mannich (alk)acrylamide microparticles are produced at high solids contents without a significant increase in bulk viscosity by inverse microemulsion polymerization and provide superior dewatering characteristics.
|
16. In a composition comprising water and (alk)acrylamide-based polymer, said (alk)acrylamide polymer being substituted with at least about 1 mole percent of tertiary aminomethyl groups which continually self cross-link the polymer at ambient conditions, the improvement wherein the composition is a microemulsion having dispersed polymer micelles of average diameter from about 350 to about 1000 Å.
11. In a composition comprising water and (alk)acrylamide-based polymer, said (alk)acrylamide polymer being substituted with at least about 1 mole percent of tertiary aminomethyl groups which continually self cross-link the polymer at ambient conditions, the improvement wherein the polymer comprises polymer micelles derived from a microemulsion, which micelles have an average particle size of from about 300 to 2000° Å in diameter.
1. A In a composition comprising (alk)acrylamide-containing polymeric microparticles, said (alk)acrylamide polymer being #10# a mannich (alk)acrylamide-based polymer substituted with at least about 1 mole percent of tertiary aminomethyl groups and which polymer undergoes extensive interpolymer crosslinking, the improvement comprising preparing said polymer as polymer micelles having an average particle size of from about 200 to about 4000 Å in diameter, which aminomethyl groups continually self cross-link the polymer at ambient conditions wherein said polymer micelles are derived from a microemulsion.
20. An inverse microemulsion comprising dispersed polymer micelles containing water and an acrylamide-based polymer substituted with at least about 1 mole percent of quaternized tertiary aminomethyl groups which are capable of continually self cross-linking the polymer at ambient conditions, said microemulsion containing greater than 10 percent, by weight, of polymer solids based on said microemulsion and said polymer micelles having average diameters from about 300 to about 2000 Å.
2. A composition as defined in
3. A composition as defined in
4. A microemulsion composition comprising the polymer as defined in
5. A microemulsion composition as defined in
6. A composition as defined in
8. A composition as defined in
10. A microemulsion composition according to
12. The composition of
13. The composition of
17. The composition of
21. The microemulsion of
|
|||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||
This reissue application is a continuation of reissue application Ser. No. 08/274,180 filed Jul. 12, 1994, now abandoned, which is a reissue of Ser. No. 07/428,730 filed Oct. 30, 1989, now U.S. Pat. No. 4,956,399, which is a continuation in part of Ser. No. 07/285,927 filed Dec. 19, 1988, now abandoned.
This invention relates to high solids inverse microemulsion, Mannich acrylamide polymers and their use as flocculants. More particularly, this invention relates to compositions comprising microparticles containing (alk)acrylamide polymers substituted with tertiary aminomethyl groups and having an average particle size of from about 200 to about 4000 Å in diameter.
High molecular weight Mannich polyacrylamides (PAMS) are well known and are used in a variety of flocculant applications. A major drawback of Mannich PAMS is their tendency to cross-link. This problem becomes more severe as the polymer solids are increased. Consequently, these polymers are generally made as dilute, aqueous solutions in an attempt to slow down the rate of interpolymer cross-linking. The solids level must also be kept low, particularly for very high molecular weight Mannich PAMS, owing to the ability of these polymers to viscosify water. As a result, solids levels of very high molecular weight Mannich PAMS must generally be well below 10%, and more typically 6% or less so that the solutions can be pumped and handled conveniently.
Several approaches have been tried to overcome these problems. One approach has been to make the Mannich PAMS at the site of use by inverting high solids inverse emulsion PAMS in water containing dialkylamines and formaldehyde. U.S. Pat. No. 4,021,394 and U.S. Pat. No. 4,022,741 describe continuous processes for the preparation of Mannich PAMS which entails inverting an inverse emulsion PAM in a process stream containing formaldehyde and a secondary amine and subjecting the stream to turbulence by in-line mixing to produce a 1-15% aqueous solution of Mannich PAM. This approach, however, suffers from the need to store multiple chemicals on site and from the problems inherent in running chemical reactions at such locations. Another approach has been to prepare dry Mannich PAMS, as described in U.S. Pat. No. 3,864,312; U.S. Pat. No. 3,539,535 and U.S. Pat. No. 3,790,529 or blends of dry PAMS with dry, low-molecular weight Mannich-base forming compounds which, when dissolved in water, react to produce Mannich PAMS, as described in EPO Patent No. 0,210,784. These approaches, in general, suffer from cross-linking problems, the reversibility of the Mannich reaction, the difficulty and length of time required to dissolve high molecular weight polymers, and other problems. Another approach has been to make the Mannich PAM in inverse emulsions, such as described in U.S. Pat. No. 3,979,348; U.S. Pat. No. 4,093,542 and U.S. Pat. No. 4,010,131. While this approach produces a product with substantially higher solids, the average particle size thereof ranges from about 10,000-20,000 Å in diameter, and consequently, cross-linking of the many polymer chains in each particle renders the products less effective. The cross-linking rate can be reduced somewhat by adding fairly large quantities of stabilizers, such as described in U.S. Pat. No. 4,113,685 and U.S. Pat. No. 4,073,763, but cross-linking continues and the products thus possess a very limited shelf life.
Accordingly, there exists a need for a Mannich acrylamide polymer which can be prepared at high solids levels without extensive interpolymer cross-linking such that it may be economically transported and easily handled by the end user without the need for any on-site preparation. Such a Mannich acrylamide polymer composition would satisfy a long felt need and constitute a notable advance in the art.
Surprisingly, it has now been discovered that Mannich acrylamide polymers, in the form of inverse microemulsions, give superior performance relative to the Mannich acrylamide polymers of the prior art and can be conveniently prepared at high solids content while maintaining a very low bulk viscosity. In contrast to solution and inverse emulsion Mannich acrylamide polymers of the prior art which contain large quantities of polymer molecules in the same aqueous environment, the Mannich acrylamide polymers of the present invention are isolated as individual, or at most, several, polymer molecules in each aqueous microemulsion micelle. Thus, the problem of large scale debilitating interpolymer cross-linking inherent in the solution and inverse emulsion products of the prior art is overcome.
Additionally, in contrast to the high bulk viscosities of the more stable dilute solution acrylamide polymers of the prior art, the novel microemulsion Mannich acrylamide polymers of the present invention can be made at high solids levels while still maintaining an extremely low bulk viscosity.
Even more unexpected with regard to the microemulsion Mannich acrylamide polymers of the instant invention is the fact that even though cross-linking thereof still occurs, the cross-linked polymers are capable of successfully performing an effective flocculants in the dewatering of suspended solids, whereas the cross-linked inverse emulsion and solution Mannich acrylamide polymers fail.
According to the present invention, there is provided compositions comprising (alk)acrylamide-containing polymeric microparticles, the (alk)acrylamide polymer being substituted with at least about 1 mole percent of tertiary aminomethyl groups and having an average particle size of from about 200 to about 4000 Å in diameter. It is preferred that the average particle size range from about 300 to about 2000 Å in diameter and even more preferred that it ranges from about 350 to 1000 Å in diameter. Also provided by the present invention are microemulsions comprising the above-defined modified polymers wherein the polymer solids content is greater than 10 percent, by weight, based on said composition and, preferably, greater than 20 percent, by weight.
The above defined compositions preferably comprise polyacrylamide substituted with said aminomethyl groups.
Also, according to the present invention are provided processes for the preparation of compositions as defined above. In one embodiment, the composition is prepared by
(a) admixing
(i) an aqueous solution of at least one (alk)acrylamide monomer and, optionally, at least one ethylenically unsaturated comonomer;
(ii) an oil solution comprising at least one hydrocarbon liquid; and
(iii) an effective amount of surfactant or surfactant mixture so as to form an inverse microemulsion;
(b) subjecting the inverse microemulsion obtained in step (a) to polymerization conditions;
(c) reacting the polymerized polymer obtained in step (b) with an effective amount of a formaldehyde and a secondary amine or a complex thereof; and
(d) optionally, quaternizing the resultant polymer.
