JP5780632B2 - Coagulation treatment agent and sludge dewatering method using the same - Google Patents

Description

The present invention relates to a coagulation treatment agent and a sludge dewatering method using the same, and more specifically, a cationic or amphoteric water-soluble polymer obtained by polymerizing a specific monomer in the presence of a crosslinkable monomer. The present invention relates to an aggregating agent containing (A) and a vinylamine-based aqueous polymer (B), and a sludge dewatering method using the same.

In order to improve the dewaterability of sludge, a large number of aqueous solution polymers having a crosslinkable or branched coexisting crosslinkable monomer are disclosed. Patent Document 1 and Patent Document 2 both disclose the use of a polymer of (meth) acrylic cationic monomer, acrylamide and a crosslinkable monomer as a sludge dehydrating agent. In the examples of these patent documents, a water-in-oil emulsion is used as the form, the copolymerization ratio of the (meth) acrylic cationic monomer is 50 to 60 mol%, and the (meth) acrylic cationic monomer is used. There is no description regarding highly cationic polymers such as a copolymerization rate of 80 to 100 mol% of the monomer. Furthermore, a blend of two or more kinds of polymers has been proposed for the purpose of improving the function. Patent Document 3 discloses a blend of a high cross-linking degree polymer and a low cross-linking degree polymer using a (meth) acrylic cationic monomer. Only mol% is described, and Patent Document 4
A formulation comprising a cationic polymer of 40-80 mol% crosslinkable polymer, a cationic polymer of 30-60 mol% crosslinkable amphoteric polymer and an acidic substance is disclosed. Therefore, it can be seen that there is no example of using a polymer having a copolymerization rate of 80 to 100 mol% of a crosslinkable (meth) acrylic cationic monomer as an aggregating agent.

On the other hand, a vinylamine copolymer is disclosed as a sludge dehydrating agent (Patent Document 4). It can be produced by hydrolyzing N-vinylformamide polymer in acidity or alkalinity, but because of its high price, it is blended with a crosslinkable aqueous polymer to reduce the cost by increasing the amount or to improve the effect on the high pH side. (Patent Document 5 or Patent Document 6). Patent Document 5 or Patent Document 6 is a blend with a (meth) acrylic crosslinkable aqueous polymer. In Examples, the copolymerization ratio of the cationic monomer is 20 to 80 mol%, 60%, respectively. It can be seen that -80 mol% is described, and 80 mol% to 100 mol% of the polymer is not described.

Japanese Patent Laid-Open No. 2-219887 JP-A 61-293510 JP 2005-144346 A JP-A-6-39208 JP 2010-159387 A JP 2004-25097 A

An object of the present invention is to develop a sludge dewatering agent having a high flocculation and cake moisture content reducing ability for sewage mixed raw sludge, sewage surplus sludge, sewage digested sludge, and various surplus sludge in a sewage treatment plant. Specifically, the vinylamine-based aqueous polymer exhibits excellent effects on various surplus sludges, but is expensive and has a very limited treatment pH range. Therefore, a part of the vinylamine-based aqueous polymer is used as it is, and a prescription for replacement with a commercially available (meth) acrylic aqueous polymer is examined.

As a result of intensive investigations to solve the above problems, the present inventors have reached the invention described below. That is, it has been found that the problem can be solved by an aggregating treatment agent characterized by containing the following (A) and (B).
(A): 80 to 100 mol of the monomer represented by the following general formula (1) or (2), 0 to 20 mol of the monomer represented by the following general formula (3), a nonionic monomer Polymerization of the monomer or monomer mixture consisting of 0 to 20 mol of a monomer with addition of 20 to 300 ppm of a crosslinkable monomer by mass with respect to the monomer or monomer mixture. Cationic or amphoteric aqueous polymer.
(B): An aqueous polymer having a vinylamine structural unit represented by the following general formula (4).

General formula (1)
(R ₁ is hydrogen or a methyl group, R ₂ and R ₃ are hydrogen, an alkyl or alkoxyl group having 1 to 3 carbon atoms, which may be the same or different, and R ₄ is an alkyl or alkoxyl group having 1 to 3 carbon atoms, An alkyl group having 1 to 3 carbon atoms, an alkyl group or aryl group having 7 to 20 carbon atoms, A represents an oxygen atom or NH, B represents an alkylene group or an alkoxylene group having 2 to 4 carbon atoms, X ₁ ⁻ represents an anion. Represent each)
General formula (2)
(R ₅ represents hydrogen or a methyl group, R ₆ and R ₇ each represent an alkyl group having 1 to 3 carbon atoms, an alkoxy group, and X ₂ ⁻ represents an anion)
General formula (3)
_{(R 8} is hydrogen, methyl or carboxymethyl group, Q represents ^{_{SO 3 -, C 6 H 4}} SO 3 -, CONHC (CH 3) 2 CH 2 SO 3 -, C 6 H 4 COO - or COO ^-,
R ₉ represents hydrogen or COO ⁻ , and Y ₁ ⁺ represents a hydrogen ion or a cation, respectively)
General formula (4)
R ₉ represents hydrogen or a methyl group, H ⁺ Z ⁻ represents an inorganic acid and / or an organic acid, and H ⁺ Z ⁻ = 0 when not neutralized.

The cationic or amphoteric aqueous polymer or the aqueous polymer having a vinylamine structural unit can be blended with the water-in-oil emulsion. Moreover, after manufacturing these water-in-oil emulsions, they can be agglomerated by emulsion breaking, and then dried to be finely divided into powders. Further, the water-in-oil emulsion of the cationic or amphoteric water-soluble polymer can be emulsion-breaked and agglomerated, dried and then powdered and blended.

The emulsion break of the water-in-oil emulsion is one or more selected from an ionic surfactant, a nonionic surfactant having an HLB value of 11 to 20, and an oil-soluble polymer compound having a hydrophilic group and a hydrophobic group. Use an emulsion breaker. The oil-soluble polymer compound is a copolymer of a monomer having a hydrophobic group and a monomer having a hydrophilic group. Examples of the monomer having a hydrophobic group include a monomer having an aromatic ring such as styrene or α-methylstyrene or an aromatic ring to which an alkyl group is added, an aromatic ring having 6 to 20 carbon atoms such as an α-olefin, or an aliphatic vinyl compound. It is. Moreover, the alkyl (meth) acrylate which has a C4-C18 alkyl group can also be used. Examples of the monomer having a hydrophilic group include dimethylaminopropyl (meth) acrylamide that is dialkylaminoalkylacrylamide, dimethylaminoethyl (meth) acrylate that is dialkylaminoalkyl (meth) acrylate, and the like.

The aggregation treatment agent of the present invention allows 20 to 300 ppm by mass relative to the total amount of monomers with respect to a monomer or monomer mixture containing a specific (meth) acrylic cationic monomer as an essential component. Formulation of polymerized cationic or amphoteric aqueous polymer (A) having a copolymerization rate of (meth) acrylic cationic monomer of 80 to 100 mol% and aqueous polymer (B) having a vinylamine structural unit It consists of things. The cationic or amphoteric aqueous polymer (A) referred to in the present invention is water-swellable even when it becomes water-soluble depending on the addition amount of the crosslinkable monomer that coexists during polymerization or the monomer composition to be copolymerized. It may become. These are collectively called aqueous polymer. Only the cationic or amphoteric aqueous polymer (A) can reduce the moisture content of the cake at the time of sludge dehydration, but the amount added increases and the processing cost increases. In addition, the vinylamine-based aqueous polymer (B) alone can reduce the moisture content of the cake when dewatering mixed raw sludge and excess sludge, but the vinylamine-based aqueous polymer (B) itself is expensive and increases the processing cost. . In addition, digested sludge having a sludge pH as high as about 8 cannot significantly cope with the aggregation performance. Therefore, by blending (A) and (B), it is possible to expand the types of sludge that can cope with an increase in processing cost as well as a decrease in the moisture content of the cake.

