METHOD FOR PRODUCING PAPER OR CARDBOARD

Abstract

The invention relates to a method for producing paper or cardboard comprising the steps (A) adding a final polymer A to a first aqueous suspension of fibrous material, thereby creating a second aqueous suspension of fibrous material containing the final polymer A, wherein the final polymer A can be obtained by radical polymerization of the monomers (i) 30 to 90 mol% of a monomer of formula I (I), wherein R1 = H or signifies C1-C6 alkyl. (ii) 3 to 60 mol% of a C1-C4 alkyl ester of acrylic acid or a C1-C4 alkyl ester of methacrylic acid, (iii) 0 to 45 mol% of a monoethylenically unsaturated carboxylic acid, a monoethylenically unsaturated sulfonic acid or a monoethylenically unsaturated phosphonic acid, or salt forms thereof, (iv) 0 to 9 mol% of acrylonitrile or methacrylonitrile, (v) 0 to 35 mol% of one or more ethylenically unsaturated monomers other than a monomer (i), (ii), (iii) and (iv),wherein the total amount of all monomers (i), (ii), (iii), (iv) and (v) is 100% molar, to obtain a starting polymer V, e - hydrolyzing the starting polymer V to obtain the final polymer A, wherein the NC(=O)R1 groups of formula (I) of the monomers (i) polymerized in the starting polymer V are hydrolyzed at least in part and in doing so, form the primary amino groups, wherein the ester groups of the monomers (ii) polymerized in the starting polymer V are converted at least in part and at least part of the conversion is the formation of five-membered lactam structural units with the primary amino groups obtained or the formation of carboxylic acid groups or salt forms thereof, (B) dehydrating the second aqueous suspension of fibrous material containing the final polymer A on a water-permeable substrate to form a wet paper structure, (C) dehydrating the wet paper structure,thus forming paper or cardboard. The resulting paper or cardboard has good dry strength. Other objects of the invention are a paper or cardboard obtainable by the method, a final polymer A, and a starting polymer V.

Description

METHOD FOR PRODUCING PAPER OR CARDBOARD The invention relates to a method for producing paper or board comprising the steps of adding a final polymer A to a first aqueous suspension of fibrous material, dewatering the second aqueous suspension of fibrous material obtained containing the final polymer A on a permeable substrate to water to form a wet paper structure and dewatering the wet paper structure to form a paper or board. The paper or cardboard obtained has good dry strength. Other subjects of the invention are a paper or board obtainable by this method and a final polymer A and a starting polymer V. The starting polymer V is the synthetic precursor of the final polymer A. Current trends in the paper industry have in part a profoundly negative influence on the dry strength of a paper or board. For example, waste paper recycling rates are increasing. This is associated with a deterioration in the quality of the fiber. Shorter cellulosic fibers, reduced swelling behavior and roughness of the fiber are experienced. In principle, the use of cheap raw materials is attractive, even if in practice it is associated with shorter cellulose fibers. Reducing the grammage of a paper or cardboard to save raw material is a recurring theme. The water circuits of the paper manufacturing machines are being progressively dismantled. Therefore, methods for producing paper or board which ensure a good dry strength of the obtained paper or board are of interest. DE 4328975 A describes as the subject of the invention polymers for paper production which contain a proportion of 2-aminodihydropyrrole structural units of 20 to 90 mol%. To produce the polymers according to the examples, first, radical polymerization of N-vinylformamide and acrylonitrile is performed to provide a starting polymer. This starting polymer is accumulated at the end of the polymerizations in the form of a suspension in water. After filtration, the starting polymer is treated with concentrated hydrochloric acid and heating to approximately 100°C results in amidinization. The final polymer thus formed is precipitated with acetone and dried. For the final polymer F produced, whose starting polymer is obtained by radical polymerization of 50 mol% N-vinylformamide and 50 mol% acrylonitrile, a lactam content, specifically 1 mol%, is indicated as the sole polymer: VIA / l / U¿ 104U among other things, the final polymers are added to a suspension of fibrous material. The papers are produced using a TAPPI standard Fourdrinier machine. The ash content of paper produced using the final polymer F is determined. The paper strength of papers produced using other final polymers is also determined by measuring a break factor. The final produced polymers G, K, Q and R have no or only a small content of 2-amino-dihydropyrrole structural units and therefore do not correspond to the invention and give poorer results in practical examples. EP 0528409 A describes, as a subject of the invention, polymers consistent with those of DE 4328975 A cited above as flocculating agent. The final polymer F from DE 4328975 A can be found again in the Examples part as final polymer P. The final polymers of the examples are added to the slurry to improve the filterability. Similar to DE 4328975 A, the final polymers not according to the invention have no or only a small content of 2-amino4-dihydropyrrole structural units. DE 4441940 A describes, as a subject of the invention, polymers containing the five-membered lactams as structural units (=pyrrolidin-2-one structural units) in a proportion of 20 to 100 mole %. An increased thermostability for the final polymers therein is demonstrated in the Examples part. The final polymers are recommended for use as thermoplastic resin modifiers, polymeric additive for tertiary petroleum recovery, lubricants, detergent dispersants, scale inhibitors, quench oil polymers, drilling mud thickeners, pipeline thickeners, binders and Similar. To produce the polymers according to the examples, the radical polymerization of N-vinylformamide and acrylamide, and in one case of N-vinylformamide, acrylamide and acrylamide-2-methylpropanesulfonic acid, and in another case of N-vinylformamide and methacrylamide is carried out in first, in each case to form a starting polymer. In the case of N-vinylformamide and acrylamide, the starting polymer is precipitated with methanol and, in the other two cases, the starting polymer is filtered as a polymer gel. The starting polymers thus obtained are treated with aqueous hydrochloric acid. The mixture is precipitated and then dried by adding acetone or methanol. Water solubility is estimated and reduced viscosity determined as appropriate. For the final polymer C produced, whose starting polymer is obtained by radical polymerization of 50 mol% N-vinylformamide and 50 mol% acrylamide, the following composition is specified: For the final polymer M produced, whose starting polymer is obtained by radical polymerization of 40 mol% N-vinylformamide, 40 mol% acrylamide and 20 mol% acrylamide-2-methylpropane sulfonic acid, the following composition is specified : For the final polymer N produced, whose starting polymer is obtained by radical polymerization of N-vinylformamide and methylacrylamide, the following composition is specified: US 4898915 describes, as a subject according to the invention, polymers comprising structural units with an aromatic or aliphatic amino group and structural units with at least one nitrile, aldehyde, carboxylic acid or carboxylic acid ester substitution. In the examples, the starting polymers are obtained by polymerization of monomers with protected amino groups and acrylic acid esters in toluene, said polymerization being catalyzed by Lewis acid. The crude starting polymers are separated by decantation and addition of methanol, filtered as dissolved in chloroform and precipitated with a further addition of methanol. To obtain final polymers, the starting polymers thus obtained are treated with hydrazine in chloroform to liberate the primary amino groups. Specifically, in Example 3, methyl acrylate is polymerized with N-vinylphthalimide, catalyzed by ethylaluminum sesquichloride. This starting polymer is dissolved in Example 6 in chloroform and treated with hydrazine. Methoxy groups, amino groups and lactam units are described for the final polymer obtained. In Example 7, the final polymer obtained in Example 6 is treated with an aqueous potassium hydroxide solution at 70°C, after which the provision of a polymer having alternating amino and carboxylic acid groups is described. The final polymers are recommended for use as antistatic agents or as thickeners in oil recovery. In A novel synthetic procedure for N-vinylformamide and free radical polymerization, S. Sawayama et al., Mitsubishi Kasei R&D Review, 1993, Vol. 7, p. 55-61, the copolymerization of N-vinylformamide with acrylamide and the copolymerization of N-vinylformamide with styrene, in each case in different molar ratios, is described in chapter 3.5 and figure 4. In Alternating copolymerization of methyl acrylate with donor monomers having a protected amine Group, R. N. Majumdar et al., Journal of Polymer Science, 1983, Vol. 21, p. 1717-1727, Example 6 of the aforementioned US Pat. No. 4,898,915 is described, inter alia, and is titled as the hydrazinolysis of an alternating copolymer of methyl acrylate and N-vinyl thalimide. Figure 4 shows the 13C-NMR of a copolymer of methyl acrylate and N-vinylphthalimide and the 13CNMR of an alternating copolymer of methyl acrylate and N-vinylphthalimide. In Amine functional polymers based on Nethenylformamide, R. K. Pinschmidt et al., Progress in Organic Coatings, 1996, 27, p. 209-218, section 2.1. describes the polymerization of 32 mole % N-vinylformamide, 38 mole % butyl acrylate and 30 mole % methyl methacrylate in a solvent, eg alcohol, ketone or alcohol / toluene, with the radical initiator Vazo 52. The basic hydrolysis of (meth)acrylate / N-vinylformamide copolymers and terpolymers with potassium hydroxide in an alcohol-containing solvent is described as being rapid in section 2.2. In the case of a starting polymer obtained from the polymerization of acrylate:N-vinylformamide=1:1, a lactam-containing polymer known from the aforementioned US 4898915 is precipitated. Section 3.4 and Scheme 3 describe the hydrolysis and lactam formation of copolymers of N-vinylformamide and (meth)acrylates. A high lactam content leads to insolubility in normal solvents. In N-vinylformamide - building block for novel polymer structures, R.K. Pinschmidt et al., Puré Applied Chemistry, 1997, A34(10), p. 1885-1905, the hydrolysis of copolymers of N-vinylformamide and (meth)acrylates or acrylonitrile under acidic conditions is described as being simple and providing high yield, among other things. This is attributed to the absence of strong charge repulsion between the vinylamine units in these strongly alternating copolymers. The lactam is formed very rapidly in case of neutralization or basic hydrolysis. This is shown schematically in Figure 9, and the structure of the lactam is referred to as insoluble. GB 752290 describes, as a subject according to the invention, polymers comprising five-membered lactams as structural units (=pyrrolidin-2-one structural units). To produce the polymers according to the examples, acryloyl chloride is first subjected to radical polymerization to form a starting polymer. This starting polymer is dissolved in dimethylformamide and converted with sodium azide or hydroxylamine. After filtration and the addition of acetone, the final polymer is precipitated, dissolved in water and precipitated with the addition of hydrochloric acid. Among others, a final polymer with 70 mol% lactam structural units, 23 mol% acid groups and 7 mol% amino groups, and a final polymer with 63 mol% lactam structural units, 24.5 mol% acid groups and 12.5 mol% amino acids. The groups are described. The final polymers are recommended, among other things, as film formers and for use in photographic coatings. In Determination of the sequence distribution and ionization constant of poly(acrylic acid-co-vinylamine) by C13 NMR, C. Chang et al., Journal of Polymer Science, Polymer Symposium, 1986, 74, p. 17-30, the final polymers resulting from the Schmidt reaction of polyacrylic acid with hydrazoic acid and containing a primary amino group and carboxylic acid groups are examined by nuclear magnetic resonance. Lactam formation is described for the final polymers examined, in which 12% or 30% or 52% of the carboxylic acid groups were converted to amino groups. In Polymers and group interaction. IV. Hofmann reaction on polyvinylamides, M. Mullier et al., Journal of Polymer Science, 1957, XXIII, p. 915-930, inter alia, the Hofmann rearrangement products of polyacrylamide and polymethacrylamide are discussed. In the examples, the polyacrylamides are converted with sodium hypochlorite as starting polymers, after which polymers with amino groups are produced as final polymers. A high proportion of five-membered lactam structural units is assigned to these final polymers. Table 1 shows the following for the final polymer Polymer I, which is obtained from the Hofmann reaction of polyacrylamide with 1 equivalent of sodium hypochlorite: Table 1 shows the following for the final polymer Polymer II, which is obtained from the reaction of Hofmann's polymethacrylamide with 1 equivalent of sodium hypochlorite: JP 2016-186023 A describes, in the example 1, the radical polymerization of 43 mole % N-vinylformamide and 57 mole % methyl methacrylate in methyl ethyl ketone. Example 2 describes the radical polymerization of 24 mole % N-vinylformamide and 76 mole % methyl methacrylate in methyl ethyl ketone. The polymers obtained are of interest for optical lenses, etc. JP 2017-061602 A describes, in the example 3, the radical polymerization of 32 mole % N-vinylformamide and 68 mole % methyl methacrylate in methyl ethyl ketone. The polymer obtained is of interest for optical components. JP 2017-039867 A describes, in the example 4, the radical polymerization of 20 mole % N-vinylformamide and 80 mole % methyl methacrylate in methyl ethyl ketone. Example 5 describes the radical polymerization of 32 mole % N-vinylformamide and 68 mole % methyl methacrylate in methyl ethyl ketone. The polymers obtained are of interest for optical components. JP 2017-039868 A describes, in the example 2, the radical polymerization of 32 mole % N-vinylformamide and 68 mole % methyl methacrylate in methyl ethyl ketone. Example 3 describes the radical polymerization of 48 mole % N-vinylformamide and 52 mole % methyl methacrylate in methyl ethyl ketone. Example 4 describes the radical polymerization of 20 mole % N-vinylformamide and 80 mole % methyl methacrylate in methyl ethyl ketone. The polymers obtained are of interest for optical components. There is a need for additional methods of producing paper or board, in which the obtained paper or board has good dry strength. If additives are used in these methods, it is further advantageous that the production thereof can also be carried out on an industrial scale as easily as possible. What has been found is a method of producing paper or board containing steps (A) adding a final polymer A to a first slurry of fibrous material, whereby a second slurry of fibrous material is created containing the polymer final A, wherein the final polymer A can be obtained by - radical polymerization of the monomers (i) 30 to 90 mol% of a monomer of formula I H H \ N ' Η / ζ ___R ' H Q (I), where R1= H o means Ci-Ce alkyl. (ii) 3 to 60 mole % of a C1-C4 alkyl ester of acrylic acid or a C1-C4 alkyl ester of methacrylic acid, (iii) 0 to 45 mole % of a monoethylenically unsaturated carboxylic acid, a monoethylenically unsaturated sulfonic acid or a monoethylenically unsaturated phosphonic acid, or salt forms thereof, (iv) 0 to 9 mole % acrylonitrile or methacrylonitrile, (v) 0 to 35 mole % of one or more ethylenically unsaturated monomers that are different of a monomer (i), (ii), (iii) and (iv), wherein the total amount of all monomers (i), (ii), (iii), (iv) and (v) is 100% molar, to obtain a starting polymer V, and - hydrolyzing the starting polymer V to obtain the final polymer A, wherein the NC(=O)R1 groups of formula (I) of the monomers (i) polymerized in the starting polymer are hydrolyzed V at least in part and at In doing so, they form the primary amino groups, wherein the ester groups of the polymerized monomers (ii) in the starting polymer V are at least partly converted and at least part of the conversion is the formation of five-membered lactam structural units. with the primary amino groups obtained or the formation of carboxylic acid groups or salt forms thereof, (B) dewatering the second aqueous slurry of fibrous material containing the final polymer A on a water-permeable substrate to form a paper structure wet, (C) dehydrate the wet paper structure, whereby the paper or cardboard is formed. In step (A) by first aqueous suspension of fibrous material is meant a composition containing (aa) water and (a-b) fibrous material containing cellulose fibers. An alternative name for the suspension of fibrous material is pulp. To obtain the first aqueous suspension of fibrous material, mechanical and / or chemical methods can be used. For example, grinding an aqueous suspension of fibrous material is a mechanical process to shorten fibers and, in the case of cellulose fibers, also to defibrillate the fibers. The dehydration capacity of the aqueous fibrous suspension is determined by the fineness achieved. One method for measuring the fineness of a suspension of fibrous material is the determination of the dehydration kinetics by means of the Schopper-Riegler test in Schopper degree (°SR). Natural and / or recovered fibers can be used as the fibrous material. All wood fibers or annual plants conventionally used in the paper industry can be used. Annual plants suitable for producing fibrous materials are, for example, rice, wheat, sugar cane and Kenaf. Wood material, for example, softwood or hardwood, includes wood pulp, thermomechanical pulp (TMP), chemical-thermomechanical pulp (CTMP), pressure-ground woodpulp, semi-chemical pulp, high-yield pulp, and mechanical pulp. refiner (RMP), for example. Rough ground wood material generally has a fineness of 40-60° SR relative to normal ground wood material 60-75° SR and fine ground wood material with 70-80° SR. Pulps, eg, from softwoods or hardwoods, include chemically digested sulphate, sulphite or soda pulp. The pulp may also be bleached or unbleached. Unbleached pulp, also referred to as unbleached kraft pulp, is preferred. Uncrushed pulp generally has 13-17° SR relative to low or medium crush pulp with 20-40° SR and high crush pulp with 50-60° SR. The recovered fibers can come, for example, from waste paper. Optionally, the waste paper can also undergo a de-inking process beforehand. Mixed waste paper can generally have about 40° SR relative to waste paper from a deinking process with about 60° SR. The fibers recovered from waste paper can be used alone or mixed with other fibers, in particular natural ones. A method is preferred in which the first aqueous suspension of fibrous material has a dehydration kinetics according to the Schopper-Riegler test between 13 and 70° SR, most preferably between 20 and 60° SR, and particularly preferably between 30 and 50° SR is preferred. The first slurry of fibrous material can be obtained, for example, by recycling existing paper or board, eg by mechanically treating the waste paper in a pulper together with water until the slurry of fibrous material has the desired consistency. Another example of the combination of two fiber sources is the mixing of a primary fibrous slurry with the returned waste of a coated paper that is produced with the use of the primary fibrous slurry. The first aqueous suspension of fibrous material may contain not only water (a-a) and fibrous material (a-b), but also other components, which are deliberately added to the suspension of fibrous material as appropriate or provided by using waste paper or paper. existing as applicable. By dry content, here is meant the ratio between the mass of a sample after drying and the mass of the sample before drying, expressed in percentage values ​​by weight. The dry content is preferably determined by drying at 105°C to constant mass. For this, drying is achieved at 105°C (± 2°C) in a constant mass drying cabinet. Constant mass is achieved here when, with dry contents from 1 to 100%, the first rounded decimal of the percentage value no longer changes and, with dry contents from 0 to less than 1%, the second rounded decimal of the percentage value no longer changes. . Drying is carried out at ambient pressure, optionally 101.32 KPa, without correcting any deviation derived from the weather and sea level. In the Examples part, information for practical implementation can be found under the determination of the dry content. Reference is made in this document to a thick material with a dry content of more than 1.5 to 6% by weight in relation to the first aqueous suspension of fibrous material (corresponds approximately to a concentration of fibrous material of more than 15 to 60 g / L if almost exclusively fibrous material is present), preferably from 2.0 to 4.0% by weight. As a distinction here, a dry content of 0.1 to 1.5% by weight based on the aqueous fibrous material suspension (corresponds to a fibrous material concentration of 1 to 15 g / L if almost exclusively fibrous material is present), in particular 0.3 to 1.4% by weight, is called usually fine material. The dry content or dry weight of an aqueous suspension of fibrous material comprises all constituents which are non-volatile or preferably non-volatile during the determination of the dry content by drying at 105°C to constant mass. The dry content of the first aqueous suspension of fibrous material is preferably between 0.1 and 6% by weight, very preferably between 0.12 and 5% by weight, particularly preferably between 0.15 and 4% by weight, very particularly preferably between more than 1.5 and 4.0% by weight, and particularly preferably between 2.0 and 4.0% by weight. A method is preferred in which in step (A) the first aqueous suspension of fibrous material has a dry content between 0.1 and 6% by weight. The final polymer A in step (A) is added to a first suspension of fibrous material, whose dry content is greater than 1.5 and up to 6.0% by weight. The second slurry of fibrous material formed containing the final polymer A is then most preferably diluted to a dry content of 0.1 to 1.5% by weight. The final polymer A in step (A) is preferably added to a first suspension of fibrous material, the dry content of which is between 0.1 and up to 1.5% by weight. A method is preferred in which in step (A) the final polymer A is added to the first aqueous suspension of fibrous material, which has a dry content of more than 1.5 to 6% by weight at the time of addition. After the addition of the final polymer A to the first aqueous suspension of fibrous material, a period of time is allowed to elapse preferably from 0.5 seconds to 2 hours, most preferably from 1.0 seconds to 15 minutes, and particularly preferably from 2 to 20 seconds with dehydration in step (B). In this way a reaction time of the final polymer A is ensured. The amount of final polymer A added is preferably from 0.01 to 3.0% by weight relative to the dry content of the first aqueous suspension of fibrous material. The final polymer amount A is calculated here as polymer content. The polymer content specifies the final polymer content A without counterions in the aqueous solution in % by weight, ie counterions are not taken into account. The polymer content is therefore the sum of the proportions by weight of all structural units of the final polymer A in g that are contained in 100 g of an aqueous dispersion or solution of the final polymer A. In the Examples part, information for practical implementation can be found under polymer content. A quantity of 0.02 to 1.0% by weight is most preferred, particularly preferably 0.06 to 0.8% by weight, very particularly preferably 0.09 to 0.6% by weight, particularly preferably 0.12 to 0.5% by weight, very especially preferably from 0.15 to 0.5% by weight, and expressly preferably from 0.2 to 0.4% by weight. A method in which in step (A) the final polymer is added in an amount of 0.2 to 0.5% by weight to the first fibrous material slurry, wherein the dry content of the first fibrous material slurry is greater than 1.5 and up to 6.0% by weight, is preferred. The second suspension of fibrous material formed containing the final polymer A is most preferably subsequently diluted to a dry content between 0.1 and up to 1.5% by weight. The synthetic precursor of the final polymer A is the starting polymer V, which can be obtained by radical polymerization of monomers (i), (ii), optionally (iii), optionally (iv) and optionally (v). Solution, precipitation, inverse suspension or emulsion polymerization is available for polymerization of monomers (i), (ii), optionally (iii), optionally (iv) and optionally (v) to form the starting polymer V. Solution polymerization in an aqueous medium is preferred. Suitable aqueous media are water and mixtures of water and at least one water-miscible solvent, for example, IVIA / l / U¿ 104U an alcohol. Examples of alcohol are methanol, ethanol, n-propanol, ethylene glycol or propylene glycol. The polymerization is carried out radically, for example by using radical polymerization initiators, eg peroxides, hydroperoxides, which are known as redox catalysts, or by using radically decomposing azo compounds. Examples of peroxides are alkaline or ammonium peroxydisulfates, diacetyl peroxide, dibenzoyl peroxide, succinyl peroxide, di-tert-butyl peroxide, tert-butyl perbenzoate, tert-butyl perpivalate, tert-butyl peroxy2-ethylhexanoate, tert-Butyl permaleinate, eumene hydroperoxide, diisopropyl peroxydicarbamate, bis-(o-toluoyl) peroxide, didecanoyl peroxide, dioctanoyl peroxide, dilauroyl peroxide, tert-butyl perisobutyrate, tert-butyl peracetate or peroxide di-tert-amyl. An example of a hydroperoxide is tert-butyl hydroperoxide. Examples of azo compounds that decompose radically are azo-bis-isobutyronitrile, 2,2'-azobis(2-methylpropionamidine) dihydrochloride or 2-2'azo-bis-(2-methyl-butyronitrile). Examples of what are known as redox catalysts are ascorbic acid / iron(II) sulfate / sodium peroxodisulfate, tert-butylhydroperoxide / sodium disulfite, tert-butylhydroperoxide / sodium hydroxymethane sulfinate or H2O2 / CU1. The polymerization is carried out, for example, in water or a mixture containing water as a solvent in a temperature range from 30 to 150°C, preferably from 40 to 110°C, where the process can be carried out at ambient pressure, reduced pressure or increased pressure. For solution polymerization, a water-soluble polymerization initiator is selected, for example, 2,2'-azo-bis(2-methylpropionamidine) dihydrochloride. The free-radical polymerization of the monomers is preferably carried out in water or in a water-containing solvent mixture. Water or a water-containing solvent mixture containing at least 50% by weight of water relative to the total amount of solvent mixture is preferred. Particular preference is given to water or a water-containing solvent mixture which contains at least 80% by weight of water, particularly preferably at least 90% by weight and very particularly preferably at least 95% by weight of water. The polymerization is preferably carried out in water or in a water-containing solvent mixture whose pH value is greater than pH=6, very preferably between pH 6.1 and pH 9, and particularly preferably between pH 6.2 and pH 6.8. It is possible to adjust a corresponding pH, for example by adding an acid and / or base, possibly with pH regulator function. A method in which the radical polymerization of the monomers is carried out in water or in a water-containing solvent mixture is preferred. During the polymerization of monomers (i), (ii), optionally (iii), optionally (iv) and optionally (v) to form the starting polymer V, polymerization regulators can be added to the reaction. It is typical that from 0.001 to 5 mole % is used, based on the total amount of all monomers (i), (ii), (iii), (iv) and (v). Polymerization regulators are known in the literature, for example sulfuric compounds, sodium hypophosphite, formic acid or tribromochloromethane. Individual examples of sulfuric compounds are mercaptoethanol, 2-ethylhexylthioglycolate, thioglycolic acid and dodecyl mercaptan. The starting polymer V preferably has a weight average molecular weight Mw between 75,000 and 5,000,000 Daltons. The departure V polymer has very preferably an average molecular weight by weight MW between 100,000 and 4,500,000 Dalton, especially preferably between 180,000 and 2,500,000 Dalton, especially preferably between 210,000 and 1,500,000 Dalton, and especially preferably between 250,000 and 1,000,000 Dalton. The weight average molecular weight can be determined by static light scattering, eg at a pH value of 7.0 in NaNO3 solution. Examples of monomers (i) of the formula I are N-vinylformamide (R1=H), N-vinylacetamide (R1=Ci alkyl), N-vinylpropionamide (R1=C2 alkyl) and N-vinylbutyramide (R1=C3 alkyl). . C3-Ce alkyls can be linear or branched. An example of Ci-Ce alkyl is methyl, ethyl, n-propyl, 1-methylethyl, n-butyl, 2-methylpropyl, 3methylpropyl, 1.1-dimethylethyl, n-pentyl, 2-methylbutyl, 3methylbutyl, 2,2-dimethylpropyl or n-hexyl. R1 is preferably H or C1-C4 alkyl, most preferably H or C1-C2 alkyl, more preferably H or Ci alkyl and very particularly preferably H, ie monomer (i) is N-vinylformamide. A monomer of formula I in the singular also includes a mixture of different monomers of formula I as monomer (i). Preferably, the numerical proportion of the monomer with R1=H in the total number of all monomers (i) of formula I is 85 to 100%, most preferably 90 to 100%, especially preferably 95 to 100%, and very particularly preferably 99 to 100%. A method in which the monomer (i) is N-vinylformamide, d.h. R1=H in formula I is preferred. The total amount of all monomers (i) is preferably from 50 to 89 mol% with respect to all monomers polymerized to obtain starting polymer V, that is, all monomers (i), (ii), optionally (iii). ), optionally (iv)) and optionally (v), very preferably from 58 to 83 mol%, particularly preferably from 60 to 83 mol%, and most particularly preferably from 65 to 80 mol%. The condition is maintained that the sum of all monomers (i), (ii), (iii), (iv) and (v) gives 100 molar %. Examples of monomers (ii) are methyl acrylate, ethyl acrylate, n-propyl acrylate, ipropyl acrylate, n-butyl acrylate, sec-butyl acrylate, tert-butyl acrylate, methyl methacrylate, ethyl methacrylate , n-propyl methacrylate, i-propyl methacrylate, n-butyl methacrylate, sec-butyl methacrylate and tert-butyl methacrylate. Here, a singular monomer (ii) also includes a mixture of different monomers (ii) as monomer (ii). C1-C4 alkyl esters of acrylic acid and Ci alkyl esters of methacrylic acid are preferred, C1-C3 alkyl esters of acrylic acid and Ci alkyl esters of methacrylic acid are highly preferred, C1-C3 alkyl esters of acrylic acid are particularly preferred, C2-C2 alkyl esters of acrylic acid are very particularly preferred and C2 alkyl esters of acrylic acid (=ethyl acrylate) are particularly preferred. Preferably, the numerical proportion of the C2 alkyl ester of acrylic acid in the total number of all monomers (II) is from 30 to 100%, most preferably from 50 to 100%, most preferably from 80 to 100%, and very preferably from particularly preferable 95 to 100%. In the case of a C1-C4 alkyl ester of methacrylic acid preferably also a C1-C4 alkyl ester of acrylic acid is present, most preferably at least numerically a C1-C4 alkyl ester of methacrylic acid to numerically a C1-C4 alkyl ester of methacrylic acid. A method in which the monomer (ii) is a C1-C3 alkyl ester of acullic acid or Ci alkyl ester of methacrylic acid is preferred. A method in which the monomer (ii) is a C1-C2 alkyl ester of acrylic acid is preferred. A method in which the monomer (ii) is ethyl acrylate is preferred. The total amount of all monomers (ii) is preferably from 5 to 45 mol% relative to all monomers polymerized to obtain starting polymer V, that is, all monomers (i), (ii), optionally (iii). ), optionally (iv)) and optionally (v), very preferably from 8 to 39 mol%, particularly preferably from 8 to 30 mol%, very particularly preferably from 8 to 25 mol%, and particularly preferably from 8 to 21 % cool. The condition is maintained that the sum of all monomers (i), (ii), (iii), (iv) and (v) gives 100 molar %. As used herein, an ethylenically unsaturated monomer is a monomer that contains at least one C2 unit of which the two carbon atoms are connected by a carbon-carbon double bond. This is ethylene in the case of hydrogen atoms as single substituents. A vinyl derivative is present in the case of substitution with 3 hydrogen atoms. In the case of substitution with two hydrogen atoms, an E / Z isomer or an etheno1,1-diyl derivative is present. Here, monoethylenically unsaturated monomer means that precisely one C2 unit is provided in the monomer. In the case of a cationically charged group of a specific molecule or class of molecules, the salt form means that a corresponding anion ensures charge neutrality. Said anions are, for example, chloride, bromide, acid sulfate, sulfate, acid phosphate, methyl sulfate, acetate or formate. Acid chloride, formate or sulfate is preferred; chloride or formate is particularly preferred. In the case of an anionically charged group of a specified compound or class of compounds, the salt form means that a corresponding cation ensures charge neutrality. Such cations are, for example, alkali metal, alkaline earth metal, ammonia, alkylamine or alkanolamine cations. Li+, Na+, K+, Rb+, Cs+, Mg2+, Ca2~, Sr2+, Ba2+ or NH4+ are preferred. Highly preferred are Li+, Na+, K+, Mg2+, Ca2+ or NH4+, particularly preferred are Na+, K+, Ca2+ or NH4+, very particularly preferred are Na+, K+ or NH4+, particularly preferred are Na+ or K+ and very particularly preferred is Na+. Monomer (iii) also comprises a mixture of individual monomers that fall under monomer (iii). Examples of a monomer (iii) which is a monoethylenically unsaturated carboxylic acid form or salt thereof are C3 to Cs monoethylenically unsaturated mono- or dicarboxylic acids or salt forms thereof. Examples are acrylic acid, sodium acrylate, methacrylic acid, sodium methacrylate, dimethacrylic acid, ethacrylic acid, maleic acid, fumaric acid, itaconic acid, mesaconic acid, citraconic acid, methylenemalonic acid, allylacetic acid, vinyl acetic acid or crotonic acid. Examples of a monomer (iii) which is a monoethylenically unsaturated sulfonic acid or a salt form thereof are vinylsulfonic acid, acrylamido-2-methylpropanesulfonic acid, methacrylamido-2-methylpropanesulfonic acid, allylsulfonic acid, methallylsulfonic acid, sulfoethylacrylate, sulfoethylmethacrylate , sulfopropyl acrylate, sulfopropyl methacrylate, 2-hydroxy-3-methacryloxypropyl sulfonic acid or styrenesulfonic acid. Examples of a monomer (iii) which is a monoethylenically unsaturated phosphonic acid or a salt form thereof are vinylphosphonic acid monomethyl ester, allylphosphonic acid, allylphosphonic acid monomethyl ester, acrylamidomethylpropylphosphonic acid or acrylamidomethylenephosphonic acid. The monomer (iii) is preferably a monoethylenically unsaturated carboxylic acid or a monoethylenically unsaturated sulfonic acid, or salt forms thereof. The monomer (iii) is preferably a monoethylenically unsaturated C3 to Cs mono- or dicarboxylic acid, a monoethylenically unsaturated sulfonic acid or vinyl phosphonic acid or salt forms thereof. The monomer (iii) is most preferably a C3 to Cs monoethylenically unsaturated mono- or dicarboxylic acid, vinylsulfonic acid, acrylamido-2-methyl-propanesulfonic acid, methacrylamido-2-methyl-propanesulfonic acid or vinylphosphonic acid, or salt forms thereof. A C3a Cs monoethylenically unsaturated mono- or dicarboxylic acid or salt forms thereof. Acrylic acid, methacrylic acid, vinylsulfonic acid or acrylamido-2-methylpropanesulfonic acid or salt forms thereof are particularly preferred. Acrylic acid or methacrylic acid or salt forms thereof are especially preferred. Acrylic acid, sodium acrylate, methacrylic acid or sodium methacrylate are very particularly preferred. Preferably, the numerical proportion of acrylic acid and methacrylic acid or salt forms thereof in the total number of all monomers (iii) is from 30 to 100%, most preferably from 50 to 100%, particularly preferably from 80 to 100%, and very especially preferably from 95 to 100%. A method in which the monomer (iii) is a monoethylenically unsaturated carboxylic acid or a monoethylenically unsaturated sulfonic acid or salt forms thereof is preferred. A method in which the monomer (iii) is acrylic acid, methacrylic acid, vinylsulfonic acid or 2-acrylamido-2-methylpropanesulfonic acid or salt forms thereof is preferred. The total amount of all monomers (iii) is preferably from 0 to 40 mol% relative to all monomers polymerized to obtain starting polymer V, that is, all monomers (i), (ii), optionally (iii). ), optionally (iv)) and optionally (v), very preferably 0 to 30 mol%, particularly preferably 0 to 25 mol%, especially preferably 1 to 25 mol%, very especially preferably 2 to 23 mol%, expressly preferably 3 to 21 mol% and very specifically preferably from 5 to 18 mol%. The condition is maintained that the sum of all monomers (i), (ii), (iii), (iv) and (v) gives 100 mole %. Surprisingly it has been found that certain starting polymers V have an advantage for industrial production over alkaline hydrolysis to form the final polymer A. If a starting polymer V contains a monomer (iii), in the case of alkaline hydrolysis to form the final polymer A, therefore, a viscosity peak that occurs during alkaline hydrolysis is avoided or at least mitigated. The occurrence, mitigation or avoidance of the viscosity peak is described in Figure 1 and in Table A4-1 of the Examples part. The observation of a reduced or even inverted vortex in the stirrer axis during the hydrolysis tests in the Examples part serves as an indicator of the appearance of a viscosity peak and its quantitative graduation. The graduations constituted by none, minimal, low and moderate in the Examples part of this document are considered an intermediate viscosity increase that is still acceptable and manageable in the case of industrial production (scale-up). Graduations consisting of none, minimal, and low are preferred, while none and minimal are highly preferred. Accordingly, a starting polymer V having a content of monomer (iii) is preferred for use in a method. A method in which the monomer (iii) is used in an amount of 1 to 25 mol% is preferred. The total amount of all monomers (iv) is preferably from 0 to 7 mol% relative to all monomers polymerized to obtain starting polymer V, that is, all monomers (i), (ii), optionally (iii). ), optionally (iv)) and optionally (v), very preferably 0 to 5 mol%, particularly preferably 0 to 3 mol%, very particularly preferably 0.5 to 2 mol%, and particularly preferably 1 to 1.5% mole. The condition is maintained that the sum of all monomers (i), (ii), (iii), (iv) and (v) gives 100 molar %. Monomer (v) also comprises a mixture of individual monomers that fall under monomer (v). Examples of monomers (v) are (v-1) a monoethylenically unsaturated monomer, which bears no charge at pH = 7, (v-2) a diethylenically unsaturated monomer, which bears no charge at pH = 7 and whose two ethylenically double bonds are conjugated, (v-3) a monoethylenically unsaturated monomer, which carries at least one primary, secondary or tertiary amino group and which at pH = 7 carries a positive charge, or a salt form thereof, (v-4) a amine twice substituted with allyl, the nitrogen atom of which is not quaternized, (v-5) a monoethylenically unsaturated monomer, bearing at least one permanent positive charge, (v-6) a monomer comprising at least two ethylenically unsaturated double bonds , which are not conjugated, and which is different from a double allyl-substituted amine. In the case of the charge-bearing monomers (v), the salt form thereof is also understood and included accordingly. A permanent positive charge is always present as a positive charge regardless of the pH value. VIA / t / ZUZ l / UZ 104U Examples of a monomer (v-1) are α,β-ethylenically unsaturated monocarboxylic acid monoesters with C5-C18 alkanols, α,β-ethylenically unsaturated monocarboxylic acid monoesters with C2-C18alkanediols, α,β-dicarboxylic acid diesters ethylenically unsaturated with Ci-Cis alkanols or C2-C18alkanediols, primary amides of α,β-ethylenically unsaturated monocarboxylic acids, N-alkylamides of α,β-ethylenically unsaturated monocarboxylic acids, N,N-dialkylamides of α,β-ethylenically unsaturated monocarboxylic acids α,β-ethylenically unsaturated dicarboxylic acid dinitriles, vinyl alcohol esters with Ci-Cis monocarboxylic acids, allyl alcohol esters with CiC30 monocarboxylic acids, N-vinyl lactams, nitrogen-free heterocycles with one a-double bond, β-ethylenically unsaturated, vinyl aromatics, vinyl halides, vinylidene halides or C2-C8 monoolefins. Monoesters of α,β-ethylenically unsaturated monocarboxylic acids with C5-C18 alkanols are, for example, n-hexyl acrylate, n-hexyl methacrylate, n-octyl acrylate, n-octyl methacrylate, 1,1-acrylate, 3,3-tetramethylbutyl, 1.1.3,3-tetramethylbutyl methacrylate or 2-ethylhexyl acrylate. Monoesters of α,β-ethylenically unsaturated monocarboxylic acids with C2-C18alkanediols are, for example, 2-hydroxyethyl acrylate, 2-hydroxyethyl methacrylate, 2-hydroxyethyl etacrylate, 2-hydroxypropyl acrylate, 2-hydroxypropyl methacrylate, 3-hydroxypropyl acrylate. hydroxypropyl, 3-hydroxypropyl methacrylate, 3-hydroxybutyl acrylate, 3-hydroxybutyl methacrylate, 4-hydroxybutyl acrylate, 4-hydroxybutyl methacrylate, 6-hydroxyhexyl acrylate or 6-hydroxyhexyl methacrylate. Primary amides of α,β-ethylenically unsaturated monocarboxylic acids are, for example, acrylic amide or methacrylic amide. N-alkyl-amides of α,β-ethylenically unsaturated monocarboxylic acids are, for example, N-methyl acrylamide, N-methyl methacrylamide, N-isopropyl acrylamide, Nisopropyl methacrylamide, N-ethyl acrylamide, N-ethyl methacrylamide, N-(n- propyl)acrylamide, N-(npropyl)methacrylamide, N-(n-butyl)acrylamide, N-(nbutyl)methacrylamide, N-(tert-butyl)acrylamide, N-(tertbutyl)methacrylamide, N-(n-octyl) acrylamide, N-(noctyl)methacrylamide, N-(1,1,3,3-tetramethylbutyl)acrylamide, N-(1,1,3,3-tetramethylbutyl)methacrylamide, N-(2ethylhexyl)acrylamide or N-(2 -ethylhexyl)methacrylamide. N,N-dialkylamides of α,β-ethylenically unsaturated monocarboxylic acids are, for example, N,N-dimethyl acrylamide or Ν,Ν-dimethyl methacrylamide. Esters of vinyl alcohol with C1-C30 monocarboxylic acids are, for example, vinyl formate, vinyl acetate or vinyl propionate. N-vinyl-lactams are, for example, N-vinylpyrrolidone, N-vinylpiperidone, N-vinylcaprolactam, N-vinyl-5-methyl-2-pyrrolidone, N-vinyl-5-ethyl-2-pyrrolidone, N-vinyl-6-methyl-2 -piperidone, N-vinyl-6-ethyl-2-piperidone, N-vinyl-7-methyl-2-caprolactam or N-vinyl-7-ethyl-2-caprolactam. Vinyl aromatics are, for example, styrene or methylstyrene. Vinyl halides are, for example, vinyl chloride or vinyl fluoride. Vinylidene halides are, for example, vinylidene chloride or vinylidene fluoride. C2-C8 monoolefins are, for example, ethylene, propylene, isobutylene, 1-butene, 1-hexene or 1-octene. A preferred monomer (v-1) is 2-hydroxyethyl acrylate, 2-hydroxyethyl methacrylate, 2-hydroxyethyl etacrylate, 2-hydroxypropyl acrylate, 2-hydroxypropyl methacrylate, vinylpyrrolidone or vinyl acetate. Examples of a monomer (v-2) are C4-C10 defines with precisely two double bonds that are conjugated, for example, butadiene or isoprene. Examples of a monomer (v-3) are esters of α,β-ethylenically unsaturated monocarboxylic acids with amino alcohols, mono- and diesters of α,β-ethylenically unsaturated dicarboxylic acids with amino alcohols, amides of α,β-ethylenically unsaturated monocarboxylic acids with dialkylated diamines, N-vinyl imidazole or vinylpyridine. In esters of α,β-ethylenically unsaturated monocarboxylic acids with amino alcohols, the acid component is preferably acrylic acid or methacrylic acid. The amino alcohols, preferably C2-C12 aminoalcohols, can be Ci-Cg-mono- or Ci-Cg-dialkylated at the amine nitrogen. Examples are dialkylaminoethyl acrylates, dialkylaminoethyl methacrylates, dialkylaminopropyl acrylates or dialkylaminopropyl methacrylates. Individual examples are N-methylamino ethyl acrylate, N-methylamino ethyl methacrylate, N,N-dimethylamino ethyl acrylate, N,N-dimethylamino ethyl methacrylate, N,N-diethylamino ethyl acrylate, N,N-diethylamino ethyl methacrylate, of N,N-dimethylaminopropyl, N,N-dimethylaminopropyl methacrylate, N,N-diethylaminopropyl acrylate, N,N-diethylaminopropyl methacrylate, N,N-dimethylamino cyclohexyl acrylate or N,N-dimethylamino cyclohexyl methacrylate. In mono- and diesters of α,β-ethylenically unsaturated dicarboxylic acids with amino alcohols, the acid component is preferably fumaric acid, maleic acid, monobutyl maleate, itaconic acid or crotonic acid. The amino alcohols, preferably C2-C12 aminoalcohols, can be Ci-Cs-mono- or Ci-Cs-dialkylated at the amine nitrogen. Amides of α,β-ethylenically unsaturated monocarboxylic acids with dialkylated diamines are, for example, dialkylaminoethylacrylamides, dialkylaminoethylmethacrylamides, dialkylaminopropylacrylamides or dialkylaminopropylacrylamides. Individual examples are N[2-(dimethylamino)ethyl]acrylamide, N-[2-(dimethylamino)ethyl]methacrylamide, N-[3-(dimethylamino)propyl]acrylamide, N-[3(dimethylamino)propyl]methacrylamide, N -[4-(dimethylamino)butyl]acrylamide, N-[4-(dimethylamino)butyl]methacrylamide, N[2-(diethylamino)-ethyl]acrylamide or N-[2-(diethylamino)ethyl]methacrylamide. Examples of a monomer (v-4) are diallylamine or methyl diallylamine. Examples of a monomer (v-5) are diallylamines which are quaternized on the nitrogen atom, a salt form of an N-alkyl-N'-vinylimidazolium, a salt form of an N-alkylated vinylpyridinium, a salt form of an alkyl trialkyl ammonium acrylamido or a salt form of an alkyl trialkyl ammonium methacrylamido. A diallylamine quaternized on the nitrogen atom is, for example, diallyldimethylammonium chloride, diallyldiethylammonium chloride, diallyldipropylammonium chloride or diallyldibutylammonium chloride. A salt form of an N-alkyl-N'-vinylimidazolium is, for example, 1-methyl-3-vinyl-imidazol-1-ium chloride, 1-methyl-3-vinyl-imidazol-1-ium methyl sulfate or l-ethyl-3-vinylimidazol-l-ium chloride. A salt form of an N-alkylated vinylpyridinium is, for example, 1-methyl-4-vinyl-pyridin-1-ium chloride, 1-methyl-3-vinyl-pyridin-1-ium chloride, 1-methyl-2-vinyl chloride -pyridin-1-ium or l-ethyl-4-vinylpyridin-1-ium chloride. A salt form of an acrylamido alkyl trialkyl ammonium is, for example, acrylamido ethyl trimethyl ammonium chloride (trimethyl-[2-(prop-2-enoylamino)ethyl]ammonium chloride), acrylamido ethyl diethyl methyl ammonium chloride (diethyl- methyl-[3-(prop-2-enoylamino)ethyl]ammonium), acrylamido propyl trimethyl ammonium chloride (trimethyl-[3-(prop-2-enoylamino)propyl] ammonium chloride) or acrylamido propyl diethyl methyl ammonium chloride ( diethyl-methyl-3-(prop-2-enoylamino)propyl]ammonium chloride). A salt form of a methacrylamido alkyl trialkyl ammonium is, for example, methacrylamido ethyl trimethyl ammonium chloride (trimethyl-[2-(2-methylprop-2-enoylamino)ethyl]ammonium chloride), methacrylamido ethyl diethyl methyl ammonium chloride ( diethyl-methyl-[3-(2-methylprop-2-enoylamino)ethyl]ammonium chloride), methacrylamido propyl trimethylammonium chloride (trimethyl-[3-(2-methylprop-2-enoylamino)propyl]ammonium chloride) or methacrylamido propyl diethyl methylammonium chloride (diethyl-methyl-[3-(2-methylprop-2-enoylamino)propyl]ammonium chloride). An example of a monomer (v-6) is tetraallyl ammonium chloride, triallyl amine, methylene bisacrylamide, ΙνΙΛ / t / ZUZ I / UZ 104U glycol diacrylate, glycol dimethacrylate, glycerol triacrylate, pentaerythritol triallyl ether, N,N-divinylethylene urea, polyalkylene glycols or polyols esterified at least twice with acrylic acid and / or methacrylic acid, such as pentaerythritol, sorbitol and glucose. A monomer (v) which is not an ester of acrylic acid or methacrylic acid is preferred. Highly preferred is a monomer (v) which is not an ester of an ethylenically unsaturated carboxylic acid. The numerical ratio of the monomers (v-1) is preferably 50 to 100% of the total number of all the monomers (v). Particularly preferred are 80 to 100%; 95 to 100% are very particularly preferred. The following monomers (v-1) are especially preferred for the aforementioned proportions in the total number of all monomers (v): 2-hydroxyethyl acrylate, 2-hydroxyethyl methacrylate, 2-hydroxyethyl etacrylate, 2-hydroxypropyl acrylate, 2-hydroxypropyl, vinylpyrrolidone or vinyl acetate. The numerical proportion of the monomers (v-3, (v-4) and (v-5) is preferably 50 to 100% of the total number of all monomers (v). 80 to 100% are particularly preferred; of 95 to 100% are very particularly preferred. The numerical proportion of the monomers (v-3, (v-4) and (v-5) is preferably 50 to 100% of the total number of all monomers (v). 