In a second embodiment, the composition is prepared by
(a) reacting
(i) at least one (alk)acrylamide monomer and, optionally, at least one ethylenically unsaturated comonomer; and
(ii) formaldehyde and a secondary amine or a complex thereof in aqueous solution to produce a tertiary aminomethyl substituted (alk)acrylamide monomer;
(b) admixing
(i) said aqueous solution of substituted (alk)acrylamide monomer and, optional comonomer obtained in (a);
(ii) an oil solution comprising at least one hydrocarbon liquid; and (iii)an effective amount of surfactant or surfactant mixture, so as to form an inverse microemulsion;
(c) subjecting the inverse microemulsion obtained in step (b) to polymerization conditions; and
(d) optionally, quaternizing the resultant polymer.
A third embodiment sets forth a process for preparing the composition comprising
(a) admixing
(i) an aqueous solution comprising an (alk)acrylamide monomer and optionally, at least one ethylenically unsaturated comonomer, a formaldehyde and a secondary amine or a complex thereof;
(ii) an oil solution comprising at least one hydrocarbon liquid; and
(iii) an effective amount of surfactant or surfactant mixture, so as to form an inverse microemulsion;
(b) subjecting the inverse microemulsion obtained in step (a) to polymerization conditions and allowing the formaldehyde and secondary amine to react with the (alk)acrylamide amide groups; and
(c) optionally, quaternizing the resultant polymer.
Polymerization, according to the present invention, is carried out by the addition of a polymerization initiator or by subjecting the inverse microemulsion to ultraviolet or ionizing irradiation.
Formaldehydes useful in the practice of this invention are selected from formaldehyde, paraformaldehyde, trioxane or aqueous formalin, etc.
Useful secondary amines are selected from dimethylamine, methylethylamine, diethylamine, amylmethylamine, dibutylamine, dibenzylamine, piperidine, morpholine, ethanolmethylamine, ethanolmethylamine, diethanolamine or mixtures thereof.
Especially preferred is a process wherein the formaldehyde comprises formalin and the secondary amine comprises dimethylamine. It is also contemplated to employ a formaldehyde-secondary amine complex such as N,N-dimethylaminomethanol.
The ratio of formaldehyde to amine is not critical and can range from about 10:1 to 1:10, by mole, respectively. It is generally preferred, however, to use a molar ratio as close to 1:1 as practical. A sufficient quantity of the amine and formaldehyde or complex thereof is required to impart at least 1 mole percent of the tertiary aminomethyl groups to the acrylamide polymer.
According to the present invention there are also provided a method of releasing water from a dispersion of suspended solids which comprises (a) adding to the dispersion from about 10 to about 100,000 parts per million of a composition comprising (meth) acrylamide-containing polymeric microparticles, the (alk)acrylamide polymer being substituted with at least about 1 mole percent of tertiary aminomethyl groups and having a average particle size of from about 200 to about 4000 Å in diameter, and (b) dewatering the mixture of the dispersion of suspended solids and said composition. Dispersions of suspended solids comprising sewage sludge are exemplary.
Preparation of Mannich acrylamide polymers as small, aqueous inverse microemulsion droplets or micelles allows the composition to be prepared at a high polymer solids content while substantially eliminating the detrimental interpolymer cross-linking problems inherent in inverse emulsion and solution product forms thereof and while simultaneously maintaining a low product bulk viscosity.
The compositions of this invention comprise (alk)acrylamide-containing polymeric microparticles, the (alk)acrylamide polymer being substituted with at least about 1 mole percent of tertiary aminomethyl groups and having an average particle size of from about 200 to about 4000 Å in diameter and are generally prepared by an inverse microemulsion polymerization process.
The backbone of the Mannich acrylamide polymers of the present invention may comprise units of such (alk)acrylamides as acrylamide, methacrylamide, ethacrylamide and the like.
The backbones of the Mannich acrylamide polymers of the present invention may also comprise an (alk)acrylamide copolymerized with a cationic or non-ionic, water-soluble, ethylenically unsaturated comonomer in amounts up to about 90%, by weight. Water-soluble, anionic comonomers may also be used in substantially lower amounts.
Useful cationic monomers include diallyl dialkylammonium chlorides, N,N-dialkylaminoalkyl(meth)acrylates, N,N-dialkylaminoalkyl(meth)acrylamides, salts, quaternaries and mixtures thereof.
Anionic monomers useful in the practice of this invention may comprise acrylic or methacrylic acid, furmaric acid, crotonic acid; maleic acid, salts thereof; 2-acrylamido-2-methylpropane sulfonic acid; styrene sulfonic acid and their salts and the like.
Water-soluble, non-ionic monomers, suitable in the practice of this invention, generally comprise N-vinyl pyrrolidone, N,N-dialkylmethacrylamides, hydroxyalkyl methacrylates; N-vinylformamide; and the like. Small quantities, i.e. up to about 10% by weight, of other copolymerizable monomers, such as methyl acrylate; methyl methacrylate; acrylonitrile; vinyl acetate; styrene etc. may also be used.
Formaldehydes suitable for use in this invention, as mentioned above, are selected from formaldehyde; paraformaldehyde; trioxane; aqueous formalin and mixtures thereof. Secondary amines suitable for use in the practice of this invention are selected from those containing from about 2 to about 8 carbon atoms which are aliphatic, cyclic, straight chained or branched.
The compositions of the present invention may be prepared using inverse microemulsion polymerization techniques. Polymerization in microemulsions and inverse microemulsions is known to those skilled in this art. P. Speiser reported in 1976 and 1977 a process for making spherical "nanoparticles" with diameters less than 800 Å by (1) solubilizing monomers, such as acrylamide and methylenebisacrylamide and other materials, such as drugs in micelles and (2) polymerizing the monomers, see J. Pharm. Sa., 65 (12), 1763 (1976) and U.S. Pat. No. 4,021,364. Both water-in-oil and oil-in-water systems can be used to prepare these nanoparticles. While not specifically called microemulsion polymerization by the author, this prior art process does contain all the features which are currently used to define microemulsion polymerization. These reports also constitute the first examples of polymerization of acrylamide in a microemulsion. Since then, numerous publications reporting polymerization of water-soluble polymers in the inverse phase of microemulsions have appeared, see, for example, U.S. Pat. Nos. 4,521,317 and 4,681,912 and GB 2162492 A., GB 2161492 A, incorporated herein by reference.
In general, microemulsion polymerization processes are conducted by (i) preparing a monomer microemulsion by mixing an aqueous solution of monomers with a hydrocarbon liquid containing an appropriate surfactant or surfactant mixture to form an inverse microemulsion consisting of small aqueous monomer droplets dispersed in the continuous oil phase and (ii) subjecting the monomer microemulsion to free radical polymerization.
In order to obtain an inverse microemulsion, it is generally necessary to use particular conditions whose main parameters are as follows: surfactant concentration, HLB of surfactant or surfactant mixture, temperature, nature of the organic phase and composition of the aqueous phase.
Suitable monomers are non-ionic, anionic and cationic and are as defined above. The aqueous monomer solution may contain such conventional additives as are desired. For example, the solution may contain chelating agents to remove polymerization inhibitors, chain-transfer agents, pH adjusters, initiators and other conventional additives.
Essential to the formation of the microemulsion, which may be defined as a transparent and thermodynamically stable solution, comprising two liquids insoluble in each other and a surfactant, in which the micelles are usually 1000 Å or less in diameter, is the selection of appropriate organic phase and surfactant.
The selection of the organic phase has a substantial effect on the minimum surfactant concentration necessary to obtain the inverse microemulsion and may consist of a hydrocarbon or hydrocarbon mixture. Isoparaffinic hydrocarbons or mixtures thereof are the most desirable in order to obtain inexpensive formulations. Typically the organic phase will comprise mineral oil, toluene, fuel oil, kerosene, odorless mineral spirits, mixtures of any of the foregoing and the like.