The cationic or amphoteric aqueous polymer or the aqueous polymer having a vinylamine structural unit can be easily blended in the same form. For example, a water-in-oil emulsion in which a water-immiscible hydrocarbon is a continuous phase and the cationic or amphoteric water-soluble polymer or an aqueous polymer having a vinylamine structural unit is an aqueous polymer aqueous solution as a dispersed phase. This is the case. Further, after the water-in-oil emulsion is produced, it can be agglomerated by emulsion breaking, and then dried to obtain a finely divided powder. The water-in-oil emulsion of the cationic or amphoteric water-soluble polymer is emulsion-breaked and agglomerated and then powdered after drying, and the aqueous polymer having vinylamine structural units is powdered by another method. It is conceivable to blend The most commonly used method of pulverization at present is considered to be various cases, such as mixing a high-concentration aqueous solution into a thin sheet by a sheet polymerization method, granulating with a meat chopper, etc., drying and pulverizing. It is done.

Vinylamine water-soluble polymers are characterized by their ability to insolubilize and agglomerate low-molecular-weight organic substances generated in the process of microorganisms, such as mixed raw sludge, sewage sludge, or excess sludge from food processing / fishery processing wastewater. However, it has been difficult to treat this action with (meth) acrylic cationic or amphoteric polymers. One reason for this is that (meth) acrylic cationic or amphoteric polymers have a very high molecular weight and are suitable for producing large, high-strength flocs due to cross-linking and adsorption, but they are generated during microbial treatment. The sludge is highly hydrophilic and has a low fiber content. In order to agglomerate such sludge, it is presumed that an insolubilizing function not necessarily accompanied by neutralization of surface charge is necessary. The elements necessary for this function are thought to be related to molecular weight, cation equivalent, balance between hydrophilicity and hydrophobicity, but in the present invention, molecular weight adjustment, high cationicity, polymerization with addition of a crosslinking agent, and high crosslinkability. It is thought that this was achieved by using a polymer.

With only the cationic or amphoteric aqueous polymer (A), the amount of drug required for a good dehydrated state is 2 to 3 times that of the vinylamine water-soluble polymer. On the other hand, only the cationic or amphoteric aqueous polymer (B) cannot reach the water content of the dehydrated cake of the vinylamine water-soluble polymer. Surprisingly, however, when both aqueous polymers are blended in a certain ratio, the dehydrating property can be equal to or higher than that of the vinylamine water-soluble polymer. The following reasons can be considered as this cause. Cationic or amphoteric aqueous polymer (A) is adsorbed on the hydrophilic colloid component in the sludge to be hydrophobized to form fine flocs, and then vinylamine (B) is grown to be larger, denser and stronger flocs The composition can be considered.

Of the flocculating agents comprising a blend of the cationic or amphoteric aqueous polymer (A) and vinylamine structural unit-containing aqueous polymer (B) of the present invention, the aqueous polymer (A) is:
A cationic monomer and a crosslinkable monomer, and, if necessary, a nonionic monomer or an amphoteric monomer in the case of amphoteric, can be produced by polymerizing a mixture of these monomers. The product form is not particularly limited, such as a water-in-oil emulsion, powder, or a dispersion in salt water, but a particularly preferred form is a powder obtained by finely granulating and drying a water-in-oil emulsion or a water-in-oil emulsion after emulsion breakage. Type. By adopting this form, the performance of the crosslinkable aqueous polymer can be sufficiently exhibited, and the performance of the water-in-oil emulsion can be maintained as it is by drying the water-in-oil emulsion by the above method.

In order to produce the aqueous polymer (A) of the present invention, a structural modifier, that is, a crosslinkable monomer that structurally modifies the polymer is used during polymerization. This crosslinkable monomer is present in a mass of 20 to 300 ppm, preferably 50 to 300 ppm, based on the total amount of monomers. Examples of the crosslinkable monomer include N, N-methylenebis (meth) acrylamide, triallylamine, ethylene glycol dimethacrylate, diethylene glycol dimethacrylate, triethylene glycol dimethacrylate, tetraethylene glycol dimethacrylate, and dimethacrylic acid. Acid-1,3-butylene glycol, polyethylene glycol di (meth) acrylate, N-vinyl (meth) acrylamide, N-methylallylacrylamide, glycidyl acrylate, polyethylene glycol diglycidyl ether, acrolein, glyoxal, vinyltrimethoxysilane In this case, the crosslinking agent is more preferably a water-soluble polyvinyl compound, and most preferably N, N-methylenebis (meth) acrylamide. Also, using a chain transfer agent such as sodium formate, isopropyl alcohol, sodium methallyl sulfonate, etc. is also effective as a method for adjusting the cross-linking property. The amount added is 0.001 to 1.0% by mass, preferably 0.01 to 0.1% by mass relative to the total amount of monomers.

The cationic monomers used in the present invention include the following. That is, monomers used for the polymerization of the cationic or amphoteric aqueous polymer (A) are dimethylaminoethyl (meth) acrylate and dimethylaminopropyl (meth) acrylamide, an alkyl group having 1 to 3 carbon atoms, and benzyl chloride. Alternatively, it is a quaternized product of a halide having an alkyl group or aryl group having 7 to 20 carbon atoms. Examples of the monomer represented by the general formula (1) include (meth) acryloyloxyethyltrimethylammonium chloride, (meth) acryloyloxy-2-hydroxypropyltrimethylammonium chloride, (meth) acryloylaminopropyltrimethylammonium. Chloride, (meth) acryloyloxyethylbenzyldimethylammonium chloride, (meth) acryloyloxy-2-hydroxypropylbenzyldimethylammonium chloride, (meth) acryloylaminopropylbenzyldimethylammonium chloride, and the like. Examples of the monomer represented by the general formula (2) include diallylmethylammonium chloride and diallyldimethylammonium chloride.

In the case of producing a water-soluble polymer comprising an amphoteric water-in-oil emulsion, a vinyl anionic monomer is used in combination with the vinyl cationic monomer. Examples thereof include vinyl sulfonic acid, vinyl benzene sulfonic acid or 2-acrylamido-2-methylpropane sulfonic acid, methacrylic acid, acrylic acid, itaconic acid, maleic acid, phthalic acid, and p-carboxystyrene acid.

When copolymerizing nonionic monomers, (meth) acrylamide, N, N-dimethylacrylamide, acrylonitrile, 2-hydroxyethyl (meth) acrylate, diacetone acrylamide, N-vinylpyrrolidone, N- Vinylformamide, N-vinylacetamide, acryloylmorpholine and the like can be mentioned.

The copolymerization ratio of these monomers is as follows. The cationic monomer is 80 to 100 mol%, the anionic monomer is 0 to 20 mol%, and the nonionic monomer is 0 to 20 mol%. However, in the present invention, since the neutralizing action of the surface charge of the suspended particles is the first function, the cationic property is preferably high, and the cationic monomer is 90 to 100 mol%, the anionic monomer is 0 to 10 More preferably, it is a mol% and a nonionic monomer 0-10 mol%.

The cationic or amphoteric aqueous polymer (A) of the present invention preferably has a weight average molecular weight of 1,000,000 to 10,000,000, more preferably 1,000,000 to 8,000,000, still more preferably 3,000,000 to 6,000,000 by light scattering. . The sludge dehydrating agent plays a major role in neutralizing the surface charge of the hydrophilic colloid, and this action does not necessarily require an ultra-high molecular weight aqueous polymer, and the cation equivalent value plays an important role. However, at the same time, it is necessary to form a strong floc that is tightened by aggregating action due to cross-linking adsorption, and a molecular weight higher than a certain level is required. Therefore, a weight average molecular weight becomes said range. This is considered to be related to the fact that the molecular weight of a flocculant composed of a polyamidine polymer currently on the market is 3 million to 5 million.

A method for producing the vinylamine structural unit-containing aqueous polymer (B) is disclosed in JP-A-6-65329. The water-soluble copolymer having a polyvinylamine and a polyvinylamine repeating unit used in the present invention can be easily obtained by modifying a formyl group in the polymer with an N-vinylformamide polymer or copolymer. That is, the molar ratio of N-vinylformamide to other copolymerizable monomer is usually a mixture of 20:80 to 100: 0, preferably 40:60 to 100: 0. It is produced by polymerizing in the presence.