80 to 100% are particularly preferred; of 95 to 100% are very particularly preferred. The total amount of all the monomers (v) is preferably from 0 to 25 mol% with respect to all the monomers polymerized to obtain the starting polymer V, that is, all the monomers (i), (ii), optionally (iii). ), optionally (iv)) and optionally (v), very preferably 0 to 24 mol%, particularly preferably 0 to 19 mol%, especially preferably 0.01 to 15 mol%, very especially preferably 0.1 to 8 mol%, expressly preferably 0.2 to 4 mol% and very specifically preferably from 0.4 to 2 mol%. The condition is maintained that the sum of all monomers (i), (ii), (iii), (iv) and (v) gives 100 mole %. In the case of acrylamide as representative of a monomer (v-1), the amount of acrylamide is preferably 0 to 6 mol%, wherein the specified mol percent refers to the total number of all monomers (i), (ii) ), (iii), (iv) and (v) and the total number of all monomers is 100 mole %. The amount of acrylamide is very preferably 0 to 5 mol%, particularly preferably 0 to 3 mol%, very particularly preferably 0 to 2 mol%, especially preferably 0 to 1 mol%, and expressly preferably there is no acrylamide . A method in which the monomers (v) comprise an amount of 0 to 6 mole % acrylamide, the mole percent referring to the total number of all monomers (i), (ii), (iii), (iv) and (v) ), and the total number of all monomers is 100 mole %. A monomer (v-6) acts as a crosslinker. If a crosslinker is used, the amount used is preferably 0.001 to 1 mol%, based on the total number of all monomers (i), (ii), (iii), (iv) and (v) and the number total of all monomers is 100 mol%, most preferably 0.01 to 0.5 mol%, and especially preferably 0.015 to 0.1 mol%. Preferably, no monomer (v-6) is used for the radical polymerization. The starting polymer V is preferably in the form of an aqueous dispersion or solution. The water content of the aqueous solution or dispersion is most preferably 75 to 95% by weight and the content of starting polymer V is 5 to 25% by weight, wherein the content of starting polymer V is determined as content of solids. The determination of the solids content is described in the experimental part. The aqueous dispersion preferably has a pH value greater than 6. Most preferably between pH 6.1 and pH 9, and especially preferably between pH 6.2 and pH 6.8. It is possible to adjust a corresponding pH, for example by adding an acid and / or base, possibly with pH regulator function. A method in which the monomers (i) 50 to 89 mol% of a monomer of formula I (ii) 5 to 45 mol% of a C1-C4 alkyl ester of acrylic acid or a C1 alkyl ester -C4 methacrylic acid, (iii) 0 to 30 mole % of a monoethylenically unsaturated carboxylic acid, a monoethylenically unsaturated sulfonic acid or a monoethylenically unsaturated phosphonic acid, or salt forms thereof, (iv) 0 to 9 mole % of acrylonitrile or methacrylonitrile, (v) 0 to 25 mole % of one or more ethylenically unsaturated monomers that are different from a monomer (i), (ii), (iii) and (iv), are used for radical polymerization. A method in which the monomers (i) 58 to 83 mol% of a monomer of formula I (ii) 8 to 39 mol% of a C1-C4 alkyl ester of acrylic acid or a C1 alkyl ester -C4 methacrylic acid, (iii) 0 to 25 mole % of a monoethylenically unsaturated carboxylic acid, a monoethylenically unsaturated sulfonic acid or a monoethylenically unsaturated phosphonic acid, or salt forms thereof, (iv) 0 to 9 mole % of acrylonitrile or methacrylonitrile, (ν) 0 to 25 mol% of one or more ethylenically unsaturated monomers that are different from a monomer (i), (ii), (iii) and (iv), are used for radical polymerization. A method in which the monomers (i) 60 to 83 mol% N-vinylformamide, (ii) 8 to 25 mol% ethyl acrylate, (iii) 3 to 21 mol% acrylic acid or methacrylic acid or forms of salt thereof, (iv) 0 to 9 mol% of acrylonitrile or methacrylonitrile, (v) 0 to 24 mol% of one or more ethylenically unsaturated monomers that are different from a monomer (i), (ii), (iii) and (iv), are used for radical polymerization. A method in which the monomers (i) 60 to 83 mol% N-vinylformamide, (ii) 8 to 21 mol% ethyl acrylate, (iii) 3 to 21 mol% acrylic acid or methacrylic acid or forms of salt thereof, (iv) 0 to 9 mol% of acrylonitrile or methacrylonitrile, (v) 0 to 24 mol% of one or more ethylenically unsaturated monomers that are different from a monomer (i), (ii), (iii) and (iv), are used for radical polymerization. The final polymer A is obtained by partial or complete hydrolysis of the starting polymer V. As is known, for example, in the document EP 0438744 Al, page 8 / lines 26 to 34, the amide group of the monomer units (i) is polymerized in the starting polymer, that is, the NC(=O)R1 group in formula (I), can be hydrolyzed at least in part to form primary amino groups. . On cleavage of a carboxylic acid, eg formic acid or formate in the case of R1=H, a primary amino group is created. If not all amide groups are hydrolyzed, it is known, by condensation of the primary amino group with an adjacent amide group, to form a six-membered cyclic amidine in the final polymer A, possibly according to the following reaction scheme. nfrQLzn / Lznz / q / Yi In the case of polymerization of cyanogen-substituted ethylene derivatives directly on the ethylene function, for example a monomer (iv), the starting polymer V additionally contains cyanogen groups. The 5-primary amino group created by hydrolysis in the final polymer A can react with one of the cyanogen groups, as is known, to form a 5-membered cyclic amidine. In this regard, hydrolysis leads to an amide group, in this case a five-membered amidine group in the final polymer A according to IVIA / t / ZUZ I / UZ 104U with the following reaction scheme. In the reaction scheme here, the cyanogen-substituted ethylene derivative is in this case acrylonitrile into which it has been polymerized. In both cases described, hydrolysis of an amide group originating from a monomer of formula I leads to a primary amino group or an amidine group. A primary amino group or an amidine group has a positive charge at pH = and corresponds to a cationic charge in the final polymer A. The conditions for the hydrolysis of the amide groups in the final polymer A that originate from the monomers of the formula I can also lead to the hydrolysis of other groups in the starting polymer V that are sensitive to hydrolysis under these conditions. Thus, it is known, for example, from EP 0216387 A2, column 6 / lines 7 to 43, or from WO 2016 / 001016 Al, page 17 / lines 1 to 8, the hydrolysis of acetate groups in the starting polymer V that come from vinyl acetate as monomer (v-1) in which it has been polymerized. Consequently, a secondary hydroxy group is created as described below in the final polymer A. IVIA / l / U¿ 104U χ^γ^γ^Χ +2H2O O Η N R L I ¡ . Y - HO(O=)C-R\ °H N H= Ji Jl -HO(O=C)CH3 The monomers (ii) mean that ester groups are present in the starting polymer V. Under the acidic or basic conditions for the hydrolysis of the amide groups in the final polymer A originating from the monomers of formula I, a at least partial conversion of the ester groups. A conversion is the formation of a five-membered lactam structural unit with an amino group obtained. Another conversion is the formation of a carboxylic acid group. The following reaction scheme shows some of the reaction routes. which polymerize into the starting polymer V and which hydrolyze into the final polymer A can be determined experimentally by quantitative detection of the 5 carboxylic acids HOC(=O)R1 cleaved from the NC(=O)R1 groups. In the case of R1=H, the amount of formic acid or formate released can be determined, for example, enzymatically, with the aid of a test kit from Boehringer Mannheim. The number of hydrolyzed NC(=O)R1 groups of the polymerized units of formula I relative to all the polymerized units of formula I multiplied by 100 molar % gives the degree of hydrolysis (=HA). At least 50 to 100 molar % of the monomers (i) polymerized in the starting polymer V based on the number of all the monomers (i) polymerized in the starting polymer V are preferably hydrolyzed. Very preferably at least 65 to 100% is hydrolyzed, particularly 70 to 100%, very particularly 72 to 100%, especially preferably 85 to 99.9%, very particularly preferably 94 to 99.5% and expressly preferably 94 to 99%. A method is preferred in which at least 50 to 100% of the monomers (i) polymerized in the starting polymer V relative to the number of all the monomers (i) polymerized in the starting polymer V are hydrolyzed. A method is preferred in which at least 70 and at most 99.5% of the polymerized monomers (i) are hydrolyzed relative to the number of all the polymerized monomers (i) in the starting polymer V. The number of units of the monomers (ii) that are polymerized in the starting polymer V and that become the final polymer A can be determined experimentally by quantitative detection of the alcohols cleaved from the ester groups. Gas chromatography or high pressure liquid chromatography are suitable for the quantitative detection of cleaved alcohol. The number of ester groups converted from the polymerized monomers (ii) relative to all the polymerized monomers (ii) multiplied by 100 mole % gives the degree of conversion (=HE). At least 50 to 100% of the monomers (ii) polymerized in the starting polymer V relative to the number of all the monomers (ii) polymerized in the starting polymer V are preferably converted. Very preferably at least 70 to 100% is converted, particularly 86 to 100%, very particularly 90 to 100%, especially preferably 95 to 99.9%, very particularly preferably 98 to 99.5%, and expressly preferably 100%. A method is preferred in which at least 50 to 100% of the monomers (ii) polymerized in the starting polymer V are converted relative to the number of all the monomers (ii) polymerized in the starting polymer V. A method is preferred in which at least 90 and at most 99.5% of the polymerized monomers (ii) are converted relative to the number of all the polymerized monomers (ii) in the starting polymer V. A method is preferred in which at least 70 to 100% of the monomers (i) polymerized in the starting polymer V relative to the number of all the monomers (i) polymerized in the starting polymer V are hydrolyzed and at least 90 to 100% of the monomers (ii) polymerized in the starting polymer V relative to the number of all the monomers (ii) polymerized in the starting polymer V are converted. The starting polymer V is preferably subjected to alkaline, acid or enzymatic hydrolysis, most preferably alkaline or acid hydrolysis, particularly preferably alkaline hydrolysis. In the case of acid hydrolysis, the amino groups in the final polymer A are present in salt form. The degree of hydrolysis achieved (= HA) and the degree of conversion achieved (= HE) depend on the acid or base, the amount of acid or base used, the applied temperature and the duration of the reaction. The hydrolysis is preferably carried out at temperatures of 20 to 170°C, most preferably in the range of 50 to 140°C. The hydrolysis can be carried out at normal pressure, at reduced pressure or at elevated pressure, ie in the range from 100 mbar to 16 bar. Hydrolysis under normal pressure is preferred. Metal hydroxides of the first and second main groups of the periodic table of elements are suitable for alkaline hydrolysis, for example lithium hydroxide, sodium hydroxide, potassium hydroxide, magnesium hydroxide or calcium hydroxide, and ammonia and derivatives of ammonia, eg triethylamine, monoethanolamine, diethanolamine, triethanolamine or morpholine. Hydroxides of metals from the first and second main groups of the periodic table of elements are preferred, highly preferred are sodium hydroxide, potassium hydroxide, magnesium hydroxide or calcium hydroxide, sodium hydroxide or potassium hydroxide are particularly preferred, and very particularly preferred is sodium hydroxide. Mineral acids such as hydrogen halides, sulfuric acid, nitric acid and phosphoric acid as well as organic acids such as formic acid, acetic acid, propionic acid, benzosulfonic acid, alkylsulfonic acid and phosphonic acids are suitable for acid hydrolysis. Hydrochloric acid and sulfuric acid are preferred. With respect to the sum of the mole fractions of N-vinylamides and esters of (meth)acrylic acid in the starting polymer V, preferably 0.2-2.0 equivalents of acid or base are used. Most preferred are 0.5 to 1.5 equivalents, and especially preferably 0.7-1.2 equivalents. Preferably, a base or an acid is added to the starting polymer V numerically in an amount corresponding to between 30 and 150 mole % of the number of monomers (i) polymerized in the starting polymer V. The amount is most preferably between 90 and 150 mol%, particularly preferably between 100 and 140 mol%, and very particularly preferably between 110 and 130 mol%. A base or acid is preferably added in an amount of 30 to 130 mol% based on all monomers (i), (ii), (iii), (iv) and (v). The hydrolysis is preferably carried out in aqueous solution, most preferably in aqueous solution with a water content between 40 and 95% by weight with respect to the total weight of the aqueous solution, particularly preferably between 60 and 94% by weight, and very with particular preference between 75 and 93% by weight. A method is preferred in which the starting polymer V is subjected to alkaline hydrolysis to form the final polymer A. As described above, the starting polymers V containing monomer (iii) have an advantageous property in the case of alkaline hydrolysis. A method is preferred in which for the starting polymer V 1 to 25 mol % of the monomer (iii) is used for radical polymerization and the starting polymer V is subjected to alkaline hydrolysis to form the final polymer A. The final polymer A preferably contains five membered lactam structural units. The structural units of the final polymer A are, on the one hand, all monomers (i), (ii), optionally (iii), optionally (iv) and optionally (v) polymerized in the starting polymer V. Furthermore, they are also structural units that are potentially produced by hydrolysis. These include the aforementioned six-membered amidines, the aforementioned five-membered amidines, the aforementioned ethylene units with secondary hydroxy groups, the aforementioned five-membered lactams, and esters of acrylic or methacrylic acid hydrolyzed to carboxylic acid. For some of these structural units two polymerized monomers of the starting polymer V are used. Therefore, the total number of all structural units of the final polymer A is that of the total amount of all monomers (i), (ii) , (iii), (iv) and (v) that polymerize to form the starting polymer V, minus a correction number for those structural units that form from two polymerized monomers. By way of example, this is presented below based on formula (II) where R2= H o is Ci alkyl and R3= H o is Ci alkyl, a, b, c, d and e is the mole percent ratio (=mole %) of the structural unit, f is the mole percent fraction (= mole %) of at least one additional structural unit polymerized (not shown in formula (II)), and the sum of a, b, c, d, e and f is 100 mole %. A final polymer A of formula (II) is preferred. Highly preferred is a final polymer A of formula (II), wherein in formula (II) a is 0.1 to 20 mol%, b is 0 to 10 mol%, c is 25 to 85 mol%, d is from 1 to 50 mole%, e is from 1 to 50 mole%, and f is from 0 to 40 mole%, and where the sum of all structural units a, b, c, d, e and f is 100 mole% . Particularly preferably in formula (II) a is 0.1 to 20 mol%, b is 0 to 20 mol%, c is 25 to 85 mol%, d is 1 to 50 mol%, and e is 1 to 50 mole %, where the sum of all structural units a, b, c, d and e is 100 mole %. Most preferably in formula (II) R2= R3= H, a is from 0.1 to 20 mol%, b is from 0 to 20 mol%, c is 25 to 85 mol%, d is 1 to 50 mol%, e is 1 to 50 mole%, and any other different structural units f is from 0 to 40 mole%, where the sum of all structural units a, b, c, d, e and f is 100 mole%. Particularly preferably in formula (II) R2= R3= H, a is from 0.1 to 20 mol%, b is from 0 to 20 mol%, c is from 25 to 85 mol%, d is 1 to 50 mol%, and e is 1 to 50 mole%, where the sum of all structural units a, b, c, d and e is 100 mole%. The content of lactam structural units is very preferably from 10 to 60 mol%, the percentage based on the total number of all structural units of the final polymer A. The content is particularly preferably from 15 to 50% mol, very particularly preferably 17 to 35 mol%. The contents mentioned above are especially valid for a final polymer A in an aqueous environment at a pH value of 3.5 to 9 and expressly at a pH value of 3.5. A method is preferred in which the ester groups of the polymerized monomers (ii) in the starting polymer V are at least partly converted and at least part of the conversion is the formation of five-membered lactam structural units with the groups obtained primary aminos. The final polymer A preferably has a weight average molecular weight Mw between 8,000 and 8,000,000 Daltons. The final polymer A most preferably has a weight average molecular weight Mw of between 16,000 and 4,000,000 Daltons, especially preferably between 80,000 and 3,600,000 Daltons, very particularly preferably between 150,000 and 2,000,000 Daltons, and especially preferably between 170,000 and 1,200,000 Daltons . Weight average molecular weight can be determined by static light scattering. The final polymer A is preferably cationic, most preferably amphoteric-cationic. The final polymer A is cationic when the total number of all positive charges in the final polymer A is greater than the total number of all negative charges in the final polymer A at the current pH value, preferably at a pH value of 7 For this purpose, the corresponding charge-bearing structural units are considered with their charge at a formal pH value of 7. The final polymer A is amphoteric-cationic when the total number of all positive charges in the final polymer A is greater Find the total number of all negative charges in the final polymer A and at the same time the negative charges are present in the final polymer A at the current pH value, preferably at a pH value of 7. This is also true considering the units charge-carrying structures at a formal pH value of 7. The number of monomers (i) polymerized in the starting polymer V and their degree of hydrolysis in the final polymer A are the most important possibility of generating positive charges in the final polymer A. To this end, it is possible that the monomers (v ) introduce a positive charge into the starting polymer V and that this positive charge is still present in the final polymer A also after hydrolysis to give polymer A. The final polymer A preferably has a positive charge density. Most preferably, the charge density is determined by titration of polyelectrolytes with potassium polyvinylsulfonate. The charge density is most preferably determined at a pH value of 3.5 in an aqueous environment. The charge density is determined with particular preference by titration of polyelectrolytes with potassium polyvinylsulfonate at a pH of 3.5 in an aqueous medium. The positive charge density is preferably between 2 and 16 mmol / g, where 1 g refers to the polymer content in the final polymer A. 4 to 14 mmol / g is most preferred, particularly preferably 5 to 12 mmo1 / g. The final polymer A is preferably present in the form of an aqueous solution or dispersion. The water content of the aqueous dispersion or solution is most preferably 75 to 95% by weight and the final polymer A content is 5 to 25% by weight, wherein the final polymer A content is determined as polymer content. . The aqueous dispersion or solution preferably has a pH value greater than 5, very preferably between pH 6 and pH 9, particularly preferably between pH 6 and pH 8, and very particularly preferably between pH 6.1 and 6.8. It is possible to adjust a corresponding pH, for example, by adding an acid and / or a base. The positive charge density of the final polymer A, which is present as an aqueous solution or dispersion, is preferably between 20 and 120 mmol / 100 g, where 100 g refers to the final polymer A aqueous solution or dispersion. 100 mmol / 100 g, especially preferably 35 to 90 mmol / 100 g, is highly preferred. A method in which the final polymer A can be obtained by - radical polymerization of the monomers (i) 58 to 83 mol% of a monomer of formula I ΗH\N' H f / \__R ' 0), in which R1= H o means Ci-Ce alkyl. (ii) 8 to 39 mole % of a C1-C4 alkyl ester of acrylic acid or a C1-C4 alkyl ester of methacrylic acid, (iii) 0 to 25 mole % of a monoethylenically unsaturated carboxylic acid, a monoethylenically unsaturated sulfonic acid or a monoethylenically unsaturated phosphonic acid, or salt forms thereof, (iv) 0 to 9 mole % acrylonitrile or methacrylonitrile, (v) 0 to 25 mole % of one or more ethylenically unsaturated monomers that are different of a monomer (i), (ii), (iii) and (iv), Wherein the total amount of all monomers (i), (ii), (iii), (iv) and (v) is 100 mol%, to obtain a starting polymer V, and - hydrolyzing the starting polymer V to obtain the final polymer A, wherein the NC(=O)R1 groups of formula (I) of the monomers (i) polymerized in the starting polymer are hydrolyzed V at least in part and at In doing so, they form the primary amino groups, wherein the ester groups of the polymerized monomers (ii) in the starting polymer V are at least partly converted and at least part of the conversion is the formation of five-membered lactam structural units. with the primary amino groups obtained or the formation of carboxylic acid groups or salt forms thereof, The final polymer A is preferably added to the first aqueous suspension of fibrous material as an aqueous dispersion or solution of the final polymer A with a pH value of more than 5, most preferably between pH 6 and 9. particularly preferably between pH 6 and 8 , and very particularly preferably between pH 6.1 and 6.8. A method is preferred in which in step (A) the final polymer A is added as an aqueous dispersion or aqueous solution with a pH value of 5 to 9 to the first aqueous suspension of fibrous material. The second aqueous suspension of fibrous material containing the final polymer A contains (a-a) water (a-b) fibrous material (a-c) final polymer A. A possible additional constituent of the second aqueous suspension of fibrous material is (a-d) an organic polymer that is different from a fibrous material and the final polymer A. The organic polymer (a-d) can be neutral, cationic or anionic. A neutral organic polymer (a-d) can be uncharged neutral because it does not contain polymer units with a functional group that carries at least one charge at a pH value of 7. Examples of a neutral organic polymer (a-d) that does not contain none of the polymer units with a functional group that bears a charge at a pH value of 7 are polyacrylamide, poly(acrylamide-co-acrylonitrile), poly(vinyl alcohol) or poly(vinyl alcohol-co-vinyl acetate). . A natural organic polymer (a-d) can also be amphoteric-neutral because it contains polymer units with a functional group that bears a negative charge at least at a pH value of 7, and also polymer units with a functional group that bears a positive charge at pH 7. except at a pH value of 7, where in addition the number of all negative charges and the number of all positive charges of the functional groups cancel each other out. A cationic organic polymer (a-d) can be pure cationic, that is, it contains polymer units with a functional group that bears a positive charge at least at a pH value of 7, however, it does not contain polymer units with a functional group that bears a positive charge. a negative charge at least at a pH value of 7. Examples of a pure cationic organic polymer (a-d) are poly(allylamine), poly(diallylamine), poly(diallyldimethylammonium chloride), poly(acrylamide-co-diallyldimethylammonium chloride) or poly(acrylamide-co-2-( N,N,N-trimethylammonio)ethylacrylate). A cationic organic polymer (a-d) can also be amphoteric-cationic, that is, it contains polymer units with a functional group that bears a positive charge at least at a pH value of 7, and polymer units with a functional group that bears a positive charge. negative at least at a pH value of 7, and the number of all positive charges is greater than the number of all negative charges of the functional groups. A cationic organic polymer (a-d) can be pure anionic, that is, it contains polymer units with a functional group that bears a negative charge at least at a pH value of 7, however, it does not contain polymer units with a functional group that bears a negative charge. a positive charge at least at a pH value of 7. Examples of a pure anionic organic polymer (a-d) are poly(acrylic acid), poly(styrene-co-n-butylacrylate-co-acrylic acid) or poly(acrylamide-co- acrylonitrile-coacrylic acid). An anionic organic polymer (a-d) can also be amphoteric-anionic, that is, it contains polymer units with a functional group that bears a negative charge at least at a pH value of 7, and polymer units with a functional group that bears a negative charge. positive at least at a pH value of 7, and the number of all negative charges is greater than the number of all positive charges of the functional groups. In addition, the organic polymer (a-d) can also be distinguished based on whether it is linear, branched, or crosslinked. Crosslinking can be carried out, for example, by adding a crosslinking agent already during the polymerization of the starting monomers or by adding a crosslinking agent after the end of the polymerization, in particular also just before adding the organic polymer (a-d) to the second aqueous suspension. of fibrous material. For example, polyacrylamide can be crosslinked by adding the crosslinker methylenebisacrylamide to the acrylamide already during polymerization or only after polymerization with