added to the pulp suspension at the point-of-way where there is no significant shift before dehydration to form a sheet. Thus, it is preferable that at least one system component retention/dehydration added to the pulp suspension, and loose flakes suspension thus formed is then subjected to mechanical displacement, in which the flakes are mechanically destroyed, and then at least one system component retention/dehydration added to reaccelerate slurry to dewatering.

The first component of the system retention/dehydration can be added to the pulp suspension, and then flocculating the suspension formed in this way, you can pass through one or more stages of the shift. The second component of the system retention/dehydration can be added to re-reaccelerate suspension, which deflocculant can then be subjected to further mechanical offset. Kneaded refactoringassistant may also continue to flocculate the addition of the third component of the system retention/dehydration. Three component system retention/dehydration include, for example, where the cationic coagulant is used in addition to water-soluble cationic or amphoteric polymer and anionic branched polymer, for example, so-called system cat/cat and anionic branched polymer.

In the method, the anionic polymer may be added after adding the water-soluble cationic or amphoteric polymer and/or after adding a cationic coagulant. However, we have found that particularly effective results in terms of improved retention of the ash relative to the full retention, but the reduction in dehydration, when the anionic polymer is added to the pulp suspension before adding the water-soluble cationic or amphoteric polymer and also to cationic coagulant. Therefore, water-soluble branched anionic polymer optionally in advance is present in the pulp suspension before adding the water-soluble cationic or amphoteric polymer and, where used, cationic coagulant. This insertion order is unusual, as many known methods is a common practice to add a cationic component holding and especially any cationic to agulant to any anionic polymer component retention.

When water-soluble branched anionic polymer is added to the pulp suspension, it usually causes the occulation of suspended solids. Preferably the pulp suspension is subjected to at least one stage, which causes mechanical destruction before adding the water-soluble cationic or amphoteric polymer and using cationic coagulant. In General, the pulp suspension can be passed through one or more of these stages. Typically, these stages are stages of kneading, which include the stage of mixing, pumping and purification, such as one of the mixing pumps or centresin. In a more preferred object of the method of water-soluble branched polymer is added to centresin and water-soluble cationic or amphoteric polymer, and where used cationic coagulant is added to the pulp slurry after centresin.

Paper with a filler may be any suitable paper made from a pulp slurry containing wood fiber and at least 10 wt.% filler, calculated on the dry weight of the diluted mixture. For example, the paper may be lightweight coated paper (LWC), or more preferably it is SC paper (SC paper).

Under d Evesham fiber we mean, that pulp suspension includes wood pulp, which means any wood that is produced wholly or partly by mechanical means, including wood, a stone-ground (SGW), wood treated with high pressure (PGW), thermomechanical wood pulp (TMP), chemicomechanical wood pulp (STMR) or bleached chemicomechanical wood pulp (STMR). Varieties of paper with a wood filler contain different amounts of wood pulp, which is usually included to provide the desired optical and mechanical properties. In some cases, the mass used in the creation of paper with a filler, may be formed entirely of one or more of the above-mentioned wood wt. In addition to wood weight other weight is often included in the pulp suspension. Typically another mass can form at least 10 wt.% full of fiber content. These other mass included in the formulation of paper, include purified from paint mass and sulfate mass (often called Kraft pulp).

The preferred composition for paper SC differs in that the fiber fraction contains purified from paint weight wood pulp and sulphate mass. The contents of the pulp may vary between 10 and 75%, preferably between 30 and 60 wt.% full content volargne mass, purified from paint (often referred to as DIP)can be anything between 0 and 90%, usually between 20 and 60 wt.% just fiber.

The content of sulfate mass usually varies between 0 and 50%, preferably between 10 and 25 wt.% just fiber. The total amount of the components should be 100%.

The pulp slurry may contain other components such as cationic starch and/or coagulants. Usually in paper mixture can be cationic starch and/or coagulants to add system retention/dehydration of the present invention. Cationic starch may be present in amounts of between 0 and 5%, typically between 0.2 and 1 wt.% cellulose fibers. The coagulant is usually added in an amount up to 1 wt.% cellulose fiber, usually between 0.2 and 0.5%.

Optionally, the filler can be traditionally used filling material. For example, the filler may be a clay, such as kaolin, or may be calcium carbonate, which can be crushed calcium carbonate or preferably precipitated calcium carbonate (PCC). Another preferred filler material includes titanium dioxide. Examples of other filler materials include synthetic polymeric fillers.

In General, the pulp mixture used in the present invention, is preferably VK is ucati substantial amounts of filler, usually more than 10%, based on dry weight of the pulp mixture. Typically, however, the pulp mixture, which contains a significant quantity of filler is more difficult for flocculation than pulp mixture, using the opportunity to have grades that do not contain or contain less filler. This is especially true for fillers of very fine particle size, such as calcium carbonate, which precipitates, is introduced in the paper mixture as a separate Supplement, or as sometimes is adding purified from paint mass.

The present invention allows to make a highly filled paper from a pulp mixture containing high levels of filler and also contains mechanical fiber, such as SC-paper or coated paper for gravure printing, for example LWC with excellent retention and formation and preserved or reduced dehydration, which takes into account the best control dehydration of the mixture on the grid bumagodelatelnoe machine. Usually the paper weight must contain significant levels of filler in the diluted mixture, usually at least 25% or at least 30 wt.% dry suspension. Often the amount of filler in the composition of the paper pulp of polyparaphenylenes before dewatering the slurry to form a sheet, extending t is up to 70 wt.% dry suspension preferably between 50 and 65% filler. Optionally, the last piece of paper will include 40% filler by weight. It should be noted that conventional varieties of paper SC contain between 25 and 35% filler in the sheet.

Preferably the control method using bumagodelatelnuju machine with extremely rapid dehydration, especially those bumagodelatelnye cars that have twin-wire forming part of the extremely rapid dehydration, particularly those machines, called GAP formers or Hybridformers. The invention is particularly suitable for the production of paper grades with a high content of wood mass, such as SC-paper on bumagodelatelnyh machines, where the excess of the initial dehydration should happen otherwise. The method allows the retention, dehydration and the formation to be balanced in an optimized manner usually bumagodelatelnyh machines as GAP formers and Hybridformers.

In the method of the present invention, we find that in General the initial total retention and the retention of ash can be adapted to any suitable level depending on the needs of fashion and production. Grade SC-paper is usually produced at lower levels of total holding and holding ash than other varieties of paper such as bond paper, filled kop is Rosalina paper, cardboard or newsprint. At all levels of initial total retention amount from 30 to 60 wt.%, usually between 35 and 50%. Typically, the retention rate of ash can be in the range from 15 to 45 wt.%, usually between 20 and 35%.

The following examples illustrate the invention.

Examples

Methods

Preparation of polymers

All polymers and coagulants prepared as a 0.1% aqueous solution, relative to the active substances. Premixes consist of 50% of high-molecular polymer and 50% of the coagulant and mixed together as a 0.1% aqueous solutions before they are added to the composition of the paper pulp.

Starch was prepared as a 1%aqueous solution.

The polymers used for the examples

Polymer A: linear polyacrylamide, IV=9, 20% of the charge of the cation. A copolymer of acrylamide with methylchloride Quaternary ammonium salt of dimethylaminoethylacrylate (80/20 wt./wt.) intrinsic viscosity above 9.0 DL/g

Polymer B: branched Anionic copolymer of acrylamide to acrylamide sodium (60/40) made with 3.5-5.0 frequent. per million by weight of the branching agent methylene (bis) acrylamide. The product is supplied as a dispersion in mineral oil basis with 50% of active substances.

Polymer C: a 50%aqueous polyamine=solution of poly (epichlorhydrine) with 50% of active substances, 6-7 .0 mEq/g, IV=0.2; GPC molecular weight of 140,000

Polymer D: DADMAC in aqueous solution with 20% and the active substances and IV 1.4 DL/g, 6.2 mEq/g

Polymer E: Modified polyethylenimine in aqueous solution with 24% of the active substances.

