Patent Application
20230399445
The present disclosure relates to methods for manufacturing a polymer dispersion, to polymer dispersions and their use.
The present disclosure relates to methods for manufacturing a polymer dispersion, to polymer dispersions and their use. The methods of manufacturing the polymer dispersion comprise the steps of providing a reaction mixture in an aqueous medium comprising a polymeric dispersant and a monomer composition comprising radically polymerizable monomers, and subjecting the monomer composition in the reaction mixture to a radical polymerization to synthesize a dispersed polymer so as to form the polymer dispersion, wherein the ratio of the polymeric dispersant to the dispersed polymer in the polymer dispersion is in a specified narrow range. These polymer dispersions are designated as water-in-water (w/w) polymer dispersions.
The water-in-water polymer dispersions are useful as flocculants, dewatering (drainage) aids and retention aids in papermaking besides applications in other technical fields. Paper is manufactured by firstly making an aqueous slurry of cellulosic fibers which slurry has a water content of more than 95 wt-%. The final paper sheet has a water content of less than 5 wt-%. The dewatering (drainage) and retention represent crucial steps in papermaking and are important for an efficient paper making process. High-performance w/w polymer dispersions represent a key factor in the paper making process.
A well-known flocculant is given by a w/w polymer dispersion, which is produced by copolymerizing ethylenically unsaturated monomers in an aqueous system comprising a polymeric dispersant resulting in a dispersion comprising the polymeric dispersant and the synthesized copolymer. The U.S. Pat. Nos. 8,476,391B2 and 7,323,510B2 represent early publications of such w/w polymer dispersions. It is well-accepted knowledge in this technical field that the addition of separately synthesized copolymers on the one hand and polymer dispersants on the other hand results in a products having completely different properties compared to the w/w polymer dispersions as disclosed in the above patent documents. It requires the copolymerization within a system comprising the polymeric dispersant in order to obtain high-performance flocculant products e.g. for the paper making process.
These circumstances make the manufacturing of the w/w polymer dispersions to a multi-parameter system. The kind of the ethylenically unsaturated monomer, their ratio, the kind of the polymer dispersant are only a very few parameters influencing the properties of the w/w polymer dispersion. An improvement of the properties of the final product of the w/w polymer dispersion has been subject of numberless attempts in research and development.
Besides the properties of the final product of the w/w polymer dispersion, there have been identified challenges regarding the manufacturing process itself. It was observed that some batches showed instabilities during the manufacturing process. Some dispersions start to gel during the manufacturing process. Further, some of the products show instabilities some time after completion of the manufacturing process. Such instabilities are supported e.g. by alternating temperature when shipped to the customer.
The underlaying problem relates to the provision of a process for manufacturing w/w polymer dispersions ensuring a high degree of stability during the manufacturing process and ensuring a high shelf-life under unfavorable circumstances like e. g. alternating temperatures. In particular, the degree of stability relates to the ratio of batches with an insufficient stability to batches with an adequate stability, which ratio should be zero. The underlaying problem relates to solving these drawbacks.
Polymer dispersions and methods for manufacturing the polymer dispersions are provided herein. In an embodiment, a method for manufacturing a polymer dispersion includes the steps of
In another embodiment, a polymer dispersion includes
The present disclosure will hereinafter be described in conjunction with the following drawing figures, wherein like numerals denote like elements, and wherein:
The following detailed description is merely exemplary in nature and is not intended to limit the disclosure or the application and uses of the subject matter as described herein. Furthermore, there is no intention to be bound by any theory presented in the preceding background or the following detailed description. It is to be appreciated that all values as provided herein, save for the actual examples or objective measurement parameters, are approximate values with endpoints or particular values intended to be read as “about” or “approximately” the value as recited.