a crosslinker such as glyoxal. Both types of crosslinking can also be combined as appropriate. Particular mention should be made here of a crosslinked organic polymer, which generally has a high degree of crosslinking already during the polymerization of the monomer. It is present in the second aqueous suspension of fibrous material containing the final polymer A in particulate form, in particular in the form of so-called organic microparticles. The organic polymer (a-d) can be further distinguished also on the basis of whether it is natural, modified natural or synthetic. A natural organic polymer is normally obtained from nature, in which the appropriate isolation steps are applied as appropriate, although no directed chemical-synthetic modification is performed. An example of a natural organic polymer (a-d) is unmodified starch. Cellulose is not an example of a natural organic polymer (a-d), it is a fibrous material (a-b) here. A modified natural organic polymer is modified by one step of the chemical-synthetic method. An example of a modified natural organic polymer (a-d) is cationic starch. A synthetic organic polymer (a-d) is obtained chemically-synthetically from individual monomers. An example of a synthetic organic polymer (a-d) is polyacrylamide. A method is preferred in which in step (A) an organic polymer (a-d) is added to the first fibrous material suspension or the second fibrous material suspension containing the final polymer A. Most preferably an organic polymer ( a-d) which is a modified natural organic polymer. The organic polymer (a-d) is especially preferably cationic starch. The cationic starch is very particularly preferably the only organic polymer (a-d) that is added in step (A) to the first fibrous material suspension in addition to the final polymer A or to the second fibrous material suspension containing the final polymer A. A possible additional component of an aqueous suspension of fibrous material containing the final polymer A is (a-e) a filler. A filler (a-e) is an inorganic particle, in particular an inorganic pigment, All pigments based on metal oxides, silicates and / or carbonates conventionally used in the paper industry, in particular pigments from the group gue consisting of calcium carbonate, which can be used in the form of ground lime, chalk, marble (GCC) or precipitated calcium carbonate (PCC), talc, kaolin, bentonite, satin white, calcium sulphate, barium sulphate and titanium dioxide, can be used as pigments inorganic. An inorganic particle is also a colloidal solution of polysilicic acid in which the silicic acid particles generally have a particle size between 5 and 150 nm. A load (a-e) of the present invention also comprises two or more different loads. Consequently, the charge (a-e) divides as a possible additional component of an aqueous suspension of fibrous material into a first charge (ae-1), a second charge (a-e-2), etc. Inorganic pigments with an average particle size (average volume) <10 pm, preferably 0.3 to 5 pm, in particular 0.5 to 2 pm, are preferably used. The average particle size (average volume) of the inorganic pigments and of the particles of the powder composition is determined within the scope of this step generally by the quasi-elastic light scattering method (DIN-ISO 13320-1), for example, using a Mastersizer 2000 from Malvern Instruments Ltd. A method is preferred in which in step (A) a filler (a-e) is added to the first fibrous material suspension or the second fibrous material suspension containing the final polymer A. The total amount of filler (a-e) is preferably from 0 to 40% by weight relative to the paper or cardboard formed and based on a dry content of 100% by weight of the filler (a-e) and a dry content of the paper or cardboard of 100% by weight. The total amount of filler (a-e) is very preferably 5 to 30% by weight, particularly preferably 15 to 25% by weight and very particularly preferably 15 to 20% by weight. The formed paper or board preferably contains a total amount of filler (a-e) of 5 to 30% by weight. Papers of this type are, for example, wood-free papers. The formed paper or board preferably contains a total amount of filler (a-e) of 5 to 20% by weight. Papers of this type are used above all as packaging papers. The formed paper or board preferably contains a total amount of filler (a-e) of 5 to 15% by weight. Papers of this type are used above all for printing newspapers. The paper or board formed preferably contains a total amount of filler (a-e) of 25 to 40% by weight. Papers of this type are, for example, SC (supercalendered) papers. In step (A), the final polymer A is added to the first slurry of fibrous material, preferably before adding a filler (a-e). The final polymer A is most preferably added before a filler (a-e) and before an organic polymer (a-d), with the exception of cationic starch. The final polymer A is particularly preferably added to the first aqueous fibrous material suspension before loading (a-e), before an organic polymer (a-d) with the exception of cationic starch and before another paper auxiliary (a-f). . In step (A), any added filler (a-e) is preferably added to the second slurry of fibrous material containing the final polymer A, having a dry content of 0.1 to 1.5% by weight. This addition corresponds to what is known as thick matter addition. The second fibrous material suspension containing the final polymer A is already present at this dry content or is prediluted starting from a dry content of more than 0.15 to 6.0% by weight to a dry content of 0.1 to 1.5% by weight. In step (A), any added filler (a-e) is preferably added to the second slurry of fibrous material containing the final polymer A, wherein a first part of the total amount of filler (a-e) is to be add is added to the final polymer-containing fibrous material slurry A having a dry content of more than 0.15 to 6.0% by weight, and a second part of the total amount of filler (a-e) to be added is added to the suspension of fibrous material containing the final polymer (A) once it has been diluted to a dry content of 0.1 to 1.5% by weight. The first part and the second part form the total amount of charge (a-e) to be added. The weight ratio of the first part to the second part is between 5 and 0.2. Another possible constituent of an aqueous suspension of fibrous material containing the final polymer A is another paper auxiliary (a-f). Another paper auxiliary (a-f) is different from the above-mentioned components (a-b), the final polymer A as (a-c), (a-d) and (a-e). Another paper auxiliary (a-f) is, for example, an internal sizing agent, a water-soluble salt of a trivalent metal cation, a defoamer, a non-polymeric wet strength agent, a biocide, an optical brightener or a dye. of paper. Examples of a sizing agent are alkyl ketene dimers (AKD), alkenyl succinic acid anhydrides (ASA) and resin sizing. Examples of a water-soluble salt of a trivalent metal cation are aluminum(III) salts, in particular AICI3 such as A1C13'6H2O, A12(SO4)3 such as ΆΙ2(SO4)3 18H2O, or ΚΆ1(SO4 ) 2 · I2H2O . The other paper auxiliaries (a-f) can preferably be added in customary amounts. Preferably, another paper auxiliary (af) is added to the second slurry of fibrous material containing the final polymer A having a dry content of 0.1 to 1.5% by weight. This addition corresponds to what is known as thick matter addition. The second fibrous material suspension containing the final polymer A is already present at this dry content or is prediluted starting from a dry content of more than 0.15 to 6.0% by weight to a dry content of 0.1 to 1.5% by weight. Another paper auxiliaries (a-f) of the present invention also comprises two or more different paper auxiliaries. Accordingly, the other paper auxiliary (a-f) as a potential additional component of a second aqueous suspension of fibrous material containing the final polymer A is divided into a first additional paper auxiliary (a-f-1), a second additional paper auxiliary (a-f-2), etc. Often, in the case of paper production, more than one organic polymer (a-d) and more than one filler (a-e) that is inorganic are added to an aqueous suspension of fibrous material. In the case of an organic polymer (a-d), it is used, for example, to influence the technical properties of the paper production method itself or the technical properties of the produced paper. Therefore, retention agents, dewatering agents, wet strength agents, or other dry strength agents are used. Examples of retention agents are cationic, amphoteric or anionic organic polymers (a-d). Examples are an anionic polyacrylamide, a cationic polyacrylamide, a cationic starch, a cationic polyethyleneimine or a cationic polyvinylamine. In addition, inorganic fillers (a-e) can also be added as retention agents, which function as what are known as anionic microparticles. In particular, these include colloidal silicic acid or bentonite. Combinations of the examples mentioned above are possible. In particular, a dual system consisting of a cationic polymer with an anionic microparticle or an anionic polymer with a cationic microparticle is a potential combination. A synthetic organic polymer (a-d) or a dual system is preferred as the retention agent. In the case of a dual system as retention agent, for example a cationic organic first polymer (a-d-1) is present in combination with an anionic inorganic microparticle, for example a suitable bentonite, as a first filler (a-e-1 ) . Examples of another dry strength agent are a synthetic organic polymer (a-d), for example polyvinylamine, polyethyleneimine, polyacrylamide or glyoxylated polyacrylamide, a natural organic polymer (a-d) such as unmodified starch, or a modified natural organic polymer (a-d). such as a cationically modified starch or an oxidatively or enzymatically degraded starch. Preferably, another dry strength agent is added to either the first fibrous slurry or the second fibrous slurry containing the final polymer A, both of which have a dry content of greater than 1.5 to 6.0% by weight. Addition to the first aqueous fibrous material suspension or the second aqueous fibrous material suspension containing the final polymer A, each with a dry content of 0.1 to 1.5% by weight, is possible. In step (B), the second slurry of fibrous material containing the final polymer A is applied to the water-permeable substrate. The water-permeable substrate has a top side and a bottom side and fine openings, which allow the passage of water but substantially prevent the passage of fibrous constituents. The second suspension of fibrous material containing the final polymer A is applied evenly to the water permeable substrate. The top side of the water-permeable substrate is a surface that is substantially flat at the time of application, that is, flat apart from hairline openings or other irregularities induced by the material and any curvature of a certain radius. This makes it possible to produce a uniformly thin, maximally homogeneous web of wet fibrous material or a wet paper structure or a wet paper sheet. After the application of the second aqueous suspension of fibrous material containing the final polymer A, parts of the water (aa) run through the fine openings, after which a sheet is formed on the upper side, thus producing the structure wet paper. A wet paper structure produced in this way is flat, ie it has a very small height in relation to the length and width. The fibrous material of the second fibrous material slurry containing the final polymer A and other possible components that are to be present in the finally produced paper or board, for example a filler (a-e), are ideally retained here in their entirety or at least substantially in the wet paper structure that is formed. Possible additional components of the second aqueous suspension of fibrous material containing the final polymer A, which are added to help retention of the other components, to help dewatering or to help uniform sheet formation, for example, an organic polymer (a-d) take effect during this process. Normally, these possible additional components of the fibrous material suspension also remain wholly or at least substantially in the produced fibrous material web. The proportion of the wet paper structure, which determines the dry content of the wet paper structure, contains the retained constituents of the fibrous material, possible other components that should be present in the finally produced paper, and possible additional components. Depending on their retention behaviour, these components, for example, of the specified fibrous material are organic polymers, fillers and other paper auxiliaries. The wet paper structure is strong enough at the end of step (B) to be removable from the water-permeable substrate. The water-permeable substrate in step (B) is preferably a screen. The sieve, which has a sieve upper part and a sieve lower part, has sieve meshes as fine openings. The sieve, for example, contains a metal or plastic mesh. In the case of a paper machine, the screen is most preferably an endless screen. Once the formed wet paper structure has been separated from an endless screen, the endless screen returns to the material feed, where a new second slurry of fibrous material containing the final polymer A is applied to the circulating screen without end. The screen is most preferably an endless screen that rotates around a number of cylinders. The dry content of the wet paper structure that is formed in step (B) is preferably 15 to 25% by weight, most preferably 18.7 to 24% by weight, particularly preferably 18.8 to 23% by weight, very particularly preferably from 18.9 to 22% by weight, particularly preferably from 19.0 to 21% by weight, and very particularly preferably from 19.0 to 20.7% by weight. A method is preferred in which in step (B) the wet paper structure has a dry content between 18.5 and 25% by weight. A method in which in step (A) the final polymer A is added to the first aqueous slurry of fibrous material, having a dry content of more than 1.5 to 6% by weight at the time of addition, and in the that in step (B) it is preferred that the wet paper structure have a dry content between 18.5 and 25% by weight. In step (C), the wet paper structure obtained in step (B) is dehydrated to form a paper or board. The dewatering in step (C) comprises the following steps (C-1) dewatering the wet paper structure by pressing, whereby a wet paper sheet is formed, (C-2) dewatering the wet paper sheet by supplying heat, for what forms paper or cardboard. The pressing of the wet paper structure in step (C-l) leads to further dehydration and a corresponding increase in dry content. When press dewatered, mechanical pressure is exerted on the wet paper structure. Removal of water by mechanical pressure saves more energy than drying by heat supply. By placing the moist paper structure on a water absorbent sheet or tape, eg a felt-like fabric, dehydration is maintained by absorbing the compressed water. A cylinder is suitable for exerting pressure on the mixed material of the composite layer. In particular, a suitable solution is to guide the mixed layer material through two cylinders, possibly while lying on the water-absorbent tape. The cylinder surface is made, for example, of steel, granite or hard rubber. The surface of a cylinder can be coated with a water-absorbing material. Water-absorbent materials have a high level of absorbency, porosity, moisture, and elasticity. A wet sheet of paper is formed at the end of step (C—1). The wet paper sheet is strong enough at the end of step (C-1) to be fed to the next step (C-2) without mechanical support. The wet paper sheet preferably has a dry content between 35 and 65% by weight, most preferably between 37 and 60% by weight, most preferably between 38 and 55% by weight, especially preferably between 40 and 50% by weight. In step (C-2), further dewatering of the wet paper sheet in step (C-1) is performed, whereby paper or cardboard is formed. Heat is supplied to the moist paper sheet, for example, by heated plates, on which the moist paper is placed, by heated cylinders, on which the moist paper sheet is guided, by infrared emitters, by hot air that is guided on the damp sheet of paper, or by a combination of two, three or all of these measures. The obtained paper or cardboard has the highest strength compared to a wet paper structure or the wet paper sheet. It is presumed that from a dry content of the 80% by weight, the hydroxyl groups of the cellulose fibers are strongly connected by hydrogen bonding, which complements the previous mechanical felting of the fibers. A measure of the resistance of the paper or cardboard obtained is, for example, the internal resistance. The dry content of the obtained paper or board is preferably at least 88% by weight. The dry content of the paper or board is most preferably between 89 and 100% by weight, particularly preferably between 90 and 98% by weight, and most preferably between 91 and 96% by weight. Depending on the mass per unit area, which is also called areal density or basis weight, the name of the flat shaped article created from the second slurry of fibrous material containing the final polymer A changes. A dry shaped article with a mass per unit area from 7 g / m2 to 225 g / m2 is called paper here, and one with a mass per unit area of ​​225 g / m2 is called cardboard. The grammage of the paper or cardboard is preferably from 20 to 400 g / m2, very preferably from 40 to 280 g / m2, particularly preferably from 60 to 200 g / m2, very particularly preferably from 80 to 160 g / m2, of particularly preferably 90 to 140 g / m2 and very particularly preferably 100 to 130 g / m2. The paper or cardboard formed is preferably a packaging paper, most preferably a corrugated paper. The preferences described for the method of production of paper or cardboard also apply to the other objects of the invention. Another object of the invention is a paper or cardboard that can be obtained by a method containing steps (A) adding a final polymer A to a first aqueous suspension of fibrous material, whereby a second aqueous suspension of fibrous material is created containing the final polymer A, ΜΛ / l / U¿ 104U where the final polymer A can be obtained by - radical polymerization of the monomers (i) 30 to 90 mol% of a monomer of formula I in which R1 = H o means Ci-Ce alkyl. (ii) 3 to 60 mole % of a C1-C4 alkyl ester of acrylic acid or a C1-C4 alkyl ester of methacrylic acid, (iii) 0 to 45 mole % of a monoethylenically unsaturated carboxylic acid, a monoethylenically unsaturated sulfonic acid or a monoethylenically unsaturated phosphonic acid, or salt forms thereof, (iv) 0 to 9 mole % acrylonitrile or methacrylonitrile, (v) 0 to 35 mole % of one or more ethylenically unsaturated monomers that are different of a monomer (i), (ii), (iii) and (iv), wherein the total amount of all monomers (i), (ii), (iii), (iv) and (v) is 100% molar, to obtain a starting polymer V, and - hydrolyzing the starting polymer V to obtain the final polymer A, wherein the NC(=O)R1 groups of formula (I) of the monomers (i) polymerized in the starting polymer V are hydrolyzed at least in part and at In doing so, they form the primary amino groups, wherein the ester groups of the polymerized monomers (ii) in the starting polymer V are at least partly converted and at least part of the conversion is the formation of five-membered lactam structural units. with the primary amino groups obtained or the formation of carboxylic acid groups or salt forms thereof, (B) dewatering the second aqueous slurry of fibrous material containing the final polymer A on a water-permeable substrate to form a paper structure wet, (C) dehydrate the wet paper structure, whereby the paper or cardboard is formed. The paper or cardboard preferably has an internal resistance of 165 to 400 J / m2, very preferably 190 to 350 J / m2, particularly preferably 200 to 300 J / m2, and very particularly 220 to 280 J / m2, where the internal resistance corresponds to that of the TAPPI T833 pm-94 standard. Another object of the invention is a final polymer A, obtainable by - radical polymerization of the monomers (i) 58 to 83 mol% of a monomer of formula I (I), in which R1 = H o means Ci-Ce alkyl. (ii) 8 to 39 mole % of a C1-C4 alkyl ester of acrylic acid or a C1-C4 alkyl ester of methacrylic acid, (iii) 0 to 25 mole % of a monoethylenically unsaturated carboxylic acid, a monoethylenically unsaturated sulfonic acid or a monoethylenically unsaturated phosphonic acid, or salt forms thereof, (iv) 0 to 9 mole % acrylonitrile or methacrylonitrile, (v) 0 to 25 mole % of one or more ethylenically unsaturated monomers that are different of a monomer (i), (ii), (iii) and (iv), wherein the total amount of all monomers (i), (ii), (iii), (iv) and (v) is 100% molar, to obtain a starting polymer V, and - hydrolyzing the starting polymer V to obtain the final polymer A, wherein the NC(=O)R1 groups of formula (I) of the monomers (i) polymerized in the starting polymer V are hydrolyzed at least in part and at In doing so, they form the primary amino groups, wherein the ester groups of the polymerized monomers (ii) in the starting polymer V are at least partly converted and at least part of the conversion is the formation of five-membered lactam structural units. with the primary amino groups obtained or the formation of carboxylic acid groups or salt forms thereof, A final polymer A in which the monomers are (i) 60 to 83 mol% N-vinylformamide, (ii) 8 to 21 mol% ethyl acrylate, (iii) 2 to 21 mol% acrylic acid or methacrylic acid or salt forms thereof, (iv) 0 to 9 mole % acrylonitrile or methacrylonitrile, (v) 0 to 24 mole % of one or more ethylenically unsaturated monomers that are different from a monomer (i), (ii), ( iii) and (iv), are used as starting polymer for radical polymerization. Another object of the invention is a starting polymer V that can be obtained by radical polymerization of the monomers. (i) 58 to 83 mol% of a monomer of formula I H H in which R1 = H o means Ci-Ce alkyl. (ii) 8 to 39 mole % of a C1-C4 alkyl ester of acrylic acid or a C1-C4 alkyl ester of methacrylic acid, (iii) 0 to 25 mole % of a monoethylenically unsaturated carboxylic acid, a monoethylenically unsaturated sulfonic acid or a monoethylenically unsaturated phosphonic acid, or salt forms thereof, (iv) 0 to 9 mole % acrylonitrile or methacrylonitrile, (v) 0 to 25 mole % of one or more ethylenically unsaturated monomers that are different of a monomer (i), (ii), (iii) and (iv), wherein the total amount of all monomers (i), (i i), (iii), (iv) and (v) is 100 % cool. A starting polymer V in which the monomers are (i) 60 to 83 mol% N-vinylformamide, (ii) 8 to 21 mol% ethyl acrylate, (iii) 2 to 21 mol% acrylic acid or methacrylic acid or salt forms thereof, (iv) 0 to 9 mole % of acrylonitrile or methacrylonitrile, (v) 0 to 24 mole % of one or more ethylenically unsaturated monomers that are different from a monomer (i), (ii ), (iii) and (iv), are used for radical polymerization. Figure 1 schematically shows, by means of curve A, the time profile in hours of the viscosity in mPas in the case of alkaline hydrolysis of a first starting polymer obtained from 70% molar N-vinylformamide and 30% molar acrylate. of methyl. Curve B schematically shows the time profile in hours of the viscosity in mPas in case of alkaline hydrolysis of a second starting polymer obtained from 70 mol% N-vinylformamide, 20 mol% methylate acrylate and 10 mol% N-vinylformamide. sodium acrylate. e xamples The percentages in the examples are percentages by weight, unless otherwise indicated. A) Additives A-l) Methods to characterize polymers The solids content of a polymer solution is determined by spreading 0.5 to 1.5 g of the polymer solution on a 4 cm diameter sheet metal plate and then drying in a recirculating air cabinet at 140°C for two hours. (= 2 hrs) . The ratio between the mass of the sample after drying under the above conditions and the mass of the initial weighed sample multiplied by 100 gives the solids content of the polymer solution in wt%. The degree of hydrolysis of the N-vinylformamide units (=HA) is the mole % ratio of the hydrolyzed N-vinylformamide units to the N-vinylformamide units originally provided in the polymer. The degree of hydrolysis is determined by enzymatic analysis of the formic acid or formate released during hydrolysis (Boehringer Mannheim test equipment). The degree of conversion of the (meth)acrylate units (=EU) is the mole % ratio of the converted (meth)acrylate units relative to the originally supplied (meth)acrylate units. The term conversion is understood here as the cleavage of the ester unit, for example by hydrolysis, to form a (meth)acrylate unit or the corresponding salt form thereof by reaction with an adjacent amino group, forming lactam as a result. The degree of conversion can be determined by analyzing the alcohol released during the conversion. The latter is achieved, for example, with the help of HPLC or gas chromatography depending on the alcohol released. The polymer content specifies the polymer content without counterions in the aqueous solution in % by weight, ie counterions are not taken into account. The