System = Polymer A, added after the sieve

System B = Premix 50% of polymer A and 50% polymer C, added after the sieve

System C = Premix 50% of polymer A and 50% polymer E, added after the sieve

System D = Premix 50% of polymer A and 50% polymer D added after SITA and

System E = Polymer A, is added before the sieve

System F = Premix 50% of polymer A and 50% polymer D is added before the sieve

Paper composition

Composition 1 bond paper

This alkali, pulp slurry bond paper includes solid particles, which are composed of approximately 90 wt.% fiber and about 10% of the filler of precipitated calcium carbonate (PCC). Used RCA was "Calopake F" in the dry form from Specialty Minerals Lifford/UK. Applied fiber fraction was a mixture of 70/30 wt.% bleached bleached birch and pine, chopped Schopper Riegler degree of grinding of 48°to provide enough supplements for the real testing conditions. The composition was diluted with tap water to the consistency of approximately 0.61 wt.%, contained components approximately 18.3 wt.%, split approximately 50% of small fractions of fly ash and 50% of small fractions of fibers. 0.5 kg/t of chloride of polyalanine (Alcofix 905) and 5 kg/t (total if estvo solids) cationic starch (Raisamyl 50021) with the value of DS 0.035 in terms of dry weight, added to paper pulp. the pH of the composition of high-grade paper is 7.4±0.1, conductivity approximately 500 µs/m and Zeta-potential of approximately - 14.3 MB.

Composition 2 high-grade paper

This alkaline composition of high-grade paper made from a mixture of 70/30 wt.% discolored bleached birch and pine trees, which were crushed in a Schopper Riegler degree of grinding of 52°, and added a suspension of precipitated calcium carbonate to the ash content of approximately 21.1 wt.%. The pulp slurry was diluted to 0.46 wt.% solid particles contained additives approximately 32 wt.%, which included approximately 61% ash additives and 39% fiber supplements. 5 kg/t (total solids) cationic starch (Raisamyl 50021) with the value of DS 0.035, based on dry weight, added to the paper pulp. the pH factor of the final wood composition is 7.5±0.1, conductivity approximately 360 µs/m and Zeta-potential of approximately 22 mW.

Composition 3 high-grade paper

The pulp mixture produced by the consistency of 0.46 wt.% accordingly composition 2 high-grade paper. The ash content of approximately 18.9%, the Zeta-potential is 22 MB.

Composition 4 high-grade paper

This alkaline composition of high-grade paper made from a mixture of 70/30 wt.% bleached birch and ascocendas pine, which were crushed in a Schopper Riegler degree of grinding of 45°, and added a suspension of precipitated calcium carbonate to the ash content of approximately 46% by weight. The pulp slurry was diluted to 0.58 wt.% solid particles contained additives approximately 53 wt.%, which included approximately 84% ash additives and 16% fiber supplements. 5 kg/t (total solids) cationic starch (Raisamyl 50021) with the value of DS 0.035, based on dry weight, added to the paper pulp. The conductivity increased with calcium chloride to 1750 µs/m LV end-woody composition is 7.5±0.1, Zeta-potential is 7 MB.

Purified from paint wood pulp (DIP)

The composition is purified from paint recycled pulp is a mixture of ONP/OMG (old newsprint / old log) approximately 100 Canadian standard degree of grinding. Supplemented with a suspension of precipitated calcium carbonate (Omya F14960) to the ash content of approximately 56.7 wt.%. This composition was diluted with tap water to a final consistency of about 0.45 wt.%, including supplements approximately 65 wt.%, with approximately 82% ash additives and 18% fiber supplements. the pH of the final paper composition is 7.4±0.1, conductivity approximately 370 µs/m and Zeta-potential of about -50 mV. Highly filled DIP composition is, for example, approach the soup for the production of SCB-paper.

Wood composition 1

Wood pulp, bleached peroxide 60 Canadian standard degree of grinding, complemented Calopake F", RCA in dry form from Specialty Minerals Lifford/UK prior to the ash content of the additives is approximately 20.6 wt.% and diluted to a consistency of about 4.8 g/l, containing added approximately 33.8 wt.% which are components of the additives is approximately 54.5% ash additives and 45.5% fiber supplements. The final composition has a Schopper Riegler degree of grinding approximately 40°. To paper pulp added 0.5 kg/t of polyaluminosilicate (Alcofix 905) and 5 kg/t (total solids) cationic starch (Raisamyl 50021) with the value of DS 0.035 in terms of dry weight. The PH of the composition of high-grade paper is 7.4±0.1, conductivity is approximately 500 µs/m, and Zeta-potential of approximately - 23.5 MB.

Wood composition 2

Wood pulp, bleached peroxide 60 Canadian standard degree of grinding, supplemented with a suspension of precipitated calcium carbonate (Omya F14960) to the ash content of the additives is approximately 10.2 wt.% and diluted to a consistency of about 4.6 g/l, containing added approximately 28 wt.%, in which additives are separated by approximately 35% fly ash additives and 65% fiber supplements. To paper pulp added 5 kg/t (total solids) cationic starch(Raisamyl 50021) with the value of DS 0.035 in terms of dry weight. LV end-woody composition is 7.5±0.1, conductivity of approximately 400 µs/m and Zeta-potential of about -30 mV.

Wood composition 3

Wood pulp, bleached peroxide 60 Canadian standard degree of grinding, supplemented with a suspension of precipitated calcium carbonate (Omya F14960) to the ash content of the additives is approximately 21.8 wt.% and diluted to a consistency of about 0.45 wt.%, containing added about 40 wt.%, supplements containing approximately 56% ash additives and 44% fiber supplements. To paper pulp added 5 kg/t (total solids) cationic starch (Raisamyl 50021) with the value of DS 0.035 in terms of dry weight. the pH of the final wood composition is 7.5±0.1, conductivity of approximately 400 µs/m and Zeta-potential of approximately - 31 mV.

Wood composition 4

Wood pulp, bleached peroxide 60 Canadian standard degree of grinding, supplemented with a suspension of precipitated calcium carbonate (Omya F14960) to the ash content of the additives is approximately 48% wt.% and diluted to the consistency of approximately 0.46 wt.%, containing added about 56 wt.%, which included approximately 80% of the ash additives and 20% fiber supplements. To paper pulp added 5 kg/t (total solids) cationic starch (Raisamyl 50021) with the value of DS 0.035 in baresch the ones on dry weight. LV end-woody composition is 7.5±0.1, conductivity of approximately 400 µs/m and Zeta-potential of approximately - 36 mV.

SC-composition 1

The pulp mixture is used to give examples of a typical paper composition containing the wood to make the SC-paper. It consists of 18% purified from paint weight, 21.5% of unbleached wood, a stone-ground, and 50% of mineral filler containing 50% precipitated calcium carbonate (PCC) and 50% clay. RCC is Omya F14960, aqueous dispersion of precipitated calcium carbonate with 1% auxiliary substances for use in the SC-paper. Clay was Intramax SC Slurry from IMERYS. The final mixture had the consistency of 0.75%, total ash content of approximately 54%, degree of grinding 69° SR (Schopper Riegler method), conductivity 1800 µs/m and the content of the filler 65%, which included approximately 80% of the ash filler and 20% fiber fill. To paper pulp added 2 kg/t (total solids) cationic starch (Raisamyl 50021) with the value of DS 0.035 in terms of dry weight.

SC-song 2

The pulp mixture with 50%ash content made with the consistency of 0.75%, respectively, of composition 1, except that used other purified from paint weight. The degree of grinding 64°SR, the content of the fillers is 50 wt.%.

Free/initial dehydration

Properties dehydration determined by use of the modified device Schopper-Riegler with rear exit blocked so that water dehydration was through the front opening. The performance of the dewatering presented as the rate of dehydration, describing how many milliliters released over the net Schopper-Riegler per minute. The sequence dosing is the same as outlined for experiments with a scanning laser microscope and the moving belt casting machine. Paper dehydrated mixture after stirring for 75 seconds in accordance with the regulations of the SLM.