According to a first aspect, the present disclosure relates to a method for manufacturing a polymer dispersion comprising the steps of
The method comprises the provision of a reaction mixture comprising the monomers to be copolymerized and a polymeric dispersant. The monomers are polymerized in presence of the polymeric dispersant in an aqueous medium. According to well-established technical knowledge, a polymer dispersion obtained by the method according to the present disclosure cannot be obtained in that the monomer composition is subjected to a copolymerization, whereupon subsequently after the copolymerization, the polymeric dispersant is added. Unique properties are conferred to the polymer dispersion by applying the method according to the present disclosure, which polymer dispersion represents the final product comprising the copolymer obtained from the radically polymerizable monomers together with the polymeric dispersant.
It was surprisingly found that the ratio of the polymeric dispersant to the dispersed polymer in the polymer dispersion, thus in the final product, plays an important role regarding the stability of the reaction mixture during the polymerization. In particular, it was surprisingly found that the narrow range as given above improves stability of the reaction mixture during the polymerization and the stability of the final product such that shelf-life is increased, when the final product is subjected to unfavorable circumstances like e. g. alternating temperatures. Although the ratio is determined in the final product, the way of obtaining the final product is beneficial in view of the stability as described above. A person skilled in the art understands that said ratio in the final product is achieved among others by adjusting the amount of polymeric dispersant to the amount of copolymer envisaged to be present in the final product. The way of adjusting said ratio is exemplarily shown in the Examples below. The ratio dispersant to dispersed phase is adjusted in the way that the resulting aqueous dispersion shows a low viscosity and good stability. In addition, the ratio is also very important for the polymerization itself. If the ratio of dispersant and dispersed phase does not fit to each other, the torque during the reaction becomes extremely high attaining such an extent that the polymerization must be stopped. In a more general embodiment, the ratio of the polymeric dispersant to the dispersed polymer in the polymer dispersion can be in the range 0.65:1 to 0.98:1, preferred in the range of 0.7:1 to 0.95:1, more preferred in the range of 0.72:1 to less than 0.92:1, even more preferred in the range of more than 0.74:1 to 0.9:1, in particular in the range of 0.76:1 to 0.88:1.
In a preferred embodiment, the viscosity of the polymer dispersion amounts to 1,800 mPas to less than 6,700 mPas , preferably 2,000 mPas to 6,000 mPas, more preferred 2,200 mPas to 5,500 mPas, most preferred 2,500 mPas to 5,000 mPas, as measured with a Brookfield viscometer with spindle 4 at 20° C. and an angle speed of 10 rpm.
The viscosity is preferably the bulk viscosity which refers to the viscosity right after having obtained the cooled down product.
In a further preferred embodiment, step B is performed by agitating while measuring torque of a motor-driven agitator. Alternatively, step B is performed by agitating and torque of a motor-driven agitator is kept below 65 N/cm. If torque is 65 N/cm or higher, a gelling is observed resulting in a final product which does not provide the required properties as a flocculant.
It is known by a person skilled in the art, that the product viscosity distinguishes from the viscosity of the reaction mixture during the method of manufacturing. A problem reveals from these circumstances, i.e. the viscosity may increase to a value such that the reaction is to be interrupted. If the viscosity during the method of manufacturing increases to a specific value which is accompanied by an increase of torque, the mixing is interrupted. If the method is conducted such that the ratio of the polymeric dispersant to the dispersed polymer in the polymer dispersion is in the narrow range, a save accomplishment of the method is guaranteed.
In a preferred method, the monomer composition comprising the radically polymerizable monomers which are selected from the group of one or more of the following:
where
where
where
where
where
In the framework of the present present disclosure, a cationic monomer is a monomer carrying permanently a positive charge.
According to the preferred embodiment, one or more of the above monomers given under items i. to iv are used as monomers in the monomer composition to be polymerized. It is preferred that a copolymer is polymerized, i.e. that two of the above monomers given under items i. to iv are provided for the monomer composition to be polymerized. It is preferred that one monomer of item i. and one monomer of item ii. are provided for the monomer composition subjected to the copolymerization. In a preferred embodiment, the radically polymerizable monomers comprise a radically polymerizable non-ionic monomer according to general formula (I); and a radically polymerizable cationic monomer according to general formula (II). These monomers being copolymerized are beneficial for solving the above problems.
