Process for the production of high molecular weight copolymers of diallyl dimethyl ammonium chloride and acrylamide in an aqueous dispersed phase

Abstract: Water-soluble, high molecular weight, linear copolymers of diallyl dimethyl ammonium chloride and acrylamide, are prepared by emulsion copolymerization of a major portion of the acrylamide monomer via stage-­ addition, and the addition of a chain transfer agent at the conclusion of said copolymerization to prevent branching and cross-linking.

Description: This invention relates to high molecular weight, water soluble, linear copolymers of diallyl dimethyl ammonium chloride and acrylamide of varying cationicities, and to methods of preparing the same. Copolymers of this type are useful as cationic flocculants in the treatment of industrial water, as sludge conditioners for the treatment of municipal water systems, and as drainage and retention aids in the manufacture of paper. Diallyl dimethyl ammonium chloride (DADMAC) is a quaternary monomer, which when polymerized, yields water soluble polymers that are cationic in nature. The polymerization of acrylamide, on the other hand, produces water soluble polymers that are essentially nonionic in nature. Thus, the copolymerization of DADMAC and acrylamide monomers results in the formation of water soluble copolymers having various degrees of cationicity, depending upon the amount of DADMAC that is incorporated into the final copolymer. The copolymerization of DADMAC and acrylamide monomers in solution is well known. US-A-2,923,701, for example, describes the simultaneous copolymerization of acrylamide and DADMAC in solution by the addition of a redox catalyst, such as ammonium persulfate and potassium metabisulfite, to an aqueous mixture of the monomers. Copolymers of DADMAC and acrylamide can also be obtained utilizing emulsion polymerization techniques in accordance with the teachings of US-A-3,920,599. Stable water-in-oil copolymer emulsions are prepared, which can then be inverted by means of suitable hydrophilic, water-soluble surfactants to form water soluble solutions that are used as such. 4,070,930 discloses the preparation of stable emulsion copolymers of DADMAC and acrylamide, which can be inverted by the addition of water. An improved process for the incorporation of DADMAC into an acrylamide polymer by means of either emulsion or solution polymerization techniques is disclosed in EP-A-0 188 721. This improvement comprises the step of polymerizing DADMAC and acrylamide in the presence of a copolymerizable monomer, such as a quaternary substituted acrylamide or methacrylamide. The monomer utilized with acrylamide must have a greater reactivity than DADMAC. EP-A-0 247 774 discloses cationic copolymers having improved performance characteristics which are prepared from a premix containing the nonionic monomer and a portion of the cationic monomer. The premix is emulsified, the remaining cationic monomer added, and the entire reaction mixture is copolymerized. US-A-4,152,200 discloses the preparation of a cationic copolymer having improved drainage characteristics in the preparation of formed paper. This copolymer is prepared by means of a water-in-oil emulsion process comprising the incremental addition of a cationic monomer to the nonionic monomer during the course of the polymerization. This reference expressly teaches the addition of cationic monomers to solutions of nonionic monomers. In contradistinction thereto, the present invention discloses and claims the preparation of different copolymers by means of the continuous addition of a nonionic monomer to a cationic monomer during the course of polymerization. The present invention relates to a process for the preparation of high molecular weight, water-soluble, linear copolymer of DADMAC and acrylamide having a uniform DADMAC to acrylamide ratio. More particularly this process comprises the steps of: a) preparing a water-in-oil monomer emulsion by mixing an oil phase containing an oil soluble emulsifying agent, with an aqueous phase comprising a mixture of DADMAC monomer, a portion of the total amount of acrylamide required, a polymerization initiator, and a water dispersable emulsifying agent; b) initiating the copolymerization of said monomer emulsion by increasing the temperature of the emulsion to a temperature ranging from 30°C to 40°C; c) adding the remaining acrylamide monomer to the monomer emulsion via continuous stage addition, preferably over a period of from 0.5 to 8 hours, at a temperature ranging from 20 to 50°C to form a copolymer emulsion; d) homogeneously mixing a chain transfer agent into said copolymer emulsion to form a copolymer emulsion mixture; and e) heating said copolymer emulsion mixture, preferably at a temperature ranging from 60 to 90°C for preferably a period of time ranging from 0.1 to 4.0 hours, to minimize residual monomer content. This invention also relates to high molecular weight water soluble linear copolymers of DADMAC and acrylamide prepared in accordance with the process of this invention. Such copolymers are particularly useful as flocculants for sludge conditioning in the treatment of municipal and industrial water and waste water systems over a wide range of pH. The copolymers described herein are also useful as drainage and retention aids in the manufacture of paper. As previously indicated, the preparation of DADMAC and acrylamide copolymers is well known. In general, however, the existing prior art copolymers are non-uniform in their