The ratio by weight of the amounts of aqueous phase and hydrocarbon phase is chosen as high as possible, so as to obtain, after polymerization, a microemulsion of high polymer content. Practically, this ratio may range, for example from about 0.5 to about 3:1, and usually approximates 1:1.
The one or more surfactants are selected in order to obtain an HLB (Hydrophilic Lipophilic Balance) value ranging from about 8 to about 12. Outside this range, formation of inverse microemulsions generally cannot be attained. In addition to the appropriate HLB value, the concentration of surfactant must be optimized, i.e., sufficient to form an inverse microemulsion. Too low a concentration of surfactant leads to the formation of standard inverse emulsions and too high a concentration results in increased costs and does not impart any significant benefit. Typical surfactants useful in the practice of this invention may be anionic, cationic or nonionic. Preferred surfactants include sorbitan monooleate, polyoxyethylene (20) sorbitan monooleate, sodium dioctylsulfosuccinate, oleamidopropyldimethyl amine, sodium isostearyl-2-lactate and the like.
Polymerization of the microemulsion may be carried out in any manner known to those skilled in the art. Initiation may be effected with a variety of thermal and redox free radical initiators, including peroxides, e.g. t-butyl peroxide; azo compounds, e.g. azobisisobutyronitrile; inorganic compounds, such as potassium persulfate and redox couples, such as ferrous ammonium sulfate/ammonium persulfate. Initiator addition may be effected any time prior to the actual polymerization per se. Polymerization may also be effected by photochemical irradiation processes, such as ultraviolet irradiation or by ionizing irradiation from a cobalt 60 source.
It is possible to perform the Mannich substitution reaction at various stages in relation to the inverse microemulsion polymerization. The formaldehyde and secondary amine may be added after the inverse microemulsion polymerization of the (alk)acrylamide and then reacted with the resultant polymer to form the tertiary aminomethyl group on the (alk)acrylamide polymer backbone. It is also possible to react the (alk)acrylamide monomer with the formaldehyde and secondary amine prior to the inverse microemulsion formation and before polymerization of the monomers. Also contemplated, is adding the formaldehyde and secondary amine to the aqueous solution prior to polymerizing and then polymerizing the (alk)acrylamide monomer and carrying out the Mannich reaction.
If desired, the Mannich polymers produced by the procedures of the present invention may be quaternized as is known in the art, such as by reacting the Mannich polymers with such quaternizing agents as methyl chloride, dimethyl sulfate, benzyl chloride and the like under known conditions.
The polymers of the present invention can conveniently be employed as flocculants prepared in the form of dilute aqueous solutions. These solutions can be prepared by inverting the microemulsion into water, optionally in the presence of a breaker surfactant, or by recovering the polymer from the microemulsion, such as by stripping or by adding the microemulsion to a solvent which precipitates the polymer, e.g. isopropanol or acetone, filtering off the resultant solids, drying and redispersing in water. The microemulsion can also be stripped to increase the percentage of polymer solids thereof.
Concentrating dispersions of suspended solids is carried out by adding an effective amount of the compositions of this invention, in solution form, to the suspension to remove water there to produce an effluent of desired characteristics.
The products of this invention are useful in facilitating a wide range of solid-liquid separation operations. The cationic polymers may be used in the dewatering of biologically treated suspensions, such as sewage and other municipal of industrial sludges, the drainage of cellulosic suspension such as those found in paper production, e.g. paper waste, and the settlement of various inorganic suspensions, i.e. refinery waste, food waste etc.
The following examples illustrate the present invention. They are not to be constructed to limit the claims in any manner whatsoever.
Standard Viscosity (SV) is measured by adding 50 gms of a 0.2% aqueous polymer solution to 50 gms of water, stirring the resulting mixture for 5 minutes to completely dissolve the salt, adjusting the pH to 5 and determining the viscosity at 25±0.1°C using a Brook-field viscometer (LVT model) with UL adapter at 50 rpm. Cationic equivalent (CEQ) is measured by the technique described in J. Chem. Ed., 62 (7), 627 (1985).
PAC Microemulsion Preparation100 gms of an aqueous solution (pH=3.5) containing 42.3 gms of acrylamide and 0.02 gms of 2-hydroxyethyl ethylenediaminetriacetic acid are pumped at the rate of 4.4 ml/min into 150 gms of an organic solution containing 128.5 gms of an isoparaffinic solvent having a b. p. 207°-254°C (IPS), 21.9 gms of polyoxyethylenesorbitol hepaoleate (PESH) and 7.8 gms of sorbitan sesquioleate (SS). A clear, monomer containing microemulsion is obtained.
0.424 gms of 2,2'-azobis-4-methoxy-2,4-dimethylvaleronitrile in 2 mls of ethyl acetate is added to the monomer containing microemulsion which was previously sparged for 40 minutes using nitrogen. Polymerization is conducted at 30°C The product is a clear, stable polyacrylamide (PAM) microemulsion (S.V.=3.8 cps).
N,N-dimethyaminomethanol (DMAM) is prepared by slowly adding 7.7 gms of 95 percent paraformaldehyde to a 100 ml flask containing 27.50 gms of a 55 percent aqueous solution of dimethylamine and 6.60 gms of deionized water, keeping the exotherm below 45°C The resultant DMAM solution is then filtered yielding a clear solution possessing 53.20 gms of DMAM solids.
30.0 gms of the above PAM microemulsion are placed in a suitable reactor. The emulsion is warmed to 30°C Next 10.0 gms of the DMAM solution prepared above are added to the PAM microemulsion at a rate of 0.08 ml/min. with gentle stirring. The resulting Mannich PAM microemulsion is stored at ambient temperature until use. After 24 hours, the polymer has a CEQ of 5.75 meq/g and S.V. of 2.5 cps.
The efficiency of dewatering a typical municipal sludge is determined as follows: 200 gms of sludge are carefully weighed into screw cap jars. Aqueous solutions of Mannich PAM flocculants are prepared by adding the microemulsion (or in the comparative examples, a solution of commercial Mannich PAM) to water so that the polymer concentration is 0.2 weight percent. Various doses of the polymer solutions are added to the sludge samples, water is added to bring the total weight to 250 gms, the mixtures are agitated for 90 seconds, the resulting flocculated sludge is poured into a Buchner funnel containing a filter cloth, and the free drainage is determined by measuring the volume of filtrate collected in 10 seconds. The results are set forth in Table 1, below.
| TABLE 1 |
| MANNICH PAM |
| OF |
| EXAMPLE NO. DOSE (ml) FILTRATE (ml) |
| 1 10 100 |
| 12.5 152 |
| 15 158 |
| 17.5 160 |
| 20 140 |
| 1C 10 60 |
| 12.5 120 |
| 15 140 |
| 17.5 160 |
| 20 128 |
| C = commercially available product |
Table 1 clearly shows the superior performance of the Mannich PAM microemulsion of Example 1 as compared to a typical, commercially available, solution Mannich PAM.
Examples 2-7 describe the preparation of PAM microemulsions which are used for the preparation of a series of Mannich PAM microemulsions.
To 150 gms of an organic solution containing 128.5g of IPS, 21.9 gms of PESH and 7.8 gms of SS are slowly added 100 gms of a pH 3.5 aqueous solution containing 42.3g of acrylamide and 0.02 gm of N-(2-hydroxyethyl)ethylenediaminetriacetic acid with stirring. The resulting clear, monomer microemulsion is sparged for 40 minutes with nitrogen. 0.0424 gm of 2,2'-azobis-4-methoxy-2,4 dimethylvaleronitrile in 2 mls of ethyl acetate is then added and the microemulsion polymerized at 30°C The resulting product is a clear, stable PAM microemulsion having a Standard Viscosity (S.V.) of 3.8 cps and a particle size average of 650 Å (median value as measured by transmission electron microscopy).