Even further, it is preferred that one monomer of item i. one monomer of item ii. and one monomer of item iv are provided for the monomer composition subjected to the copolymerization.
In a preferred embodiment, the monomer composition comprising the radically polymerizable monomers at least comprises the non-ionic monomer of formula (I) being selected from those in which R1 means hydrogen or methyl, and R2 and R3 are both hydrogen, hydrogen and C1-C3 alkyl, hydrogen and hydroxyethyl, or both C1-C3 alkyl, and/or the cationic monomer of formula (II) being selected from those in which R1 means hydrogen or methyl, and Z1 is O, NH or NR4, wherein R4 means methyl, Y1 is C2-C6 alkylene, preferably ethylene or propylene, Y5, Y6 and Y7 are all methyl, and Z− is a halogen.
In a preferred embodiment, the radically polymerizable monomers comprise a radically polymerizable non-ionic monomer according to general formula (I) which is selected from the group of (meth)acrylamide, N-methyl(meth)acrylamide, N,N-dimethyl(meth)acrylamide, N-ethyl(meth)acrylamide, N,N-diethyl(meth)acrylamide, N-methyl-N-ethyl(meth)-acrylamide, N-isopropyl(meth)acrylamide, N-hydroxyethyl(meth)acrylamide, or a combination thereof.
In another preferred embodiment, the radically polymerizable monomers comprise a radically polymerizable cationic monomer according to general formula (II) which is selected from the group of trimethylammonium-C2-C6-alkyl(meth)acrylate halides, trimethylammonium-C2-C6-alkyl(meth)acrylamide halides, or a combination thereof. In a most preferred embodiment, the monomer composition comprises a radically polymerizable monomer being (meth)acrylamide together with a radically polymerizable monomer selected from trimethylammonium-C2-C6-alkyl(meth)acrylate halides, in particular being an acryloyl oxyethyl trimethylammonium halide.
The choice of the comonomers used in the copolymerization may have an influence on the perfect ratio of the polymeric dispersant to the dispersed polymer in the polymer dispersion. The preferred comonomers used in the polymerization together with the preferred ratio results in favorable stability properties during reaction and thereafter.
According to a preferred embodiment, the monomer composition comprising radically polymerizable monomers comprises a cross-linker. Cross-linkers are known to the skilled person. In this preferred embodiment, the monomer composition preferably contains 0.0001 to 1.25 wt.-% of one or more preferably ethylenically unsaturated cross-linkers, based on the total weight of monomers. If ethylenically unsaturated cross-linkers are present, they contain 2, 3, 4 or 5 ethylenically unsaturated groups that are radically polymerizable.
Examples of cross-linkers with two radically polymerizable ethylenically unsaturated groups include:
where
Examples of cross-linkers according to general formula (V) include polypropylene glycol di(meth)acrylates with m in the range 4-25; polybutylene glycol di(meth)acrylates with m in the range 5-40; and, preferably, polyethylene glycol di(meth)acrylates with m in the range 2-45, e.g. diethylene glycol di(meth)acrylate, triethylene glycol di(meth)acrylate, tetraethylene glycol di(meth)acrylate; and, more preferably, polyethylene glycol di(meth)acrylates with m in the range 5-20;
Examples of cross-linkers having 3 or more ethylenically unsaturated radically polymerizable groups include glycerin tri(meth)acrylate, 2,2-dihydroxymethyl-1-butanol tri(meth)acrylate, trimethylolpropane triethoxy tri(meth)acrylate, trimethacrylamide, (meth)allylidene di(meth)-acrylate, 3-allyloxy-1,2-propanediol di(meth)acrylate, triallyl amine, triallyl cyanurate or triallyl isocyanurate; and also (as representative compounds with more than 3 ethylenically unsaturated radically polymerizable groups) pentaerythritol tetra(meth)acrylate and N,N,N′N′-tetra(meth)acryloyl-1,5-pentanediamine.
An example of a cross-linker having 5 ethylenically unsaturated radically polymerizable groups is dipentaerithritol-pentaacrylate.