composition and tend to be highly branched and cross-linked. In addition, the prior art copolymers are of relatively low molecular weight, having intrinsic viscosities generally less than 6 dl/g. The present invention overcomes these deficiencies of the prior art and enables the preparation of high molecular weight copolymers of DADMAC and acrylamide via an emulsion process having intrinsic viscosities ranging from 10 to 25 dl/g. More particularly, DADMAC and acrylamide copolymers are prepared which have intrinsic viscosities ranging from 15 to 20 dl/g. It is generally recognized by those skilled in the art that the intrinsic viscosity is an indication of polymer molecular weight. Thus, in general, the higher the intrinsic viscosity, the greater is the molecular weight of the particular polymer or copolymer prepared. When prepared in accordance with the teachings of this invention, copolymers of varying cationicities can be prepared, thereby enabling the preparation of copolymers that can be tailored to their use. Furthermore, such copolymers are uniform in composition. That is to say, copolymers are prepared which contain little, if any, residual monomer, and which have a uniform DADMAC to acrylamide ratio throughout the entire length of the copolymer chain. One difficulty in the preparation of DADMAC and acrylamide copolymers, that have a uniform distribution throughout the length of the copolymer chain, is due to the difference in reactivity of the acrylamide monomer with respect to the DADMAC monomer. This difference in reactivity results in a non-uniform distribution of the DADMAC monomer throughout the copolymer chain. Thus, at the onset of the copolymerization reaction, a relatively larger number of acrylamide monomer units are initially incorporated into the polymer chain due to the greater reactivity of the acrylamide monomer. Accordingly, at the conclusion of the copolymerization reaction, relatively more of the DADMAC monomer units remain unused and remain either as free monomer, or form low molecular weight homopolymers. These excess DADMAC monomers, or low molecular weight DADMAC homopolymers, remain either as a residual mixture or they become incorporated into the copolymer chain, which results in a non-uniform distribution of copolymer units throughout the copolymer chain. This is particularly true in the case of copolymers in which the final DADMAC content is greater than 20 percent on a molar basis of the total copolymer content. Another difficulty in the preparation of high molecular weight linear copolymers of DADMAC and acrylamide is due to the manner in which the DADMAC monomer polymerizes. Normally, the DADMAC monomer polymerizes by incorporating both of the allyl bonds within the same molecule to form a linear polymer chain. A small proportion of the DADMAC monomer, however, can polymerize via the incorporation of only one of its allyl bonds, thereby leaving a pendant double bond remaining in the molecule. These pendant double bonds can subsequently initiate branching, particularly at higher temperatures, to produce cross-linked polymers that have a reduced solubility in water, see Jaeger et al., Journal of Macromolecular Science, Part A Chemistry, 593-614, (1984). This greater reactivity of the acrylamide monomer, in combination with the tendency of the DADMAC monomer to polymerise via branching or cross-linking, results in the formation of non-linear DADMAC and acrylamide copolymers having relatively low intrinsic viscosities. Such copolymers are not particularly well suited as flocculants in water and waste water systems for sludge conditioning, or as drainage and retention aids in the manufacture of paper. These problems have now been overcome by means of the present invention, which enables the preparation of high molecular weight, linear copolymers of DADMAC and acrylamide of uniform composition having little, if any, branching and crosslinking in the polymer chain. In general, the process of this invention utilizes a controlled addition or stage-addition of the acrylamide monomer during the emulsion copolymerization reaction. Surprisingly, it has been discovered that the continuous stage-addition of the acrylamide monomer produces high molecular weight copolymers of DADMAC and acrylamide which, heretofor have not, as yet, been available. Copolymers having high DADMAC conversions can be prepared that contain a uniform distribution of DADMAC and acrylamide monomer units throughout the entire length of the copolymer chain with little, if any, residual DADMAC or acrylamide monomer remaining in the finished product. The process of this invention also utilizes the addition of a chain transfer agent to prevent branching and cross-linking of the polymer chain from occurring, particularly at elevated temperatures. To initiate copolymerization, a water-in-oil emulsion is prepared which contains the DADMAC monomer and a portion of the acrylamide monomer to be employed. The oil phase of the emulsion can be any water insoluble, aliphatic or aromatic liquid organic substance. Organic liquids such as benzene, xylene, toluene, mineral oils, mineral spirits, kerosene, naphthas and perolatums can be employed. In general, the oil phase comprises from 20 to 50 volume percent of the total emulsion composition. Preferably, the oil phase comprises from 25 to 30 volume percent of the emulsion composition. A particularly useful oil from the standpoint of its physical and chemical properties is the branched-chain isoparaffin solvent sold