Since the formyl group is hydrolyzed with an acid or alkali, a part of the copolymerized monomer is also hydrolyzed to generate a carboxyl group in many cases. Therefore, when copolymerizing, it is convenient when acrylonitrile or the like is copolymerized. Other acrylamide, methyl acrylate, ethyl acrylate, npropyl acrylate, 2-hydroxyethyl acrylate, ethyl methacrylate, npropyl methacrylate, isopropyl methacrylate, nbutyl methacrylate, isobutyl methacrylate, methacrylic acid-sec Examples thereof include butyl and 2-hydroxyethyl methacrylate. Since these monomers generate anionic groups, the molar ratio in the copolymer is preferably less than 20 mol%.

As a polymerization method for producing the above N-vinylformamide copolymer, any of bulk polymerization, solution polymerization using water and various organic solvents, and precipitation polymerization can be used. As a preferable polymerization solvent, water, an organic solvent having a boiling point of 60 to 110 ° C., and a mixture of water and a hydrophilic organic solvent having a boiling point of 60 to 110 ° C. are used. When the monomer is polymerized in the form of a solution, the monomer concentration, polymerization method, and shape of the polymerization reactor are appropriately selected in consideration of the molecular weight of the target polymer and polymerization heat generation. Polymerization is carried out by the method. That is, polymerization is started in a solution state under a monomer concentration of 5 to 20% by weight, and the polymerization is started under a method of obtaining a polymer as a solution or a precipitate, under a monomer concentration of 20 to 60% by weight. And a method of obtaining a gel or precipitate containing a polymer and a solvent, a method of polymerizing a solution having a monomer concentration of 20 to 60% by weight in an emulsified or dispersed state in a solvent in which the monomer is not dissolved, and the like. Illustrated.

As the radical polymerization initiator, any of general initiators usually used for the polymerization of water-soluble or hydrophilic monomers is used. In order to obtain a polymer in good yield, an azo compound is used. preferable. When water is used as the polymerization solvent, a water-soluble azo compound is preferable, and examples thereof include 2,2'-azobis-2-amidinopropane hydrochloride and acetate, 4,4'-azobis-4-cyano. Examples include sodium salt of valeric acid, hydrochloride and sulfate of azobis-N, N'-dimethyleneisobutylamidine. The amount of these polymerization initiators used is usually in the range of 0.01 to 1% by weight based on the weight of the monomer. The polymerization reaction is generally performed at a temperature of 30 to 100 ° C. under an inert gas stream.

The obtained N-vinylformamide copolymer can be used in the form of a new vinylamine copolymer by modification in the form of a solution or dispersion as it is, or by dilution or dehydration or drying by a known method to form a powder. Can be combined. As the modification method used in this case, any method of modifying the N-vinylformamide copolymer under basic and acidic conditions can be used. When basic hydrolysis is carried out in water, the ester group in the polymer tends to be converted to a carboxyl group, which tends to yield an amphoteric copolymer containing a large amount of anionic groups. Become. However, in order to produce a polyvinylamine imparted with hydrophobicity, it is preferably modified under acidic conditions. As a preferable modification method of the N-vinylformamide copolymer, there are a method of acid hydrolysis in water, a method of acid hydrolysis in a hydrophilic solvent such as alcohol containing water, alcoholysis under acidic conditions, and formyl. Examples thereof include a method of modifying the group while separating it as a formate ester, and particularly preferred is alcoholysis under acidic conditions. By this method, a vinylamine copolymer substantially free of carboxyl groups can be obtained.

As the modifier used for acid modification, any compound that acts on strong acid can be used, for example, hydrochloric acid, bromic acid, hydrofluoric acid, sulfuric acid, nitric acid, phosphoric acid, sulfamine. Examples include acids and alkane sulfonic acids. The usage-amount of modifier | denaturant is suitably selected according to the target modification | denaturation rate from the range of 0.1-2 times mole normally with respect to the formyl group in a polymer. Further, the denaturation reaction is usually carried out at 40 to 100 ° C.

The ratio of the vinylamine structural unit in the vinylamine structural unit-containing aqueous polymer (B) to the total constitution is preferably 10 to 90 mol%, and more preferably 30 to 90 mol%. The weight average molecular weight by the light scattering method is preferably 1 million to 10 million, more preferably 3 million to 7 million.

Examples of oily substances composed of hydrocarbons used as dispersion media in the production of water-in-oil emulsions for both cationic or amphoteric aqueous polymers (A) and vinylamine structural unit-containing aqueous polymers (B) include paraffins. Or mineral oils such as kerosene, light oil, and middle oil, or hydrocarbon synthetic oils having characteristics such as boiling point and viscosity in substantially the same range as these, or a mixture thereof. As content, it is the range of 20 mass%-50 mass% with respect to the water-in-oil type emulsion whole quantity, Preferably it is the range of 20 mass%-35 mass%.

Examples of at least one surfactant having an amount effective to form a water-in-oil emulsion and HLB are HLB 3-11 nonionic surfactants, specific examples of which include sorbitan monooleate, Examples include sorbitan monostearate, sorbitan monopalmitate, and polyoxyethylene nonylphenyl ether. The amount of these surfactants to be added is 0.5 to 10% by weight, preferably 1 to 5% by weight, based on the total amount of the water-in-oil emulsion.

After the polymerization, a hydrophilic surfactant called a phase inversion agent is added to make the emulsion particles covered with the oil film easy to adjust to water, and the water-soluble polymer therein is easily dissolved. Dilute with and use for each application. Examples of hydrophilic surfactants are cationic surfactants and HLB 9-15 nonionic surfactants, such as polyoxyethylene polyoxypropylene alkyl ethers and polyoxyethylene alcohol ethers.

The polymerization conditions are usually appropriately determined depending on the monomer used and the copolymerization mol%, and the temperature is in the range of 0 to 100 ° C. In particular, when the water-in-oil emulsion polymerization method is applied, it is carried out in the range of 20 to 80 ° C, preferably 20 to 60 ° C. For the initiation of polymerization, a radical polymerization initiator is used. These initiators may be either oil-soluble or water-soluble, and can be polymerized by any of azo, peroxide, and redox systems. Examples of oil-soluble azo initiators are 2,2′-azobisisobutyronitrile, 1,1-azobiscyclohexanecarbonitrile, 2,2′-azobis-2-methylbutyronitrile, 2,2 Examples include '-azobis-2-methylpropionate, 4,4'-azobis- (4-methoxy-2,4-dimethyl) valeronitrile.

Examples of water soluble azo initiators are 2,2'-azobis (amidinopropane) dichloride, 2,2'-azobis [2- (5-methyl-imidazolin-2-yl) propane] hydrogen dichloride And 4,4′-azobis (4-cyanovaleric acid). Examples of redox systems include a combination of ammonium peroxodisulfate and sodium sulfite, sodium hydrogen sulfite, trimethylamine, tetramethylethylenediamine and the like. Examples of peroxides include ammonium or potassium peroxodisulfate, hydrogen peroxide, benzoyl peroxide, lauroyl peroxide, octanoyl peroxide, succinic peroxide, t-butylperoxy-2-ethylhexanoate, and the like. Can be mentioned.

A production method of a type in which a water-in-oil emulsion is dried and pulverized is performed as follows. After the water-in-oil emulsion is produced, the emulsion is broken and solidified, and the solidified product is crushed or finely divided and dried. If further pulverization is required, pulverize and adjust the particle size to obtain a product.

A known method can be used as a method for causing an emulsion break. Particularly effective is a method of adding an emulsion breaker and breaking the emulsion by applying mechanical shear. Furthermore, an emulsion break can be efficiently performed by heating.