polymer content is the sum of the proportions by weight of all polymer structural units in g that are present in 100 g of the aqueous solution. It is determined mathematically. For this purpose, potentially charge-bearing structural units in the charged form are taken into account, ie, for example, amino groups in the protonated form and acid groups in the deprotonated form. Counter ions of charged structural units, such as a sodium cation, chloride, phosphate, formate, acetate, etc., are not taken into account. The calculation can be made in such a way that, for a batch, starting from the amounts of use of monomers, and considering the degree of hydrolysis (HA) and the degree of conversion (UE) as appropriate, the molar amounts of the structural units of the polymer present at the end of the reaction are determined and converted into proportions by weight with the aid of the molar masses of the structural units. The sum of the proportions by weight gives the total amount of polymer in this batch. The polymer content is given from the ratio between the total amount of polymer and the total mass of the batch. The K values ​​are measured according to H. Fikentscher, Cellulosechemie (Cellulose Chemistry), Volume 13, 48-64 and 71-74 under the conditions specified there. Details in parentheses indicate the concentration of the polymer solution and solvent. The charge densities are determined by titration of polyelectrolytes with potassium vinylsulfonate at a pH value of 3.5 (see D. Horn, Progress in Colloid & Polymer Science, 65 (1978), pages 251-264). Only fully demineralized water is used in the production of the polymers, unless otherwise stated. Monomer abbreviations: EA: ethyl acrylate MA: methyl acrylate SEE: N-vinylformamide Sodium acrylate: sodium salt of acrylic acid Sodium methacrylate: sodium salt of methacrylic acid Na AMPS: 2-acrylamido-2methipropanesulfonic acid sodium salt Na-vinylsulfonate: vinylsulfonic acid sodium salt DADMAC: diallyl dimethyl ammonium chloride APTAC: (3-acrylamidopropyl)trimethyl ammonium chloride AM: acrylamide During the hydrolysis processes, to evaluate if a viscosity peak is provided intermediately, the eddy produced by the vortex was controlled in the paddle stirrer (glass stirrer with a rounded Teflon paddle 10 with a diameter of 7.0 cm and a height of 2.5 cm) evaluated as follows: Viscosity Peak Eddy Change None Eddy is reduced by less than 10% Minimal Eddy is reduced by more than 10%, but less than 50% Low Eddy is reduced by more than 50% until complete eddy disappearance Moderate The whirlpool is reversed; product tucks up less than 1 cm Strong Swirl reverses; product bows up more than 1 cm, but less than 3 cm Very strong Swirl reverses; product bows up more than 3 cm and less than 6 cm (ie as far as bearing sleeve) End Vortex reverses; the product is argued as far as the bearing sleeve; agitator speed must be reduced to 1 / 4 to prevent product from infiltrating the bearing sleeve Very extreme Agitator must be stopped Composition of final polymers of formula III ( = mole %) of the structural unit and the sum of a, b, c d and e is 100 mole %. (1. ) a = amidinium / (amidinium + VFA + vinyl ammonium + acrylate anion + lactam) * 100 b = VFA / (amidinium + VFA + vinyl ammonium + acrylate anion + lactam) * 100 c = vinyl ammonium / ( amidinium + VFA + vinyl ammonium + acrylate anion + lactam) * 100 d = acrylate anion / (amidinium + VFA + vinyl ammonium + acrylate anion + lactam) * 100 e = lactam / (amidinium + VFA + vinyl ammonium + anion of acrylate + lactam) * 100 (2. ) VFA [mmol / 100 g]: Concentration of VFA structural units, as present in the final product. acrylate anion [mmol / 100 g]: concentration of acrylate anion structural units, as present in the final product vinyl ammonium [mmol / 100 g]: concentration of vinyl ammonium structural units, as present in the final amidinium product [mmol / 100 g]: concentration of the amidinium structural units, as present in the final product lactam [mmol / 100 g]: concentration of the lactam structural units, as present in the final product Final product The final product here refers to the polymer solution that is obtained on the basis of the hydrolysis feed. (3. ) With a degree of conversion HE of 100 mol%, the following is provided: amidinium = (VEA0- FA) * FAD / (FFA + FAD) VFA = (VEA0- FA) * FEA / (FEA + FAD) vinyl ammonium = FA - lactam - amidinium acrylate anion = Na-AS° + MA° + EA° - FA + LD lactam = FA - LD (4. ) FA [mmol / 100 g]: formate content in the final product LD [mmol / 100 g] : charge density in the final product (alternatively: [meq / 100 g]) FFA: integration area of ​​the 13C-NMR signal of the carbon of the carbonyl group of the VFA structural unit in a polymer between 164 and 168 ppm FAD: area of ​​integration of the 13 carbon C-NMR signal of the imine of the amidinium structural unit in a polymer at 152 ppm VFA° [mmol / 100 g]: concentration of VFA units that would be present in the final product if no further reaction of the polymerized monomers took place - calculated from the start of polymerization Na-AS° [mmol / 100 g] : concentration of Na acrylate units that would be present in the final product if no further reaction of the polymerized monomers took place - calculated from the start of polymerization MA°, EA° [mmol / 100 g]: concentration of methyl- or ethyl acrylate units that would be present in the final product if no further reaction of the polymerized monomers took place - calculated from the start of polymerization A-2) Production of starting polymers by polymerization Starting polymer VE1: Copolymer (VFA / MA = 70% mole / 30% mole) 150.4 g of VFA (99%) were provided as feed 1. 77.3 g of MA were provided as feed 2. 1.13 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride were dissolved in 112.1 g of water at room temperature (=RT) as feed 3. 0.67 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 67.2 g of water at RT as feed 4. 187.3 g of water were provided as feed 5. 782.6 g of water and 2.8 g of 75% by weight phosphoric acid were placed in a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm (= revolutions per minute) about 3.9 g of a 25% by weight sodium hydroxide solution were added, giving a pH of 6.5. The receiver was then heated for 30 min at 70°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to prevent oxygen diffusion. At a constant internal temperature of 70°C, all 3 feeds 1 to 3 were started at the same time. Feed 1 was fed in 3 hr, feed 2 in 3.5 hr, and feed 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 70°C. Feed 4 was then added over 5 min and the reaction mixture was held for a further 1.5 hr at 70°C. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 300 mbar by means of a water jet pump so that the reactor contents began to boil. Under these conditions, 187.3 g of water distilled off. The vacuum was then broken with air, Feed 5 was added and the reaction mixture was cooled to RT. A light yellow viscous solution with a solids content of 18.8% was obtained. The K value of the copolymer was 84 (0.5% by weight in water). Starting polymer VE2: Copolymer (VFA / MA = 70% mole / 30% mole) 150.4 g of VEA (99%) were provided as feed 1. 77.3 g of MA were provided as feed 2. 1.13 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 112.1 g of water at RT as feed 3. 0.67 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 67.2 g of water at RT as feed 4. 176.6 g of water were provided as feed 5. 782.6 g of water and 2.5 g of 75% by weight phosphoric acid were introduced into a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 3.9 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 69°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to prevent oxygen diffusion. At a constant internal temperature of 69°C, all 3 feeds 1 to 3 were started at the same time. Feed 1 was fed in 3 hr, feed 2 in 3.5 hr, and feed 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 69°C. Feed 4 was then added over 5 min and the reaction mixture was held for a further 1.5 hr at 69°C. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 320 mbar by means of a water jet pump so that the contents of the reactor began to boil. Under these conditions, 176.6 g of water distilled off. The vacuum was then broken with air, Feed 5 was added and the reaction mixture was cooled to RT. A viscous yellow solution with a solids content of 19.1% was obtained. The K value of the copolymer was 84 (0.5% by weight in water). Starting polymer VE3: Terpolymer (VFA / MA / Na acrylate = 70% mole / 29% mole / 1% mole) As feed 1, a mixture of 9.3 g of 32% by weight aqueous sodium acrylate solution, adjusted to pH 6.4, 158.2 g of VFA (99%) and 210.0 g of water was provided. 78.6 g of MA were provided as feed 2. 1.19 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 117.5 g of water at RT as feed 3. 0.71 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 70.5 g of water at RT as feed 4. 172.7 g of water were provided as feed 5. 547.4 g of water and 2.5 g of 75% by weight phosphoric acid were placed in a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 4.1 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 69°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to prevent oxygen diffusion. At a constant internal temperature of 69°C, all 3 feeds 1 to 3 were started at the same time. Feed 1 was fed in 3 hr, feed 2 in 3.5 hr, and feed 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 69°C. Feed 4 was then added over 5 min and the reaction mixture was held for a further 1.5 hr at 69°C. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 320 mbar by means of a water jet pump so that the reactor contents began to boil. Under these conditions, 172.7 g of water distilled off. The vacuum was then broken with air, Feed 5 was added and the reaction mixture was cooled to RT. A viscous yellow solution with a solids content of 19.6% was obtained. The K value of the terpolymer was 90 (0.5% by weight in a 5% by weight aqueous NaCl solution). Starting polymer VE4: Terpolymer (VFA / MA / Na acrylate = 70% mole / 28% mole / 2% mole) As feed 1, a mixture of 18.5 g of 32% by weight aqueous sodium acrylate solution, adjusted to pH 6.4, 158.0 g of VEA (99%) and 200.0 g of water was provided. 75.8 g of MA were provided as feed 2. 1.18 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 117.1 g of water at RT as feed 3. 0.71 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 70.3 g of water at RT as feed 4. 184.0 g of water were provided as feed 5. 551.7 g of water and 2.6 g of 75% by weight phosphoric acid were placed in a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 4.1 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 70°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to prevent oxygen diffusion. At a constant internal temperature of 70°C, all 3 feeds 1 to 3 were started at the same time. Feed 1 was fed in 3 hr, feed 2 in 3.5 hr, and feed 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 70°C. Feed 4 was then added over 5 min and the reaction mixture was held for a further 1.5 hr at 70°C. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 300 mbar by means of a water jet pump so that the reactor contents began to boil. Under these conditions, 184.0 g of water distilled off. The vacuum was then broken with air, Feed 5 was added and the reaction mixture was cooled to RT. A viscous yellow solution with a solids content of 19.4% was obtained. The K value of the terpolymer was 90 (0.5% by weight in a 5% by weight aqueous NaCl solution). Starting polymer VE5: Terpolymer (VFA / MA / Na acrylate = 70% mole / 25% mole / 5% mole) As feed 1, a mixture of 46.1 g of 32% by weight aqueous sodium acrylate solution, adjusted to pH 6.5, 157.5 g of VFA (99%) and 200.0 g of water was provided. 67.4 g of MA were provided as feed 2. 1.17 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 116.1 g of water at RT as feed 3. 0.70 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 69.7 g of water at RT as feed 4. 196.6 g of water were provided as feed 5. 534.7 g of water and 2.6 g of 75% by weight phosphoric acid were placed in a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 4.2 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 70°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to prevent oxygen diffusion. At a constant internal temperature of 70°C, all 3 feeds 1 to 3 were started at the same time. Feed 1 was fed in 3 hr, feed 2 in 3.5 hr, and feed 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 70°C. Feed 4 was then added over 5 min and the reaction mixture was held for a further 1.5 hr at 70°C. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 300 mbar by means of a water jet pump so that the reactor contents began to boil. Under these conditions, 196.6 g of water distilled off. The vacuum was then broken with air, Feed 5 was added and the reaction mixture was cooled to RT. A viscous yellow solution with a solids content of 19.4% was obtained. The K value of the terpolymer was 93 (0.5% by weight in a 5% by weight aqueous NaCl solution). Starting polymer VE6: Terpolymer (VFA / MA / Na acrylate = 70% mole / 25% mole / 5% mole) As feed 1, a mixture of 43.0 g of 32% by weight aqueous sodium acrylate solution, adjusted to pH 6.5, 147.0 g of VFA (99%) and 200.0 g of water was provided. 62.9 g of MA were provided as feed 2. 0.33 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 32.5 g of water at RT as feed 3. 1.42 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 140.9 g of water at RT as feed 4. 164.8 g of water were provided as feed 5. 565.7 g of water and 2.4 g of 75% by weight phosphoric acid were placed in a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 3.9 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 60°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to avoid diffusion of oxygen. At a constant internal temperature of 60°C, all 3 feeds 1 to 3 were started at the same time. Feed 1 was fed in 3 hr, feed 2 in 3.5 hr, and feed 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 60°C. Feed 4 was then added over 5 min and the reaction mixture was held for a further 1.5 hr at 60°C. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 280 mbar by means of a water jet pump so that the reactor contents began to boil. Under these conditions, 164.8 g of water distilled off. The vacuum was then broken with air, Feed 5 was added and the reaction mixture was cooled to RT. A viscous yellow solution with a solids content of 13.9% was obtained. The K value of the terpolymer was 138 (0.1% by weight in a 5% by weight aqueous NaCl solution). Starting polymer VE7: Terpolymer (VFA / MA / Na acrylate = 70% mole / 20% mole / 10% mole) As feed 1, a mixture of 91.6 g of 32% by weight aqueous sodium acrylate solution, adjusted to pH 6.5, 156.7 g of VFA (99%) and 200.0 g of water was provided. 100 53.9 g of MA were provided as feed 2. 1.15 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 114.3 g of water at RT as feed 3. 0.69 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 68.6 g of water at RT as feed 4. 184.4 g of water were provided as feed 5. 506.5 g of water and 2.6 g of 75% by weight phosphoric acid were introduced into a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 4.2 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 70°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to avoid diffusion of oxygen. At a constant internal temperature of 70°C, all 3 feeds 1 to 3 were started at the same time. Feed 1 was fed in 3 hr, feed 2 in 3.5 hr, and feed 3 in 4 hr. In the end 101 of feed 3, the batch was held for an additional hour at 70°C. Feed 4 was then added over 5 min and the reaction mixture was held for a further 1.5 hr at 70°C. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 320 mbar by means of a water jet pump so that the reactor contents began to boil. Under these conditions, 184.4 g of water distilled off. The vacuum was then broken with air, Feed 5 was added and the reaction mixture was cooled to RT. A viscous yellow solution with a solids content of 19.7% was obtained. The K value of the terpolymer was 94 (0.5% by weight in a 5% by weight aqueous NaCl solution). IVIA / 1 / ZUZ I / UZ I omj Starting polymer VE8: Terpolymer (VFA / MA / Na acrylate = 70% mole / 15% mole / 15% mole) As feed 1, a mixture of 136.7 g of 32% by weight aqueous sodium acrylate solution, adjusted to pH 6.5, 155.9 g of VEA (99%) and 200.0 g of water was provided. 40.0 g of MA were provided as feed 2. 1.14 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 112.6 g of water at RT as feed 3. 0.68 g of 2,2'-azobis dihydrochloride were dissolved 102 (2-methylpropionamidine) in 67.5 g of water at RT as feed 4. 227.5 g of water were provided as feed 5. 478.7 g of water and 2.6 g of 75% by weight phosphoric acid were placed in a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 4.2 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 70°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to prevent oxygen diffusion. At a constant internal temperature of 70°C, all 3 feeds 1 to 3 were started at the same time. Feed 1 was fed in 3 hr, feed 2 in 3.5 hr, and feed 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 70°C. Feed 4 was then added over 5 min and the reaction mixture was held for a further 1.5 hr at 70°C. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to IVIA / 1 / ZUZ I / UZ I omj 103 approximately 320 mbar by means of a water jet pump so that the contents of the reactor began to boil. Under these conditions, 227.5 g of water distilled off. The vacuum was then broken with air, Feed 5 was added and the reaction mixture was cooled to RT. A viscous yellow solution with a solids content of 19.9% ​​was obtained. The K value of the terpolymer was 99 (0.5% by weight in a 5% by weight aqueous NaCl solution). Starting polymer VE9: Terpolymer (VFA / MA / Na acrylate = 70% mole / 10% mole / 20% mole) As feed 1, a mixture of 181.4 g of 32% by weight aqueous sodium acrylate solution, adjusted to pH 6.5, 155.0 g of VFA (99%) and 200.0 g of water was provided. 26.6 g of MA were provided as feed 2. 1.12 g of 2,2'azobis(2-methylpropionamidine) dihydrochloride was dissolved in 110.8 g of water at RT as feed 3. 0.67 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 66.5 g of water at RT as feed 4. 200.5 g of water were provided as feed 5. 451.1 g of water and 2.6 g of 75% by weight phosphoric acid were introduced into a 2 1 glass apparatus with 104 anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 4.1 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 70°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to prevent oxygen diffusion. At a constant internal temperature of 70°C, all 3 feeds 1 to 3 were started at the same time. Feed 1 was fed in 3 hr, feed 2 in 3.5 hr, and feed 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 70°C. Feed 4 was then added over 5 min and the reaction mixture was held for a further 1.5 hr at 70°C. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 320 mbar by means of a water jet pump so that the reactor contents began to boil. Under these conditions, 200.5 g of water distilled off. The vacuum was then broken with air, Feed 5 was added and the reaction mixture was cooled to RT. 105 A viscous yellow solution with a solids content of 20.2% was obtained. The K value of the terpolymer was 102 (0.5% by weight in a 5% by weight aqueous NaCl solution). Starting polymer VE10: Terpolymer (VFA / MA / Na acrylate = 70% mol / 25% mol / 5% mol) As feed 1, a mixture of 55.9 g of 30% by weight aqueous sodium methacrylate solution, adjusted to pH 6.5, 156.1 g of VEA (99%) and 200.0 g of water was provided. 66.8 g of MA were provided as feed 2. 1.17 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 116.1 g of water at RT as feed 3. 0.70 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 69.7 g of water at RT as feed 4. 185.7 g of water were provided as feed 5. 52 6.7 g of water and 2.6 g of 75% by weight phosphoric acid were introduced into a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm, approximately 4.1 g of a 106 25% by weight sodium hydroxide solution, giving a pH of 6.5. The receiver was then heated for 30 min at 68°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to prevent oxygen diffusion. At a constant internal temperature of 68°C, all 3 feeds 1 to 3 were started at the same time. Feed 1 was fed in 3 hr, feed 2 in 3.5 hr, and feed 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 68°C. Feed 4 was then added over 5 min and the reaction mixture was held for a further 1.5 hr at 68°C. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 320 mbar by means of a water jet pump so that the reactor contents began to boil. Under these conditions, 185.7 g of water distilled off. The vacuum was then broken with air, Feed 5 was added and the reaction mixture was cooled to RT. A viscous yellow solution with a solids content of 19.2% was obtained. The K value of the terpolymer was 94 (0.5% by weight in a 5% by weight aqueous NaCl solution). ΙνΙΛ / t / ZUZ I / UZ 104U 107 Starting polymer VE11: Terpolymer (VFA / MA / Na AMPS = 70% mol / 25% mol / 5% mol) As feed 1, a mixture of 66 g of 50% by weight aqueous NaAMPS solution, adjusted to pH 6.5, 144.6 g of VFA (99%) and 210.0 g of water was provided. 61.9 g of MA were provided as feed 2. 1.17 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 116.1 g of water at RT as feed 3. 0.71 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 69.8 g of water at RT as feed 4. 186.7 g of water were provided as feed 5. 532.8 g of water and 2.6 g of 75% by weight phosphoric acid were placed in a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 4.1 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 69°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feeding was stopped and conduction continued. 108 nitrogen only through the reflux condenser to prevent diffusion of oxygen. At a constant internal temperature of 69°C, all 3 feeds 1 to 3 were started at the same time. Feed 1 was fed in 3 hr, feed 2 in 3.5 hr, and feed 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 69°C. Feed 4 was then added over 5 min and the reaction mixture was held for a further 1.5 hr at 69°C. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 300 mbar by means of a water jet pump so that the reactor contents began to boil. Under these conditions, 186.7 g of water distilled off. The vacuum was then broken with air, Feed 5 was added and the reaction mixture was cooled to RT. A viscous yellow solution with a solids content of 20.0% was obtained. The K value of the terpolymer was 89 (0.5% by weight in a 5% by weight aqueous NaCl solution). Starting polymer VE12: Terpolymer (VFA / MA / Na vinylsulfonate = 70% mol / 25% mol / 5% mol) As feed 1, a mixture of 79.6 g of 25% by weight aqueous sodium vinylsulfonate solution, adjusted to pH 6.5, 153.9 g of VFA (99%) and 200.0 g of water was provided. 109 65.9 g of MA were provided as feed 2. 1.17 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 116.2 g of water at RT as feed 3. 0.70 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 69.7 g of water at RT as feed 4. 164.5 g of water were provided as feed 5. 506.1 g of water and 2.6 g of 75% by weight phosphoric acid were placed in a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 4.1 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 65°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to prevent oxygen diffusion. At a constant internal temperature of 65°C, all 3 feeds 1 to 3 were started at the same time. Feed 1 was fed in 3 hr, feed 2 in 3.5 hr, and feed 3 in 4 hr. In the end 110 of feed 3, the batch was held for an additional hour at 65°C. Feed 4 was then added over 5 min and the reaction mixture was held for a further 1.5 hr at 65°C. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 300 mbar by means of a water jet pump so that the reactor contents began to boil. Under these conditions, 164.5 g of water distilled off. The vacuum was then broken with air, Feed 5 was added and the reaction mixture was cooled to RT. A viscous yellow solution with a solids content of 20.7% was obtained. The K value of the terpolymer was 87 (0.5% by weight in a 5% by weight aqueous NaCl solution). Starting polymer VE13: Terpolymer (VFA / MA / DADMAC = 65% mole / 30% mole / 5% mole) A mixture of 138.7 g VFA (99%) and 200.0 g water was provided as Feed 1. 76.8 g of MA were provided as feed 2. 1.16 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 115.2 g of water at RT as feed 3. 0.70 g of 2,2'azobis(2-methylpropionamidine) dihydrochloride was dissolved in 69.2 g of water at RT as 111 feeding 4. 174.4 g of water were provided as feed 5. 