under the name "Isopar M". Typical specifications of this narrow-cut isoparaffinic solvent are set forth as shown below: Density at 12°C 0.786 g/l Color (Saybolt) 30 Refractive Index, n²⁰ D 1.436 Viscosity (25°C) 2.46 mPa·s (cp) Boiling point Characteristics (°C) Start 204 5 % 212 10 % 215 50 % 224 90 % 236 95 % 242 Dryness 247 Residue (mg/100 ml) < 1 Aromatic Content (percent) 0.3 Sulfur Content ppm < 1 Flash Point °C 75 The oil phase also contains a primary emulsifier which serves to stabilize the emulsion during polymerization. The primary emulsifying agent can be selected from any of a large group of surfactants that are oil soluble and that have an HLB value in the range of from 2 to 10, preferably less than 7. Suitable primary emulsifiers include the sorbitan esters, phthalic esters, the reaction product of oleic acid with isopropanolamide, fatty acid glycerides, glycerine esters as well as ethoxylated derivates thereof. These primary emulsifiers can be used alone or in combination. As such all of the primary emulsifiers should not be used in amounts greater than 5 percent by weight of the total emulsion. Preferably, the amount should range from 1.0 to 2.0 percent by weight of the total emulsion. The preferred primary emulsifying agent for the oil phase is oleic monoisopropanol amide. The dispersed phase is the aqueous phase which essentially comprises an aqueous solution of the DADMAC monomer and an initial portion of the total amount of acrylamide to be employed. A polymerization initiator or polymerization initiator package together with a water dispersible emulsifying agent can be conveniently added at this point to the aqueous phase. The dispersed aqueous phase comprises in general, from 50 to 80 volume percent of the total emulsion composition. Preferably, the dispersed phase comprises 70 to 75 volume percent of the emulsion. However, in order to prepare emulsions having a high polymer content, the dispersed aqueous phase can comprise as much as 75 to 80 volume percent of the emulsion composition. A second emulsifying agent, added to the aqueous phase, has been found to be particularly advantageous in stabilizing the water-in-oil emulsion during the copolymerization reaction. Any conventional oil soluble, water dispersible surfactant having an HLB ranging from 2 to 8 can be employed as an emulsifying agent for the aqueous phase. Examples of suitable surfactants include sorbitan monooleate, the reaction products of oleic acid with ispropanolamide, sorbitan stearate, decyl sodium phthalate, hexadecyl sodium phthalate, and glyceride mono and diesters of lauric and stearic acids. Sorbitan monooleate dispersed in the aqueous phase is the preferred secondary emulsifying agent. The amount of DADMAC monomer to be employed is dependant upon the desired cationicity of the final copolymer. An important advantage of this invention is that copolymers of varying cationicities can be precisely prepared in accordance with the teachings of this invention. The greater the number of DADMAC units that are introduced into the polymer chain, the greater will be the cationicity of the resulting copolymer. Thus, copolymers useful as cationic flocculants in water clarification systems or as sewage dewatering agents, require copolymers having a higher degree of cationicity than cationic flocculants useful as drainage and/or retention aids in the manufacture of paper. The copolymers contemplated by the present invention cover a wide range of cationicities, preferably from 5 to 95 mole percent cationicity. That is to say, in a copolymer consisting of 100 monomer units, the copolymers described comprise from 5 to 95 DADMAC monomer units, and conversely from 95 to 5 acrylamide monomer units. Preferably, copolymers comprising from 5 to 75 mole percent cationicity can be prepared. Still more preferably, polymers having from 10 to 50 mole percent cationicity can be prepared in accordance with the teachings of this invention. It is especially preferred that the DADMAC to acrylamide ratio is from 25 to 50 mole percent. The copolymerization reaction is generally initiated using free radical polymerization techniques known to those skilled in the art. Compounds which form mainly water soluble radicals are suitable as polymerization initiators. Such compounds are conveniently dissolved in the aqueous phase. For example, azostarters such as 2,2-azobis-(N,N′-dimethylene-isobutyramidine) dihydrochloride, 2,2′-azobis-(2-amidinopropane) dihydrochloride, 2,2′-azobis-(N,N′dimethyleneisobutyramidine), 4,4′-azobis-(4-cyanopentane-carboxylic acid), 2,2′-azobis(4-methoxy-2,4-dimethylvalero-nitrile), 2,2′-azobis(2,4-dimethylvaleronitrile), (1-Phenylethyl)azodiphenyl-methane, 2,2′-azobisisobutyro-nitrile, dimethyl 2,2′-azobisisobutyrate, and 2,2′-azobis-(2-methyl-butyronitrile) can be employed. Peroxide polymerization initiators can also be employed, as for example, dibenzoyl peroxide, dilaurylperoxide, di-2-ethylhexylperoxydicarbonate, dicyclohexylperoxydicarbonate, bis-(4-tert. butylcyclohexyl)peroxydicarbonate, tert. butylperpivalate, tert. butyl-perbenzoate, tert. butylpermaleinate, di-tert. butyl-peroxide, tert.