An emulsion break can be achieved by adding a surfactant to one of the emulsion break methods to change the emulsification balance. As the surfactant, an ionic surfactant or a nonionic surfactant having an HLB value of 11 to 20 is used. Examples of the nonionic surfactant include polyoxyethylene, polyoxyethylene alkyl ether, polyoxyethylene alkylphenyl ether, polyoxyethylene polypropylene alkyl ether, and alkylamine. Examples of ionic surfactants include anionic surfactants such as alkyl sulfonates, alkyl benzene sulfonates, and alkyl ether carboxylates, and cationic surfactants such as alkyl ammonium salts, alkyl trimethyl ammonium salts, and alkyl pyridinium salts. Is mentioned.

Next, a method for emulsion breaking with a polymer compound having a hydrophilic group and a hydrophobic group will be described. The polymer compound having a hydrophilic group and a hydrophobic group is preferably one that substantially dissolves in the oil phase that is the continuous phase of the W / O emulsion. When a polymer compound having a hydrophilic group and a hydrophobic group is added to a W / O emulsion, the hydrophilic group is adsorbed on the surface of the aqueous phase particles, eliminating the emulsifier at the interface and destabilizing the emulsified state. By doing so, the emulsified state can be destroyed. The polymer compound having a hydrophilic group and a hydrophobic group can be obtained by copolymerizing a monomer having a hydrophilic group and a monomer having a hydrophobic group.

Examples of the monomer having a hydrophilic group include methoxy or phenoxy polyethylene glycol (polymerization degree of polyoxyethylene, hereinafter referred to as n =, 4, 9 or 23) (meth) acrylate, polyethylene glycol (n = 4, 9 or 23). ) Mono (meth) acrylate, polyethylene glycol mono (meth) allyl ether, methoxypolyethylene glycol monoallyl ether and the like. Further, ionic monomers are more preferable. For example, dimethylaminopropyl (meth) acrylamide which is dialkylaminoalkylacrylamide, dimethylaminoethyl (meth) acrylate which is dialkylaminoalkyl (meth) acrylate, (meth) acrylic acid, itacon Acid, fumaric acid, maleic acid,
Examples thereof include vinyl sulfonic acid, (meth) allyl sulfonic acid, sulfoethyl (meth) acrylate, styrene sulfonic acid, and acrylamide-2-methylpropane sulfonic acid.

Examples of the monomer having a hydrophobic group include a monomer having an aromatic ring such as styrene or α-methylstyrene or an aromatic ring to which an alkyl group is added, an aromatic ring having 6 to 20 carbon atoms such as an α-olefin, or an aliphatic vinyl compound. It is. Moreover, the alkyl (meth) acrylate which has a C4-C18 alkyl group can also be used. That is, butyl acrylate, 2-ethylhexyl acrylate, lauryl acrylate, stearyl acrylate, butyl methacrylate, 2-ethylhexyl methacrylate, lauryl methacrylate, stearyl methacrylate, and the like.

If the ratio of the hydrophilic monomer is too large, it cannot be dissolved in the oil phase. Therefore, if the ratio of the hydrophobic monomer is too large, the action as an emulsion breaker is weakened. The ratio of the hydrophobic monomer to the hydrophilic monomer is 90:10 to 30:70, preferably 70:30 to 40:60, as a molar ratio of hydrophobic monomer: hydrophilic monomer. is there. The average molecular weight of the polymer having a hydrophilic group and a hydrophobic group as measured by GPC is 5,000 to 100,000, preferably 10,000 to 50,000.

The polymer compound having a hydrophilic group and a hydrophobic group is preferably produced by solution polymerization in a hydrocarbon solvent of the same type as the hydrocarbon solvent used in the water-in-oil emulsion described later. By using a hydrocarbon solvent of the same type as the hydrocarbon solvent used in the water-in-oil polymer emulsion, workability is good when used as an emulsifier in the production of a water-in-oil polymer emulsion. Polymerization is performed at a monomer concentration of 20 to 80%, preferably 40 to 60%. The polymerization temperature is 30 to 180 ° C, preferably 40 to 150 ° C. For initiation of polymerization, an oil-soluble radical polymerization initiator is used. Polymerization can be carried out by any of azo, peroxide and redox systems, but azo is preferred. Examples of oil-soluble azo initiators are 2,2′-azobisisobutyronitrile, 1,1′-azobis (cyclohexanecarbonitrile), 2,2′-azobis (2-methylbutyronitrile), 2,2′-azobis (2-methylpropionate), 4,4-azobis (4-methoxy-2,4dimethyl) valeronitrile and the like.

The amount of emulsion breaker added is not particularly specified, but if the amount added is too small, the time required for emulsion break becomes too long. Since the emulsion breaker remains as an impurity after drying, it is not preferable that the amount added is too large. Therefore, the addition amount of the emulsion breaker is 0.1 to 10% by mass, preferably 0.5 to 3% by mass with respect to the amount of the water-in-oil emulsion.

In a system in which the emulsified state is unstable, an emulsion break can be caused only by applying a mechanical share. As a means for multiplying mechanical share, a method using a homogenizer or a mixer can be mentioned. Furthermore, an emulsion breaker can be caused in a short time by adding an emulsion breaker and multiplying the mechanical share.

Furthermore, an emulsion break can be efficiently caused by heating. The higher the heating temperature is, the shorter the time until the emulsion breaks is. However, when the heating temperature is too high, there is a problem that the hydrophilic polymer contained is deteriorated. Therefore, heating temperature is 50-150 degreeC, Preferably it is 70 degreeC-120.

The particle size can be controlled either before or after drying. In the case of controlling the particle size before drying, the method is not particularly limited, but a device for granulating a hydrogel such as a cutter, a meat chopper, and an extrusion molding machine is employed. Depending on the drying method, the agglomerate of hydrophilic polymer composed of a water-in-oil emulsion is pulverized and granulated to an appropriate size.

There is no restriction | limiting in particular in the drying method after granulation, Methods, such as hot air drying, conductive heat transfer drying, and radiant heat drying, can be used. In particular, hot air drying with good drying efficiency such as fluidized drying and aeration drying is preferable. By treating the solid matter dried after drying with a pulverizer or the like, fine particles having an average particle size on the order of micrometers can be obtained in addition to relatively large particles.

Among the aggregating agents containing the vinylamine aqueous polymer of the present invention, one aqueous polymer is a cationic or amphoteric crosslinkable aqueous polymer obtained by polymerizing a specific monomer in the presence of a crosslinkable monomer. It is. Moreover, the sludge recommended as a treatment target of the aqueous polymer of the present invention is sludge having a low fiber content such as digested sludge and surplus sludge generated by microbial treatment of each industrial wastewater. Or it is a sludge which contains many highly hydrophilic components, such as hydrophilic colloids, such as a mixture of surplus sludge and raw sludge. For these sludges with low fiber content, so-called linear water-soluble polymers are unlikely to form a strong floc that is applied to a sludge dewatering machine. That is, the linear water-soluble polymer exists in a state where the molecules are spread in water. It is considered that the aggregating action of a high-molecular weight cationic water-soluble polymer such as a polymerization system is caused by a binding action of a large number of suspended particles by a so-called “cross-linking adsorption action” by a molecular chain of the water-soluble polymer. However, the linear water-soluble polymer is in an extended state, and the aggregated floc formed by adsorbing the suspended particles therein is large but fluffy and difficult to become strong. Even if the amount added is increased to increase the strength, there is no improvement in floc. The cause of this is an extended state, so there are many contact sites with the suspended particles, and as a result, apparent charge saturation is likely to occur. It is only necessary to increase the agitation strength and destroy the generated floc to create a new adsorption surface. However, the above phenomenon occurs again, and eventually a small and strong floc is not generated.