The procedure of Example 2 is again followed and produces a polyacrylamide microemulsion with an S.V. of 3.7 cps.
The procedure of Example 2 is used to prepare the PAM microemulsions of Examples 4-6 with the exception that the amount of emulsifier is altered as shown in Table II, below, to vary the resultant PAM microemulsion particle size.
| TABLE 2 |
| PAM MICRO- PARTICLE |
| EMULSION PESH-g SS-g SIZE (Å).alpha. S. V. (cps) |
| Example 4 18.72 6.66 590 3.7 |
| Example 5 15.60 5.55 710 3.5 |
| Example 6 12.48 4.44 960 3.6 |
| .alpha. = as measured by transmission electron microscopy |
| S. V. = Standard Viscosity |
Example 7 shows the preparation of a PAM microemulsion with a different emulsifier system.
To 145 gms of an organic solution containing 120 gms of IPS, 14.82 gms of PESH and 11.12 gms of the reaction product of diethanolamine and oleic acid (DOA) are slowly added 100 gms of a pH 3.5 aqueous solution containing 42.3 gms of acrylamide and 0.02 gm of N-(2-hydroxyethyl)-ethylenediaminetriacetic acid with stirring. The resulting clear, monomer containing microemulsion is sparged for 40 minutes with nitrogen. 0.0423 gm of 2,2'-azobis-4-methoxy2,4-dimethylvaleronitrile in 2 mls of ethyl acetate are then added and the microemulsion is polymerized at 30°C The resulting product is a clear, stable PAM microemulsion having an S.V. of 3.1 cps.
Example 8 describes the preparation of dimethylamine/formaldehyde (DMA/CH2 O) adducts used to prepare Mannich PAM microemulsions from the PAM microemulsions of Examples 2, 3, 6 and 7.
A. 10.08 gms of 95 percent paraformaldehyde are slowly added to a reaction vessel containing 26.3 gms of a 55 percent aqueous solution of dimethylamine keeping the exotherm below 45°C The resulting solution is filtered yielding a clear solution.
B. To 30.0 gms of the solution prepared in Example 8A are added 3.05 gms of 100 percent dimethylamine with mixing, bringing the DMA/CH2 O ratio from 1/1 to 1.25/1.
Examples 9-15 describe the preparation of Mannich PAM microemulsions with differing amounts of dimethylaminomethyl substitution from the PAM microemulsions of Examples 2, 3 and 6 and the DMA/CH2 O adduct from 8B.
30.0 gms of the PAM microemulsion from Example 2 are placed in a reaction vessel at ambient temperature. To this are slowly added 11.0 gms of the DMA/CH2 O adduct from Example 8B, with stirring, yielding a clear, Mannich PAM microemulsion. After approximately 24 hours, the microemulsion is inverted into water resulting in a Mannich PAM with an S.V. of 3.9 cps and a CEQ of 6.2 meq/g. The identical procedure is used to prepare the Mannich PAM microemulsions of Examples 10-15, which differ only in the amount of DMA/CH2 O adduct charged and the PAM microemulsion, as shown in Table 3.
| TABLE 3 |
| DMA/ PAM MICRO- |
| CH2 O EMULSION OF |
| EXAMPLE adduct(g) EXAMPLE NO. CEQ(meq/g) S. V. (cps) |
| 9 11.0 Ex. 2 6.2 3.9 |
| 10 6.6 Ex. 2 3.5 4.8 |
| 11 4.4 Ex. 2 3.3 4.6 |
| 12 2.2 Ex. 2 -- 4.1 |
| 13 1.1 Ex. 3 -- 2.7 |
| 14 1.5 Ex. 3 -- 2.7 |
| 15 11.0 Ex. 6 -- 4.1 |
Example 16 is a repeat of Example 8A, with the exception being a slight dilution of the clear solution to reduce the adduct concentration.
22.3 gms of 95 percent paraformaldehyde are slowly added to a vessel containing 57.78 gms of a 55 percent aqueous solution of dimethylamine keeping the exotherm below 45°C The resulting solution is filtered yielding a clear solution. 12.30 gms of deionized water are then added.
Examples 17-19 describe the preparation of Mannich PAM microemulsions from PAM microemulsions of Examples 2, 6 and 7 and with a DMA/CH2 O (1/1) adduct.
30.0 gms of the PAM microemulsion from Example 2 are placed in a vessel at ambient temperature. To this are slowly added 10.0 gms of the DMA/CH2 O adduct of Example 16 with stirring, yielding a Mannich PAM microemulsion. After approximately 24 hours, the microemulsion is inverted into water resulting in a Mannich PAM solution with an S.V. of 3.7 cps and a CEQ of 5.6 meq/g. The identical procedure is used to prepare the Mannich PAM microemulsions of Examples 18-19 as shown in Table 4, except different PAM microemulsions are used.
| TABLE 4 |
| DMA/ PAM MICRO- |
| CH2 O EMULSION OF |
| EXAMPLE adduct(g) EXAMPLE NO. CEQ(meq/g) S. V. (cps) |
| 18 10.0 Ex. 7 5.1 2.4 |
| 19 10.0 Ex. 6 5.4 3.3 |
Example 20 describes the preparation of PAM microemulsion via redox initiation.
To 149.64 gms of an organic solution containing 128.5 gms of IPS, 21.9 gms of PESH and 7.8 gms of SS are slowly added 100 gms of a pH 3.0 aqueous solution containing 42.3 gms of acrylamide, 0.00428 gm of sodium bromate and 0.02 gm of N-(2-hydroxyethyl)ethylenediaminetriacetic acid with stirring. The resulting clear, monomer microemulsion is sparged for 40 minutes with nitrogen. SO2 gas is then bubbled into the microemulsion while holding the polymerization temperature at 25°C The resulting product is a clear, stable PAM microemulsion having an S.V. of 3.58 cps.
Examples 21 and 22 show the preparation of a morpholine/formaldehyde adduct and the Mannich PAM microemulsion prepared from this adduct.
10.08 gms of 95 percent paraformaldehyde are slowly added to a reaction vessel containing 27.84 gms of morpholine and 15.45 gms of water keeping the exotherm below 45°C The resulting solution is filtered yielding a clear solution.
30.0 gms of the PAM microemulsion from Example 2 are placed in a vessel at ambient temperature. To this are slowly added 11.80 gms of the morpholine/CH2 O adduct of Example 21 with stirring yielding a clear, Mannich PAM microemulsion. After approximately 17 days, the microemulsion is inverted into water giving a Mannich PAM solution with an S.V. of 1.4 cps and a CEQ of 3.1 meq/g.
Example 23 shows the preparation of a Mannich PAM microemulsion where formaldehyde and diethylamine are charged sequentially into the PAM microemulsion.
30.0 gms of the PAM microemulsion of Example 3 are placed in a vessel at ambient temperature. To this are slowly added 2.85 gms of 37.2 percent aqueous formaldehyde with stirring. Next, 2.56 gms of diethylamine are slowly added to the microemulsion with stirring, yielding a slightly hazy, Mannich PAM microemulsion. After 24 hours, the microemulsion is inverted into water giving a Mannich PAM solution having an S.V. of 2.1 cps and a CEQ of 3.0 meq/g.
Examples 24 and 25 show the preparation of a diethylamine/dimethylamine/formaldehyde (0.5/0.5/1) adduct and the Mannich PAM microemulsion prepared from this adduct.
10.08 gms of 95 percent paraformaldehyde are slowly added to a reaction vessel containing 12.83 gms of a 56 percent aqueous solution of dimethylamine, 11 67 gms of diethylamine and 8.32 gms of water, keeping the exotherm below 45°C The resulting solution separates into two layers The bottom layer, which weighs 32.6 gms is shown by NMR to be the desired diethylamine/dimethylamine/ formaldehyde (0.5/0.5/1) adduct. This layer is collected and used in Example 25 to prepare a Mannich PAM microemulsion.