Particularly preferred cross-linkers are selected from the group constsiting of methylene bisacrylamide, polyethylene glycol diacrylate, triallylamine, and tetraallyl ammonium chloride.
Further preferred cross-linkers include asymmetrically cross-linkable monomers, i.e. cross-linkable monomers which rely on different functional groups with respect to the incorporation reaction into the polymer backbone and the cross-linking reaction. Examples of such asymmetrically cross-linkable monomers include N′-methylol acrylamide, N′-methylol methacrylamide and glycidyl(meth)acrylate.
Cross-linkers of this type have the advantage that cross-linking may be initiated subsequently. Thus, cross-linking may be performed under different conditions than the radical polymerization of the main-backbone. Preferably, cross-linking is initiated after changing the reaction conditions, 6.9. the pH value (addition of acid or base), the temperature, and the like. Optionally, the monomer composition further comprises a hydrophobic monomer, preferably a hydrophobic (meth)acrylic acid C4-18-alkyl ester; and/or an ethylenically unsaturated monomer.
In a preferred embodiment, the radically polymerizable monomers are selected from the non-ionic monomer of formula (I) and/or the cationic monomer of formula (II), wherein the amount of the radically polymerizable monomers being selected from the non-ionic monomer of formula (I) and/or the cationic monomer of formula (II) is between 80 and less than 100 wt-%, preferred 85 and 99 wt-%, most preferred 90 and 95 wt-% based on the total amount of radically polymerizable monomers, wherein the remainder is selected from the group of any other ethylenically polymerizable monomer, a monomer of formula (III), a monomer of formula (IV), the ethylenically unsaturated cross-linker containing 2, 3, 4 or 5 ethylenically unsaturated groups, or a combination thereof
In this regard, the sum of the values in wt-% needs not to amount to 100 wt-%, since further ethylenically unsaturated monomers besides the monomers of formulae (I) and/or (II) may be contained in the monomer composition, i.e. in the reaction mixture, which have to be taken into account when determining the total amount of monomers. Preferably, however, the monomer composition includes monomers (a) and (b) so that the sum of the two values in wt-% amounts to 100 wt-%, i.e. no further monomers are present.
In a preferred embodiment, the monomer composition comprises
where
where
where
In this regard again, the sum of the values in wt-% needs not to amount to 100 wt-%, since further ethylenically unsaturated monomers besides the monomers of formulae (I) and/or (II) and/or the ethylenically unsaturated cross-linker may be contained in the monomer composition, i.e. in the reaction mixture, which have to be taken into account when determining the total amount of monomers. Preferably, however, the monomer composition includes monomers (a) and (b) so that the sum of the two values in wt-% amounts to 100 wt-%, i.e. no further monomers are present.
In the present application, all percentages with regard to the monomer composition is based on the total amount of monomers.
According to the present disclosure, the copolymerization is performed in the presence of a polymeric dispersant.
In the state of the art, alternative aqueous polymeric systems are stabilized by low molecular weight salts. A high salt content ensures the stability of the polymeric system. Distinguishing from these systems, the stabilization of the w/w polymer dispersion according to the present disclosure is basically ensured by the polymeric dispersant. This system renders moot a high salt concentration as in state of the art aqueous polymeric systems. In a preferred embodiment, the polymer dispersion has a salt content of less than 15 wt.%, more preferred a salt content of 0.1 to 10 wt.-%, most preferred 1 to 5 wt.-% based on the polymer dispersion. With the term “salt content”, low molecular weight salts are meant. The polymeric electrolytes do not count for the calculation of the salt content.
In a preferred embodiment, the polymeric dispersant is selected from the group of a cellulose derivative, polyvinyl acetate, starch, starch derivative, dextran, polyvinylpyrrolidone, polyvinylpyridine, polyethylene imine, polyamine, polyvinyl imidazole, polyvinyl succinimide, polyvinyl-2-methylsuccinimide, polyvinyl-1,3-oxazolidone-2, polyvinyl-2-methylimidazoline, itaconic acid, (meth)acrylic acid, (meth)acrylic acid ester, (meth)acrylic acid amide, or a combination thereof; preferably a (meth)acryloyl amidoalkyl trialkylammonium halide or a (meth)acryloxyalkyl trialkylammonium halide.