On the other hand, the crosslinkable water-soluble polymer suppresses the spread of molecules in water by crosslinking. For this reason, it exists as a “density packed” molecular form, and when the crosslinking proceeds further, it becomes a water-swellable fine particle. The polymer flocculant usually used in the above-mentioned “density packed” molecular form is efficient when it is water-soluble. When the crosslinkable water-soluble polymer is added to the sludge, it adsorbs to the suspended particles and acts as an adhesive between the particles, resulting in aggregation of the particles. At this time, it is presumed that since it is in a “dense packed” molecular form, it binds to the particle surface at multiple points to form a tighter and stronger floc. Bonding at multiple points is excellent in adsorption performance to suspended particles, so that there are few unadsorbed water-soluble polymers, they are not released into sludge, and sludge viscosity does not increase. In addition, the cationic group present inside the molecule in a round shape does not contribute to charge neutralization of the suspended particles, but acts as a molecule with an apparently low degree of cationization, and is redispersed by cationic saturation. Will be less. As a result, it is considered that a strong floc that has been squeezed with a small size is formed, and when the machine is dehydrated, the water drainage is good and the moisture content of the cake is reduced.

Vinylamine water-based polymers are characterized by their ability to insolubilize and agglomerate low-molecular-weight organic substances generated in the process of microorganisms such as mixed raw sludge, sewage surplus sludge, or surplus sludge from food processing / fishery processing wastewater. It is thought that there is, but it has been difficult to treat this action with a (meth) acrylic cationic or amphoteric polymer. One reason for this is that (meth) acrylic cationic or amphoteric polymers have a very high molecular weight and are suitable for producing large, high-strength flocs due to cross-linking and adsorption, but they are generated during microbial treatment. The insolubilizing function of the highly hydrophilic sludge that does not involve neutralization of the surface charge or necessarily neutralization of the surface charge was low. This is thought to be influenced by molecular weight, cation equivalent, balance between hydrophilicity and hydrophobicity. In the present invention, these factors are polymerized by adjusting molecular weight, adding high cationicity, and adding a crosslinking agent. It is thought that the polymer could be hydrophobized and controlled by using a polymer.

At present, there is no general method for displaying the degree of crosslinking of the crosslinkable polymer. In the above-mentioned Patent Document 3, it is defined by “ionic recovery rate”, and in Japanese Patent Application Laid-Open No. 2005-144346, “charge inclusion rate” is defined. These charges are measured by applying the fact that they are less likely to appear outside. Here, it will be explained first that the degree of crosslinking is expressed by measuring viscosity. The aqueous polymer of the present invention has an AQV as its 0.2% by weight aqueous solution viscosity, and SLV as its viscosity in a 0.5% by weight 1N saline solution of the amphoteric water-soluble polymer.
30 ≦ AQV / SLV ≦ 300 (at 25 ° C.)
It is preferable that This number can be used to represent the degree of crosslinking. Crosslinkable ionic water-soluble polymers are cross-linked in the molecule, and therefore have the property that molecules are difficult to spread in water, and should be less spread in water than linear polymers. However, as the degree of crosslinking increases, the viscosity when measured with a B-type viscometer (a type of rotational viscometer) increases. The cause is presumed to be due to friction or entanglement between the rotor of the B-type viscometer (rotor at the time of measurement) and the solution, but it is not exactly known. On the other hand, the viscosity of the crosslinkable ionic water-soluble polymer in salt water decreases as the degree of crosslinking increases. Since the molecule is contracted by the cross-linking, it is considered that the influence is greatly influenced by a large amount of ions in the salt water. Therefore, for these reasons, the ratio of the two viscosity measurements, AQV / SLV, increases as the degree of cross-linking increases (if the cross-linking progresses further and becomes water-insoluble, this relationship does not hold). In the crosslinkable cationic or amphoteric aqueous polymer of the present invention, this value is about 30 to 300. In view of the fact that this value is about 10 to less than 30 for a linear water-soluble polymer or a weakly crosslinked aqueous polymer, the crosslinkable cationic or amphoteric aqueous polymer of the present invention is highly crosslinked. It can be seen that this is a water-soluble polymer.

Further, the above-described charge inclusion rate will be described. The charge inclusion rate is defined as follows. That is, definition 1) In the case of a water-soluble cationic polymer and an amphoteric and water-soluble polymer having a positive difference in the copolymerization rate between a cationic monomer and an anionic monomer, the charge inclusion rate [%] = (1− α / β) × 100
α is a titration amount obtained by titrating a water-soluble cationic polymer or an amphoteric water-soluble polymer aqueous solution adjusted to pH 4.0 with acetic acid with a potassium polyvinyl sulfonate aqueous solution. β is a water-soluble cationic polymer or an amphoteric water-soluble polymer aqueous solution adjusted to pH 4.0 with acetic acid, and an aqueous polyvinyl sulfonate potassium solution is used to neutralize the charge of the water-soluble cationic polymer or amphoteric water-soluble polymer. A titration amount obtained by adding a sufficient amount to perform, and then subtracting the titration amount titrated with an aqueous polydiallyldimethylammonium chloride solution from the blank value. Here, the blank value is a titration amount obtained by titrating a potassium polyvinylsulfonate aqueous solution with a polydiallyldimethylammonium chloride aqueous solution when no water-soluble cationic polymer or amphoteric water-soluble polymer aqueous solution was added.
Definition 2) Charge inclusion ratio [%] = (1−α / β) × 100 in the case of a water-soluble polymer that is amphoteric and has a negative difference in copolymerization rate between a cationic monomer and an anionic monomer
α is a titration amount obtained by titrating a water-soluble amphoteric polymer aqueous solution adjusted to pH 10.0 with ammonia with a polydiallyldimethylammonium chloride aqueous solution. β is a water-soluble amphoteric polymer aqueous solution adjusted to pH 10.0 with ammonia, and a polydiallyldimethylammonium chloride aqueous solution is added in an amount sufficient to neutralize the charge of the water-soluble amphoteric polymer, and then a potassium polyvinyl sulfonate aqueous solution Titration volume obtained by subtracting the titration volume titrated with the blank value. Here, the blank value is a titration amount obtained by titrating a diallyldimethylammonium chloride aqueous solution with a potassium polyvinyl sulfonate aqueous solution when no water-soluble amphoteric polymer aqueous solution was added.

That is, it can be said that a water-soluble polymer having a high charge encapsulation rate is a water-soluble polymer having a high degree of crosslinking, and a water-soluble polymer having a low charge encapsulation rate is a water-soluble polymer having a low crosslinking rate. The reason for this is explained as follows. A linear water-soluble polymer has a substantially “stretched” shape in a dilute solution. On the other hand, the crosslinkable water-soluble polymer has a rounded particle shape in the solution, and the ionic group present inside the particle is unlikely to appear on the outside and reacts slowly with the opposite charge. It is thought to happen.

For crosslinkable water-soluble cationic polymers and crosslinkable water-soluble amphoteric polymers that are amphoteric and have a positive difference in the copolymerization rate between the cationic monomer and the anionic monomer, the charge inclusion rate is It becomes as follows.
Charge inclusion rate [%] = (1−α / β) × 100
The titration amount α is obtained by dropping an aqueous solution of potassium polyvinyl sulfonate having an opposite charge onto a crosslinkable cationic (amphoteric) water-soluble polymer as a sample, and then “surface” (particles) of the water-soluble cationic (amphoteric) polymer. Meaning an ionic electrostatic reaction on an ionic group present on the surface portion.

Next, potassium polyvinyl sulfonate having an opposite charge more than the amount sufficient to neutralize the theoretical charge amount of the crosslinkable cationic (amphoteric) water-soluble polymer was added, the reaction time was sufficient, and then the surplus Of polyvinyl sulfonate is titrated with an aqueous diallyldimethylammonium chloride solution. Separately, titrate the potassium polyvinyl sulfonate solution with diallyldimethylammonium chloride aqueous solution without adding a crosslinkable cationic (amphoteric) water-soluble polymer, and give a blank value. This value is β after subtracting the titration amount when the functional polymer is added. The β value is considered to correspond to the theoretical charge calculated from the chemical composition of the crosslinkable cationic (amphoteric) water-soluble polymer. In other words, the cross-linkable cationic (amphoteric) water-soluble polymer has a large amount of opposite charge, so it is considered that not only the surface cationic charge but also the internal charge is electrostatically neutralized. . If the degree of crosslinking is high, α is smaller than β, and the (1-α / β) value is larger than 1 and the charge inclusion rate is large (that is, the degree of crosslinking is high).