30.0 gms of the PAM microemulsion of Example 3 are placed in a vessel at ambient temperature. To this is slowly added the diethylamine/dimethylamine/formaldehyde adduct of Example 24 with stirring to yield a clear, Mannich PAM microemulsion. After approximately 24 hours, the microemulsion is inverted into water giving a Mannich PAM with an S.V. of 2.8 cps and a CEQ of 4.04 meq/g.
Examples 26-28 describe the preparation of PAM copolymer microemulsions using acrylic acid (AA), 2-acrylamido-2-methylpropanesulfonic acid (AMMPS), and diallyl dimethylammonium chloride (DADM), respectively, as the comonomers with acrylamide. Examples 29-31 describe the preparation of Mannich PAM microemulsions from these systems.
To 299.3 gms of an organic solution containing 240 gms of IPS, 43.78 gms of PESH and 15.5 gms of SS are slowly added 200 gms of a pH 3.15 aqueous solution containing 80.38 gms of acrylamide, 4.29 gms of acrylic acid and 0.028 gms of N-(2-hydroxyethyl)-ethylenediaminetriacetic acid with stirring. The resulting clear monomer microemulsion is sparged for 40 minutes with nitrogen. 0.0424 gm of 2,2'azobis-4-methoxy-2,4-dimethylvaleronitrile, in 2 mls of ethyl acetate, are then added and the microemulsion is polymerized at 30°C The resulting product is a clear, stable acrylamide-acrylic acid copolymer microemulsion with an S.V. of 3.48 cps.
To 150 gms of an organic solution containing 120.0 gms of IPS, 15.0 gms of PESH and 15.0 gms of SS are slowly added 100 gms of a pH 8.5 aqueous solution containing 31.22 gms of acrylamide, 11.18 gms of AMMPS and 0.02 gm of N-(2-hydroxyethyl)-ethylenediaminetriacetic acid with stirring. The resulting monomer microemulsion is sparged for 40 minutes with nitrogen. 1.0 gm of a 4.24 percent solution of 2,2'azobis(2,4-dimethylpentane) nitrile in ethyl acetate and then added and the microemulsion is polymerized at 50°C The resulting product is a clear, stable, acrylamide-AMMPS copolymer microemulsion with an S.V. of 3.0 cps.
To 137.1 gms of an organic solution containing 120 gms of decane, 14.20 gms of PESH and 2.90 gms of polyoxyethylene sorbitan monooleate (POSO) are slowly added 106.97 gms of an aqueous solution containing 17.23 gms of acrylamide, 25.92 gms of DADM and 0.02 gm of N-(2-hydroxyethyl)-ethylenediaminetriacetic acid with stirring. The resulting clear, monomer microemulsion is sparged for 40 minutes with nitrogen. 0.0424 gm of 2,2'-azobis-4methoxy-2,4-dimethylvaleronitrile in 0.8 gm of ethyl acetate is then added and the microemulsion is polymerized at 30°C The resulting product is a clear, stable acrylamide-DADM copolymer microemulsion with an S.V. of 2.3 cps.
30.0 gms of the acrylamide/acrylic acid copolymer microemulsion of Example 26 are placed in a vessel at ambient temperature. To this are slowly added a solution of 9.50 gms of the DMA/CH2 O adduct of Example 16 and 0.36 gm of dimethylamine with stirring yielding a Mannich acrylamide-acrylic acid copolymer microemulsion. After approximately 24 hours, the microemulsion is inverted into water giving a Mannich copolymer with an S V. of 4.1 cps and a CEQ of 6.33 meq/g.
30.0 gms of the acrylamide/AMMPS copolymer microemulsion of Example 27 are placed in a vessel at ambient temperature. To this are slowly added 7.06 gms of a solution of the DMA/CH2 O adduct of Example 16 and 0.645 gm of dimethylamine with stirring yielding a Mannich acrylamide-AMMPS copolymer with an S.V. of 1.7 cps and a CEQ of 4.1 meq/g.
30 0 gms of the acrylamide/DADM copolymer microemulsion of Example 28 are placed in a vessel at ambient temperature. To this are slowly added 4.06 gms of a solution of the DMA/CH2 O adduct of Example 16 and 0.41 gm of dimethylamine with stirring yielding a Mannich acrylamide-DADM copolymer microemulsion. After approximately 24 hours, the microemulsion is inverted into water giving a Mannich copolymer with an S.V. of 2.3 cps and a CEQ of 6.70 meq/g.
Examples 32-35 describe the preparation of inverse emulsion PAMS with particle sizes of 3600 Å; 6600 Å; 11,400 Å and 20,500 Å which are then converted to Mannich PAM inverse emulsions by reacting them with DMA/CH2 O (1.25/1 and 1/1) adducts in Examples 36-39 and 40-43, respectively. The products of Examples 17, 19 and 40-43 are then used to determine the effect of particle size on flocculation performance.
The general procedure used to prepare the inverse emulsion PAMS is as follows: DOA and an A/B/A block copolymer of about 5000 m.w. wherein the A units comprise palmitic acid and 12-hydroxystearic acid (1:5) and the B units are polyethyleneoxide (m.w. 1500), hereinafter PHP, are dissolved in low odor paraffin solvent (OPS) to produce an oil solution. An aqueous monomer solution is prepared by dissolving a 52 percent aqueous solution of acrylamide, the disodium salt of ethylenediaminetetraacetic acid (EDTA-2Na) 2,2'azobis(2-amidinopropane) hydrochloride and Na2 SO4 in water, and then adjusting the pH to 3.0-3.5 with 10 percent sulfuric acid. The aqueous monomer solution is then added to the oil solution and emulsified. The resulting inverse emulsion is sparged with nitrogen and then initiated with UV light at 25°C The polymerization is continued for approximately 3.5 hours. The particle size average is a median value as measured by a Horiba particle size analyzer. The composition of the inverse emulsions and the resulting polymer characteristics are shown below in Table 5.
| TABLE 5 |
| Example Example Example Example |
| 32 33(C) 34(C) 35(C) |
| ON PHASE |
| OPS 70.8 70.8 70.8 70.8 |
| DOA 7.5 7.5 7.5 7.5 |
| PHP 1.25 1.25 1.25 1.25 |
| Acrylamide (52%) 86.6 86.6 86.6 86.6 |
| EDTA.2Na (10%) 0.23 0.23 0.23 0.23 |
| Na2 SO4 (1.93%) 3.58 3.58 3.58 3.58 |
| AQUEOUS PHASE |
| Azo Cat. (2%) 0.45 1.13 2.25 2.25 |
| Water 94.5 93.8 92.7 92.7 |
| POLYMER |
| Conversion, % 97.4 96.0 97.8 98.5 |
| S. V., cps 3.7 3.6 3.1 3.8 |
| Particle size Å 3,600 6,600 11,400 22,500 |
| *all components are given in grams |
| S. V. = standard viscosity |
| C = comparative |
The following is a general description of the method used to prepare the Mannich PAM inverse emulsions of Examples 36-43. 30.0 gms of PAM inverse emulsion from the previous designated example is placed in a vessel at ambient temperature. To this is slowly added a solution of DMA/CH2 O adduct with stirring yielding a stable Mannich PAM inverse emulsion. After several days, the Mannich PAM inverse emulsion is inverted into water giving a Mannich PAM and the S.V. and the CEQ are determined. The compositions of the examples and the resulting characteristics are shown in Table 6, below.