554.6 g of water and 37.0 g of a 65% by weight aqueous DADMAC solution and 2.6 g of 75% by weight phosphoric acid were placed in a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer. and nitrogen feeding tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 4.3 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 67°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. The nitrogen feed was then stopped, and during the further course of the polymerization nitrogen was continued to be passed only through the reflux condenser to avoid oxygen diffusion. At a constant internal temperature of 67 °C, all 3 feeds 1 to 3 were started at the same time. Feed 1 was fed in 3 hr, feed 2 in 3.5 hr, and feed 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 67°C. Feed 4 was then added over 5 min and the reaction mixture was held for a further 1.5 hr at 67°C. The reflux condenser was later replaced by a descending condenser and the 112 internal pressure was slowly reduced to approximately 330 mbar by means of a water jet pump so that the contents of the reactor began to boil. Under these conditions, 174.4 g of water distilled off. The vacuum was then broken with air, Feed 5 was added and the reaction mixture was cooled to RT. A viscous yellow solution with a solids content of 19.8% was obtained. The K value of the terpolymer was 82 (0.5% by weight in water). Starting polymer VE14: Terpolymer (VFA / MA / APTAC = 65% mole / 30% mole / 5% mole) 134.9 g of VFA (99%) were provided as feed 1. 74.7 g of MA were provided as feed 2. A mixture of 39.8 g of a 75% by weight aqueous solution of APTAC and 200 g of water was provided as feed 3. 1.17 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 115.3 g of water at RT as feed 4. 0.70 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 69.2 g of water at RT as feed 5. 170.9 g of water were provided as feed 6. 557.5 g of water and 2.6 g of acid were introduced 113 75% by weight phosphoric in a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 4.3 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 69°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to prevent oxygen diffusion. At a constant internal temperature of 69°C, all 4 feeds 1 to 4 were started at the same time. Feed 1 was fed in 3 hr, feed 2 in 3.5 hr, and feed 4 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 69°C. Feed 4 was then added over 5 min and the reaction mixture was held for a further 1.5 hr at 69°C. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 330 mbar by means of a water jet pump so that the reactor contents began to boil. Under these conditions, 170.9 g of water distilled off. The vacuum was then broken with air, and 114 feed 5 and the reaction mixture was cooled to RT. A viscous yellow solution with a solids content of 19.6% was obtained. The K value of the terpolymer was 87 (0.5% by weight in water). Starting polymer VE15: Terpolymer (VFA / MA / Na acrylate = 70% mole / 15% mole / 15% mole) As feed 1, a mixture of 133.1 g of 32% by weight aqueous sodium acrylate solution, adjusted to pH 6.5, 151.7 g of VFA (99%) and 200.0 g of water was provided. 45.3 g of EA were provided as feed 2. 1.14 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 112.7 g of water at RT as feed 3. 0.68 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 67.6 g of water at RT as feed 4. 537.8 g of water were provided as feed 5. 481.0 g of water and 2.6 g of 75% by weight phosphoric acid were placed in a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm, approximately 4.1 g of a 115 25% by weight sodium hydroxide solution, giving a pH of 6.5. The receiver was then heated for 30 min at 72°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to avoid diffusion of oxygen. At a constant internal temperature of 72°C, all 3 feeds 1 to 3 were started at the same time. Feed 1 was fed in 3 hr, feed 2 in 3.5 hr, and feed 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 72°C. Feed 4 was then added over 5 min and the reaction mixture was held for a further 1.5 hr at 72°C. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 340 mbar by means of a water jet pump so that the reactor contents began to boil. Under these conditions, 137.8 g of water distilled off. The vacuum was then broken with air, Feed 5 was added and the reaction mixture was cooled to RT. A viscous yellow solution, slightly cloudy, with a solids content of 15.1% was obtained. The K value of the terpolymer was (0.5% by weight in a 5% by weight aqueous NaCl solution). ΙνΙΛ / Ε / ΖνΖΊ / υΖΊ O4U 116 Starting polymer VE16: Terpolymer (VFA / EA / Na acrylate = 70% mole / 20% mole / 10% mole) As feed 1, a mixture of 55.3 g of 32% by weight aqueous sodium acrylate solution, adjusted to pH 6.5, 94.5 g of VFA (99%) and 200.0 g of water was provided. 37.6 g of EA were provided as feed 2. 0.72 g of 2,2'azobis(2-methylpropionamidine) dihydrochloride was dissolved in 71.6 g of water at RT as feed 3. 0.43 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 43.0 g of water at RT as feed 4. 612.8 g of water and 1.6 g of 75% by weight phosphoric acid were placed in a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 2.4 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 65°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Next, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to 117 prevent diffusion of oxygen. At a constant internal temperature of 65°C, 10% of Feed 1 was first added in 3 minutes and mixed briefly. The remainder of feed 1 (90%) and feeds 2 and 3 were started simultaneously. The remainder of Feed 1 was fed in 3 hr, Feed 2 in 3.5 hr, and Feed 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 65°C. Feed 4 was then added over 5 min and the reaction temperature was increased to 70°C. The batch was held at 70°C for 1.5 hr. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 340 mbar by means of a water jet pump so that the contents of the reactor began to boil. Under these conditions, 114.1 g of water distilled off. The vacuum was then broken with air and the reaction mixture was cooled to RT. A viscous yellow solution, slightly cloudy, with a solids content of 15.2% was obtained. The K value of the terpolymer was 99 (0.5% by weight in a 5% by weight aqueous NaCl solution). Starting polymer VE17: Terpolymer (VFA / EA / Na acrylate = 70% mole / 20% mole / 10% mole) As feed 1, a mixture of 55.3 g of aqueous solution of sodium acrylate at 32% by weight, adjusted 118 at pH 6.5, 94.5 g of VFA (99%) and 200.0 g of water. 37.6 g of EA were provided as feed 2. 0.72 g of 2,2'azobis(2-methylpropionamidine) dihydrochloride was dissolved in 71.6 g of water at RT as feed 3. 0.43 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 43.0 g of water at RT as feed 4. 612.8 g of water and 1.6 g of 75% by weight phosphoric acid were placed in a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 2.4 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 64°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to prevent oxygen diffusion. At a constant internal temperature of 64°C, 10% of Feed 1 was first added in 3 minutes and mixed briefly. The remainder of feeding 1 (90%) and feedings 2 and 3 were started 119 simultaneously. The remainder of Feed 1 was fed in 3 hr, Feed 2 in 3.5 hr, and Feed 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 64°C. Feed 4 was then added over 5 min and the reaction temperature was increased to 70°C. The batch was held at 70°C for 1.5 hr. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 340 mbar by means of a water jet pump so that the contents of the reactor began to boil. Under these conditions, 138.7 g of water distilled off. The vacuum was then broken with air and the reaction mixture was cooled to RT. A viscous yellow solution, slightly cloudy, with a solids content of 15.6% was obtained. The K value of the terpolymer was 103 (0.5% by weight in a 5% by weight aqueous NaCl solution). Starting polymer VE18: Terpolymer (VFA / EA / Na acrylate = 70% mole / 20% mole / 10% mole) As feed 1, a mixture of 55.3 g of 32% by weight aqueous sodium acrylate solution, adjusted to pH 6.5, 94.5 g of VEA (99%) and 200.0 g of water was provided. 37.6 g of EA were provided as feed 2. 0.72 g of 2,2'azobis(2-methylpropionamidine) dihydrochloride was dissolved in 71.6 g of water at RT as 120 power 3. 0.43 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 43.0 g of water at RT as feed 4. 612.8 g of water and 1.6 g of 75% by weight phosphoric acid were placed in a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 2.6 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 65°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to avoid diffusion of oxygen. At a constant internal temperature of 65°C, 10% of Feed 1 was first added in 3 minutes and mixed briefly. The remainder of feed 1 (90%) and feeds 2 and 3 were started simultaneously. The remainder of Feed 1 was fed in 3 hr, Feed 2 in 3.5 hr, and Feed 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 65°C. Feed 4 was then added 121 in 5 min and the reaction temperature was increased to 70°C. The batch was held at 70°C for 1.5 hr. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 340 mbar by means of a water jet pump so that the contents of the reactor began to boil. Under these conditions, 126.7 g of water distilled off. The vacuum was then broken with air and the reaction mixture was cooled to RT. A viscous yellow solution, slightly cloudy, with a solids content of 15.4% was obtained. The K value of the terpolymer was 101 (0.5% by weight in a 5% by weight aqueous NaCl solution). IVIA / t / ZUZ I / UZ 104U Starting polymer VE19: Copolymer (VFA / MA = 70% mole / 30% mole) 150.4 g of VFA (99%) were provided as feed 1. 77.3 g of MA were provided as feed 2. 1.13 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 112.1 g of water at RT as feed 3. 0.67 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 67.2 g of water at RT as feed 4. 168.4 g of water were provided as feed 5. 122 784.9 g of water and 2.8 g of 75% by weight phosphoric acid were placed in a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 3.9 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 70°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. The nitrogen feed was then stopped, and during the further course of the polymerization nitrogen was continued to be passed only through the reflux condenser to avoid oxygen diffusion. At a constant internal temperature of 70°C, all 3 feeds 1 to 3 were started at the same time. Feed 1 was fed in 3 hr, feed 2 in 3.5 hr, and feed 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 70°C. Feed 4 was then added over 5 min and the reaction mixture was held for a further 1.5 hr at 70°C. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 320 mbar by means of a water jet pump so that the reactor contents began to boil. Under these conditions, nfrQLzn / Lznz / q / Yi 123 distilled off 168.4 g of water. The vacuum was then broken with air, Feed 5 was added and the reaction mixture was cooled to RT. A viscous yellow solution with a solids content of 18.6% was obtained. The K value of the copolymer was 82 (0.5% by weight in water). Starting polymer VE20: Copolymer (VFA / MA = 60% mole / 40% mole) 126.4 g of VFA (99%) were provided as feed 1. 101.0 g of MA were provided as feed 2. 1.13 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 112.0 g of water at RT as feed 3. 0.68 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 67.2 g of water at RT as feed 4. 188.5 g of water were provided as feed 5. 785.2 g of water and 2.5 g of 75% by weight phosphoric acid were introduced into a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. to one At a speed of 100 rpm approximately 3.9 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 67°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to prevent oxygen diffusion. At a constant internal temperature of 67°C, all 3 feeds 1 to 3 were started at the same time. Feed 1 was fed in 3 hr, feed 2 in 3.5 hr, and feed 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 67°C. Feed 4 was then added over 5 min and the reaction mixture was held for a further 1.5 hr at 67°C. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 300 mbar by means of a water jet pump so that the reactor contents began to boil. Under these conditions, 188.5 g of water distilled off. The vacuum was then broken with air, Feed 5 was added and the reaction mixture was cooled to RT. A viscous yellow solution with a solids content of 18.7% was obtained. The K value of the copolymer was 84 (0.5% by weight in water). IVIA / t / ZUZ I / UZ 104U 125 Starting polymer VE21: Copolymer (VFA / MA = 80% mole / 20% mole) 175.4 g of VFA (99%) were provided as feed 1. 52.6 g of MA were provided as feed 2. 1.13 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 112.0 g of water at RT as feed 3. 0.68 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 67.2 g of water at RT as feed 4. 163.6 g of water were provided as feed 5. 784.7 g of water and 2.5 g of 75% by weight phosphoric acid were introduced into a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 3.9 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 69°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped, and during the further course of the polymerization only nitrogen was continued to be conducted. 126 through the reflux condenser to prevent diffusion of oxygen. At a constant internal temperature of 69°C, all 3 feeds 1 to 3 were started at the same time. Feed 1 was fed in 3 hr, feed 2 in 3.5 hr, and feed 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 69°C. Feed 4 was then added over 5 min and the reaction mixture was held for a further 1.5 hr at 69°C. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 310 mbar by means of a water jet pump so that the reactor contents began to boil. Under these conditions, 163.6 g of water distilled off. The vacuum was then broken with air, Feed 5 was added and the reaction mixture was cooled to RT. A viscous yellow solution with a solids content of 19.0% was obtained. The K value of the copolymer was 84 (0.5% by weight in water). ΜΛ / t / ZUZ1 / UZ1 04U Starting polymer VE22: Terpolymer (VFA / MA / Na acrylate = 70% mole / 25% mole / 5% mole) As feed 1, a mixture of 46.1 g of 32% by weight aqueous sodium acrylate solution, adjusted to pH 6.5, 157.5 g of VFA (99%) and 200.0 g of water was provided. 67.4 g of MA were provided as feed 2. 127 1.17 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 116.1 g of water at RT as feed 3. 0.70 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 69.7 g of water at RT as feed 4. 552.6 g of water were provided as feed 5. 534.7 g of water and 2.6 g of 75% by weight phosphoric acid were placed in a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 4.2 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 74°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to prevent oxygen diffusion. At a constant internal temperature of 74°C, all 3 feeds 1 to 3 were started at the same time. Feed 1 was fed in 3 hr, feed 2 in 3.5 hr, and feed 3 in 4 hr. At the end of feed 3, the batch was held for one more hour. 128 to 74°C. Feed 4 was then added over 5 min and the reaction mixture was held for a further 1.5 hr at 74°C. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 300 mbar by means of a water jet pump so that the reactor contents began to boil. Under these conditions, 152.6 g of water distilled off. The vacuum was then broken with air, Feed 5 was added and the reaction mixture was cooled to ΤΆ. A slightly viscous yellow solution with a solids content of 14.5% was obtained. The K value of the terpolymer was 81 (0.5% by weight in a 5% by weight aqueous NaCl solution). Starting polymer VE23: Terpolymer (VFA / EA / Na acrylate = 70% mole / 25% mole / 5% mole) As feed 1, a mixture of 44.0 g of 32% by weight aqueous sodium acrylate solution, adjusted to pH 6.5, 150.6 g of VFA (99%) and 200.0 g of water was provided. 186.9 g of EA were provided as feed 2. 1.17 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 116.1 g of water at RT as feed 3. 0.70 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 69.7 g of water at RT as 129 feeding 4. 536.0 g of water and 2.6 g of 75% by weight phosphoric acid were placed in a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 4.1 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 67°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to prevent oxygen diffusion. At a constant internal temperature of 67°C, 10% of Feed 1 was first added in 3 minutes and mixed briefly. The remainder of feed 1 (90%) and feeds 2 and 3 were started simultaneously. The remainder of Feed 1 was fed in 3 hr, Feed 2 in 3.5 hr, and Feed 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 67°C. Feed 4 was then added over 5 min. The batch was kept at 67 °C for 1.5 hr. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to 130 about 320 mbar by means of a water jet pump so that the contents of the reactor began to boil. Under these conditions, 186.9 g of water distilled off. The vacuum was then broken with air and the reaction mixture was cooled to RT. A viscous yellow solution, slightly cloudy, with a solids content of 19.9% ​​was obtained. The K value of the terpolymer was 90 (0.5% by weight in a 5% by weight aqueous NaCl solution). Starting polymer VE24: Terpolymer (VFA / EA / Na acrylate = 70% mole / 20% mole / 10% mole) As feed 1, a mixture of 88.4 g of 32% by weight aqueous sodium acrylate solution, adjusted to pH 6.5, 151.1 g of VEA (99%) and 200.0 g of water was provided. 60.2 g of EA were provided as feed 2. 1.16 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 114.4 g of water at RT as feed 3. 0.69 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 68.6 g of water at RT as feed 4. 158.4 g of water were provided as feed 5. 508.6 g of water and 2.6 g of 75% by weight phosphoric acid were introduced into a 2 1 glass apparatus with 131 anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 4.1 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 67°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to prevent oxygen diffusion. At a constant internal temperature of 67°C, feeds 1, 2 and 3 were started at the same time. Feed 1 was fed in 3 hr, feed 2 in 3.5 hr, and feed 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 67°C. Feed 4 was then added over 5 min and the reaction mixture was held for a further 1.5 hr at 67°C. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 300 mbar by means of a water jet pump so that the reactor contents began to boil. Under these conditions, 158.4 g of water distilled off. The vacuum was then broken with air and the reaction mixture was cooled to RT. 132 A cloudy, yellow, viscous solution with a solids content of 20.1% was obtained. The K value of the terpolymer was 99 (0.5% by weight in a 5% by weight aqueous NaCl solution). Starting polymer VE25: Terpolymer (VFA / EA / Na acrylate = 70% mole / 10% mole / 20% mole) As feed 1, a mixture of 178.2 g of 32% by weight aqueous sodium acrylate solution, adjusted to pH 6.5, 152.3 g of VFA (99%) and 200.0 g of water was provided. 30.3 g of EA were provided as feed 2. 1.12 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 111.0 g of water at RT as feed 3. 0.67 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 66.5 g of water at RT as feed 4. 185.7 g of water were provided as feed 5. 453.2 g of water and 2.6 g of 75% by weight phosphoric acid were placed in a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm, approximately 4.1 g of a 133 25% by weight sodium hydroxide solution, giving a pH of 6.5. The receiver was then heated for 30 min at 68°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to prevent oxygen diffusion. At a constant internal temperature of 68°C, feeds 1, 2 and 3 were started at the same time. Feed 1 was fed in 3 hr, feed 2 in 3.5 hr, and feed 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 68°C. Feed 4 was then added over 5 min and the reaction mixture was held for a further 1.5 hr at 68°C. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 310 mbar by means of a water jet pump so that the reactor contents began to boil. Under these conditions, 185.74 g of water distilled off. The vacuum was then broken with air and the reaction mixture was cooled to RT. A cloudy, yellow, viscous solution with a solids content of 20.3% was obtained. The K value of the terpolymer was 101 (0.5% by weight in a 5% by weight aqueous NaCl solution). 134 Starting polymer VE26: Terpolymer (VFA / EA / Na acrylate = 70% mole / 20% mole / 10% mole) As feed 1, a mixture of 55.3 g of 32% by weight aqueous sodium acrylate solution, adjusted to pH 6.5, 94.5 g of VEA (99%) and 200.0 g of water was provided. 37.6 g of EA were provided as feed 2. 0.72 g of 2,2'azobis(2-methylpropionamidine) dihydrochloride was dissolved in 71.6 g of water at RT as feed 3. 0.43 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 43.0 g of water at RT as feed 4. 612.8 g of water and 1.6 g of 75% by weight phosphoric acid were placed in a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 2.4 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 65°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Next, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to 135 prevent diffusion of oxygen. At a constant internal temperature of 65°C, 10% of Feed 1 was first added in 3 minutes and mixed briefly. The remainder of feed 1 (90%) and feeds 2 and 3 were started simultaneously. The remainder of Feed 1 was fed in 3 hr, Feed 2 in 3.5 hr, and Feed 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 65°C. Feed 4 was then added over 5 min and the reaction temperature was increased to 70°C. The batch was held at 70°C for 1.5 hr. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 300 mbar by means of a water jet pump so that the reactor contents began to boil. Under these conditions, 120.5 g of water distilled off. The vacuum was then broken with air and the reaction mixture was cooled to RT. A viscous yellow solution, slightly cloudy, with a solids content of 15.1% was obtained. The K value of the terpolymer was 102 (0.5% by weight in a 5% by weight aqueous NaCl solution). IVIA / t / ZUZ I / UZ 104U Starting polymer VE27: Terpolymer (VFA / MA / AM = 70% mole / 25% mole / 5% mole) A mixture of 22.6 g of 50% by weight aqueous AM solution, 159.9 g of VFA (99%) and 136 210.0 g of water. 68.5 g of MA were provided as feed 2. 1.19 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 117.9 g of water at RT as feed 3. 0.71 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 70.7 g of water at RT as feed 4. 189.6 g of water were provided as feed 5. 541.8 g of water and 2.6 g of 75% by weight phosphoric acid were placed in a 2 1 glass apparatus with anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 4.1 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 69°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to prevent oxygen diffusion. At a constant internal temperature of 69°C, all 3 feeds 1 to 3 were started at the same time. Feed 1 was fed in 3 hr, the 137 feeding 2 in 3.5 hr and feeding 3 in 4 hr. At the end of feed 3, the batch was held for an additional hour at 69°C. Feed 4 was then added over 5 min and the reaction mixture was held for a further 1.5 hr at 69°C. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 310 mbar by means of a water jet pump so that the reactor contents began to boil. Under these conditions, 189.6 g of water distilled off. The vacuum was then broken with air, Feed 5 was added and the reaction mixture was cooled to RT. A viscous yellow solution with a solids content of 21.9% was obtained. The K value of the terpolymer was 89 (0.5% by weight in water). Starting polymer W1: Copolymer (VFA / Na acrylate = 70 mol% / 30 mol%) As feed 1, a mixture of 316.7 g of 32% by weight aqueous sodium acrylate solution, 180.5 g of VFA (99%) and 141.0 g of water was provided. 1.79 g of 2,2'-azobis(2-methylpropionamidine) dihydrochloride was dissolved in 17 6.9 g of water at RT as feed 2. 573.4 g of water and 3.0 g of 75% by weight phosphoric acid were introduced into a 2 1 glass apparatus with 138 anchor stirrer, reflux condenser, internal thermometer, and nitrogen feed tube. The reactor was located in a water bath with a heating-cooling unit, which automatically controlled the internal temperature. At a speed of 100 rpm approximately 5.2 g of a 25% by weight sodium hydroxide solution was added, giving a pH of 6.5. The receiver was then heated for 30 min at 80°C and at the same time nitrogen (20 L / hr) was introduced to displace oxygen in the apparatus. Subsequently, the nitrogen feed was stopped and nitrogen was continued to be passed only through the reflux condenser to avoid diffusion of oxygen. At a constant internal temperature of 80°C, feeds 1 and 2 were started at the same time. Feed 1 was fed in 1.5 hr and feed 2 in 2.5 hr. At the end of feed 2, the batch was held for an additional hour at 80°C. The reflux condenser was then replaced by a descending condenser and the internal pressure was slowly reduced to approximately 460 mbar by means of a water jet pump so that the contents of the reactor began to boil. Under these conditions, 178.7 g of water distilled off. The vacuum was then broken with air and the reaction mixture was cooled to RT. A yellowish viscous solution with a solids content of 24.1% was obtained. The K value of the copolymer was 88 (0.5% by weight in 5% aqueous NaCl solution). 