The initial General retention and retention of ashes

Paper sheets 19 cm2were made with the moving belt casting machine using 400-500 ml paper mixture, depending on the type of composition and consistency. Leaves were weighed to determine the initial total retention and the retention of ash using the following formula:

FPTR [%] = weight of the leaf [g] / total number of paper mixture, calculated on the dry weight [g]*100

FPTAR [%] = ash content in the sheet [g] / total number of paper mixture, calculated on the dry weight [g]*100

The initial retention of the ashes, for simplicity, cha is called holding the ashes, relatively full holding, directly associated with the ash content in the sheet. It is typical for the retention of filler. In order to demonstrate the invention, by means of real paper sheet compositions, the ratio between the effects of retention of ash and dehydration shows how the speed of free dehydration, divided by the ash content in the sheet.

Moving the tape casting machine (MBF) from Helsinki University of Technology, simulates the wet part of a normal clinocerinae bumagodelatelnoe machine (odnoetajnaya machine) on a laboratory scale and is used to make sheets of handmade character. Suspension mass formed on the fabric, which is exactly the same as used in industrial machines for the production of paper and cardboard. Moving perforated timing belt produces suscribase and pulsating action, modeling elements remove water, the blades and vacuum copying frame, located in the wire section. Under the timing belt is a vacuum copying frame. The level of vacuum, the speed of the belt and the effective time of suction and other operating parameters are controlled by computer system. The normal frequency range ripple 50-100 Hz and the effective time ranges suction from 0 to 500 MS. In addition to the grid has the I mixing chamber, like Britt Jar, where the composition is kneaded driven propeller stirrer before dehydration to form the sheet. A detailed description of the MBF is given in "Advanced wire part simulation with a moving belt former and its applicability in scale up on rotogravure printing paper", Strengell, K, Stenbacka, U, Ala-Nikkola, J. Pulp & Paper Canada 105 (3) (2004), T62-66. Retention and dewatering chemicals dosed in this mixing chamber, outlined in the Protocol below (see table 1). It should be noted that the dosing protocols for experiments with a scanning laser microscopy and MBF are the same in order to combine the results of the Schopper Riegler, scanning laser microscopy and MBF.

Table 1:
Moving the tape casting machine computer-controlled trial Protocol
Time [seconds]Action
0Beginning with stirring at 1500 rpm
12Add 1wowmeans of restraint
30Stirring at 500 rpm; adding 2thretaining additives
45Mixing at 1500 rpm
75Initial dehydration to form sheet

SLM (laser Scanning microscopy)

Scanning laser microscopy, often called FBRM (measurement of the reflectance of the laser focused beam)used in the following examples, is a measure of the size distribution of the particles in the present and outlined in US Pat. No. 4871251 issued Preikschat, F.. and E. (1989). It consists of 780 nm is focused rotating laser beam that passed through the target suspension at a speed of 2-4 m/s Particles and flakes, crossed by a laser beam, reflect part of the light back to the sensor. The time duration of light reflection is detected and converted into the length of the chord [m/s*s=m]. Measurements are not influenced by the velocity filter sample <1800 rpm, while the scanning speed of the laser is much faster than the speed of mixing. Ripple of reflected light used to form the histogram 90 registered channels of particle size between 0.8 and 1000 micrometers with the number of particles per time divided by the length of the chord. The original data can be represented in different ways, for example as the number of particles or chord length divided by time. The average is arithmetic, the medial and their derivatives numbers as well as different ranges of particle size can be selected to describe the observed way. Industrial tools are available under the trademark "Lasentec FBRM" from Mettler Toledo, Switzerland. For more information about using SLM in order to control the occulation can be found in the "Flocculation monitoring: focused beam reflectance measurement as measurement tool", Blanco, A, Fuente, E, Negro, C, Tijero, C. in Canadian Journal of Chemical Engineering (229), 80(4), 734-740. Published by: Canadian Society for Chemical Engineering.

The purpose of the SLM experiments is to determine the number of flakes, here described as a spatial parameter of the chord length at the upper range of the size distribution of the particles at the time when the sheet is formed on the grid. In accordance with the Protocol this time is 75 seconds. Large pulp aggregates contribute to the uneven appearance of the paper sheet and the deterioration in the formation. Figure 1 shows the unweighted distribution of chord length depending on the channel boundaries in microns. As usual in theory of particles, the length of the chord is applied in the third degree, in order to emphasize the large aggregates. Thus figure 2 illustrates the distribution of the chord length, brought in the third degree flocculating SC, depending on the channel boundaries in microns. As can be seen from figures 1 and 2, the range between 170 and 460 nm OPI which indicates the upper limit of the length of the chord for touching song. Therefore, the number of particles in this particular range is measured as a unit per second.

The experiment consists of taking 500 ml paper mixture and place it in the appropriate mixing beaker. The composition is mixed and kneaded with a variable speed motor and propeller, like the standard customized Britt Jar. Applied sequence dosing is the same as used for moving the tape casting machine and is shown below (see table 2):

Table 2:
Scanning laser microscopy Protocol test
Time [seconds]Action
0Beginning with agitation set at 1500 Rev/min
12Add 1thretaining additives
30Set stirring at 500 rpm; adding 2thretaining additives
45Set stirring at 1500 rpm
75 Stop experiment

Example I: Composition 1 bond paper E

Example I shows the principle of retention and dewatering for the composition of the chemical pulp as described in WO-A-9829604 containing the first polymeric cationic additive retention (E)to form cellulose flakes, mechanically crush the flakes, reaccelerate suspension, adding a second water-soluble branched anionic polymer additive retention (polymer)to form a sheet. As expected, the total retention and the retention of ash as well as the rate of dehydration are increased simultaneously. For example, 800 g/t system E will lead to a complete hold about 95%, for holding the ashes of approximately 73% and the speed of dehydration 625 ml/min In contrast, only 200 g/t system E, followed by a 100 g/t polymer B, lead to similar results retention and higher speeds dehydration 652 ml/min (see Tables I.1, I.2 and figure I). Thus, no effect of separation does not occur, which would allow bumagosmolyanoy to establish the desired ratio between the total holding or retention of ash and, in addition, the rate of dehydration.

Without the addition of polymer B, dosage of system E = variabletd align="center"> 87.5
Table I.1:
Dosing system EThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
20093.664.16.954583.9
40093.666.87.158883.9
80094.573.17.762584.7
100097.676.77.9638

Table I.2:
100 g/t polymer B = const, dosage of system E = variable
Dosing system EThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
5087.560.66.956678.5
10090.263.97.162580.8
20095.372.57.665285.4

Dosing system EThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
30098.076.27.871487.9

Example II: Composition 2 high-grade paper with A

This example shows the effect of the polymer In the pre-added to the system A, on separation phenomena of retention and dewatering in bond paper. As shown in figure II.1, the profile of the dewatering system And divided by the ash content in the sheet remains unchanged. From this it follows that this is the preferred form of the invention is not working for the chemical pulp or in other words, it is inappropriate for besignificantly fibers (see tables II.1, II.2 and figure II.2).

In addition, the retention worsens on an active polymer basis, identified as polymer B + A (see figure II.2). The way flocculation becomes what I wasteful and does not provide any technical specifications, neither benefit cost for bumagounichtozhiteli.