| TABLE 6 |
| Inverse DMA/ |
| Emul. of CH2 O wt. DMA/ Polymer Polymer |
| Example Ex. No. RATIO CH2 O(g) SV (cps) CEQ(meq/g) |
| 36 32 1.25 11.0 3.9 (3 days) 5.7 |
| 37 33 1.25 11.0 3.8 (3 days) 6.0 |
| 38 34 1.25 11.0 3.7 (3 days) 6.3 |
| 39 35 1.25 11.0 3.9 (3 days) 5.8 |
| 40 32 1.0 10.0 3.9 (2 days) 5.2 |
| 41 33 1.0 10.0 3.8 (2 days) 4.9 |
| 42 34 1.0 10.0 3.2 (2 days) 5.5 |
| 43 35 1.0 10.0 3.9 (2 days) 5.3 |
The performance of the Mannich PAM microemulsion of Example 9 is determined by free-drainage sludge dewatering tests as follows: 200 gms of sewage sludge from the Stamford, CT waste treatment plant is carefully weighed into screw cap jars. Aqueous solutions of Mannich PAM flocculant are prepared so that the concentration of polymer is 0.2%. Various doses of the solutions are added to the sludge samples, the sludge is agitated for 90 seconds, the resulting flocculated sludge is poured into a Buchner funnel containing a filter cloth, and the free drainage is determined by measuring the volume of filtrate collected in 10 seconds. The improved performance of Mannich PAM microemulsion from Example 9 (10 days old) compared to a commercially available Mannich PAM is clearly seen in TABLE 7.
| TABLE 7 |
| Mannich PAM |
| of Example No. Dose (ml) Filtrate (ml) |
| 9 9.5 70 |
| 10.5 108 |
| 11.0 135 |
| 12.5 125 |
| 13.0 125 |
| 15.0 105 |
| 9C 11.5 65 |
| 12.5 85 |
| 13.0 85 |
| 15.0 98 |
| 16.5 120 |
| 17.5 125 |
| 20.0 120 |
| C = commercially available product |
The significance of particle size on performance is determined by free-drainage testing of the aged (72 day old) microemulsions and inverse emulsions as shown in Table 8, below. The test results clearly show the increase in flocculant dose required as the particle size increases.
| TABLE 8 |
| Emulsion of Micelle Aged Polymer Aged Polymer |
| Example No. Size (Å) SV (cps) CEQ (meq/g) |
| 17 650 1.2 5.5 |
| 19 960 1.1 5.4 |
| 40 3,600 1.2 <0.2 |
| 41 6,600 1.1 <0.2 |
| 42 10,400 1.1 <0.2 |
| 43 20,500 1.1 <0.2 |
| Emulsion of |
| Example No. Dose (ml) Filtrate (ml) |
| 17 15 120 |
| 17.5 160 |
| 20 165 |
| 22.5 160 |
| 19 15 90 |
| 17.5 145 |
| 20 170 |
| 22.5 180 |
| 40 20 100 |
| 22.5 135 |
| 25 180 |
| 30 180 |
| 41c 20 55 |
| 30 100 |
| 35 165 |
| 37.5 180 |
| 40 185 |
| 42c 30 128 |
| 32.5 148 |
| 35 175 |
| 40 185 |
| 43c 30 98 |
| 40 130 |
| 50 175 |
| C = comparative |
The procedure of Example 1 is again followed except that the Mannich PAM microemulsion is subjected to treatment with dimethyl sulfate to quaternize the Mannich PAM. A quaternized polymer is recovered.
The procedure of Example 1 is again followed except that the acrylamide is replaced by an equivalent amount of methacrylamide. Substantially identical results are achieved.
The product of Example 27 is again followed, except that the AMMPS is replaced by 1-methacryloyl-4-methyl piperazine. Treatment of the resultant polymer as in Example 30 produces a similar Mannich copolymer.
To 246.05 grams of an organic solution containing IPS (199.7 gms), PESH (31.6 gms) and SS (13.9 gms) are slowed added 242.5 gms of a pH 3.0 aqueous solution containing acrylamide (109.8 gms) sodium bromate (0.0055 g) and N-(2-hydroxyethyl)ethylenediaminetriacetic acid (0.10 g) with stirring. The resulting, slightly cloudy, monomer microemulsion is sparged for 40 minutes with nitrogen. SO2 gas is then bubbled into the resultant microemulsion and the polymerization temperature kept at 55°C The SO2 gas is prepared by passing nitrogen gas through a 0.5% sodium metabisulfite solution. The resulting product is a clear, stable, polyacrylamide microemulsion having an S.V. of 2.7 cps.
A. Paraformaldehyde (92.4 gms, 95%) is slowly added to a suitable vessel containing a dimethylamine (218.4 gms, 60.4% aqueous solution) while keeping the exotherm below 45°C The resulting solution is allowed to cool with stirring and is then filtered yielding a clear solution.
B. To 70.0 gms of the product of Example 50A are added 17.13 gms of deionized water.
C. To 190.0 gms of the product of Example 50A are added 15.04 gms of dicyanadiamide, 18.62 gms of sodium bisulfite, and 12.86 gms deionized water. The solution is filtered yielding a clear solution.
150 gms of the PAM microemulsion of Example 49 are placed in a reaction vessel at ambient temperature. To this are slowly added 62.7 gms of the DMA/CH2 O adduct from Example 50B, with stirring, yielding a hazy, Mannich PAM microemulsion. After approximately 24 hours, the microemulsion is inverted into water giving a Mannich PAM with an S.V. of 2.65 cps and a CEQ of 6.6 meg/g.
150 gms of the PAM microemulsion of Example 49 are placed in a reaction vessel at ambient temperature. To this are slowly added 62.7 gms of the DMA/CH2 O adduct from Example 50C., with stirring, yielding a clear, Mannich PAM microemulsion. After approximately 24 hours, the microemulsion is inverted into water giving a Mannich PAM with an S.V. of 2.65 cps and a CEQ of 6.2 meg/g.
75 gms of the Mannich PAM microemulsion of Example 52 are placed in a pressure reactor mounted on a shaker. To this are added 8.5 gms of methylchloride at ambient temperature over a period of approximately 2 hours, keeping the pressure of the reactor under 30 psi. The resulting product is a clear, stable, quaternized Mannich PAM having an S.V. of 2.1 cps.
50 gms of the Mannich PAM microemulsion of Example 52 are placed in a pressure reactor mounted on a shaker. To this are added 4.5 gms of methylchloride at ambient temperature over a period of approximately 2 hours, keeping the pressure of the reactor under 30 psi. The resulting product is a clear, stable, quaternized Mannich PAM having an S.V. of 2.2 cps.
50 gms of the Mannich PAM microemulsion of Example 52 are placed in a pressure reactor mounted on a shaker. To this are added 2.9 gms of methylchloride at ambient temperature over a period of approximately 2 hours, keeping the pressure of the reactor under 30 psi. The resulting product is a clear, stable, quaternized Mannich PAM having an S.V. of 2.4 cps.
50 gms of the Mannich PAM microemulsion of Example 51 are placed in a pressure reactor mounted on a shaker. To this are added 6.0 gms of methylchloride at ambient temperature over a period of approximately 2 hours, keeping the pressure of the reactor under 30 psi. The resulting product is a clear, stable, quaternized Mannich PAM having an S.V. of 1.8 cps.
150 gms of the PAM microemulsion of Example 49 are placed in a reaction vessel at ambient temperature. To this are slowly added 25.1 gms of the DMA/CH2 O adduct from Example50C., with stirring, yielding a hazy, Mannich PAM microemulsion. After approximately 24 hours, the microemulsion is inverted into water giving a Mannich PAM with an S.V. of 2.65 cps.
50 gms of the Mannich PAM microemulsion of Example 57 are placed in a pressure reactor mounted on a shaker. To this are added 2.7 gms of methylchloride at ambient temperature over a period of approximately 2 hours, keeping the pressure of the reactor under 30 psi. The resulting product is a clear, stable, quaternized Mannich PAM having an S.V. of 1.4 cps.