The charge inclusion rate of the crosslinkable water-soluble amphoteric polymer that is amphoteric and has a negative difference in the copolymerization rate between the cationic monomer and the anionic monomer can be explained in the same manner as described above. The only difference is that the pH is made alkaline with ammonia to dissociate the anionic group.

Regarding charge inclusion, 20% to 30% are weakly crosslinked aqueous polymers, 30% to 50% are moderately crosslinked aqueous polymers, and more than 50% are highly crosslinked aqueous polymers. it can. The aqueous polymer of the present invention is an aqueous polymer having a moderate degree of crosslinking of charge inclusion ratio of 30% or more. Here, AQV / SLV and the charge inclusion rate are compared. Sample-1 described in Table 1 of Paragraph 0063 is a highly crosslinked aqueous polymer having an AQV / SLV value of 45 and a charge inclusion rate of 47. On the other hand, Comparative-1 was polymerized with the addition amount of the crosslinking monomer coexisting outside the scope of the present invention, the AQV / SLV value was 11, the charge inclusion rate was 20%, and the weakly crosslinked aqueous high Comparative-2 is polymerized without addition of a crosslinking monomer, and their values are 7 and 13, which are almost linear polymers. In Comparative-3, the monomer composition is outside the scope of the present invention, but the crosslinking agent is within the scope of the present invention, the AQV / SLV value is 35, the charge inclusion rate is 40%, and the crosslinked aqueous polymer It is.

The agglomeration treatment agent comprising the aqueous polymer of the present invention is an organic sludge (so-called raw sludge, excess sludge, mixed raw sludge, digested sludge, coagulation / floating sludge, and mixtures thereof) produced in the treatment of sewage, human waste, and industrial wastewater. ) Is usually added as a 0.1 to 0.2 mass% aqueous solution. The addition amount is 0.2 to 2% by mass, preferably 0.3 to 1.0% by mass, as solid content with respect to sludge. Although not particularly limited to the target sludge, it is particularly effective and preferable for sludge having a low fiber content, sludge having a high organic content (VSS / SS), and sludge having a high degree of spoilage.

The blending ratio of the cationic or amphoteric aqueous polymer (A) and the vinylamine-based aqueous polymer (B) is by mass, and preferably (A) :( B) = 60: 40 to 10:90, more preferably (A). : (B) = 40: 60 to 10:90 (all are expressed in mass%). If the cationic or amphoteric aqueous polymer (A) is higher than 60% by mass relative to the whole, the amount added during sludge dehydration will increase, and if it is less than 10% by mass, the water content of the dehydrated cake cannot be reduced.

Further, the sludge dewatering agent comprising the amphoteric water-soluble polymer of the present invention may be used alone for sludge dewatering, but the dewatering effect may be further improved, but it is used in combination with such an inorganic flocculant. You can also Examples of the inorganic flocculant include salt iron, iron sulfate, polyiron, PAC, and sulfuric acid band. The addition amount with respect to sludge is 0.1-2 mass% normally with respect to sludge solid content, Preferably it is 0.3-1.0 mass%.

The type of dehydrator used can correspond to a belt press, a centrifugal dehydrator, a screw press, a multi-disc dehydrator, a rotary press, and the like.

(Examples) The present invention will be described in detail below with reference to examples, but the present invention is not limited to these examples.

(Production Example 1)
A reaction vessel equipped with a stirrer and a temperature controller was charged with 12.5 g of polyoxyethylene tridecyl ether (2.5% by mass of emulsion) and dissolved in 126.0 g of isoparaffin having a boiling point of 190 ° C. to 230 ° C. Separately, 103.1 g of deionized water, 250.0 g of an 80% aqueous solution of acryloyloxyethyltrimethylammonium chloride (hereinafter abbreviated as DMQ), and 3.0 g of a 1% by mass aqueous solution of methylenebisacrylamide (150 ppm by weight monomer) Collected and mixed to dissolve completely. Thereafter, the pH was adjusted to 3.95, the oil phase and the aqueous solution were mixed, and stirred and emulsified with a homogenizer at 1000 rpm for 15 minutes.

After adding 1.0 g of isopropyl alcohol 10 mass% aqueous solution (0.05 mass% monomer) to the obtained emulsion, maintaining the temperature of the monomer solution at 30 to 33 ° C. and performing nitrogen substitution for 30 minutes 2,2'-azobis [2- (5-methyl-2-imidazolin-2-yl) propane] dihydrochloride 2.0 g (0.01% by weight monomer) was added. The polymerization reaction was started. The reaction was completed at a reaction temperature of 32 ± 2 ° C. for 12 hours to complete the reaction. This sample name is designated as Sample-1. Viscosity (AQV) when the aqueous polymer concentration is 0.1% by mass for the sample used for the test, B type viscometer (rotary viscometer) at 25% at a viscosity (SLV) in 1N saline at 25% by mass And a weight-average molecular weight measured by a light scattering method using a PCD titration apparatus manufactured by Mutech.

By the same operation, an aqueous polymer having a composition as shown in Table 1, DMC = 100 (sample-2), DD = 100 (sample-3), and DMPQ = 100 (sample-4) were synthesized.

(Production Example 2)
A reaction vessel equipped with a stirrer and a temperature controller was charged with 12.5 g of polyoxyethylene tridecyl ether (2.5% by mass of emulsion) and dissolved in 126.0 g of isoparaffin having a boiling point of 190 ° C. to 230 ° C. Separately, 103.1 g of deionized water, 250.0 g of an 80% aqueous solution of acryloyloxyethylbenzyldimethylammonium chloride (hereinafter abbreviated as DMBZ), and 3.0 g of a 1% by mass aqueous solution of methylenebisacrylamide (150 ppm relative to the monomer). Each was taken and each was mixed and completely dissolved. Thereafter, the pH was adjusted to 4.03, the oil phase and the aqueous solution were mixed, and stirred and emulsified with a homogenizer at 1000 rpm for 15 minutes.

After adding 1.0 g of isopropyl alcohol 10 mass% aqueous solution (0.05 mass% monomer) to the obtained emulsion, maintaining the temperature of the monomer solution at 30 to 33 ° C. and performing nitrogen substitution for 30 minutes 2,2'-azobis [2- (5-methyl-2-imidazolin-2-yl) propane] dihydrochloride 2.0 g (0.01% by weight monomer) was added. The polymerization reaction was started. The reaction was completed at a reaction temperature of 32 ± 2 ° C. for 12 hours to complete the reaction. This sample name is designated as Sample-5. Viscosity (AQV) when the aqueous polymer concentration is 0.1% by mass for the sample used for the test, B type viscometer (rotary viscometer) at 25% at a viscosity (SLV) in 1N saline at 25% by mass And a weight-average molecular weight measured by a light scattering method using a PCD titration apparatus manufactured by Mutech.

(Production Example 3)
A reaction vessel equipped with a stirrer and a temperature controller was charged with 12.5 g of polyoxyethylene tridecyl ether (2.5% by mass of emulsion) and dissolved in 126.0 g of isoparaffin having a boiling point of 190 ° C. to 230 ° C. Separately, 101.0 g of deionized water, 246.1 g of 80% aqueous solution of acryloyloxyethylbenzyldimethylammonium chloride (hereinafter abbreviated as DMQ), 4.4 g of 50% by mass of acrylamide (hereinafter abbreviated as AAM), and 1% by mass of methylenebisacrylamide 3.0 g of aqueous solution (with respect to the monomer of 150 ppm by mass) was sampled, and each was mixed and completely dissolved. Thereafter, the pH was adjusted to 3.95, the oil phase and the aqueous solution were mixed, and stirred and emulsified with a homogenizer at 1000 rpm for 15 minutes.