-butylhydroperoxide, hydrogen peroxide, ammonium persulfate, potassium persulfate, sodium persulfate, and redox catalysts in combination with reducing agents such as iron(II)-ammonium sulfate, ascorbic acid, sodium methyl sulfinate, disodium disulfite and sodium hydrogen sulfite can be employed. These initiators can be used either alone or in combination with one another. The rate of decomposition of the more readily decomposed peroxides can be reduced by the addition of organic metal complex compounds, as for example, copper acetyl acetonate. Thus the rate of peroxide decomposition can be adapted, for example, to the particular polymerization temperature selected. Preferred redox catalysts are those selected from one or several peroxides in combination with a reducing agent. Especially preferred are persulfates or peresters or mixtures of persulfates and peresters as a component of the redox polymerization initiators. The polymerization initiators are used in amounts ranging from 0.001 to 5 percent by weight, and preferably from 0.02 to 2 percent by weight, relating to the amount of monomers employed. Sufficient water should be employed in the aqueous phase to facilitate emulsion formation and to homogeneously dissolve all of the components present in the aqueous phase. As starter solutions, aqueous monomer solutions containing from 40 to 70 percent of monomer can advantageously be employed. Preferably, aqueous monomer solutions containing from 50 to 60 percent monomer are employed. If necessary, additional water can be added during the course of the copolymerization reaction to the copolymer emulsion in order to provide optimum conditions for the reaction to proceed. It is immaterial whether the oil phase is added to the aqueous phase or vice versa . The two phases are slowly added together with vigorous stirring at 5,000 to 20,000 rpm. The resulting emulsion is deoxygenated with nitrogen and the temperature of the emulsion mixture is slowly increased to initiate copolymerization. The optimum temperature at which polymerization occurs ranges from 20 to 50°C. Preferably, polymerization is conducted at a temperature ranging from 30 to 40°C. Still more preferably, a temperature of 35°C is optimally employed. During the course of the polymerization reaction, acrylamide monomer is continuously added to the DADMAC monomer via a process of stage addition. That is to say, an initial amount of acrylamide is present in the aqueous emulsion phase at the outset of the copolymerization reaction. As the reaction proceeds, fresh acrylamide monomer is continuously added to the copolymerization mixture at a predetermined rate. Usually 12 to 20 percent of the total amount of acrylamide is added at the outset to the reaction mixture. More preferably, from 15 to 17 percent of the total amount of acrylamide monomer required is generally added to initiate copolymerization. The copolymerization reaction of DADMAC and acrylamide is an exothermic reaction. Thus, once copolymerization begins, the temperature of the reaction mixture rapidly increases. At this point the remaining amount of acrylamide monomer is introduced to the reaction mixture via a process of stage-addition with the polymerization temperature preferably being maintained at 35°C. As indicated, as soon as the initial copolymerization has begun, the remaining acrylamide monomer solution is stage-added. The period of time during which stage addition takes place is dependant upon the amount of DADMAC monomer units that are to be introduced into the polymer chain. Thus a copolymer having a 10 mole percent cationicity requires approximately one hour for stage addition, whereas a copolymer having 30 mole percent cationicity requires approximately 3 hours for stage addition to take place. Copolymers having up to 90 mole percent cationicity require approximately 8 hours for stage addition to take place. These periods of time will, of course, vary slightly depending upon the type and design of reactor employed, the degree of mixing and the temperature at which the copolymerization is conducted. For large scale preparations, the particular parameters to be employed can be optimized via standard procedures known to those skilled in the art. The stage-added acrylamide monomer solution is separately deoxygenated, and preferably continuously introduced in such a manner that a slightly decreasing feed rate is achieved throughout the total period of stage addition. Thus, for example, during the first quarter of the period for stage addition, approximately 30 to 35 percent of the acrylamide monomer solution is stage-added; during the second quarter of the stage addition period, 25 to 30 percent of the acrylamide monomer solution is stage-added; during the third quarter 20 to 25 percent of the monomer solution is stage-added; and the last 15 to 20 percent of the acrylamide monomer solution is introduced during the final quarter of the stage addition period. For the production of large quantities of copolymers, a metering pump can be advantageously employed. Copolymers of DADMAC and acrylamide prepared at a temperature of 35°C are completely soluble in water, irrespective of how large their molecular weights may be. Copolymers prepared at temperatures above 40°C tend to be insoluble or only partially soluble in water. This insolubility is presumed to be the result of the increased tendency for the DADMAC monomer to polymerize via branching and cross-linking at higher temperatures. The more branched and cross-linked the copolymers become, the less soluble they are in water. Indeed, one of the qualitative tests for the degree of branching and cross-linking for this type of copolymer is its solubility in water. Inasmuch as the polymerization reaction is exothermic in nature, control of the reaction temperature is critical. In order to maintain close control over the reaction temperature, the