In a preferred embodiment, the cationic polymeric dispersant is substantially linear, i.e. is not derived from monomer mixtures containing cross-linkers.
In a preferred embodiment, the polymeric dispersant is derived from one or more radically polymerizable, ethylenically unsaturated monomers. Preferably, the polymeric dispersant is derived from one type of a radically polymerizable, ethylenically unsaturated monomer, i.e. the polymeric dispersant is essentially a homopolymer. The term “essentially” means in this regard, that no second type of a monomer is purposely added when synthesizing the polymeric dispersant.
Preferably, the polymeric dispersant is derived from one or more cationic monomers, more preferably from a single cationic monomer.
In a further preferred embodiment, the polymeric dispersant is a homopolymer made of the cationic monomer of formula (II)
where
where
Preferably, Y1, Y2 and Y3 are identical, preferably methyl. In a preferred embodiment, Z1 is O or NH, Y0 is ethylene or propylene, R1 is hydrogen or methyl, and Y1, Y2 and Y3 are methyl. The cationic monomer according to general formula (II) may be an ester (Z1═O), such as trimethylammonium-ethyl(meth)acrylate (ADAME quat.). Preferably, however, the cationic monomer according to general formula (I) is an amide (Z1═NH), particularly trimethylammonium-propyl acrylamide (DIMAPA quat).
Preferred radically polymerizable cationic monomers according to general formula (II) include quaternized dialkylaminoalkyl (meth)acrylates or dialkylaminoalkyl(meth)acrylamides with 1 to 3 C atoms in the alkyl or alkylene groups, more preferably the methyl chloride-quaternized ammonium salt of dimethylamino methyl(meth)acrylate, dimethylamino ethyl(meth)acrylate, dimethylamino propyl(meth)acrylate, diethylamino methyl(meth)acrylate, diethylamino ethyl-(meth)acrylate, diethylamino propyl(meth)acrylate, dimethylamino methyl(meth)acrylamide, dimethylamino ethyl(meth)acrylamide, dimethylamino propyl(meth)acrylamide, diethylamino methyl(meth)acrylamide, diethylamino ethyl(meth)acrylamide, diethylamino propyl(meth)-acrylamide.
Quaternized dimethylaminoethyl acrylate and dimethylaminopropylacrylamide are particularly preferred. Quaternization may be affected using dimethyl sulfate, diethyl sulfate, methyl chloride or ethyl chloride. In a preferred embodiment, monomers are quaternized with methyl chloride.
In a preferred embodiment, the polymeric dispersant is a homopolymer of trimethylammonium propyl acrylamide chloride (DIMAPA quat) designated by IUPAC as (3-acrylamidopropyl)trimethylammonium chloride (APTAC).
Preferably, the polymeric dispersant is derived from a monomer composition comprising a cationic monomer selected from the group of (alk)acrylamidoalkyltrialkyl ammonium halides (e.g., trimethylammonium-alkyl(meth)acrylamide halides), (alk)acryloyloxyalkyl trialkyl ammonium halides (e.g., trimethylammoniumalkyl(meth)acrylate halides), alkenyl trialkyl ammonium halides, dialkenyl dialkyl ammonium halides (e.g., diallyldialkylammonium halides), or a combination thereof. More preferably, the polymeric dispersant is a cationic polymer derived from a monomer composition comprising a cationic monomer selected from the group of trimethylammonium-alkyl(meth)acrylate halides, trimethylammoniumalkyl(meth)acrylamide halides, diallyldialkylammonium halides, or a combination thereof. Preferably, the aforementioned cationic monomers comprise 6 to 25 carbon atoms, more preferably 7 to 20 carbon atoms, most preferably 7 to 15 carbon atoms and in particular 8 to 12 carbon atoms.