Table 11.1:
Without the addition of polymer B, dosage of system A = variable
Dosage system AndThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
20078.842.711.464953.2
40080.151.413.575854.1
60082.357.314.7 82655.6
80082.459.415.286655.7
120083.063.216.195756.1

Table II.2:
250 g/t polymer B = const, dosage of system A = variable
Dosage of system AThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
40076.838.710.662 51.9
60079.644.111.767353.8
80080.847.712.469954.6
100080.450.313.272754.4
140081.955.814.479155.4

Example III: Composition 3 high-grade paper with systems C and D

Example III emphasizes the data obtained from example II, particularly the anionic branched polymer B, added pre-K systems cat/cat with an intermediate stage of kneading, does not provide similar or improved retention of ash and reduced dehydration at a time. System C is a typical system cat/cat based on polyacrylamide and polyethyleneimine, while the system D presents DD containing system cat/cat (see Tables is III.1-4 as well as figures III.1 and III.2).

60.9
Table III.1:
Without the addition of polymer B, dosage of system S =
Desire-CAS system CThe initial total holdingThe initial total holding ashThe ash content in the sheetSpeed free obasogie
of
The bulk
[g/t][%][%][%][ml/min][g/m2]
5066.75.31.571456.3
10067.910.02.871457.4
20072.124.36.4698
30074.932.18.175063.3

Dosage system CThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
40076.644.310.981164.7
50079.148.311.593866.9

/tr>
Table III.2:
250 g/t polymer B = const., dosing system With = variable
Dosage system CThe initial total holding The initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
5072.828.27.366761.5
10072.232.68.571461.0
20072.629.87.869861.3
30075.236.89.278963.5
40074.038.09.776962.5
50075.341.110.381163.7
60076.449.112.1100064.6

Table III.3:
Without the addition of polymer B, dosage of system D = variable
Dosage of DThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
10068.417.34.771459.1
20070.033.68.773261.6
30072.938.89.776964.2
40076.043.610.881164.4
50076.838.59.578964.9

Table III.4:
250 g/t polymer B = const., dosage of D = variable
Dosage of DThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
5071.629.57.873260.5
10072.324.76.571461.1
20074.029.47.569862.6
30073.739.710.278962.3
50075.045.911.681163.4
60078.251.312.485766.0

Example IV the Composition is 4 high-grade paper with A

The purpose of this example is to show that the separation of the retention of ash and dehydration also not achieved at higher levels of ash in the composition of high-grade paper as it would be used for the production of vysokonapolnennyh office paper (see Tables IV.1, IV.2 and figure IV).

Table IV.1:
Without the addition of polymer B, dosage of system A = variable
Dosage system AndThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
20062.427.320.162553.2
400 69.241.927.967058.9
60071.348.631.469460.7
100073.455.034.473562.6

Table IV.2:
250 g/t polymer B = const., dosage of system A = variable
Dosage system AndThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
200 68.737.224.967058.6
40069.940.826.870859.6
60071.346.930.372160.8
100072.953.233.675062.1

Example V: Purified from paint recycled pulp (DIP) systems A and B

Example V demonstrates, for example, by DIP composition that the effect of separation, as defined in the invention, does not occur in the composition of recycled fiber. Retention and dehydration at the same time increased irrespective of the only high occulant or system cat/cat uses. Thus, economical independent control of dehydration is not provided (see Table V.1-4 as well as figures V.1 and V.2).

td align="center" namest="c0" nameend="c5"> Without the addition of polymer B, dosage of system A = variable
Table V.1:
Dosage of system AThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
40054.427.228.393836.0
60060.836.233.8101440.2
80066.445.038.4121043.9
120073.155.142.7 150048.3

Table V.2:
250 g/t polymer B = const., dosage of system A = variable
Dosage of system AThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
40055.725.526.087235.8
60062.435.031.8113639.8
80068.945.037.0 129342.8

Table V.3:
Without the addition of polymer B, dosage of system =
Dosage BThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
60051.822.224.385234.2
80056.326.726.998737.2
100059.433.632.0 101439.3
160066.344.538.1113643.8

Table V.4:
250 g/t polymer B = const, the dosage system =
Dosage BThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
40054.226.727.9107135.8
60060.231.629.7 113639.8
80064.741.436.3129342.8

Example VI: Wood composition 1 E

Wood composition in this example, similarly prepared composition 1 bond paper, based on adding RACES and starch. System E similarly applied in connection with 100 g/t polymer Century, Unexpectedly the total retention and the retention of ash increased, and the rate of dehydration decreased at the same time. For example, 800 g/t system E leads to an overall holding approximately 77%, for holding the ashes of approximately 47% and the speed of dehydration 1008 ml/min In contrast 400 g/t E, followed by a 100 g/t polymer B, lead to similar results hold and lower speed dehydration 929 ml/min (see Table VI.1, VI.2 and figure VI). Thus the increase in the total retention and the retention of the ash is separated from the speed of dehydration. Bumagodelatel can now adjust the desired ratio between the retention of ash and dehydration, the alignment of these two components.

Table VI.1:
Without the addition of polymer B, dosage of system E = variable
Dosing system EThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
60077.837.810.090554.8
80077.247.112.6100854.4
120077.051.413.7110354.3

Table VI.2:
100 g/t polymer B = const., dosing system E = variable
Dosing system EThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
20072.639.011.188251.2
40076.746.712.592954.1

Dosing system EThe initial total holdingThe initial total holding ashThe ash content in the sheetThe bulk
60076.751.513.8100854.1

Example VII: Wood composition 2 systems A and E

Figure VII.1 and VII.2 clearly show that the use of the polymer In the system connection A and B in tree composition, brings significant improvement in the retention of the ash relative to the full retention while reducing dehydration (see also Table VII.1-4). Based on this effect, as well as further adaptation of the dosage can be adjusted as desired relationship between retention and dehydration. Composition, leading to levels of ash approximately 6-8 wt.% in the sheet, could, for example, to simulate the composition of newsprint.

Table VII.1:
Without the addition of polymer B, dosage of system A=variable
Dosage of system AThe initial total holdingThe initial total holding ash The ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
20082.034.14.272755.4
40085.951.76.186658.1
60087.962.27.2101059.4
80090.263.67.2107061.0
120090.474.88.4121261.1

Table VII.2:
250 g/t polymer B = const., dosage of system A = variable
Dosage system AndThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
20083.049.46.167356.1
40085.756.56.775857.9
60086.962.17.379158.7
800 88.067.27.886659.5

Table VII.3:
Without the addition of polymer B, dosage of system =
Dosage BThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
40056.439.34.872756.4
60057.346.05.579157.3
800 57.950.86.182657.9
100058.852.06.186658.8
160060.463.17.295760.4

Table 4:
250 g/t polymer B = const, the dosage system =
Dosage BThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
200 54.341.15.264954.3
40057.854.96.572757.8
60058.764.87.686658.7
80060.269.47.995760.2

Example VIII: Wood composition 3 with systems A, B, D, E, and G

Examples running on wood composition 2, indicate that the scope of the invention also applies to highly filled paper wood-containing pulp, such as improved newsprint or LWC. In the figure VIII.1 of the polymer decreases In free/initial dewatering systems A. If only a occulant added to the polymer In here called E obtained similar results of dehydration (see Tables 1, 2, 3 and figure 1). System cat/cat B, D and G represent polyamine and DD containing polymer mixtures behave as the system is and show strong effects of separation (see Table 4-8 and figure VIII.2 and 3).