139 A-3) Production of the final polymers by hydrolysis of the starting polymers Final polymer AE1: Starting polymer hydrolyzed in acid VE1 (VFA / MA = 70% mol / 30% mol) 150.1 g of the obtained polymer solution were mixed with the starting polymer VE1 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.3 g of a 40% by weight aqueous sodium bisulfite solution and then heated to 80°C. Next, 30.0 g of 37% by weight hydrochloric acid (120 mol% on VFA) was added. The mixture was kept for 5 hrs at 80°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 64.8 g of 25% by weight sodium hydroxide solution. A slightly cloudy, yellowish and viscous polymer solution with a polymer content of 8.3% was obtained. The degree of HA hydrolysis was 98 mol% and the degree of HE conversion was 100 mol%. Final polymer AE2: alkaline hydrolyzed starting polymer VE2 (VFA / MA = 70% mole / 30% mole) 170.5 g of the polymer solution obtained were mixed with the starting polymer VE2 in a four-tube flask. 140 500 mL necks with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.5 g of a 40% by weight aqueous sodium bisulfite solution and then heated to 80° c. Next, 56.3 g of a 25% by weight aqueous sodium hydroxide solution (120 mol% on VFA) were added. The mixture was kept for 5 hrs at 80°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 20.1 g of 37% by weight hydrochloric acid and 1.3 g of water. A slightly cloudy, yellowish and viscous polymer solution with a polymer content of 7.9% was obtained. The degree of HA hydrolysis was 96 mol% and the degree of HE conversion was 100 mol%. Final polymer AE3: alkaline hydrolyzed starting polymer VE3 (VFA / MA / Na acrylate = 70% mol / 29% mol / 1% mol) 173.4 g of the obtained polymer solution were mixed with the starting polymer VE3 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.6 g of a 40% by weight aqueous solution of sodium bisulfite and 55.0 g of water and then heated to 80°C. Next, 59.3 g of a 25% by weight aqueous sodium hydroxide solution (120% 141 molar on VFA). The mixture was kept for 5 hrs at 80°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 21.7 g of 37% by weight hydrochloric acid and 9.4 g of water. A slightly cloudy, yellowish and viscous polymer solution with a polymer content of 7.7% was obtained. The degree of HA hydrolysis was 99 mol% and the degree of HE conversion was 100 mol%. Final polymer AE4: Alkali hydrolyzed terpolymer VE4 (VFA / MA / Na acrylate = 70% mol / 28% mol / 2% mol) 174.1 g of the obtained polymer solution were mixed with the starting polymer VE4 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.6 g of a 40% by weight aqueous solution of sodium bisulfite and 54.0 g of water and then heated to 80°C. Next, 58.8 g of a 25% by weight aqueous sodium hydroxide solution (120 mol% on VFA) were added. The mixture was kept for 5 hrs at 80°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 22.5 g of 37% by weight hydrochloric acid and 7.0 g of water. A slightly cloudy, yellowish and viscous polymer solution with a polymer content of 7.7% was obtained. The degree of HA hydrolysis was 98 mol% and the degree of HE conversion was 100 mol%. 142 Final polymer AE5: VE5 hydrolyzed alkaline terpolymer (VFA / MA / Na acrylate = 70% mol / 25% mol / 5% mol) 173.6 g of the obtained polymer solution were mixed with the starting polymer VE5 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.6 g of a 40% by weight aqueous solution of sodium bisulfite and 62.0 g of water and then heated to 80°C. Next, 58.5 g of a 25% by weight aqueous sodium hydroxide solution (120 mol% on VFA) were added. The mixture was kept for 5 hrs at 80°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 23.8 g of 37% by weight hydrochloric acid. A slightly cloudy, yellowish and viscous polymer solution with a polymer content of 7.6% was obtained. The degree of HA hydrolysis was 99 mol% and the degree of HE conversion was 100 mol%. Final polymer AE6: Alkaline hydrolyzed terpolymer VE6 (VFA / MA / Na acrylate = 70 molar% / 25 molar% / 5 molar%) 149.9 g of the obtained polymer solution were mixed with the starting polymer VE6 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.0 g of an aqueous solution of 143 40% by weight sodium bisulfite and 136.0 g of water and then heated to 80°C. Next, 36.2 g of a 25% by weight aqueous sodium hydroxide solution (120 mol% on VFA) were added. The mixture was kept for 5 hrs at 80°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 13.7 g of 37% by weight hydrochloric acid and 7.5 g of water. A slightly cloudy, yellowish and viscous polymer solution with a polymer content of 4.5% was obtained. The degree of HA hydrolysis was 93 mol% and the degree of HE conversion was 100 mol%. Final polymer AE7: Alkaline hydrolyzed terpolymer VE7 (VFA / MA / Na acrylate = 70% mol / 20% mol / 10% mol) 170.4 g of the obtained polymer solution were mixed with the starting polymer VE7 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.6 g of a 40% by weight aqueous sodium bisulfite solution and 57.0 g of water and then heated to 80°C. Next, 58.90 g of a 25% by weight aqueous sodium hydroxide solution (120 mol% on VFA) were added. The mixture was kept for 5 hrs at 80°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 25.1 g of 37% by weight hydrochloric acid and 4.5 g of water. A polymer solution slightly 144 cloudy, yellowish and viscous with a polymer content of 7.5%. The degree of HA hydrolysis was 99 mol% and the degree of HE conversion was 100 mol%. Final polymer AE8: VE8 alkaline hydrolyzed terpolymer (VFA / MA / Na acrylate = 70% mole / 15% mole / 15% mole) 171.0 g of the obtained polymer solution were mixed with the starting polymer VE8 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.6 g of a 40% by weight aqueous solution of sodium bisulfite and 63.0 g of water and then heated to 80°C. Next, 57.8 g of a 25% by weight aqueous sodium hydroxide solution (120 mol% on VFA) were added. The mixture was kept for 5 hrs at 80°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 27.5 g of 37% by weight hydrochloric acid. A slightly cloudy, yellowish and viscous polymer solution with a polymer content of 7.5% was obtained. The degree of HA hydrolysis was 94 mol% and the degree of HE conversion was 100 mol%. Final polymer AE9: Alkaline hydrolyzed terpolymer VE9 (VFA / MA / Na acrylate = 70 molar% / 10 molar% / 20 molar%) 177.9 g of the polymer solution were mixed 145 obtained with the starting polymer VE9 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.7 g of an aqueous sodium bisulfite solution. 40% by weight sodium and 65.0 g of water and then heated to 80°C. Next, 61.5 g of a 25% by weight aqueous sodium hydroxide solution (120 mol% on VEA) were added. The mixture was kept for 5 hrs at 80°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 31.3 g of 37% by weight hydrochloric acid and 1.8 g of water. A slightly cloudy, yellowish and viscous polymer solution with a polymer content of 7.2% was obtained. The degree of HA hydrolysis was 99 mol% and the degree of HE conversion was 100 mol%. Final polymer AE10: Alkaline hydrolyzed terpolymer VE10 (VFA / MA / Na acrylate = 70% mol / 25% mol / 5% mol) 170.2 g of the VE10 polymer solution obtained above in a 500-mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser were mixed at a stirring speed of 80 rpm with 1.5 g of a solution mixture of 40% by weight aqueous sodium bisulfite and 50.0 g of water and then heated to 80°C. Next, 56.3 g of an aqueous solution of 146 25% by weight sodium hydroxide (120 mol% on VFA). The mixture was kept for 5 hrs at 80°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 22.2 g of 37% by weight hydrochloric acid and 8.4 g of water. A slightly cloudy, yellowish and viscous polymer solution with a polymer content of 7.2% was obtained. The degree of HA hydrolysis was 97 mol% and the degree of HE conversion was 100 mol%. Final polymer AE11: Alkaline hydrolyzed terpolymer VE11 (VFA / MA / Na A <PS = 70% mol / 25% mol / 5% mol) 172.1 g of the obtained polymer solution were mixed with the starting polymer VE11 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.5 g of a 40% by weight aqueous sodium bisulfite solution and 65.5 g of water and then heated to 80°C. Next, 55.9 g of a 25% by weight aqueous sodium hydroxide solution (120 mol% on VFA) were added. The mixture was kept for 5 hrs at 80°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 22.7 g of 37% by weight hydrochloric acid and 7.8 g of water. A slightly cloudy, yellowish and viscous polymer solution with a polymer content of 7.5% was obtained. The degree of HA hydrolysis was 94% molar and the degree of 147 HE conversion was 100 mole %. Final polymer AE12: Alkaline hydrolyzed terpolymer VE12 (VFA / MA / Na vinylsulfonate = 70% mol / 25% mol / 5% mol) 178.5 g of the obtained polymer solution were mixed with the starting polymer VE12 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.7 g of a 40% by weight aqueous solution of sodium bisulfite and 75.0 g of water and then heated to 80°C. Next, 62.8 g of a 25% by weight aqueous sodium hydroxide solution (120 mol% on VFA) were added. The mixture was kept for 5 hrs at 80°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 25.4 g of 37% by weight hydrochloric acid and 5.6 g of water. A slightly cloudy, yellowish and viscous polymer solution with a polymer content of 7.7% was obtained. The degree of HA hydrolysis was 98 mol% and the degree of HE conversion was 100 mol%. Final polymer AE13: Alkaline hydrolyzed terpolymer VE13 (VFA / MA / DADMAC = 65% mol / 30% mol / 5% mol) 177.6 g of the obtained polymer solution were mixed with the starting polymer VE13 in a four-tube flask. 148 500 mL necks with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.5 g of a 40% by weight aqueous sodium bisulfite solution and 70.0 g of water and then was heated to 80°C. Next, 53.8 g of a 25% by weight aqueous sodium hydroxide solution (120 mol% on VFA) were added. The mixture was kept for 1 hr at 80°C. The product obtained could no longer be stirred. The test ended. Final polymer AE14: Alkaline hydrolyzed terpolymer VE14 (VFA / MA / APTAC = 65% mol / 30% mol / 5% mol) 178.0 g of the obtained polymer solution were mixed with the starting polymer VE14 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.4 g of a 40% by weight aqueous solution of sodium bisulfite and 60.0 g of water and then heated to 80°C. Next, 51.8 g of a 25% by weight aqueous sodium hydroxide solution (120 mol% on VFA) were added. The mixture was kept for 5 hrs at 80°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 18.1 g of 37% by weight hydrochloric acid and 19.1 g of water. A slightly cloudy, yellowish and viscous polymer solution with a polymer content of 7.5% was obtained. The degree of HA hydrolysis was 95 mol% and the degree of 149 HE conversion was 100 mol%. Final polymer AE15: Alkaline hydrolyzed terpolymer VE15 (VFA / EA / Na acrylate = 70% mol / 15% mol / 15% mol) 222.5 g of the obtained polymer solution were mixed with the starting polymer VE15 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.5 g of a 40% by weight aqueous solution of sodium bisulfite and 10.0 g of water and then heated to 80°C. Next, 56.3 g of a 25% by weight aqueous sodium hydroxide solution (120 mol% on VFA) were added. The mixture was kept for 5 hrs at 80°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 25.6 g of 37% by weight hydrochloric acid and 1.1 g of water. A polymer solution slightly cloudy, yellowish and viscous. Polymer content: 7.5% Formate content FA: 91.4 mmol / 100 g Degree of hydrolysis HA: 98 mol% Degree of conversion HE: 100% mol Charge density LD: 64.0 mmol / 100 g Viscosity (20 1 / min, RV , spindle 3) : 185 mPas FAD (13C-NMR, 152.3 ppm) : 1.11 150 FFA (13C-NMR, 164-167ppm) : VFA°: EA°: Na-AS° 93.7mmol / 100g 20.0mmol / 100g 20.0mmol / 100g. Final polymer AE16: Alkaline hydrolyzed terpolymer VE16 (VFA / MA / Na acrylate = 70% mol / 20% mol / 10% mol) 652.7 g of the obtained polymer solution were mixed with the starting polymer VE16 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 4.5 g of a 40% by weight aqueous sodium bisulfite solution and 185.3 g of water and then heated to 80°C. Next, 165.3 g of a 25% by weight aqueous sodium hydroxide solution (120 mol% on VFA) were added. The mixture was kept for 6 hrs at 80°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 70.2 g of 37% by weight hydrochloric acid and 12.7 g of water. A slightly cloudy, yellowish and viscous polymer solution was obtained. Polymer content: 6.6% FA formate content: 74.0 mmol / 100 g Degree of hydrolysis HA: 94 mol% HE conversion rate: 100 mol% 151 LD Charge Density: 51.3 mmol / 100 g Viscosity (20 1 / min, RV, Spindle 3) FAD (13C-NMR, 152.3 ppm): FFA (13C-NMR, 164-167 ppm) : VFA° 268 mPas 1.86 2.78 79.5 mmol / 100 g EA°: 22.7 mmol / 100 g Na-AS°: 11.4 mmol / 100 g. Final polymer AE17: Alkaline hydrolyzed terpolymer VE17 (VFA / MA / Na acrylate = 70% mol / 20% mol / 10% mol) 249.5 g of the obtained polymer solution were mixed with the starting polymer VE17 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.8 g of a 40% by weight aqueous solution of sodium bisulfite and 20.0 g of water and then heated to 80°C. Next, 53.9 g of a 25% by weight aqueous sodium hydroxide solution (100 mol% on VFA) were added. The mixture was kept for 6 hrs at 80°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 20.7 g of 37% by weight hydrochloric acid. A slightly cloudy, yellowish and viscous polymer solution was obtained. Polymer content: 8.4% 152 Formate content FA: 83.4 mmol / 100 g Degree of hydrolysis HA: 85 mol% Degree of conversion HE: 100% mol Charge density LD: 56.7 mmol / 10 0 g Viscosity (50 1 / min, RV, spindle 3) 1172 mPas FAD (13C-NMR, 152.3 ppm): 0.90 FFA (13C-NMR, 164-167 ppm) 3.82 VFA°: 98.3 mmol / 100 g EA°: 28.1 mmol / 100 g Na-AS°: 14.0 mmol / 100 g Final polymer AE18: Alkaline hydrolyzed terpolymer VE18 (VFA / MA / Na acrylate = 70% mol / 20% mol / 10% mol) 248.8 g of the obtained polymer solution were mixed with the starting polymer VE18 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.7 g of a 40% by weight aqueous solution of sodium bisulfite and 20.0 g of water and then heated to 50°C. Next, 63.7 g of a 25% by weight aqueous sodium hydroxide solution (120 mol% on VFA) were added. The mixture was kept for 24 hrs at 50°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 27.9 g of 37% by weight hydrochloric acid. 153 A slightly cloudy, yellowish and viscous polymer solution was obtained. Polymer content: 8.2% Formate content FA: 88.2 mmol / 100 g Degree of hydrolysis HA: 91 mol% Degree of conversion HE: 100% mol Charge density LD: 67.7 mmol / 100 g Viscosity (50 1 / min, RV , spindle 3) 866 mPas FAD (13C-NMR, 152.3 ppm): 0.77 FEA (13C-NMR, 164-167 ppm) : 3.14 VEA0: 97.7 mmol / 100 g EA°: 27.9 mmol / 100 g Na-AS°: 14.0mmol / 100g Final polymer AE19: Alkaline hydrolyzed copolymer VE19 (VFA / MA = 70% mol / 30% mol) 121.3 g of the obtained polymer solution were mixed with the starting polymer VE19 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.1 g of a 40% by weight aqueous sodium bisulfite solution and then heated to 80°C. Next, 39.5 g of a 25% by weight aqueous sodium hydroxide solution (120 mol% on VEA) were added. The mixture was kept for 5 hrs at 80°C. The product obtained is 154 cooled to RT and adjusted to pH 6.0 by adding 14.5 g of 37% by weight hydrochloric acid. A slightly cloudy, yellowish and viscous polymer solution was obtained. Polymer content: 7.9% Formate content FA: 97.5 mmol / 100 g Degree of hydrolysis HA: 99 molar% Degree of conversion HE: 10 0 % no1 Charge density LD: 64.3 inmol / 10 0 g Viscosity (20 1 / min , RV, spindle 3) 794 mPas FAD (13C-NMR, 152.3 ppm) : 10.0 FFA (13C-NMR, 164-167 ppm) < 0.01 VEA0: 98.8 mmol / 100 g MA°: 42.3 mmol / 100 g. Final polymer AE20: Alkaline hydrolyzed copolymer VE20 (VFA / MA = 60% mol / 40% mol) 180.0 g of the obtained polymer solution were mixed with the starting polymer VE20 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.3 g of a 40% by weight aqueous sodium bisulfite solution and then heated to 80°C. Next, 51.4 g of a 25% by weight aqueous sodium hydroxide solution (125 mol% on VFA) were added. The 155 mixture was kept for 5 hr at 80°C. The product obtained is cooled to RT and adjusted to pH 6.0 by adding 14.2 g of 37% by weight hydrochloric acid and 10.4 g of water. A cloudy, yellowish and viscous solution was obtained. Polymer content: polymer slightly 8.3% Formate content FA: Degree of hydrolysis HA: Degree of conversion HE: 76.5 mmol / 100 94% mole 10 0 % mo1 g Charge density LD: 34.0 mmol / 100 g Viscosity (20 1 / min, RV, spindle 3 FAD (13C-NMR, 152.3 ppm): FEA (13C-NMR, 164-167 ppm) : ) 2320 mPas 5.1 0.9 VEA0: 98.8 mmol / 100 g MA°: 42.3 mmol / 100 g. Final polymer ΆΕ21: Alkaline hydrolyzed copolymer VE21 (VFA / MA = 80% mole / 20% mole) 197.6 g of the obtained polymer solution were mixed with the starting polymer VE21 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 2.1 g of a 40% by weight aqueous sodium bisulfite solution and then heated to 80°C. Next, 73.8 g of an aqueous solution of 156 25% by weight sodium hydroxide (116 mol% on VFA). The mixture was kept for 5 hrs at 80°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 32.5 g of 37% by weight hydrochloric acid and 130.2 g of water. A slightly cloudy, yellowish and viscous polymer solution was obtained. Polymer content: 7.0% Formate content FA: 105.8 mmo1 / 100 g Degree of hydrolysis HA: 98 mol% Degree of conversion HE: 100% mol Charge density LD: 79.5 mmol / 100 g Viscosity (20 1 / min, RV , spindle 3) 755 mPas FAD (13C-NMR, 152.3 ppm): 10.0 FEA (13C-NMR, 164-167 ppm) : 2.9 VFA0: 108 mmo1 / 100 g MA°: 42.3 mmol / 100 g. Final polymer AE22: VE22 alkaline hydrolyzed terpolymer (VFA / MA / Na acrylate = 70% mole / 25% mole / 5% mole) 265.8 g of the obtained polymer solution were mixed with the starting polymer VE22 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.8 g of an aqueous solution of 157 40% by weight sodium bisulfite and then heated to 80°C. Next, 67.1 g of a 25% by weight aqueous sodium hydroxide solution (120 mol% on VFA) were added. The mixture was kept for 5 hrs at 80°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 26.0 g of 37% by weight hydrochloric acid and 3.3 g of water. A slightly cloudy, yellowish and viscous polymer solution was obtained. Polymer content: 7.7% Formate content FA: 94.8 mmol / 100 g Degree of hydrolysis HA: 98 mol% Degree of conversion HE: 10 0 % mo1 Charge density LD: 66.0 mmol / 100 g Viscosity (20 1 / min, RV, spindle 3) 325 mPas FAD (13C-NMR, 152.3 ppm): 1.90 FFA (13C-NMR, 164-167 ppm) : 2.80 VFA0: 96.7 mmol / 100 g MA°: 34.6 mmol / 100 g Na- AS°: 6.9 mmo1 / 100 g. Final polymer AE23: Alkaline hydrolyzed terpolymer VE23 (VFA / EA / Na acrylate = 70% mol / 25% mol / 5% mol) 174.4 g of the obtained polymer solution were mixed with the starting polymer VE23 in a four-tube flask. 158 500 mL necks with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.6 g of a 40% by weight aqueous sodium bisulfite solution and 64.0 g of water and then was heated to 50°C. Next, 57.5 g of a 25% by weight aqueous sodium hydroxide solution (120 mol% on VFA) were added. The mixture was kept for 24 hrs at 50°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 22.7 g of 37% by weight hydrochloric acid and 6.5 g of water. A polymer solution slightly IVIA / l / U¿ 104U cloudy, yellowish and viscous. Polymer content: 7.8% Formate content FA: 89.0 mmol / 100 g Degree of hydrolysis HA: 97 mol% Degree of conversion HE: 100% mol Charge density LD: 66.9 mmol / 100 g Viscosity (50 1 / min, RV , spindle 3) 715 mPas FAD (13C-NMR, 152.3 ppm): 2.0 FFA (13C-NMR, 164-167 ppm) : 2.8 VFA0: 92.5 mmol / 100 g EA°: 33.0 mmol / 100 g Na-AS°: 6.6 mm or 1 / 100 g. 159 Final polymer AE24: Alkaline hydrolyzed terpolymer VE24 (VFA / EA / Na acrylate = 70% mol / 20% mol / 10% mol) 173.1 g of the obtained polymer solution were mixed with the starting polymer VE24 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 2.6 g of a 40% by weight aqueous sodium bisulfite solution and 65.0 g of water and then heated to 80°C. Next, 58.1 g of a 25% by weight aqueous sodium hydroxide solution (120 mol% on VFA) were added. The mixture was kept for 6 hrs at 80°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 24.6 g of 37% by weight hydrochloric acid and 6.0 g of water. A polymer solution slightly IVIA / t / ZUZ I / UZ 104U cloudy, yellowish and viscous. Polymer content: 7.7% Formate content FA: Degree of hydrolysis HA: Degree of conversion HE: 87.9 mmol / 100 96% mole 10 0 % mo1 g Charge density LD: Viscosity (20 1 / min, RV, spindle 3) FAD (13C-NMR, 152.3 ppm): FFA (13C-NMR, 164-167 ppm) : 55.0 mmol / 100 735 mPas 1.93 2.65 g SEE0: 92.85mmo1 / 100g 160 Na-AS°: 13.3mmol / 100g 26.5mmol / 100g. Final polymer AE25: Alkaline hydrolyzed terpolymer VE25 (VFA / EA / Na acrylate = 70% mol / 10% mol / 20% mol) 185.3 g of the obtained polymer solution were mixed with the starting polymer VE25 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.7 g of a 40% by weight aqueous sodium bisulfite solution and 65.0 g of water and then heated to 80°C. Next, 63.2 g of a 25% by weight aqueous sodium hydroxide solution (120 mol% on VFA) were added. The mixture was kept for 6 hrs at 80°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 31.2 g of 37% by weight hydrochloric acid and 1.3 g of water. A slightly cloudy, yellowish and viscous polymer solution was obtained. Polymer content: 7.3% FA formate content: 92.0 mmol / 100 g Degree of hydrolysis HA: 99 mole % HE conversion rate: 100 mol% LD Charge Density: 70.1 mmol / 100 g Viscosity (20 1 / min, RV, spindle 3) 535 mPas FAD (13C-NMR, 152.3 ppm) : 2.18 161 FFA (13C-NMR, 164-167 ppm) : VFA°: EA°: Na-AS°: 2.20 92.85mmo1 / 100g 26.5mmol / 100g 13.3mmol / 100g. Final polymer AE26: Alkaline hydrolyzed terpolymer VE26 (VFA / EA / Na acrylate = 70% mol / 20% mol / 10% mol) 169.1 g of the obtained polymer solution were mixed with the starting polymer VE26 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.2 g of a 40% by weight aqueous solution of sodium bisulfite and 20.0 g of water and then heated to 50°C. Next, 29.0 g of a 25% by weight aqueous sodium hydroxide solution (82 mol% on VEA) were added. The mixture was kept for 24 hrs at 50°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 10.7 g of 37% by weight hydrochloric acid and 5.3 g of water. A slightly cloudy, yellowish and viscous polymer solution was obtained. Polymer content: 7.9% FA formate content: 63.2 mmol / 100 g Degree of hydrolysis HA: 72 mol% HE conversion rate: 100 mol% 162 LD Charge Density: 39.8 mmol / 100 g Viscosity (50 1 / min, RV, Spindle 3) 594 : mPas FAD (13C-NMR, 152.3 ppm): 4.1 FFA (13C-NMR, 164-167 ppm) : 4.0 VFA °: 88.4 mmol / 100 g EA°: 25.3 mmol / 100 g Na-AS°: 12.6 mmol / 100 g. Final polymer AE27: VE18 alkaline hydrolyzed terpolymer (VFA / EA / Na acrylate = 70% mol / 20% mol / 10% mol) 1006.2 g of the polymer solution obtained with the starting polymer VE18 were mixed, under stirring, with 12 6.4 g of water in a hermetic 2L steel reactor with stirrer, internal thermometer, heating / cooling jacket, pressure gauge, relief valve pressure, reflux condenser and a pressure-tight feed vessel and heated to 107°C. A pressure of 2.8 bar was built up. 256.8 g of a 25% by weight aqueous sodium hydroxide solution (120 mol% VFA) were provided in the feed vessel. The sodium hydroxide solution was forced into the reactor at a pressure of 5 bar and mixed. A temperature of 100°C was reached and was maintained for 60 min. The reactor was then cooled down to RT as quickly as possible. 306.9 g of the product were adjusted 163 obtained at pH 6.0 by adding 26.4 g of 37% by weight hydrochloric acid and 3.7 g of water. A slightly cloudy, yellowish and viscous polymer solution was obtained. Polymer content: 7.3% Formate content FA: 90.1 mmol / 100 g Degree of hydrolysis HA: 94 mol% Degree of conversion HE: 10 0 % mo1 Charge density LD: 6 6.5 inmol / 100 g Viscosity (20 1 / min , RV, spindle 3) 1030 mPas FAD (13C-NMR, 152.3 ppm): 1.79 FFA (13C-NMR, 164-167 ppm) : 1.46 VFA°: 97.2 mmol / 100 g EA°: 27.8 mmol / 100 g Na-AS°: 13.9 mmol / 100 g. Final polymer AE28: Alkaline hydrolyzed terpolymer VE18 (VFA / EA / Na acrylate = 70% mol / 20% mol / 10% mol) 990.2 g of the polymer solution obtained with the starting polymer VE18 were mixed, under stirring, with 12 6.4 g of water in a hermetic 2L steel reactor with stirrer, internal thermometer, heating / cooling jacket, manometer, relief valve pressure vessel, reflux condenser and a feed vessel 164 pressure-tight and heated to 125°C. A pressure of 4 bars was built up. 126.4 g of a 50% by weight aqueous sodium hydroxide solution (120 mol% VFA) were provided in the feed vessel. The sodium hydroxide solution was forced into the reactor at a pressure of 6 bar and was IVIA / t / ZUZ I / UZ 104U I mix. A temperature of 120°C was reached and maintained for 30 min. The reactor was then cooled down to RT as quickly as possible. 