boiling point of an azotrope formed by the reaction mixture can be employed. Thus, where the branched chain isoparaffin solvent sold under the name "Isopar M" is employed, the condensate of the vapor above the emulsion phase consists of about 12 percent by volume of solvent and 88 percent by volume of water. If the polymerization reaction is conducted at a reduced pressure of from 50 to 55 millibars (5 - 5.5 kPa), a constant temperature of 35 ± 1.0°C is obtained. It is very important to keep the emulsion mixture well mixed and in intimate contact with the stage-added acrylamide monomer throughout the entire stage-addition process, so as to obtain a homogeneous distribution of DADMAC throughout the copolymer chain. Insufficient mixing results in non-homogenous polymerization, whereas too rapid or too intensive mixing results in polymer degradation. The degree and amount of mixing required to obtain a homogeneous distribution of DADMAC throughout the copolymer chain varies widely depending upon the size and the shape of the particular apparatus employed. Reaction mixers used in the preparation of thick emulsions or other similar materials, that provide intimate mixing via a shearing action, are particularly well adapted to this process. As soon as all of the acrylamide monomer has been stage-added to the emulsion mixture and permitted to react, a chain transfer agent is added. The addition of a chain transfer agent at the conclusion of the copolymerization process is an essential step in the present invention for the preparation of high molecular weight linear copolymers. Normally, chain transfer agents are introduced at the beginning of a polymerization process. However, in accordance with the process of the invention, the chain transfer agent is added at the conclusion of the copolymerisation process so as to prevent any branching or cross-linking of formed copolymer chains from occurring. Suitable chain transfer agents include, for example, lower alkyl alcohols having from 1 to 5 carbon atoms, mercaptoethanol, mercaptopropanol, thioglycolic acid, dodecylmercaptan, formic acid, halogenated hydrocarbons, such as bromoethane or carbon tetrachloride, and sodium hypophosphite. Preferably, a solution of sodium hypophosphite is employed. The chain transfer agents as used herein are utilized in amounts ranging from 0.1 to 3 percent by weight with respect to the monomers employed. Upon addition, they must be thoroughly mixed into the emulsion mixture. Following the addition of the chain transfer agent, the emulsion mixture is preferably heated to 75°C and maintained at that temperature for a period of from 0.1 to 4.0 hours. This period of heating serves to minimize the residual monomer content of the copolymer produced. This is especially important for environmental reasons with respect to any residual acrylamide monomer that may be present. Thus, in addition to enhancing the uniformity of the copolymers so prepared, the copolymers prepared are non-hazardous and are environmentally compatible. Generally, less than 100 ppm of acrylamide is present in the final product. The copolymer emulsion mixture containing the desired product is cooled and, if desired, the copolymer can be isolated as such. For example, the cooled emulsion can be poured into an excess of acetone, filtered and dried to form a fine white powder. Alternatively, the emulsion can be vacuum distilled to remove the solvents, or spray dried. The dried product so obtained is a white, granular, pourable powder, which is completely soluble in water, and which has an intrinsic viscosity ranging from 10 to 25 dl/g, as determined by viscosity measurements conducted in a 4 percent sodium chloride solution. Alternatively, the copolymerized emulsion can be inverted to an oil-in-water emulsion for use in aqueous stock solutions. In order to make the copolymer emulsion self-inverting upon the addition of water, a sufficient amount of a suitable breaker surfactant must be employed. The particular breaker surfactant that will perform optimally with a given emulsion system can be readily determined by methods known to those skilled in the art. Typical breaker surfactants are those having high HLB numbers greater than 10, such as ethoxylated octyl and nonyl phenols, ethoxylated nonyl phenol formaldehyde resins, polyethylene oxide esters of fatty acids, dioctyl esters of sodium sulfosuccinate, and polyethoxylated alcohols. Suitable mixtures and combinations of breaker surfactants can also be employed. The nature of the breaker surfactant employed must be such as to provide a stable emulsion mixture upon addition to water. Preferably, a polyethoxylated aliphatic secondary alcohol having nine ethylene oxide units and a hydrophobic chain of 12 to 14 carbon atoms can be employed as a breaker surfactant for the copolymer emulsion systems described herein. Typically, the breaker surfactant is added in an amount from 0.5 to 10 percent by weight, based upon the total emulsion. Preferably from 2 to 5 percent of breaker surfactant, and still more preferably from 3 to 4 percent by weight of emulsion is employed. Upon addition to water the water-in-oil emulsion containing the breaker surfactant inverts and is converted to an oil-in-water emulsion. Once prepared, the emulsions of the present invention can be chemically modified in any manner known to the art. The term "chemically modified" is intended to cover any further treatment of the dispersed water soluble copolymer emulsions, including the addition of