The performance of the quaternized Mannich PAMs of Examples 53-56 and 58 is determined by free drainage sludge dewatering tests as follows: 200 gms of sewage sludge from a municipal waste treatment plant are carefully weighed into jars. Aqueous solutions of the quaternized Mannich PAM flocculant are prepared so that the concentration of polymer is 0.2%. Various doses of the resultant solutions are added to the sludge samples, the sludge agitated for 5 seconds at 300 rpm with an overhead mixer, the resulting flocculated sludge poured into a Buchner funnel containing a filter cloth and the free drainage determined by measuring the milliliters of filtrate collected in 10 seconds. The efficacy of the quaternized polymers (QP) as flocculants is clearly seen in Table 9, below, where they are compared to a commercially available cationic flocculant with similar charge.
| TABLE 9 |
| QP of Example Dosage (lbs/ton) Filtrate Vol. (ml.) |
| 53 3.72 140 |
| 5.58 155 |
| 7.44 155 |
| 9.30 160 |
| 54 3.72 140 |
| 5.58 155 |
| 7.44 155 |
| 9.30 160 |
| 55 3.72 145 |
| 5.58 155 |
| 7.44 170 |
| 9.30 165 |
| 56 3.72 130 |
| 5.58 155 |
| 7.44 165 |
| 9.30 170 |
| 58 3.72 48 |
| 5.58 50 |
| 7.44 60 |
| 9.30 95 |
| 11.16 110 |
| 13.02 115 |
| 14.88 120 |
| 16.74 128 |
| Comm. 1.86 125 |
| 3.72 140 |
| 5.88 148 |
| 7.44 148 |
| Comm. = Commercially available copolymer of acrylamide and |
| acryloxyethyl-trimethylammonium chloride (45/55). |
Following the testing procedure set forth above, (Example 59) except where modified as indicated, other quaternary polymers falling within the scope of the instant invention are tested as flocculants. The results are set forth in Table 10, below.
| TABLE 10 |
| Dosage Filtrate Cake |
| QP of Example (lbs/ton) Vol. (ml.) Solids |
| Sludge #2 |
| 46 (S. V. = 1.2)1 25.0 140 21.2 |
| 27.5 148 21.0 |
| 30.0 142 21.5 |
| 32.5 136 21.1 |
| Comm.1 22.5 114 19.7 |
| 25.0 142 19.9 |
| 27.5 134 20.6 |
| 30.0 142 18.6 |
| Sludge #3 |
| 46 (S. V. = 2.0)2 40.0 130 10.5 |
| 48.0 126 10.5 |
| 56.0 128 10.7 |
| 46 (S. V. = 1.2)2 40.0 13.1 10.2 |
| 48.0 134 10.8 |
| 56.0 134 11.4 |
| Comm.2 24.0 125 9.1 |
| 32.0 120 8.3 |
| 40.0 108 8.8 |
| Sludge #4 |
| 46 (S. V. = 1.45) 1.4 14 ** |
| 2.7 33 37.1 |
| 4.1 65 41.4 |
| 5.4 80 42.0 |
| 6.8 90 41.3 |
| Comm. 1.4 22 ** |
| 2.7 58 39.5 |
| 4.1 45 32.9 |
| 5.4 37 30.2 |
| Sludge #5 |
| 46 (S. V. = 2.0)3 8.23 160 14.8 |
| 12.35 205 15.3 |
| 16.46 220 15.8 |
| 20.58 230 16.3 |
| 24.69 230 16.9 |
| 46 (S. V. = 2.4)3 8.23 130 14.2 |
| 12.35 210 15.3 |
| 16.46 220 16.0 |
| 20.58 235 16.5 |
| 24.69 236 16.7 |
| Comm3 8.23 160 14.1 |
| 10.29 200 14.7 |
| 12.35 208 15.0 |
| 16.46 226 15.1 |
| 20.58 214 14.7 |
| Sludge #6 |
| 53 (S. V. = 2.4) 6.3 134 22.5 |
| 8.4 158 24.4 |
| 10.5 152 23.4 |
| 12.6 160 24.5 |
| Comm.*** 4.2 146 21.2 |
| 5.3 143 21.2 |
| 6.3 145 21.5 |
| 8.4 138 21.1 |
| Shear Dosage Filtrate Cake |
| Sludge #7 |
| 46 (S. V. = 2.5) 300 rpm/5 min 10 70 13.1 |
| 300 rpm/10 min 10 85 13.3 |
| 300 rpm/5 min 11.7 98 14.0 |
| 300 rpm/10 min 11.7 88 13.3 |
| 300 rpm/10 min 13.3 95 14.0 |
| 300 rpm/10 min 15.0 100 14.6 |
| Comm. 300 rpm/8 min 6.7 82 12.8 |
| 300 rpm/15 min 6.7 70 13.0 |
| 300 rpm/5 min 8.3 70 12.3 |
| 300 rpm/10 min 8.3 85 13.0 |
| 300 rpm/15 min 8.3 82 13.9 |
| 300 rpm/15 min 10.0 95 13.8 |
| 300 rpm/15 min 11.7 92 12.6 |
| 300 rpm/30 min 11.7 89 14.1 |
| 1 = 10 sec. at 300 rpm agitation |
| 2 = mixer set at 51/2 for 10 sec. and 21/2 for 20 sec. |
| 3 = 350 rpm/20 sec. agitation |
| **= not measurable |
| ***= 300 rpm/15 sec. agitation |
The above mentioned patents and publications are incorporated herein by reference.
Many variations of the present invention will suggest themselves to those skilled in this art in light of the above detailed description. For example, instead of employing acrylamide as the (alk)acrylamide monomer; methacrylamide and ethacrylamide may be used. Polymerization may be initiated by any known method such as ionizing radiation in addition to ultraviolet or redox initiation. A wide variety of secondary amines are suitable for use in the Mannich reaction such as piperidine, diethanolamine, dibutylamine and amylmethylamine; as are a wide variety of formaldehydes, including trioxane.
All such obvious modification are within the full intended scope of the appended claims.
Although the above discussion is directed primarily to the use of (meth)acrylamide-based polymers which before reaction are substantially linear, it is also possible to use lightly to moderately cross-linked (meth)acrylamide-based polymers which can be prepared by adding small amounts of cross-linking monomers, such as methylenebisacrylamide etc., to the aqueous acrylamide monomer solutions of either of the processes described above prior to polymerization.