295.8 g of the obtained product were adjusted to pH 6.0 by adding 26.1 g of 37% by weight hydrochloric acid and 2.9 g of water. A slightly cloudy, yellowish and viscous polymer solution was obtained. Polymer content: 7.2% Formate content FA: 94.7 mmol / 100 g Degree of hydrolysis HA: 97.4 mol% Degree of conversion HE: 100% mol Charge density LD: 68.8 mmol / 100 g Viscosity (20 1 / min, RV , spindle 3) 940 mPas FAD (13C-NMR, 152.3 ppm): 1.31 FFA (13C-NMR, 164-167 ppm) 1.01 VFA°: 97.2 mmol / 100 g EA°: 27.8 mmol / 100 g Na-AS°: 13.9mmol / 100g. 165 Final polymer AE29: VE27 alkaline hydrolyzed terpolymer (VFA / MA / AM = 70% mol / 25% mol / 5% mol) 156.0 g of the obtained polymer solution were mixed with the starting polymer VE27 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 1.6 g of a 40% by weight aqueous sodium bisulfite solution and 72.9 g of water and then heated to 80°C. Next, 60.3 g of a 25% by weight aqueous sodium hydroxide solution (120 mol% on VFA) were added. The mixture was kept for 5 hrs at 80°C. The obtained product was cooled to RT and adjusted to pH 6.0 by adding 24.1 g of 37% by weight hydrochloric acid and 7.5 g of water. A slightly cloudy, yellowish and viscous polymer solution with a polymer content of 7.9% was obtained. The degree of HA hydrolysis was 93 mol% and the degree of HE conversion was 100 mol%. Final polymer AVI: Hydrolyzed alkaline copolymer W1 (VFA / Na acrylate = 70 mol / 30 mol%) 206.1 g of the obtained polymer solution were mixed with the starting polymer W1 in a 500 mL four-necked flask with stirring paddle, internal thermometer, dropping funnel, and reflux condenser at a stirring speed of 80 rpm with 2.3 g of an aqueous solution of 166 40% by weight sodium bisulfite and then heated to 80°C. Next, 77.0 g of a 25% by weight aqueous sodium hydroxide solution (110 mol% on VFA) were added. The mixture was kept for 5 hrs at 80°C. The obtained product was cooled to RT and adjusted to pH 8.5 by adding 32.3 g of 37% by weight hydrochloric acid and 9.6 g of water. A slightly cloudy, yellowish and viscous polymer solution with a polymer content of 9.9% was obtained. The degree of HA hydrolysis was 100 mole %. A-4) Summary of details of the polymers produced General descriptions of the details of the polymers produced are summarized in Tables A-4-1 and A-4-2. IVIA / l / U¿ 104U 167 Table A-4-1 Observations on viscosity during hydrolysis to final polymers from the 4J to ® R O ft Yes M M 0 O •H ft β Ό O M ounSuiu Peak Viscosity | extreme extreme | extreme I moderate I I minimal I | none | low j none | none [ none I minimum I none I | minimum I none none I none Polymer content [%] co CO 03 tó b- r- to LO I’ CN I- LO 100 j 7.7 fr'8 | 001 in o o 100 I 7.2 Degree of conversion HE [mol%] o o o o o o o o I 001 o o ico 1 o o o o o O O Degree of hydrolysis HA [mol% 0) <0 03 01 05 0)' 0> 01 co 0) 01 0) co or Oí 01 03 0) 03 co 0) o to 01 in CO cO 01 03 Hydrolysis HCI, 120 mole % | NaOH, 120 mole% I NaOH, 125 mole% | NaOH, 11S mole % | 1 ΐ®|θω % ozt HOBN NaOH, 120 mol% | re o ε ÍN X o ra NaOH, 120 mol% | NaOH, 120 mole % | NaOH. 120 mole % | NaOH, 120 mole % | NaOH, 120 mole % | I NaOH. 120 mole % I NaOH, 120 mole % | NaOH. 120 mole % I NaOH. 120 mole % I NaOH, 120 mole % | K value of starting polymer co NT 03 co co O or O 01 <Ώ 0) CO CO 01 01 CD 04 O s s 01 CQ O s 03 Monomers for starting polymer (mol%)] VFA / MA - 70 / 30 VFA / MA = 70 / 30 o or ££J il < < > VFA / MA = 80 / 20 VFA / MA / Na acrylate = 70 / 29 / 1 VFA / MA / Na acrylate = 70 / 28 / 2 10 ¿O OJ O a re φ •o o re Q JO < < μ VFA'MA / Na acrylate = 70 / 25 / 5 VFA / MA / Na acrylate - 70 / 20 / 10 VFA / MA / Na acrylate - 70 / 15 / 15 VFA / MA / Na acrylate = 70 / 10 / 20 VFA / EA / Na acrylate = 70 / 25 / 5 VFA / EA / Na acrylate = 70 / 25 / 5 VFA / EA / Na acrylate - 70 / 20 / 10 I VFA / EA / Na acrylate = 70 / 20 / 10 VFA / EA / Na acrylate = 70 / 20 / 10 VFA / MA / Na methacrylate = 70 / 25 / 5 Final polymer |AE1 and AE2 | AE20 IZBV j I AES | AE4 sav j í AE6 I AE7 83V j í AES i AE22 833V j t53V j í AE17 i AE15 | AE10 ΜΛ / l / U¿ 104U 168 VIA / t / ZUZ l / UZ 104U 169 Table A-4-2: Composition calculated for final polymers with structural formula III Lactam (e) (mol %]) 1 26.2 í IO LO 04 04 uo 31.1 | I 47.7 i 24.5 í 26.5 ! I 20.4 Ϊ | SO 19.7 í 25.9 í 21.2 í 23.2 Acrylate anion (d) [mol %| 12.0 12.9 13.9 C-4 có 10 có 13.4 O ! 11.7 i 16.1 σι CO 16.4 16.1 04 ID 14.2 VioH ammonium (o) [mol %1 60.1 55.3 1 56.2 | 1'65 33.1 i 72.7 I I 60.1 I SOS 9Z9 O fO 56.2 ! 60.3 VFA (b) [% mol] I·'· or eó | 10.4 LO (Ó O Os o LO Ó V- CO CQ C4 O 8Έ1 | en OÍ v- Amidinium (a) [molar %) o 10 04 04 <0 Í0 σι íp o r-j <\i <0 or 14.2 ΙΌ <o <q grado de hidrólisis ha molar] cn c0 sí σ>o 'tf CJ) <3> σι in 0> & (O in § ÍM 'S' in <n K value of starting polymer δ s j eot δ 04 íO CÓ X δ 8 s o 102 I o δ Monomers for starting polymer [molar %) | VFA / EA / Na acrylate = 70 / 15 / 16 I VFA / EA / Na acrylate = 70 / 20 / 10 ¡ | VFAEA / Na acrylate = 70 / 20 / 10 I VFA / EA / Na acrylate = 70 / 20 / 10 1 VFA / MA = 70 / 30 I VFA / MA = 60 / 40 or 04 O <or II > I VFA / MA / Na acrylate = 70 / 25 / 5 I I VFA / EA / Na acrylate = 70 / 25 / 5 ¡ o o k cg (P T5 o ra u ra < w < ÍL. | VFA / EA / Na acrylate = 70 / 10 / 20 ¡ I VFA / EA / Na acrylate = 70 / 20 / 10 I VFA / EA / Na acrylate = 70 / 20 / 10 !|VFA / EA / Na acrylate = 70 / 20 / 10 Final polymer I AE15b) |AE16bl íq¿13V | |A£18b' 1 AE19b> I AE20h' I AE21 b> I AE22bi I AE23» | AE24b> | AE25 b> ÍO 04 UJ | AE28bt φ •P or '•Ú ΜΛ / t / ZUZ l / UZ 104U 170 B) Paper B-l) Production of paper material A pulp produced by impinging paper webs in a pulper was used as a paper material for paper production. The paper web consisted of a testliner 2 specification raw packaging paper with an areal density of 120 g / m2, originating from Thurpapier in Weinfelden (Switzerland). The pulp was obtained by disintegrating the paper webs in potable water and mechanically processing them in a pulper to approximately 3.5% solids content. Then the pulp generally had a fineness of about 50° SR (SchopperRiegler). B-2) Treatment of paper material with final polymers The final polymer treatment was performed either on thick matter with a solids content of about 3.5% of the pulp, or on fine matter with a solids content of about 0.8% of the pulp. In the case of thick matter treatment, 500 g of pulp was placed in a large glass beaker. Next, a 2% aqueous solution of the final polymer was added, with stirring. The indicated percentage refers to the polymer content in the final polymer. Pulp 171 was treated with 1.315 g of final polymer 2% aqueous solution or with 2.63 g of final polymer 2% aqueous solution, ie 1.315 g or 2.63 g to give 500 g of pulp. This corresponds to a treatment with 0.15% or 0.3% of final polymer in relation to the dry paper material. Next, 100 g of the treated pulp were introduced into another glass container and then diluted with drinking water to a solids concentration of 0.8%. In the case of the fine matter treatment, 114.3 g of pulp were placed in a large glass beaker. Next, the pulp was diluted with drinking water to a solid concentration of 0.8%. The additives were added with stirring as a 2% aqueous solution of the final polymer. The indicated percentage refers to the polymer content in the final polymer. The thinned pulp was treated with 0.3 g of final polymer 2% aqueous solution or with 0.6 g of final polymer 2% aqueous solution. This corresponds to a treatment with 0.15% or 0.3% of final polymer in relation to the dry paper material. B-3) Production of paper sheets The aim was to produce paper sheets with a areal density of 120 g / m2 from a final polymer treated paper stock with a solids content of 0.8%. The paper sheets were produced on a sheet former 172 dynamic sheets of TechPap (France) . A slurry of paper stock, ie paper stock treated with a final polymer as appropriate, was sprayed onto a screen. The sieve was clamped on a rapidly rotating vertical drum. Dewatering and sheet formation in this system were determined, in addition to the sheet structure, in particular by the centrifugal forces inside the rotating drum. By varying the speed of rotation of the drum, the centrifugal force acting on the formed sheet structure can be varied. The result is a variation of the dehydration of the sheet, which leads to a variation of the dry content in the formed structure of the wet paper. What is meant here is the dry content of the wet paper structure directly after removal from the screen held in the drum of the dynamic sheeter. The drum rotation speed can be varied in 5 stages between 600 and 1100 rpm, whereby the dry content can be set in a range between 15% by weight and 21% by weight. A small part of the sheet structure, still wet, was used to directly determine the dry content after removing the wet paper structure from the dynamic sheet former screen. After removal from the drum of the dynamic sheeter, the wet paper structures were covered on both sides with blotting paper and dehydrated in a static press at 6 bar for 30 seconds, thereby forming a 173 sheet of wet paper from the structure of paper. The dry content of the wet paper sheet was then generally between 41% by weight and 43% by weight. If the lower value is reduced significantly, the thickness of the blotting paper or the number of sheets placed can be increased to reach the range mentioned above. The wet paper sheet was then covered again on both sides with fresh blotting papers and then clamped on a drying roller for 10 minutes. The surface temperature of the drying roller was approximately 100°C. A dry paper sheet was formed. After drying, the dried paper sheets were placed in an air-conditioned room for conditioning. B-4) Dry content of a paper sample and internal resistance of dry sheets of paper To determine the dry content (TG) of a paper sample, the mass of a wet sample (MF) was determined from the wet paper sample on a calibrated top-loading steel balance, with which it was possible to measure up to 0.01g. The wet paper sample preferably had an area of ​​at least 10 cm x 10 cm. The wet paper sample was then placed in a calibrated drying cabinet, which could observe a set temperature of ±2°C, and dried at a set temperature of 105°C to constant mass. This 174 was generally the case after 90 minutes. The dried paper sample, still warm, was then transferred to a desiccator, containing a suitable drying agent, such as silica gel. After cooling to room temperature, the mass of the dry paper sample (MT) was determined on the aforementioned balance. Next, the dry content of the paper sample was specified, calculated according to TG = 100 MT / MF, in % by weight. The percentage value was often specified with a decimal point. If this percentage value no longer changes to the first rounded decimal place, this indicates that a constant mass has been reached in the case of dry contents of 1 to 100% by weight. With dry contents from 0 to less than 1% by weight, the second rounded decimal point of the percentage value is the relevant indicator. Drying was carried out at ambient pressure, optionally 101.32 KPa, without correcting any deviation derived from weather and sea level. During drying, the normally prevailing air pressure was maintained, ie potentially 101.32 kPa. No correction was made if the air pressure was slightly different, caused by weather and sea level. In the case of a wet sample that did not yet have a sheet consistency, eg a suspension of fibrous material or a pulp, the wet sample was dried on a suitable large surface tray. To determine the internal resistance of a sheet 175 dry paper, this sheet was stored in an air-conditioned room under constant conditions of 23 °C and 50% relative humidity for 12 hr. Internal resistance was measured by an approach corresponding to the TAPPI T833 pm94 standard. In this case, 10 strips of paper 2.5 cm wide and 12.7 cm long were cut from two sheets of paper that had been produced and then dried as described above. Each individual paper sample was attached to a separate base plate and metal support using double-sided tape. The metal support was impacted using a pendulum, in which the paper sample to be examined was cut in a plane parallel to the paper surface. The energy required for this process was measured. The apparatus used for the measurement was an internal junction test station from TMI (Testinq Machines Inc. Iceland, New York, USA). Double-sided adhesive tape was a product of the 3M company (width 25.4 mm, type Scotch No. 140). The measuring apparatus delivered the energy required for the division in J / m2 in relation to a standardized area. The internal resistance is the average value formed from 10 individual measurements. B-5) Dry sheets of paper produced and results Three wet paper structures with dry contents of 15.7% by weight, 17.4% by weight and 20.4% by weight were produced from untreated paper material as examples of 176 reference (RB) for dry paper sheets. The wet paper structures were then pressed and dried. Wet paper structures, each with two different dry contents between 16.5 and 21% by weight per final polymer, were produced from final polymer-treated paper materials, in which a dry content was below 18.5%. by weight and a dry content was above 18.5% by weight. Table B-5-1 specifies the final polymers used and the results obtained. Table B-5-1: Final polymers used and results obtained Example Final Polymer Dose ci Dry content d| [% by weight] Internal resistance®1 [J / m2] Addition of thick material Addition of fine material RB1 a) - - 15.7 118 RB2 a) - - 17.4 125 RB3 a> - - 20.4 129 VB1 a) AVI 0.15 16.9 140 - VB2 a> AVI 0.30 17.1 147 - VB3 a) AVI 0.15 17.3 - 141 VB4 a) AVI 0.30 17.5 - 155 EB1 b) AE 19 0.15 17.7 166 - EB2 b) AE 19 0.30 17.4 178 - EB3 b) SA 19 0.15 17.2 - 169 EB4 b) AE 19 0.30 18.0 - 179 177 ΕΒ5 b) AE 2 0 0.15 17.4 164 - EB6 b> AE 2 0 0.30 18.1 177 - EB7 b) AE 2 0 0.15 17.8 - 167 EB8 b) AE 2 0 0.30 18.2 - 184 EB9 b) AE 21 0.15 17.1 166 - EB10 b| AE 21 0.30 17.4 189 - EB11 b) AE 21 0.15 17.6 - 171 EB12 b) AE 21 0.30 17.7 - 183 EB13 bl AE 2 2 0.15 17.0 167 - EB14 bl AE 2 2 0.30 17.5 179 - EB15b| AE 2 2 0.15 17.4 - 169 EB16 b| EB20 bl AE 2 3 0.30 17 .6 - 185 EB21 b| AE 2 4 0.15 16.8 172 - EB22 b) AE 2 4 0.30 17.4 188 - EB23 b) AE 2 4 0.15 17.2 - 173 EB24 bl AE 2 4 0.30 17.7 - 189 EB25 bl AE 15 0.15 17. 2 167 - EB2 6bl AE 15 0.30 17.5 183 - EB27 b) AE 15 0.15 17.6 - 173 EB28 b) AE 15 0.30 17.8 - 188 VB5 a) AVI 0.15 19.7 143 - VB6 a) AVI 0.30 18.9 154 - VB7 a> AVI 0.15 19. 5 - 149 VB8 to> AVI 0.30 19.1 - 161 EB 33 b) AE 19 0.15 19.7 221 - EB 34 b) AE 19 0.30 19.6 272 - EB 35 bl AE 19 0.15 19.9 - 229 178 EB 36 b) AE 19 0.30 19.3 - 266 EB 37 b) AE 2 0 0.15 19.8 195 - EB 38 b) AE 2 0 0.30 19.6 236 - EB 39 b) AE 2 0 0.15 19.8 - 203 EB 4 0 b) AE 2 0 0.30 19.3 - 249 EB 41 b) AE 21 0.15 19.2 194 - EB 42 b) AE 21 0.30 19.4 239 - EB 43 b) AE 21 0.15 20.1 - 197 EB 44 bl AE 21 0.30 19.6 - 243 EB45b| AE 2 2 0.15 19.6 229 - EB46 b| AE 2 2 0.30 20.1 271 - EB47 b) AE 2 2 0.15 20.5 - 223 EB48 b) AE 2 2 0.30 19.5 - 269 EB49 bl AE 2 3 0.15 19.3 219 - EB50 bl AE 2 3 0.30 19 .7 267 - EB51 b| AE 2 3 0.15 19.6 - 231 EB52 b| AE 2 3 0.30 20.3 - 272 EB53 b) AE 2 4 0.15 19.4 207 - EB54 bl AE 2 4 0.30 19.5 249 - EB55 bl AE 2 4 0.15 20.2 - 209 EB5 6 bl AE 2 4 0.30 1 9.3 - 256 EB57 b) SA 15 0.15 19.6 193 - EB58 b) AE 15 0.30 19.2 228 - EB5 9 b) AE 15 0.15 19.5 - 204 EB60 bl AE 15 0.30 19.8 - 235 Footnotes: a) comparative b) in accordance with the invention c) g of final polymer based on the content of 179 polymer added to 100g of paper material d) dry content of the wet paper structure e) internal resistance of the dry sheet of paper IVIA / t / ZUZ I / UZ 104U B-6) Summary of the data obtained The internal resistance reference values ​​(RB1 - RB3, without final polymer added) are approximately 125 J / m2. Deviations in internal resistance between dry paper sheets, whose wet paper structures have a dry content between 15.3% by weight and 20.2% by weight, are small deviations. At a dosage amount of 0.15 g / 100 g of the comparative examples (VB1, VB3, VB5, VB7), the increase in internal resistance compared with the reference examples was approximately 20 J / m2, regardless of the dosage. in the thick matter, or in the fine matter and regardless of the dry content. At a dosage amount of 0.3 g / 100 g of the comparative examples (VB2, VB4, VB6, VB8) the increase in internal resistance was approximately 30 J / m2 regardless of the dosage in the thick matter or in the fine matter and regardless of dry content. At a dosage amount of 0.15 g / 100 g of the examples according to the invention and a dry content < 18.5% by weight (in each case odd numbers from EB1 to 180 ΕΒ28), the increase in internal resistance compared to the reference examples was approximately 40 J / m 2 regardless of the dosage in thick matter or in fine matter. At a dosage amount of 0.30 g / 100 g of the examples according to the invention and a dry content < 18.5% by weight (in each case odd numbers EB1 to EB28), the increase in internal resistance compared to the reference examples was approximately 55 J / m2 regardless of the dosage in the thick material or in the fine material. At a dosage amount of 0.15 g / 100 g of the examples according to the invention and a dry content > 18.5% by weight (in each case odd numbers from EB33 to EB60), the increase in internal resistance compared to the reference examples was at least 70 J / m2 in the case of dosing in thick matter and at least 50 J / m2 in the case of dosing in fine matter. At a dosage amount of 0.30 g / 100 g of the examples according to the invention and a dry content > 18.5% by weight (in each case odd numbers from EB33 to EB60), the increase in internal resistance compared to the reference examples was at least 90 J / m2 in the thick material and at least 70 J / m2 in the fine material. When comparing the examples according to the invention with a dry content of the paper structure 181 wet of < 18.5% by weight (EB1 to EB28) with the examples according to the invention with a dry content of the wet paper structure > 18.5% by weight (EB33 to EB60), the internal strengths with the final polymer comparable , the dosing amount and the dosing are at least 20 J / m 2 higher with the highest dry content of the wet paper structure. The final AVI polymer of the comparative examples was formally composed of 70 mole % ethylene units bearing amino groups and 30 mole % ethylene units bearing carboxylic acid groups. Final polymers AE15, AE19. AE22, AE23 and AE24 of the examples according to the invention were also formally composed of approximately 70 mole % ethylene units bearing amino groups and 30 mole % ethylene units bearing carboxylic acid groups. Approximately, the degree of HA hydrolysis was 98 mole% in AE15, 99 mole% in AE19, 98 mole% in AE22, 97 mole% in AE23 and 96 mole% in AE24. With regard to the paper strengths achieved for the final polymers applied, a distinction was made as to whether, for the ethylene units containing carboxylic acid groups, only sodium acrylate was polymerized beforehand in the final polymers in the polymer. starting material, or if at least also or exclusively a methyl or ethyl ester of acrylic acid was polymerized 182 previously in the starting polymer. It was assumed that this led to a different incorporation behavior of the monomers and thus to an altered alternation of the monomer units that have been polymerized. With increased alternation, changes in the number of possible five-membered lactam structural units would be expected. N-vinylformamide is an electron-rich monomer, whereas an acrylic acid ester, on the other hand, is a low-electron-count monomer. Acrylic acid regulated in its pH to a pH value of 6 to 7 is, on the contrary, a monomer with a higher electron count. Another difference between an acrylic acid ester and an acrylate salt is solubility.< / q>

Claims

1. A method for producing paper or cardboard, comprising the steps (A) adding a final polymer A to a first aqueous suspension of fibrous material, thereby creating a second aqueous suspension of fibrous material containing the final polymer A, wherein the final polymer A can be obtained by radical polymerization of the monomers (i) 30 to 90 mol% of a monomer of formula I (I), wherein R1 = H or signifies Ci-Cs alkyl, (ii) 3 to 60 mol% of a C1-C4 alkyl ester of acrylic acid or a C1-C4 alkyl ester of methacrylic acid, (iii) 0 to 45 mol% of a monoethylenically unsaturated carboxylic acid, a monoethylenically unsaturated sulfonic acid or a monoethylenically unsaturated phosphonic acid, or salt forms thereof, (iv) 0 to 9 mol% of acrylonitrile or 184 methacrylonitrile, (v) 0 to 35 mol% of one or more ethylenically unsaturated monomers that are different from a monomer (i), (ii), (iii) and (iv),wherein the total amount of all monomers (i), (ii), (iii), (iv) and (v) is 100% molar, to obtain a starting polymer V, e - hydrolyzing the starting polymer V to obtain the final polymer A, wherein the NC(=O)R1 groups of formula (I) of the monomers (i) polymerized in the starting polymer V are at least partially hydrolyzed and in doing so form the primary amino groups, wherein the ester groups of the monomers (ii) polymerized in the starting polymer V are at least partially converted and at least part of the conversion is the formation of five-membered lactam structural units with the primary amino groups obtained or the formation of carboxylic acid groups or salt forms thereof, (B) dehydrating the second aqueous suspension of fibrous material containing the final polymer A on a water-permeable substrate to form a wet paper structure, (C) dehydrating the wet paper structure,which is how paper or cardboard is formed. 185, 2. The method according to claim 1, wherein (i) 50 to 89 mol% of a monomer of formula I, (ii) 5 to 45 mol% of a C1-C4 alkyl ester of acrylic acid or a C1-C4 alkyl ester of methacrylic acid, (iii) 0 to 30 mol% of a monoethylenically unsaturated carboxylic acid, a monoethylenically unsaturated sulfonic acid or a monoethylenically unsaturated phosphonic acid, or salt forms thereof, (iv) 0 to 9 mol% of acrylonitrile or methacrylonitrile, (v) 0 to 25 mol% of one or more ethylenically unsaturated monomers other than a monomer (i), (ii), (iii) and (iv), are used for radical polymerization.

3. The method according to claim 1, wherein (i) 58 to 83 mol% of a monomer of formula I, (ii) 8 to 39 mol% of a C1-C4 alkyl ester of acrylic acid or a C1-C4 alkyl ester of methacrylic acid, (iii) 0 to 25 mol% of a monoethylenically unsaturated carboxylic acid, a monoethylenically unsaturated sulfonic acid or a monoethylenically unsaturated phosphonic acid, or salt forms thereof, (iv) 0 to 9 mol% of acrylonitrile or methacrylonitrile, (v) 0 to 25 mol% of one or more ethylenically unsaturated monomers other than a monomer (i), (v), (ii) and (iv), are used for radical polymerization.

4. The method according to claim 1, wherein the monomer (iii) is used in an amount of 1 to 25% molar.

5. The method according to claim 1, wherein the monomer (i) is N-vinylformamide with R1 = H in formula I.

6. The method according to claim 1, wherein the monomer (ii) is selected from a C1-C3 alkyl ester of acrylic acid or Ci alkyl ester of methacrylic acid; ethyl acrylate; or a combination thereof.

7. The method according to claim 1, wherein the monomer (iii) is selected from a monoethylenically unsaturated carboxylic acid or a monoethylenically unsaturated sulfonic acid, or salt forms thereof; acrylic acid, methacrylic acid, vinylsulfonic acid, or 2-acrylamido-2-methylpropanesulfonic acid, or salt forms thereof; or a combination thereof. 187 8. The method according to claim 1, wherein the monomers (i) 60 to 83 mol% N-vinylformamide, (ii) 8 to 21 mol% ethyl acrylate, (iii) 2 to 21 mol% acrylic acid or methacrylic acid or salt forms thereof, (iv) 0 to 9 mol% acrylonitrile or methacrylonitrile, (v) 0 to 24 mol% one or more ethylenically unsaturated monomers other than a monomer (i), (ii), (iii) and (iv), are used for radical polymerization.

9. The method according to any of claims 1 to 8, wherein: - in step (A) the first aqueous suspension of fibrous material has a dry content between 0.1% by weight and 6% by weight; - in step (B) the wet paper structure has a dry content between 18.5 and 25% by weight.

10. A final polymer A obtainable by radical polymerization of the monomers (i) 58 to 83 mol% of a monomer of formula I IVIA / l / U¿ 104U 188 H H >--ν H—^R1 < / / H O (I), wherein R1 = H o signifies Ci-Ce alkyl, (ii) 8 to 39 mol% of a C1-C4 alkyl ester of acrylic acid or a C1-C4 alkyl ester of methacrylic acid, (iii) 0 to 25 mol% of a monoethylenically unsaturated carboxylic acid, a monoethylenically unsaturated sulfonic acid or a monoethylenically unsaturated phosphonic acid, or salt forms thereof, (iv) 0 to 9 mol% of acrylonitrile or methacrylonitrile, (v) 0 to 25 mol% of one or more ethylenically unsaturated monomers that are different from a monomer (i), (ii), (iii) and (iv), wherein the total amount of all monomers (i), (ii), (iii), (iv) and (v) is 100 mol%, to obtain a starting polymer V, e - hydrolyze the starting polymer V to obtain the final polymer A,wherein the NC(=O)R1 groups of formula (I) of the monomers (i) polymerized in the starting polymer V are at least partially hydrolyzed and in doing so form the primary amino groups 189, wherein the ester groups of the monomers (ii) polymerized in the starting polymer V are at least partially converted and at least part of the conversion is the formation 5 of five-membered lactam structural units with the primary amino groups obtained or the formation of carboxylic acid groups or salt forms thereof.