components without which the normally water-soluble polymeric particles would coagulate or agglomerate. Examples of such treatments are disclosed in US-A-4,052,353 and 4,171,296. The emulsion of the present invention may also be concentrated in any suitable manner, such as is disclosed in US-A-4,021,399. The following methods can be used to qualitatively and quantitatively determine the degree of DADMAC monomer incorporation into the final copolymer using the dried powder obtained from the emulsion or the self invertable emulsion. (1) Solubility in Methanol Copolymers of DADMAC and acrylamide having a DADMAC content greater than 30 mole percent are soluble in methanol. Copolymers in the range of 30 mole percent are soluble in methanol, if, in addition, the methanol contains 10 to 20 percent water. Copolymers of low DADMAC content, as well as the homopolymer of acrylamide are totally insoluble in methanol or mixtures of 80 percent methanol and 20 percent water. The fact that the 50 mole percent copolymer of Example 4 and the 30 mole percent copolymer of Example 3 are soluble in methanol and a methanol-water mixture (80 percent / 20 percent), respectively, demonstrates that no homopolyacrylamides or copolymers of low DADMAC content are present in these copolymers. (2) Colloidal Titration Using Potassium Polyvinyl Sulfate Using the method described by W Schempp et al. , Papier, 36 (10A), 41-6 (1982), the cationicity of the various copolymers produced can be determined. This procedure provides a method for determining the cationic charges bound to the particular polymer tested as expressed in eg/kg. Comparison with the theoretical calculated values, enables the calculation of the degree of DADMAC conversion. The copolymers produced in accordance with this invention are used as aids in the dewatering of a wide variety of aqueous suspensions. These copolymers are particularly useful in the dewatering of organic sludge suspensions that are proteinaceous in nature or the dewatering of suspensions that have been obtained by the biological degradation of such matter. Such suspensions can be derived from raw or processed sewage, food waste, and fermentation effluents. The copolymers of this invention are also useful in the clarification of various types of industrial waste waters. It is frequently desirable to dewater such sludges or suspensions in order to facilitate their removal and their disposal. Dewatering can be effected by the addition of an appropriate amount of the copolymer as a flocculating agent prior to the physical removal of water. Dewatering of sludges or suspensions is usually effected by the addition of an aqueous solution of the polymer having a concentration ranging from 0.01 to 1 percent by weight of polymer. Preferably from 0.05 percent to 0.5 percent of copolymer solution is employed. Typical addition rates for sewage sludge are in the range of 0.2 to 1.0 percent of polymer per total weight of sewage solids. The copolymers of this invention are also useful in the paper industry as drainage and retention acids in the manufacture of paper, and in the dewatering of aqueous effluents containing cellulosic fibers. Such uses include, for example, treating aqueous waste water from a paper mill prior to discharge of the effluent, or treating return process water for the papermaking process. Such water may contain suspensions of cellulose or other finely divided particles in concentrations ranging from 50 ppm to 1 or 2 percent by weight of solution. The copolymers of this invention are particularly useful and are generally employed as 0.01 to 1 percent solutions. However, it is sometimes more convenient to prepare 1 to 2 percent stock solutions, from which the copolymers can be utilized. The invention described and claimed herein is more particularly illustrated in conjunction with the following examples, which are not intended to limit the invention in any way. E xample 1 The aqueous phase and the oil phase to form the water-in-oil copolymer emulsion are prepared separately, mixed and emulsified by shear stirring. To prepare the aqueous phase 105.5 g of a 60 percent aqueous solution of DADMAC, 77 g of a 50 percent aqueous solution of acrylamide, 1.0 g of Versenex™ 80, a 40 percent aqueous solution of the pentasodium salt of diethylenetriaminepentaacetic acid, 0.25 g of 2,2′-azobis (N,N′-dimethylisobutyramidine) dihydrochloride, 1.00 g of sodium persulfate, 12.0 g of sorbitan monooleate and 120.8 g of water are dispersed with rapid mixing to form a hazy mixture, which is neutralized with a molar hydrochloric acid solution to a pH of 7. The oil phase is prepared by dissolving 6.0 g of oleic isopropanol amide in 255.0 g of Isopar M synthetic isoparaffin solvent. The aqueous and the oil phase are mixed together with stirring and emulsified by mixing with a high speed stirrer at 10,000 to 20,000 rpm for 2 to 3 minutes. The monomer emulsion is transferred to a glass reactor, equipped with a mixing shaft, heating jacket, vacuum control, reflux condenser and inlet ports for stage addition, stirred at about 200 rpm, and purged with nitrogen for 30 minutes to remove all oxygen. To start copolymerization the monomer emulsion is heated to a temperature of 35°C and maintained at this temperature throughout the polymerization reaction. As soon as an increase in temperature is observed, the remaining 424.3 g of a deoxygenated 50 percent aqueous solution of acrylamide is added to the copolymer emulsion over a period of one hour, via stage addition, with