Table VIII.1:
Without the addition of polymer B, dosage of system A = variable
Dosage system AndThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
20071.223.17.1107047.1
40073.836.210.7121248.8
60077.841.611.7 129951.4
80079.748.113.2139952.7
120082.159.115.7151554.3

Table VIII.2:
250 g/t polymer B = const, dosage of system A = variable
Dosage of system AThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
20072.732.09.6 101048.0
40074.640.111.7107049.3

Dosage of system AThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
60077.447.513.4113651.2
80078.953.214.7129952.2

Table 3:
250 g/t polymer B = const., dosing system E = variable
Dosing system EThe original level is high overall retention The initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
20073.030.08.995748.3
40077.742.411.9113651.3
60078.948.313.3121252.2

Table 4:
Without the addition of polymer B, dosage of system =
Dosage BThe initial about is him holding The initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
40071.122.97.0101047.0
60073.529.48.7107048.6
80074.428.98.5113649.2
100075.537.610.9121249.9
160076.238.411.0 139950.4

Table 5:
250 g/t polymer B = const., dosage system =
Dosage BThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
20072.329.89.090947.8
40075.141.312.0107049.7
60076.243.612.5 113650.4
80078.751.614.3129952.0

Table VIII.6:
Without the addition of polymer B, dosage of system D = variable
Dosage of DThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%].[%][ml/min][g/m2]
20068.215.44.995745.1
40070.822.56.9 101046.8
60071.822.46.8107047.5
80074.233.09.7113649.0
100073.733.810.0113648.7
120076.137.910.9121250.3

Table VIII.7:
250 g/t polymer B = const., dosage of D = variable
Dosage of DThe initial total holdingThe initial total holding ashThe ash content of the pisteThe speed of free dehydration The bulk
[g/t][%][%][%][ml/min][g/m2]
20072.333.310.0101047.8
40075.336.110.4113649.8
60077.847.013.2129951.4

Dosage of DThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
80077.750.214.1 129951.3
100079.351.214.1129952.4

Table VIII.8:
250 g/t polymer B = const., dosage system G = variable
Dosage system GThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
20075.935.110.175850.2
40078.342.611.8 90951.8
60080.547.112.8101053.2
80080.349.413.4107053.1
100081.758.015.5113654.0

Example IX: Wood composition 4 with A

Examples played on the wood composition 4, demonstrate that the invention also operates on a highly filled wood compositions, such as grade SC-paper. In this preferred application of the invention the retention of ash and free dehydration is extremely disconnected, shown with system A and B (see Table IX. 1-4 as well as figures IX.1 and 2). Therefore, example IX contrary to the highly filled compositions of high-grade paper and DIP (see examples IV and V), where no separation occurs.

Table IX.1:
Without added what I polymer B, dosage of system A = variable
Dosage system AndThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
20054.823.620.788946.3
40057.628.023.392348.7
60061.633.826.3104352.0
80064.137.628.21043 54.1
100058.937.130.2109149.8
120060.941.532.7114351.4

Table 2:
250 g/t polymer B = const, dosage of system A = variable
Dosage system AndThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
5054.523.120.4750 46.0
10051.724.122.480043.6
15056.527.123.080047.7
20056.028.924.882847.3
40059.037.730.792349.8

Table IX.3:
Without the addition of polymer B, dosage of system =
Dosage BThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe main the ACCA
[g/t][%][%][%]'[ml/min][g/m2]
40052.417.616.180044.3
60050.319.818.988942.5

Dosage BThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
80053.922.319.992345.5
100056.726.122.1 100047.9
160057.427.623.1100048.5

Table IX.4:
250 g/t polymer B = const., dosage system =
Dosage BThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationThe bulk
[g/t][%][%][%][ml/min][g/m2]
5053.723.120.666745.4
10053.222.920.7 70645.0
15055.725.421.877447.1
20057.930.225.182848.9
40058.836.930.192349.7

Example X: SC-composition 1 with A

In the example, X is the only system of occulant (A) is compared with and without the addition of anionic branched polymer to sieve SC-composition 1. It is evident that the addition of the anionic branched polymer reduces dehydration and increases the retention of ash at the same time (see figure X). Dosage system And decreases, which is believed to be due to the presence of large aggregates, shown as unit/s in the faction 170-460 nm, significantly decreased (see also figure XVI.2).

Table H:
Without the addition of polymer B, d is serowka system A = variable
Dosage system AndThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationfraction 170-460 micronsThe bulk
[g/t][%][%][%][ml/min][units/s][g/m2]
40055.129.428.8159.318.460.8
60058.235.833.2181.830.064.2
80062.441.936.2206.937.368.8
100064.244.337.2233.843.670.7

Table H:
250 g/t polymer B = const, dosage of system A = variable
Dosage system AndThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationfraction 170-460 micronsThe bulk
[g/t][%][%][%][ml/min][units/s][g/m2]
15053.328.729.0135.314.358.8
200 54.930.930.4132.414.160.5
25055.131.831.2140.617.360.7
30057.333.931.9133.320.763.2
35056.934.432.7153.822.562.7
40057.437.335.1150.025.663.2

Example XI: SC-composition 1 with B

In example XI system, a premix consisting of 50% polyamine and 50% of occulant, compared with and without the addition of anionic branched polymer to sieve SC-composition 1. It is evident that the addition of the anionic branched the second polymer reduces dehydration and increases the hold simultaneously (see figure XI). Dosage system, as well as a full dose of the polymer is reduced. The number of large units are shown as unit/s in the faction 170-460 nm, is similar, why influence on the formation are unlikely (see also figure XVI.2).

Table XI.1:
Without the addition of polymer B, dosage of system =
Dosing systemThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationfraction 170-460 micronsThe bulk
[g/t][%][%][%][ml/min][units/s][g/m2]
40049.421.223.2139.511.354.4
60052.624.024.6156.512.557.9
80055.733.732.7183.712.661.4
100056.936.234.3200.013.262.7
120058.537.935.0214.313.864.4
140061.841.236.1230.820.268.1

Table XI.2:
250 g/t polymer B = const., dosage system =
Dosage system which we The initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationfraction 170-460 micronsThe bulk
[g/t][%][%][%][ml/min][units/s][g/m2]
10046.920.323.3108.46.751.7
20053.027.127.6128.69.558.4
30052.428.429.3146.310.457.7
40052.9 29.830.4155.210.058.3
50056.333.932.5168.215.862.0
60056.134.132.8173.114.861.8
70058.137.234.6185.619.064.0
80059.538.735.1195.719.165.5

Example XII: SC-composition 1 with the system C

In example XII system C, a premix consisting of 50% polyethylenimine and 50% of occulant, compared with and without the addition of anionic branched polymer to sieve SC-composition 1. It is evident that the addition of the anionic branched polymer, reduces energy is dehydration and increases the retention of a lump sum (see figure XII). Dosage system C, as well as a full dose of the polymer is reduced. The number of large units, shown as a unit on the second faction 170-460 nm, is similar, why influence on the formation are unlikely (see also figure XVI.2).

Table XII.1:
Without the addition of polymer B, dosage of system S =
Dosage system CThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationfraction 170-460 micronsThe bulk
[g/t][%][%][%][ml/min][units/s][g/m2]
30048.120.322.8127.79.353.0/td>
40049.323.225.5140.68.354.3
50052.126.827.8142.99.457.4
60053.128.629.1160.713.258.5
70055.533.332.4162.211.161.2
80055.332.431.6168.212.461.0
90057.936.233.8185.613.863.8

Table 2:250 g/t polymer B = const., dosing system With = variableDosage system CThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationfraction 170-460 micronsThe bulk[g/t][%][%][%][ml/min][units/s][g/m2]30054.631.431.1140.615.160.140056.133.732.4137.414.561.960059.5 37.233.7168.214.565.680059.339.736.1187.517.665.4

Example XIII: SC-composition 1 with system D

In example XIII system D, a premix consisting of 50% DADMAC and 50% of occulant, compared with and without the addition of anionic branched polymer to sieve SC-composition 1. It is evident that the addition of the anionic branched polymer reduces dehydration and increases the hold simultaneously (see figure XIII). Dosage of D, as well as a full dose of the polymer is reduced. The number of large units, shown as a unit on the second faction 170-460 nm, is similar, why influence on the formation are unlikely (see also figure XVI.2).