Kozakiewicz, Joseph J., Huang, Sun-Yi
| Patent | Priority | Assignee | Title |
| Patent | Priority | Assignee | Title |
| 2937143, | |||
| 3142638, | |||
| 3165465, | |||
| 3235490, | |||
| 3259569, | |||
| 3276988, | |||
| 3284393, | |||
| 3380947, | |||
| 3536646, | |||
| 3539535, | |||
| 3556932, | |||
| 3624019, | |||
| 3640897, | |||
| 3719748, | |||
| 3732184, | |||
| 3734873, | |||
| 3790529, | |||
| 3840489, | |||
| 3864312, | |||
| 3875097, | |||
| 3875098, | |||
| 3897333, | |||
| 3902958, | |||
| 3917529, | |||
| 3929633, | |||
| 3956122, | Dec 18 1972 | American Cyanamid Company | Cationic arylamide-styrene copolymers and flocculation of sewage therewith |
| 3968037, | Sep 01 1972 | Calgon Corporation | Emulsion polymerization of cationic monomers |
| 3977971, | Dec 03 1974 | Betz Laboratories, Inc. | Method of feeding polymers |
| 3979348, | Jul 16 1973 | Nalco Chemical Company | Ionic polymers from acrylamide latex polymers |
| 4010131, | Jul 08 1974 | Nalco Chemical Company | Quaternary modified acrylamide polymers |
| 4021394, | Nov 12 1975 | Nalco Chemical Company | Continuous process for the preparation of a cationically modified acrylamide polymer |
| 4022741, | Nov 12 1975 | Nalco Chemical Company | Continuous process for the preparation of a cationically modified acrylamide polymer |
| 4051065, | Sep 03 1974 | Nalco Chemical Company | Apparatus for dissolving water soluble polymers and gums in water |
| 4059552, | Jun 21 1974 | The Dow Chemical Company | Cross-linked water-swellable polymer particles |
| 4073763, | Jul 19 1974 | Nalco Chemical Company | Stabilization of cationically modified acrylamide polymers |
| 4093542, | Jul 04 1973 | Chemische Fabrik Stockhausen & Cie | Flocculating agent comprising water-in-oil emulsion of H-active polymer carrying formaldehyde and amine radicals |
| 4110520, | Dec 17 1976 | Mitsubishi Kasei Corporation | Modification of water-soluble acrylic polymer |
| 4113685, | Jul 03 1974 | Chemische Fabrik Stockhausen & Cie | Flocculating agent comprising water-in-oil emulsion of stabilizer plus NH-active polymer carrying formaldehyde and amine radicals |
| 4113688, | Dec 14 1977 | Hercules Incorporated | Process for rapidly dissolving gels of water-soluble polymers by extrusion, cutting and then slurrying under high shearing forces |
| 4172066, | Jun 21 1974 | The Dow Chemical Company | Cross-linked, water-swellable polymer microgels |
| 4179370, | Jul 03 1974 | Chemische Fabrik Stockhause & Cie | Flocculating agent comprising water-in-oil emulsion of stabilizer plus NH-active polymer carrying formaldehyde and amine radicals |
| 4245070, | Apr 30 1975 | RHONE-POULENC INDUSTRIES, | Method of polymerizing vinyl chloride in seeded microsuspension |
| 4251410, | May 26 1976 | Sandoz Ltd. | Reaction products of a polyacrylamide formaldehyde, a secondary amine and an-nh group-containing functional derivative of an acid |
| 4282928, | Jul 08 1977 | The Dow Chemical Co. | Method for controlling permeability of subterranean formations |
| 4322330, | Jul 31 1979 | Wacker-Chemie GmbH | Adhesive for floor coverings, process of its production and its application |
| 4363886, | Oct 15 1979 | Diamond Shamrock Corporation | Preparation of amphoteric water-in-oil self-inverting polymer emulsion |
| 4382864, | Aug 08 1980 | Kurita Water Industries Ltd. | Process for dewatering sludges |
| 4391932, | Jan 22 1982 | Nalco Chemical Company | Polycationic latices of dimethylaminopropyl-acrylamide, and their use of as sludge dewatering agents and/or paper retention aids |
| 4405728, | Jan 15 1982 | Nalco Chemical Company | Compositions for on-site mannich polymer process |
| 4521317, | Apr 09 1982 | Institut Francais du Petrole | Process for manufacturing a microlatex in a continuous oil phase by polymerization of a water-soluble monomer in a water-in-oil microemulsion, resultant microlatices, and their use for enhanced oil recovery |
| 4528321, | Apr 06 1983 | Allied Colloids Limited | Polymer dispersions and their preparation |
| 4529794, | Mar 29 1984 | Diatec Polymers | Method of rapidly dissolving polymers in water |
| 4565836, | May 26 1983 | The Dow Chemical Company | Multi-modal emulsions of water-soluble polymers |
| 4585812, | Feb 17 1984 | Allied Colloids Limited | Polymeric dispersions |
| 4599379, | Jan 17 1984 | CIBA SPECIALTY CHEMIICALS WATER TREATMENTS LIMITED | Process for the production of polymers and aqueous solutions thereof |
| 4619967, | May 26 1983 | The Dow Chemical Company; DOW CHEMICAL COMPANY, THE | Multi-modal emulsions of water-soluble polymers |
| 4681912, | Jun 07 1984 | Institut Francais du Petrole | Process for manufacturing inverse microlatices of watersoluble copolymers, the resultant inverse microlatices and their use for improving the production of hydrocarbons |
| 4702844, | Aug 15 1984 | Ciba Specialty Chemicals Water Treatments Limited | Flocculants and their use |
| 4705640, | Apr 30 1984 | Ciba Specialty Chemicals Water Treatments Limited | Flocculants and processes for their preparation |
| 4720346, | Apr 25 1985 | Ciba Specialty Chemicals Water Treatments Limited | Flocculation processes |
| 4759856, | Apr 30 1984 | Ciba Specialty Chemicals Water Treatments Limited | Flocculation processes |
| 4789695, | Jul 26 1985 | Ciba Specialty Chemicals Water Treatments Limited | Blends of acrylamide polymers and Mannich bases |
| 4861499, | Oct 13 1987 | American Cyanamid Company | Water-dispersible hydrophobic thickening agent |
| 4954538, | Dec 19 1988 | KEMIRA OYJ | Micro-emulsified glyoxalated acrylamide polymers |
| 4956399, | Dec 19 1988 | KEMIRA OYJ | Emulsified mannich acrylamide polymers |
| 4956400, | Dec 19 1988 | KEMIRA OYJ | Microemulsified functionalized polymers |
| 4968435, | Dec 19 1988 | Ciba Specialty Chemicals Corp | Cross-linked cationic polymeric microparticles |
| 5037863, | Oct 30 1989 | KEMIRA OYJ | Emulsified functionalized polymers |
| 5037881, | Oct 30 1989 | KEMIRA OYJ | Emulsified mannich acrylamide polymers |
| 5041503, | Dec 19 1988 | KEMIRA OYJ | Micro-emulsified glyoxalated acrylamide polymers |
| 5070133, | Jun 30 1987 | Kyoritsu Yuki Co., Ltd. | High water-absorptive resin emulsion |
| 5100951, | Sep 23 1988 | Betz Laboratories, Inc. | Stable blends of cationic water-in-oil emulsion polymers and cationic aqueous solution polymers |
| 5104552, | Nov 08 1990 | American Cyanamid Company | Reduction of clay in sludges to be dewatered |
| 5132023, | Dec 18 1988 | KEMIRA OYJ | Emulsified mannich acrylamide polymers |
| 5171781, | Jan 30 1987 | Ciba Specialty Chemicals Water Treatments Limited | Polymeric compositions |
| 5171782, | Jun 25 1987 | Norsolor | Invert microlatices useful as flotation and drainage additives and for absorption and retention of aqueous fluids |
| 5171808, | Jun 11 1990 | Ciba Specialty Chemicals Corp | Cross-linked anionic and amphoteric polymeric microparticles |
| 5185061, | Apr 22 1988 | Ciba Specialty Chemicals Water Treatments Limited | Processes for the production of paper and paper board |
| CA1204535, | |||
| EP102759, | |||
| EP143328, | |||
| FR2398762, | |||
| GB1153207, | |||
| GB1346596, | |||
| GB1426897, | |||
| GB1489046, | |||
| GB2160879, | |||
| GB2161492, | |||
| GB841127, | |||
| JP63218246, | |||
| WO9303190, |
| Executed on | Assignor | Assignee | Conveyance | Frame | Reel | Doc |
| May 16 1997 | Cytec Technology Corp. | (assignment on the face of the patent) | / | |||
| Oct 01 2006 | Cytec Technology Corporation | KEMIRA OYJ | ASSIGNMENT OF ASSIGNORS INTEREST SEE DOCUMENT FOR DETAILS | 018545 | /0595 |
| Date | Maintenance Fee Events |
| Jul 13 2004 | ASPN: Payor Number Assigned. |
| Date | Maintenance Schedule |
| Jan 30 2004 | 4 years fee payment window open |
| Jul 30 2004 | 6 months grace period start (w surcharge) |
| Jan 30 2005 | patent expiry (for year 4) |
| Jan 30 2007 | 2 years to revive unintentionally abandoned end. (for year 4) |
| Jan 30 2008 | 8 years fee payment window open |
| Jul 30 2008 | 6 months grace period start (w surcharge) |
| Jan 30 2009 | patent expiry (for year 8) |
| Jan 30 2011 | 2 years to revive unintentionally abandoned end. (for year 8) |
| Jan 30 2012 | 12 years fee payment window open |
| Jul 30 2012 | 6 months grace period start (w surcharge) |
| Jan 30 2013 | patent expiry (for year 12) |
| Jan 30 2015 | 2 years to revive unintentionally abandoned end. (for year 12) |