constant stirring. The feed rate is adjusted so that approximately 29 percent of the acrylamide solution is added during the first quarter of the total time period, 26 percent is added during the second quarter, 24 percent during the third quarter, and the remaining 21 percent of the acrylamide solution is added during the final quarter of the total stage-addition of one hour. After completion of stage addition, the copolymer emulsion is maintained at 35°C for an additional 30 minutes with stirring. A 10 percent aqueous solution of sodium hypophosphite, 15 g, is slowly added to the copolymer emulsion to form a copolymer mixture that is stirred for an additional 30 minutes at 35°C. The temperature of the copolymer emulsion mixture is raised to 75°C and maintained at that temperature for 2 hours to reduce the amount of any residual monomer that may remain. The copolymer emulsion is cooled to room temperature and 40 g of a polyethoxylated aliphatic secondary alcohol having nine ethylene oxide units and a hydrophobic chain of 12 to 14 carbon atoms (sold by Deutsche BP Chemie GmbH as SOFTANOL™ 90 biological degradable surfactant) is added in small portions and mixed well over a period of 90 minutes. The final emulsion is discharged and passed through a 149 micro-meter screen to remove any coagulated gel particles that may have formed. The finished copolymer prepared in this fashion has an intrinsic viscosity of 18.3 dl/g when measured in a 4 percent sodium chloride solution at 25°C with a Brookfield LVT viscometer having a UL adapter. The cationicity, as determined by a potassium polyvinyl sulfate titration, shows an actual actual cationicity of 1.0 eq/kg, as compared to a theoretical cationicity of 1.25 eq/kg (79.8 percent DADMAC conversion). The copolymer is completely soluble in water and insoluble in methanol. Examples 2 to 4 Following essentially the same procedure as in Example 1, but making the following equivalent substitutions, uniform copolymers of DADMAC/acrylamide of varying cationicities were obtained. All weights are expressed in g. Example 2 3 4 Aqueous Phase Initial DADMAC charge (60 % solution) 158.0 276.3 422.4 Initial Acrylamide charge (50 % solution) 68.3 57.0 39.4 Water 131.4 111.4 82.2 Pentasodium salt of diethylenetriaminepentacetic acid (40 percent solution) 0.85 0.85 0.85 2,2′-azobis(N,N-dimethyleneisobutyramidine) dihydrochloride 0.25 0.25 0.25 2,2′azobis-(2-amidinopropane)-dihydrochloride 0.25 0.25 0.25 Sodium persulfate 1.0 1.0 1.0 Sorbitan monooleate 12.0 17.0 18.0 Oil Phase Isopar M synthetic isoparaffin solvent 255.0 255.0 255.0 Oleic isopropanol amide 6.0 1.0 - Stage addition 2 3 4 Acrylamide (50 percent solution) 369.8 283.0 193.5 Reaction Temp(°C) 35 35 35 Stage Addition (hrs) 2 3 4 pH of reaction mixture 7 7 7 The copolymers of DADMAC and acrylamide so obtained have the following properties: Example 2 3 4 Cationicity (mole percent) 16 30 50 Cationic Titration (eq/kg) Theoretical 1.87 3.05 4.3 Prior to Heating at 75°C 0.995 - 2.18 Final Product 1.53 2.28 3.56 DADMAC Conversion (%) Prior to Heating at 75°C 53.2 - 50.8 Final Product 81.8 74.8 82.8 Emulsion Viscosity (mPa·s) 2800 2800 2850 Intrinsic Viscosity (dl/g) 20.9 16.0 13.7 Solubility Water sol sol sol Solubility Methanol insol insol sol Comparative Examples 5 and 6 Following essentially the same procedure described in Examples 2 and 4, but without stage addition of the acrylamide monomer, copolymers of DADMAC and acrylamide are obtained which have the following properties: Example 5 6 Cationicity (mole percent) 16 50 Cationic Titration (eq/kg) Theoretical 1.87 4.3 Prior to Heating at 75°C 0.48 1.2 Final Product 1.36 3.43 DADMAC Conversion (percent) Prior to Heating at 75°C 25.7 29.8 Final Product 72.7 79.8 Intrinsic Viscosity (dl/g) 20.1 13.2 Solublility in water sol sol Solubility in methanol insol sol The properties concerning DADMAC conversion shown in Examples 5 and 6, in comparison to the results obtained in Examples 2 and 4, clearly demonstrate the advantage of stage addition. Using the process of stage addition, the DADMAC conversion prior to burn out is approximately twice as high as that obtained for the corresponding products prepared without stage addition. Moreover, even subsequent to burn out the DADMAC conversion is still higher by 3 to 10 percent. Comparative Examples 7 and 8 Following essentially the same procedure described in Examples 2 and 4, but omitting the use of sodium hypophosphite as a chain transfer agent, crosslinked DADMAC and acrylamide copolymers are obtained which are only partly soluble in water, and which demonstrate a reduction in intrinsic viscosity. Example 7 8 Cationicity (mole %) 16 50 Cationic titration (eq/kg) Theoretical 1.87 4.3 Actual 1.13 3.21 DADMAC conversion (%) 60.6 74.7 Intrinsic viscosity (dl/g) 13 10.2 Solubility in water partly sol/swells partly sol/swells Solubility in methanol insol partly sol/swells The results of the Examples 7 and 8, pertaining to the actual cationicity and intrinsic viscosity, demonstrate that crosslinking took place, in contrast to the corresponding Examples 2 and 4 in which a chain transfer agent was added. In this case the measured cationicity is reduced, because insoluble polymer particles (gel particles) include cationic charges which can not be detected by the titration method used. Intrinsic viscosity is also reduced since a certain amount of copolymer is bound by crosslinking, forming insoluble gel particles, which cannot contribute to the solution viscosity at low concentrations.