Table XI 11.1:
Without the addition of polymer B, dosage of system D=variable
Dosage of DThe initial total holding The initial total holding ashThe ash content in the sheetThe speed of free dehydrationfraction 170-460 micronsThe bulk
[g/t][%][%][%][ml/min][units/s][g/m2]
60054.829.929.4153.810.760.4
80057.533.531.5178.212.563.3
100059.938.534.7205.314.866.0

Table 2:
250 g/t polymer B = is onst, dosage of D=variable
Dosing system
D
The initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydration170-460 fraction micronsThe bulk
[g/t][%][%][%][ml/min][units/s][g/m2]
30051.729.630.9136.411.357.0
40054.333.032.8150.011.859.9
50055.233.933.2168.214.5 60.8
60056.536.234.6181.813.762.3
70056.835.934.2197.815.262.6

Example XIV: SC-song 2 system B

In example XIV system, a premix consisting of 50% polyamine and 50% of occulant, compared with and without the addition of anionic branched polymer to sieve SC-song 2. It is evident that the addition of the anionic branched polymer reduces dehydration and increases retention at a time (see figure XIV). Dosage of D, as well as a full dose of the polymer is reduced. The number of large units, shown as a unit on the second faction 170-460 nm, is similar, why influence on the formation are unlikely (see also figure XVI.2).

Table 1:
Without the addition of polymer of N, the dosage system =
Dosirak the system B The initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydration170-460 fraction micronsThe bulk
[g/t][%][%][%][ml/min][units/s][g/m2]
60050.724.223.8197.813.155.8
65052.328.727.5202.211.257.6
70050.927.527.0225.011.256.1
75051.7 27.626.7227.814.256.9
100056.633.129.2253.517.862.4

Table XIV.2:
250 g/t polymer B = const, the dosage system =
Dosing system
In
The initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydration170-460 fraction micronsThe bulk
[g/t][%][%][%][ml/min][units/s][g/m2]
20051.429.4 28.6191.59.256.6
30052.630.729.2216.915.157.9
40055.433.430.2219.519.961.0
50055.132.529.4227.814.660.7

Dosage BThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free
dehydration
170-460 fraction micronsThe bulk
80058.740.1 34.1257.117.064.7

Example XV: SC-composition 1 E

In example XV system E, the only occulant is compared with and without the addition of anionic branched polymer to sieve SC-composition 1. It is evident that the addition of the anionic branched polymer reduces dehydration and increases retention when it is dosed after the cationic species (see figure XV). Dosing system E, as well as a full dose of the polymer is reduced. The number of large units, shown as a unit on the second faction 170-460 nm, is similar, why influence on the formation are unlikely (see also figure XVI.2).

The bulk
Table XV.1:
Without the addition of polymer B, dosage of system E = variable
Dosing system
E
The initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydration170-460 fraction microns
[g/t][%][%][%][ml/min][units/s][g/m2]
40050.523.024.6138.514.655.6
60055.029.529.0162.220.760.6
80058.835.132.2193.526.164.8
100060.738.634.3211.833.466.9
120063.644.437.7233.835.1 70.1

Table XV.2:
200 g/t polymer B = const, dosage of system E = variable
Dosing system EThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free dehydrationfraction 170-460 micronsThe bulk
[g/t][%][%][%][ml/min][units/s][g/m2]

Dosing system EThe initial total holdingThe initial total holding ashThe ash content in the sheetThe speed of free
dehydration
fraction 170-460 micronsThe main Mac is a
30056.432.230.9150.015.062.1
50059.938.234.4165.118.966.0
70061.040.235.6183.724.367.3

Example XVI:

In addition to the regulation of the balance between the retention and dewatering to facilitate good creation sheet, should be minimized creation of coarse cereals, in which case the uniformity of the sheet could be unsatisfactory. Figure 1 shows a General idea of the number of large particles at the length of the chord 170-460 microns depending on the ash content in the sheet. This shows that soft occulation provided using the system cat/cat in paper production, is not weakened by the addition of the anionic branched polymer before the cationic system, here denoted as doba is of "before the sieve". Indeed, the distribution of chord length only flocculation system A significantly improved through the addition polymer B. With this in mind, this order of addition is preferred form of the invention.

Figure XVI.2 shows the presence of large particles, as accumulation units for a second length of chord applied in the third degree, depending on the chord length of the channel borders. Various flocculation system compared at similar levels of ash in the worksheet to identify the impact on the size of the flakes. Figure XVI.2 reiterates for example, the results of figure 1. The only flocculation system causes A larger flakes than the system cat/cat C with or without addition of anionic branched polymer In the same way, as the only polymer A with the addition of the anionic branched polymer B.

1. Method of making paper with filler, comprising the steps of providing a thick mixture of pulp suspension which contains wood pulp and a filler dilution thick mixture slurry to form a diluted mixture of a suspension, in which the filler is present in the diluted mixture slurry in the amount of at least 10 wt.% in terms of the dry mass of the diluted mixture suspension, flocculation thick mixture of suspension and/or razbavlen the mixture, using polymer retention system/dehydration, dehydration diluted mixture slurry through the screen to form a sheet and then drying the sheet, in which the polymeric retention system/dehydration includes
i. water-soluble branched anionic polymer and
ii. water-soluble cationic or amphoteric polymer.

2. The method according to claim 1, wherein the water-soluble cationic or amphoteric polymer is a natural polymer or a synthetic polymer which has an intrinsic viscosity of at least 1.5 DL/g, preferably at least 3 DL/g

3. The method according to claim 1 or 2, in which the water-soluble cationic or amphoteric polymer is any cationic starch, amphoteric starch or a synthetic polymer selected from the group consisting of cationic or amphoteric polyacrylamides, polyvinyl amines and polydiallyldimethyl chloride (DADMAC).

4. The method according to claim 1, wherein the water-soluble cationic polymer is used in combination with cationic coagulant.

5. The method according to claim 4, in which the water-soluble cationic or amphoteric polymer and cationic coagulant is added to the pulp slurry as a mixture.

6. The method according to claim 4 or 5, in which the cationic coagulant is a synthetic floor is Merom intrinsic viscosity of up to 3 DL/g and shows the charge density of the cation more than 3 mEq./g, preferably homopolymer of DADMAC.

7. The method according to claim 1, wherein the water-soluble branched polymer has a
(a) intrinsic viscosity higher than 1.5 DL/g and/or the viscosity Brookfield the above salt solution of approximately 2.0 MPa·s, and
(b) the magnitude of flow fluctuations tan Delta 0.005 Hz to above 0.7 and/or
(c) the coefficient of viscosity of deionized SLV, which is at least three times the coefficient of viscosity of the salt solution SLV corresponding unbranched polymer made in the absence of branching agent.

8. The method according to claim 1, wherein the water-soluble branched anionic polymer is present in the pulp suspension before adding the water-soluble cationic or amphoteric polymer and where to use the cationic coagulant.

9. The method according to claim 1, in which the pulp suspension containing water-soluble branched anionic polymer is subjected to at least one stage, which causes mechanical destruction of the addition of water-soluble cationic or amphoteric polymer and where to use the cationic coagulant.

10. The method according to claim 1, wherein the water-soluble branched anionic polymer is added before centresin and water-soluble cationic or amphoteric of polim the rum and where used cationic coagulant is added/added to the pulp slurry after centresin.

11. The method according to claim 1, in which the paper filler is SC paper (SC paper).

12. The method according to claim 1, in which the wood pulp is selected from the group consisting of a stone-ground wood (SGW), ground wood treated with high pressure (PGW), thermomechanical pulp (TSR), chemicomechanical wood pulp (STMR), bleached chemicomechanical wood pulp (STMR) and mixtures thereof.

13. The method according to claim 1, wherein a content of the pulp is between 10 and 75%, calculated on the dry weight of the pulp suspension, preferably between 30 and 60%.

14. The method according to claim 1, wherein the filler is selected from the group consisting of calcium carbonate, titanium dioxide and kaolin, preferably calcium carbonate, which precipitates.

15. The method according to claim 1, wherein the filler is present in the pulp slurry prior to dewatering, is at least 30 wt.% in terms of dry weight of the suspension, preferably between 50 and 65%.

16. The method according to claim 1, wherein the method is carried out on the paper machine GAPformer or other twin-wire paper machine.