After adding 1.0 g of isopropyl alcohol 10 mass% aqueous solution (0.05 mass% monomer) to the obtained emulsion, maintaining the temperature of the monomer solution at 30 to 33 ° C. and performing nitrogen substitution for 30 minutes 2,2'-azobis [2- (5-methyl-2-imidazolin-2-yl) propane] dihydrochloride 2.0 g (0.01% by weight monomer) was added. The polymerization reaction was started. The reaction was completed at a reaction temperature of 32 ± 2 ° C. for 12 hours to complete the reaction. This sample name is designated as Sample-6. Viscosity (AQV) when the aqueous polymer concentration is 0.1% by mass for the sample used for the test, B type viscometer (rotary viscometer) at 25% at a viscosity (SLV) in 1N saline at 25% by mass And a weight-average molecular weight measured by a light scattering method using a PCD titration apparatus manufactured by Mutech.

An aqueous polymer having a composition as shown in Table 1, DMBZ / AAM = 80/20 (Sample-7) was synthesized in the same manner.

(Production Example 4)
(Production of water-in-oil emulsion of N-vinylcarboxylic acid amide polymer oil) Isoparaffin having a boiling point of 190 ° C to 230 ° C in a four-necked 500 mL separable flask equipped with a stirrer, a reflux condenser, a thermometer and a nitrogen inlet tube. In 6 g, 13.0 g of a nonionic active agent HyperH1084 (manufactured by Croda) was charged and dissolved. Separately, 166.4 g of N-vinylformamide (pure 99.8% by mass), 0.16 g of sodium formate, and 134.9 g of ion-exchanged water were collected and added. The oil and the aqueous solution were mixed, and stirred and emulsified with a homomixer at 8000 rpm for 2 minutes. While stirring the obtained emulsion, the temperature of the monomer solution was kept in the range of 20 to 25 ° C., and after nitrogen substitution for 30 minutes, the polymerization initiator 2,2′-azobis (4-methoxy-2,4 -Dimethylvaleronitrile) (V-70 manufactured by Wako Pure Chemical Industries, Ltd.) 0.83 g (0.5% by mass of monomer) was added to initiate the polymerization reaction. The reaction was completed by polymerization for 12 hours while maintaining the temperature in the range of 20 to 25 ° C. This is designated as PNVF-1.

12. Four-necked 500 mL separable flask equipped with stirrer, reflux condenser, thermometer and dropping funnel, 252.6 g of PNVF-1 and polyoxyethylene stearyl ether (Emulgen 306P (HLB 9.4) manufactured by Kao Corporation) 6 g was sampled and stirred at 50 ° C. and sufficiently dissolved and mixed. After confirming dissolution, the mixture was heated to 80 ° C., 12.6 g of a 20% by mass hydroxylamine hydrochloride aqueous solution was added, and 123.5 g of hydrochloric acid (pure content 35% by mass) was added dropwise over 1 minute using a dropping funnel. The hydrolysis reaction was carried out for 4 hours. After the reaction, 20 g of polyoxyethylene alkyl ether (HLB13.3) was added to obtain a water-in-oil emulsion of polyvinylamine. This was designated as Sample-8, the viscosity (AQV) when the amination ratio and aqueous polymer concentration were 0.1% by mass, and the B-type viscosity at 25 ° C. with the viscosity (SLV) in 1N saline at 25 ° C. The weight average molecular weight was measured by a light scattering method.

(Production Example 5)
Samples 9 to 10 were synthesized in the same manner as in Production Example 1. The results are shown in Table 1.

(Comparative Production Example 1)
By the same operation as in Production Example 1, those obtained by polymerizing the addition amount of the crosslinkable monomer outside the scope of the present invention, those polymerized without coexistence, and Comparative-1 to Comparative-3 were synthesized. The results are shown in Table 1.

(Table 1)
DMC; methacryloyloxyethyltrimethylammonium chloride DMQ; acryloyloxyethyltrimethylammonium chloride DMBZ; acryloyloxyethyldimethylbenzylammonium chloride DMPQ; acryloylaminopropyltrimethylammonium chloride DD; diallyldimethylammonium chloride, MBA; methylenebisacrylamide, AAM; acrylamide , EM; Water-in-oil emulsion VAM; Vinylamine structural unit content (mol%)

(Combination of aqueous polymer (A) and aqueous polymer (B))
The aqueous polymer (A) Sample-1 to Sample-7 and the aqueous polymer (B) Sample-8 to Sample-10 were blended to prepare the aggregation treatment agent of the present invention. The results are shown in Table 2.

(Comparative Example 1)
(Comparison and formulation of aqueous polymer (B))
Comparison-1 to Comparison-3 and aqueous polymer (B) trial production-8 to trial production-10 were blended to prepare a comparative aggregation treatment agent. The results are shown in Table 2.

(Table 2)
Mixing ratio; mass ratio

Aqueous polymer (A) Sample-1, Sample-2, Sample-5 to Sample-7, and Comparative-1 to Comparative-3 consisting of water-in-oil emulsion described in Table 1 above, Aqueous polymer (B)
Using Sample-8 to Sample-9, agglomeration by emulsion break, subsequent granulation and further drying operation were carried out to prepare a powder type product.

(Production Example 5)
To 100 g of Sample-1, 1.0 g of dimethylaminoethyl methacrylate and 2-ethylhexyl acrylate copolymer (copolymerization ratio 50 mol%: 50 mol%) (weight average molecular weight 12000) was added and stirred with a magnetic stirrer. And agglomerated. The emulsion-breaked lump was supplied to a meat chopper having a die diameter of 4.8 mm to form a granule having a particle diameter of 4 to 6 mm. Thereafter, the granular material was dried and powdered at 105 ° C. for 1 hour using a shelf-type ventilation dryer. The obtained dry powder was crushed with a screen having a pore diameter of 2 mm. Moreover, the average particle diameter of the obtained powder was measured. This powder is designated as Sample-41.

The same operation was performed for Sample-2, Sample-5 to Sample-7, Comparative-1 to Comparative-3, Sample-8 to Sample-9, and the powder type aqueous polymer, Sample-41 to Sample-47 and the comparison were performed. -30 to Comparison -32 were created. The above results are shown in Table 3.

(Table 3)
Oil-soluble polymer; dimethylaminoethyl methacrylate 50 mol%: 2-ethylhexyl acrylate 50 mol% copolymer, weight average molecular weight 12,000

(Combination of aqueous polymer (A) and aqueous polymer (B))
The powdered aqueous polymer (A) Sample 41 to Sample-45 and the aqueous polymer (B) Sample -46 to Sample-47 were blended, and the aggregation treatment agent of the present invention, Sample-50 to Sample-59, and comparison The comparative product which mix | blended -30-comparative-32 and the aqueous | water-based polymer (B) sample-46, and comparative -40-comparative-42 were prepared. The results are shown in Table 4.

(Table 4)
Mixing ratio; mass

A sludge dewatering test was conducted using sewage digested sludge (pH 7.75, ss content 28, 100 mg / L) using the amphoteric water-soluble polymer of the present invention. 200 mL was collected in a poly beaker, samples 21 to 34 in Table 2 were added to each sludge SS content 0.80% (suspension particle mass%), the beaker was transferred and stirred 20 times. Then, it filtered with the T-1179L filter cloth (product made from nylon), measured the amount of filtrates 10 seconds later, and measured the floc intensity | strength (size) visually. Thereafter, the sludge filtered for 50 seconds is dehydrated at a press pressure of 3 kg / m ² for 1 minute. Thereafter, the filter cloth peelability was visually checked, and the cake water content (dried at 105 ° C. for 20 hours) was measured. The results are shown in Table 5.

(Comparative Example 1) Samples 1 to 3 and Samples 8 to 10 which are not blended by the same operation as in Example 3 and commercially available polyamidine flocculant comparison -A (amidine conversion rate 86 mol%) , Weight average molecular weight 3 million) and Comparative-3. The results are shown in Table 5.

(Table 5)

Moisture content of cake: mass%, 10 seconds later, filtrate amount: mL, floc strength: mm

Compared to the trial product 21 to the trial product 36, the pre-composition sample, the trial product 1 to the trial product 3, and the trial product 4 to the trial product 6 were added 2.5 times as much. It can be seen that the effects of both the drainage amount (related to the coagulation function) and the cake water content are reduced.