Claims: A process for the preparation of a water-soluble, linear copolymer of diallyl dimethyl ammonium chloride (DADMAC) and acrylamide having a uniform DADMAC to acrylamide ratio comprising the steps of: (a) preparing a water-in-oil monomer emulsion by mixing an oil phase containing an oil soluble emulsifying agent, with an aqueous phase comprising a mixture of DADMAC monomer, a portion of the total amount of acrylamide required, a polymerization initiator and a water-dispersible emulsifying agent; (b) initiating the copolymerization of said monomer emulsion by raising the temperature of the emulsion to a temperature of 30°C to 40°C; (c) adding the remaining acrylamide monomer to the monomer emulsion via continuous addition at a temperature of 20°C to 50°C to form a homogeneous copolymer emulsion; (d) thereafter homogenously mixing a chain transfer agent into said copolymer emulsion to form a copolymer emulsion mixture; and (e) heating said copolymer emulsion mixture to minimize residual monomer content. A process as claimed in Claim 1, wherein the oil phase comprises 25 to 30 volume percent of the total emulsion composition. A process as claimed in Claim 1 or Claim 2, wherein the oil phase emulsifying agent is oleic monoisopropanolamide. A process as claimed in any one of the preceding claims, wherein the water phase emulsifying agent is sorbitan monooleate. A process as claimed in any one of the preceding claims, wherein the oil phase comprises a branched-chain isoparaffin solvent. A process as claimed in any one of the preceding claims, wherein the polymerization temperature of step (c) does not exceed 40°C. A process as claimed in Claim 6, wherein the polymerization temperature of step (c) is 30°C to 40°C. A process as claimed in Claim 7, wherein said polymerization temperature is 35°C. A process as claimed in any one of the preceding claims, wherein 12 to 20 percent of the total amount of acrylamide monomer is added to step (a). A process as claimed in Claim 9, wherein 15 to 17 percent of the total amount of acrylamide monomer is added to step (a). A process as claimed in any one of the preceding claims, wherein the addition of the said remaining acrylamide in step (c) is over a period of 0.5 to 8 hours. A process as claimed in any one of the preceding claims, wherein the said remaining acrylamide is added in such a manner that a decreasing feed rate is achieved over the period of addition. A process as claimed in Claim 12, wherein 30 to 35 percent of the acrylamide is added during the first quarter of the said addition period, 25 to 30 percent is added during the second quarter, 20 to 25 percent is added during the third quarter, and 15 to 20 percent is added during the final quarter. A process as claimed in any one of the preceding claims, wherein the chain transfer agent is sodium hypophosphite. A process as claimed in any one of the preceding claims, wherein the heating of step (e) is conducted at 60 to 90°C for 0.1 to 4.0 hours. A process as claimed in any one of the preceding claims, wherein a breaker surfactant is added to the heated copolymer emulsion mixture to obtain a self inverting emulsion. A process as claimed in Claim 16, wherein the breaker surfactant is a polyethoxylate aliphatic secondary alcohol having nine ethylene oxide units and a hydrophobic chain of 12 to 14 carbon atoms. A process as claimed in any one of the preceding claims, wherein DADMAC comprises 5 to 95 mole percent of the total DADMAC and acrylamide content. A process as claimed in any one of Claims 1 to 17, wherein the DADMAC to acrylamide ratio is from 25 to 50 mole percent. A process as claimed in any one of the preceding claims, wherein the DADMAC content is greater than 20 mole percent of the total DADMAC and acrylamide content. A water-soluble, linear copolymer of diallyl dimethyl ammonium chloride (DADMAC) and acrylamide having a uniform DADMAC to acrylamide ratio throughout the polymer chain and an intrinsic viscosity of from 10 to 25 dl/g as determined in a 4 percent sodium chloride solution and obtainable by a process as claimed in any one of the preceding claims. A copolymer as claimed in Claim 21, wherein said intrinsic viscosity is from 15 to 20 dl/g. The use of a copolymer as claimed in Claim 21 or Claim 22 as a flocculant for aqueous suspension. The use of a copolymer as claimed in Claim 21 or Claim 22 as a drainage or retention aid in paper manufacture.

Inventors: GARTNER HERBERT ALFONS, GARTNER, HERBERT ALFONS
Applicants: DOW CHEMICAL CO, THE DOW CHEMICAL COMPANY
Application year: 1989
Main classification: C08F226
IPC codes: C08F226, D21H21, C02F1, C08F220