 

Same patents:

FIELD: textile, paper.

SUBSTANCE: full bleaching/extraction of craft cellulose fibres is carried out with a chorine agent. Afterwards fibres are washed and exposed to contact in solution with at least one optical bleach (OB) upstream the mixing box and the discharge box of the machine. Fibres in solution have consistency from 7 to 15%, pH of solution in process of contact of fibres with OB makes from 3.5 to 5.5, temperature of contact makes from 60 to 80°C, and time of contact is from 0.5 to 6 hours. Additional contact of OB with fibres is carried out in the device for coating application or in the gluing press. Contact may be carried out at the stage of storage, both at high density and low density of the craft-cellulose fibres, and also at the stage of refinement.

EFFECT: improved whiteness and brightness of fibres when using lower quantity of OB.

19 cl, 11 dwg, 12 tbl, 6 ex

FIELD: textile, paper.

SUBSTANCE: according to one version, method includes provision of aqueous suspension that contains cellulose fibres. Addition of cation polysaccharide and polymer P2, which is an anion polymer, to produced suspension after all points of high polymer P1 shearing force, and P1 polymer is an anion polymer. Then water is removed from produced suspension to form paper. According to the other version, auxiliary agents are added for drainage and retention to produced suspension of cellulose fibres after all points of high shearing force. The latter are represented by a cation polysaccharide and polymer P2, being an anion polymer.

EFFECT: improved drainage without deterioration in retention and forming of paper, increased speed of paper-making machine and application of lower doses of polymer.

34 cl, 5 tbl, 5 ex

The invention relates to the production of paper and can be used in the pulp and paper industry (PPI) for securities in a neutral environment on the basis of wood pulp and wood chemical thermomechanical pulp (CTMP), for example offset printing paper and newsprint paper for printing Newspapers and high offset printing methods

FIELD: textile, paper.

SUBSTANCE: method includes moistening pulp lap with water solution of sodium salt of carboxymethylcellulose (NaCMC), included into composition of the paste made of a filler (chalk), mixed with a solution of NaCMC at the filler ratio of NaCMC equal to 100:(1-2). Production of moisture-saturated air suspension of fibres with filler from it. Forming a fibrous later on a shaping mesh. Moistening of a fibrous layer between two clothes, pressing and drying of a paper leaf. The filler is added as a paste, which contains 30% of dry substance. Moistening of a fibrous layer prior to pressing is carried out with a starch solution with concentration of 0.7-1.3%.

EFFECT: increased retention of filler in paper at simultaneous increase of paper strength index.

3 cl, 1 tbl, 4 ex

FIELD: chemistry.

SUBSTANCE: aqueous polysilicate composition is meant for producing paper and cardboard and can be used in pulp and paper industry. The aqueous polysilicate composition contains a component based on polysilicate microgel combined with particles obtained from colloidal polysilicate. The method of preparing the aqueous polysilicate composition involves mixing aqueous colloidal polysilicate with an aqueous phase of polysilicate microgel. This composition or a composition obtained using the method described above can be used as a flocculant when producing paper and cardboard. The method of producing paper or cardboard involves preparation of a cellulose suspension and flocculation of said suspension using a flocculation system containing said polysilicate composition. The suspension is then drained on a mesh to form a sheet which is then dried.

EFFECT: high efficiency of the disclosed aqueous polysilicate composition owing to improved holding or draining when making paper or cardboard, as well as stability thereof during storage.

24 cl, 11 tbl, 3 ex, 9 dwg

FIELD: textile, paper.

SUBSTANCE: cellulose product comprises thermoplastic microspheres and a charged aromatic acrylamide polymer. The method to produce a cellulose product includes provision of an aqueous solution of suspension that contains cellulose fibres. Addition of thermoplastic microspheres and the charged aromatic acrylamide polymer into the suspension, and dehydration of the produced suspension. Thus made cellulose product may be used as a cardboard for liquid packing.

EFFECT: reduced porosity of a cellulose product as its volume increases and improved resistance of a wick edge to penetration of aqueous liquids for cellulose products.

25 cl, 3 tbl, 4 ex

FIELD: textile, paper.

SUBSTANCE: method of filler treatment includes formation of a mixture of an aqueous suspension of filler and aqueous anion latex. The latter is a dispersion of acrylic polymer with vitrification temperature (T v) from - 3 to 50°C. This mix is mixed with water at the temperature that is higher than T v of latex, at the same time the specified water has temperature of 40-98°C. The specified suspension of the filler comprises a solid disperse filler selected from the group containing kaolin clay, ground calcium carbonate, deposited calcium carbonate, deposited calcium sulfate, talc and mix of two or more of them. The specified acrylic polymer is selected from the group containing copolymers n-butylacrylate-acrylonitrile-sterol and copolymers n-butylacrylate-sterol. The aqueous composition of the filler contains the solid dispersed filler specified above with solid particles of anion latex polymer specified above and adsorbed on them, in aqueous carrier. The treated filler contains the solid dispersed filler specified above with solid particles of anion latex polymer specified above and adsorbed on them. The pulp charge contains pulp fibres and the solid dispersed filler specified above with solid particles of anion latex polymer specified above and adsorbed on it, in aqueous carrier. Method to make paper from the above specified pulp charge containing pulp fibres. The paper product made of pulp fibres and solid disperse filler, where the specified filler has solid particles of anion latex polymer specified above absorbed on it, with size of solid polymer particles of 30-200 nm and in amount of 1-100 kg of latex per 1 t of filler relative to dry mass of solid substances of latex and filler, and the specified filler has average size of particles of 0.1-30 mcm.

EFFECT: improved retention of the filler, continuous execution of the filler treatment method to improve fixation of anion latex on the filler for a short period of time due to irreversible fixation of anion latexes on particles of the filler and time stability of aggregated filler suspension, latex-treated deposited calcium carbonate is more acid-resistant, and when used to make paper from wood mass under neutral conditions less acid is required to control pH.

21 cl, 14 dwg, 8 ex

FIELD: textile, paper.

SUBSTANCE: method includes dissolution of cellulose and its grinding down to specified extent of grinding. Preparation of the first dispersion with application of return water, containing fibres of microcrystal cellulose, produced by its grinding in mixture with titanium dioxide and calcium hydroxide in specified amount. The second dispersion is prepared from cellulose fibres with application of return water. Then the first suspension is mixed with the second, and produced mixture is treated with carbon dioxide. In case of this treatment calcium hydroxide under action of carbon dioxide results in production of chemically deposited chalk and production of paper mass at specified ratio of components. Grinding of microcrystalline cellulose in mixture with titanium dioxide and calcium hydroxide is carried out in vibration mill with provision of impact and wear effect at mixture.

EFFECT: increased extent of fillers retention in paper, improvement of its printing properties, provision of possibility to vary bulk and porosity of paper, provision of possibility to use fully closed cycle of return water.

1 tbl, 8 ex

FIELD: textile, paper.

SUBSTANCE: according to one version, method includes provision of aqueous suspension that contains cellulose fibres. Addition of cation polysaccharide and polymer P2, which is an anion polymer, to produced suspension after all points of high polymer P1 shearing force, and P1 polymer is an anion polymer. Then water is removed from produced suspension to form paper. According to the other version, auxiliary agents are added for drainage and retention to produced suspension of cellulose fibres after all points of high shearing force. The latter are represented by a cation polysaccharide and polymer P2, being an anion polymer.

EFFECT: improved drainage without deterioration in retention and forming of paper, increased speed of paper-making machine and application of lower doses of polymer.

34 cl, 5 tbl, 5 ex

FIELD: textile; paper.