Using sludge mixed raw sludge (pH 6.61, ss content 21,300 mg / L), a sludge dewatering test was carried out using the water-soluble polymer composition of the present invention. 200 mL was collected in a poly-bicker, and pulverized sample 50 to sample-59 in Table 4 were added to each sludge SS content 0.75% (mass% of suspended particles), and the beaker was transferred and stirred 20 After the first time, the solution was filtered through a T-1179L filter cloth (made of nylon), and the amount of filtrate after 10 seconds and the floc strength (size) were measured visually. Thereafter, the sludge filtered for 50 seconds is dehydrated at a press pressure of 3 kg / m ² for 1 minute. Thereafter, the filter cloth peelability was visually checked, and the cake water content (dried at 105 ° C. for 20 hours) was measured. The results are shown in Table 6.

(Comparative Example 2)
Sample-43 to Sample-47 which are powdered samples not blended by the same operation as in Example 4, and commercially available polyamidine-based flocculant comparison-A (amidine conversion rate 86 mol%, weight average molecular weight 3 million) and comparison- Tests were performed on 40. The results are shown in Table 6.

(Table 6)

Moisture content of cake: mass%, 10 seconds later, filtrate amount: mL, floc strength: mm

The blends of trial production-50 to trial production-58, which are within the scope of the present invention, are exhibiting good effects in the same manner as the polyamidine of comparative-A. It can be seen that the effects of both the amount of filtrate (related to the coagulation function) and the moisture content of the cake are reduced despite the addition of 2.5 times.

Claims (3)

The following (A) and (B) are water-in-oil emulsions having a water-immiscible hydrocarbon as a continuous phase and a cationic or amphoteric aqueous polymer or an aqueous solution of a vinylamine aqueous polymer as a dispersed phase. After production, an emulsion breaker of an oil-soluble polymer compound having a hydrophilic group and a hydrophobic group having a weight average molecular weight of 5,000 to 100,000 is added to the water-in-oil emulsion and agglomerated by emulsion breaking. An agglomeration treatment agent characterized by being powdered after drying and containing 60:40 to 10:90 of the following (A) and the following (B) in a mass blending ratio .
(A): 80 to 100 mol of the monomer represented by the following general formula (1) or (2), 0 to 20 mol of the monomer represented by the following general formula (3), a nonionic monomer Polymerization of the monomer or monomer mixture consisting of 0 to 20 mol of a monomer with addition of 20 to 300 ppm of a crosslinkable monomer by mass with respect to the monomer or monomer mixture. A cationic or amphoteric aqueous polymer having a weight average molecular weight of 1,000,000 to 10,000,000 .
(B) An aqueous polymer having 10 to 90 mol% of vinylamine structural units represented by the following general formula (4) and having a weight average molecular weight of 1,000,000 to 10,000,000 .
General formula (1)
(R ₁ is hydrogen or a methyl group, R ₂ and R ₃ are hydrogen, an alkyl or alkoxyl group having 1 to 3 carbon atoms, which may be the same or different, and R ₄ is an alkyl or alkoxyl group having 1 to 3 carbon atoms, alkyl group or an aryl group of 7 to 20, a represents an oxygen atom or NH, B represents an alkylene group or an alkoxylene group having 2 to 4 carbon atoms, X ₁ ^- represents respectively an anion)
General formula (2)
(R ₅ represents hydrogen or a methyl group, R ₆ and R ₇ each represent an alkyl group having 1 to 3 carbon atoms, an alkoxy group, and X ₂ ⁻ represents an anion)
General formula (3)
_{(R 8} is hydrogen, methyl or carboxymethyl group, Q represents ^{_{SO 3 -, C 6 H 4}} SO 3 -, CONHC (CH 3) 2 CH 2 SO 3 -, C 6 H 4 COO - or COO ^-,
R ₉ represents hydrogen or COO ⁻ , and Y ₁ ⁺ represents a hydrogen ion or a cation, respectively)
General formula (4)
R ₁₀ represents hydrogen or a methyl group, H ⁺ Z ⁻ represents an inorganic acid and / or an organic acid, and H ⁺ Z ⁻ = 0 when not neutralized. The oil-soluble polymer compound is composed of 50 to 95 mol% of one or more monomers represented by the following general formula (5) and one or more monomers 5 to 95 represented by the following general formula (6). The aggregation treatment agent according to claim 1 , which is a cationic copolymer obtained by copolymerization of 50 mol%.
General formula (5)
Here, R ₁₄ is hydrogen or a methyl group, Z is a phenyl group, an aryl group having 7 to 18 carbon atoms, an alkyl group, or COOR ₁₅ . Here, R ₁₅ represents an alkyl group having 4 to 18 carbon atoms.
General formula (6)
R ₁₆ is hydrogen or a methyl group, R ₁₇ and R ₁₈ are alkyl groups having 1 to 3 carbon atoms,
R ₁₉ is hydrogen, an alkyl group having 1 to 3 carbon atoms, an alkoxyl group, or a benzyl group, and R ₁₇ and R ₁₈ may be different or the same. P represents oxygen or NH, and Q represents an alkylene group or alkoxylene group having 2 to 4 carbon atoms. X ₄ represents an anion. The following (A) and (B) are water-in-oil emulsions having a water-immiscible hydrocarbon as a continuous phase and a cationic or amphoteric aqueous polymer or an aqueous solution of a vinylamine aqueous polymer as a dispersed phase. After production, an emulsion breaker of an oil-soluble polymer compound having a hydrophilic group and a hydrophobic group having a weight average molecular weight of 5,000 to 100,000 is added to the water-in-oil emulsion and agglomerated by emulsion breaking. After drying, it is in the form of a finely divided powder, and the aggregating agent containing 60:40 to 10:90 in the following mass ratio (A) and (B) is added to sludge, mixed and stirred for aggregation. And then dewatering the sludge.
(A): 80 to 100 mol of the monomer represented by the following general formula (1) or (2), 0 to 20 mol of the monomer represented by the following general formula (3), a nonionic monomer Polymerization of the monomer or monomer mixture consisting of 0 to 20 mol of a monomer with addition of 20 to 300 ppm of a crosslinkable monomer by mass with respect to the monomer or monomer mixture. A cationic or amphoteric aqueous polymer having a weight average molecular weight of 1,000,000 to 10,000,000 .
(B) An aqueous polymer having 10 to 90 mol% of vinylamine structural units represented by the following general formula (4) and having a weight average molecular weight of 1,000,000 to 10,000,000 .
General formula (1)
(R ₁ is hydrogen or a methyl group, R ₂ and R ₃ are hydrogen, an alkyl or alkoxyl group having 1 to 3 carbon atoms, which may be the same or different, and R ₄ is an alkyl or alkoxyl group having 1 to 3 carbon atoms, An alkyl group having 1 to 3 carbon atoms, an alkyl group or aryl group having 7 to 20 carbon atoms, A represents an oxygen atom or NH, B represents an alkylene group or an alkoxylene group having 2 to 4 carbon atoms, X ₁ ⁻ represents an anion. Represent each)
General formula (2)
(R ₅ represents hydrogen or a methyl group, R ₆ and R ₇ each represent an alkyl group having 1 to 3 carbon atoms, an alkoxy group, and X ₂ ⁻ represents an anion)
General formula (3)
_{(R 8} is hydrogen, methyl or carboxymethyl group, Q represents ^{_{SO 3 -, C 6 H 4}} SO 3 -, CONHC (CH 3) 2 CH 2 SO 3 -, C 6 H 4 COO - or COO ^-,
R ₉ represents hydrogen or COO ⁻ , and Y ₁ ⁺ represents a hydrogen ion or a cation, respectively)
General formula (4)
R ₁₀ represents hydrogen or a methyl group, H ⁺ Z ⁻ represents an inorganic acid and / or an organic acid, and H ⁺ Z ⁻ = 0 when not neutralized.