SUBSTANCE: method (in version) concerns paper manufacturing and can be applied in pulp and paper industry. Method involves: (i) supply of water suspension containing pulp fiber, (ii) adding to suspension after the last point of severe shear force exposure of: (a) first anion component of anion organic polymer soluble in water; (b) second anion component of anion organic polymer dispersed in water or branched organic polymer; and (c) third anion component of anion material containing silicon; and (iii) dehydration of obtained suspension to produce paper. Also invention concerns composition (in version) including first, second and third anion components, and application of the composition as flocculation agent in production of pulp mass and paper for water treatment.

EFFECT: improved water drainage and retaining during paper manufacturing out of any type of pulp suspensions, accelerated operation of paper-making machine, reduced polymer dosage applied.

56 cl, 3 tbl, 4 ex

FIELD: textile; paper.

SUBSTANCE: method consists of adding to the paper sheets approximately 0.05 pounds/ton to 15 pounds/ton, in accordance with the dry fibers, one or several polymers, functioning as aldehyde, containing amino or amido group, where, at least, 15 molar percent amino or amido group function with one or several aldehydes and where the functionaling aldehyde polymers have a molecular weight of not less than approximately 100000.

EFFECT: increased activity for drying due to a reduction in the amount of polymer.

14 cl, 5 ex

FIELD: paper.

SUBSTANCE: paper base contains fibers of coniferous and deciduous wood, or their mixtures, which have average length that is more or equal to 75 mcm and have filler fixed to part of these fibers, and also less than 50 wt % of fibers have average length less than 75 mcm from total weight of base. Paper mass is produced by contact of deciduous or coniferous wood fibers or their mixtures having average length of 75 mcm and having filler fixed to part of mentioned fibers, with fibers average length of which is less than 75 mcm, from total weight of base.

EFFECT: improved smoothness of paper.

20 cl, 25 dwg, 3 tbl, 3 ex

FIELD: textiles; paper.

SUBSTANCE: betulin is meant for being used as filler for paper or cardboard manufacturing. Betulin water suspension is obtained, and then it is added to cellulose pulp during paper or cardboard manufacturing. Water is removed from paper web. Paper or cardboard manufacturing is continued using a conventional method.

EFFECT: improving retention ability of filler, formation light, strength and lightness of paper, providing high volume and low porosity for increasing water impermeability, and preventing brightness reversion of cellulose pulp.

12 cl, 2 tbl, 3 ex, 4 dwg

FIELD: textile, paper.

SUBSTANCE: paper base is designed to form a decorative material of a coating. It represents a non-processed paper containing a white pigment and/or fillers and is coated with a covering solution, containing at least one water-soluble modified starch with special distribution of molecules according to molecular weight. Also a decorative paper or decorative material is proposed to form coatings with application of the above-specified paper-base.

EFFECT: improved quality of a finished product due to increased inner strength of fixation with high non-transparency and other mechanical properties, improved stability of paper size stability and increased average size of its pores.

7 cl, 2 tbl, 6 ex

FIELD: textile, paper.

SUBSTANCE: method of filler treatment includes formation of a mixture of an aqueous suspension of filler and aqueous anion latex. The latter is a dispersion of acrylic polymer with vitrification temperature (T v) from - 3 to 50°C. This mix is mixed with water at the temperature that is higher than T v of latex, at the same time the specified water has temperature of 40-98°C. The specified suspension of the filler comprises a solid disperse filler selected from the group containing kaolin clay, ground calcium carbonate, deposited calcium carbonate, deposited calcium sulfate, talc and mix of two or more of them. The specified acrylic polymer is selected from the group containing copolymers n-butylacrylate-acrylonitrile-sterol and copolymers n-butylacrylate-sterol. The aqueous composition of the filler contains the solid dispersed filler specified above with solid particles of anion latex polymer specified above and adsorbed on them, in aqueous carrier. The treated filler contains the solid dispersed filler specified above with solid particles of anion latex polymer specified above and adsorbed on them. The pulp charge contains pulp fibres and the solid dispersed filler specified above with solid particles of anion latex polymer specified above and adsorbed on it, in aqueous carrier. Method to make paper from the above specified pulp charge containing pulp fibres. The paper product made of pulp fibres and solid disperse filler, where the specified filler has solid particles of anion latex polymer specified above absorbed on it, with size of solid polymer particles of 30-200 nm and in amount of 1-100 kg of latex per 1 t of filler relative to dry mass of solid substances of latex and filler, and the specified filler has average size of particles of 0.1-30 mcm.

EFFECT: improved retention of the filler, continuous execution of the filler treatment method to improve fixation of anion latex on the filler for a short period of time due to irreversible fixation of anion latexes on particles of the filler and time stability of aggregated filler suspension, latex-treated deposited calcium carbonate is more acid-resistant, and when used to make paper from wood mass under neutral conditions less acid is required to control pH.

21 cl, 14 dwg, 8 ex

FIELD: textile, paper.

SUBSTANCE: method includes dissolution of cellulose and its grinding down to specified extent of grinding. Preparation of the first dispersion with application of return water, containing fibres of microcrystal cellulose, produced by its grinding in mixture with titanium dioxide and calcium hydroxide in specified amount. The second dispersion is prepared from cellulose fibres with application of return water. Then the first suspension is mixed with the second, and produced mixture is treated with carbon dioxide. In case of this treatment calcium hydroxide under action of carbon dioxide results in production of chemically deposited chalk and production of paper mass at specified ratio of components. Grinding of microcrystalline cellulose in mixture with titanium dioxide and calcium hydroxide is carried out in vibration mill with provision of impact and wear effect at mixture.

EFFECT: increased extent of fillers retention in paper, improvement of its printing properties, provision of possibility to vary bulk and porosity of paper, provision of possibility to use fully closed cycle of return water.

1 tbl, 8 ex

FIELD: textile, paper.

SUBSTANCE: method includes preparation of water dispersion of cellulose fibres. Addition of calcium hydroxide in it at specified ratio in dispersion of cellulose fibres. Further treatment of dispersion with carbon dioxide in process of mixing until calcium hydroxide is fully transformed into calcium carbonate to produce paper mass. The latter comprises cellulose fibres, modified with chemically deposited chalk. At the same time calcium hydroxide is added into dispersion in amount, in conversion to calcium carbonate, equal to its specified percentage content in dry substances of paper. Dispersion of cellulose fibres is prepared with addition of return water of paper-making machine, and dispersion is treated with carbon dioxide after addition of return water to it. Paper mass is produced with specified content of components in it without account of solid substances added in it with return water. Cellulose fibre is selected from row including sulfite, sulfate cellulose, their mixture, leached wood mass of high yield on the basis of fibrillated fibres containing cellulose, hemicellulose and lignin.

EFFECT: increased strength of paper from produced paper mass due to use of closed cycle of water circulation.

1 tbl

FIELD: chemistry.

SUBSTANCE: substrate has a paper base containing cellulose fibre from deciduous wood with particle size smaller than 200 mcm after grinding in amount of not more than 45 wt % and average fibre length between 0.4 and 0.8 mm and filler in amount of 5-40 wt %, particularly 10-25 wt % in terms of the weight of cellulose.The substrate at least contains one polymer layer lying at least on one side of the paper base. There is a layer with a binding agent between the polymer layer and the paper base. The binding agent is a hydrophilic film-forming polymer made from hydroxypropylated starch and/or thermally modified starch. This layer may contain a pigment in form of calcium carbonate, kaolin, talc, titanium dioxide and/or barium sulphate.

EFFECT: reduced limpness and obtaining pure-bred production wastes.

27 cl, 3 tbl

FIELD: paper.

SUBSTANCE: paper base contains fibers of coniferous and deciduous wood, or their mixtures, which have average length that is more or equal to 75 mcm and have filler fixed to part of these fibers, and also less than 50 wt % of fibers have average length less than 75 mcm from total weight of base. Paper mass is produced by contact of deciduous or coniferous wood fibers or their mixtures having average length of 75 mcm and having filler fixed to part of mentioned fibers, with fibers average length of which is less than 75 mcm, from total weight of base.

EFFECT: improved smoothness of paper.

20 cl, 25 dwg, 3 tbl, 3 ex

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