In a preferred embodiment, the polymeric dispersant is derived from a dialkenyl dialkyl ammonium halide, preferably a diallyl dimethyl ammonium halide (DADMAC).
According to a preferred embodiment, the polymeric dispersant is a homopolymer made of a (meth)acryloyl amidopropyl trimethylammonium salt or a (meth)acryloyl oxyethyl trimethylammonium salt. In the framework of this disclosure, a homopolymer of a (meth)acrylate means, that either the homopolymer is a methacrylate or an acrylate.
In the framework of this application, the halide may be any acceptable halide as e.g. chloride, bromide or iodide; the counter ions of the salts may be any acceptable counter ions as e.g. halides, methosulfate, sulfate or others.
According to a preferred embodiment, the polymeric dispersant has a weight average molecular weight Mw as determined by size exclusion chromatography of 60,000 to 400,000 g/mol, preferred 70,000 to 350,000 g/mol, more preferred 80,000 to less than 230,000, most preferred 85,000 to less than 150,000 g/mol.
The present disclosure is in particular efficient if the total weight of the polymeric dispersant based on the total weight of the polymer dispersion is in the range of to 28 wt.-%, preferred 12 to 26 wt.%, more preferred 14 to 24 wt.-%, even more preferred 16 to 22 wt.-%.
According to a further embodiment, the total weight of the polymeric dispersant based on the total weight of the polymer dispersion is between 18 and 26 wt.-%, preferred 19 to 25 wt.-%. These preferred embodiments are in particular beneficial if the ratio of the polymeric dispersant to the dispersed polymer in the polymer dispersion is in the range of 1:1 to 1:0.9.
In a preferred embodiment, the method is performed in that step B) is conducted by sequentially or simultaneously adding to the reaction mixture at least a part of a predetermined amount of a redox initiator system comprising an oxidizing agent and a reducing agent, at least a part of a predetermined amount of a first radical initiator and at least a part of a predetermined amount of a second radical initiator.
According to a preferred embodiment, the method comprises the step of
The addition of said initiators enable the removal of the monomer such that they have no detrimental effect on stability of the obtained dispersion.
According to a preferred embodiment the charge density of the dispersed polymer amounts to 5 to 40 mole %, preferably 8 to 35 mole %, more preferred 10 to 30 mole %, most preferred 10 to 28 mole %. While the charge density of the polymeric dispersant is preferably 100 mole %, i.e. the polymeric dispersant is a 100 mole % polyelectrolyte, the dispersed polymer obtained from the copolymerization in step B) is partially a polyelectrolyte. The charge density is calculated from the monomeric constituents, whereupon number of monomeric constituents carrying a formal charge per total number of monomeric constituents results in the molar percentage of the charge density. Thus, the charge density is calculated from the monomeric constituents of the dispersed polymer.
If the charge density is in the above range, the beneficial effect in terms of stability and viscosity is enhanced. In particular, the combination of the ratio of the polymeric dispersant to the dispersed polymer in the polymer dispersion together with the charge density solves the above problems. Without being bound to any theory it could be assumed that the dispersing ability of the polymer dispersant depends on said ratio together with the property of the charge density.
According to a second aspect, the present disclosure relates to a polymer dispersion comprising
According to a third aspect, the present disclosure relates to a polymer dispersion obtained by a method for manufacturing the polymer dispersion according to the present disclosure comprising the steps of
According to a fourth aspect, the present disclosure relates to the use of the polymer dispersion according to the present disclosure
Features relating to preferred embodiments of the first aspect of the present present disclosure, which are solely disclosed relating to the first aspect of the present disclosure represent preferred embodiments of the second and third embodiment as well.
In the following, exemplary embodiments (A) to (I) are disclosed which represent particularly preferred embodiments.
Method for manufacturing a polymer dispersion comprising the steps of
Method for manufacturing a polymer dispersion comprising the steps of
Method for manufacturing a polymer dispersion comprising the steps of
where
where
Method for manufacturing a polymer dispersion comprising the steps of
Method for manufacturing a polymer dispersion comprising the steps of
where
where
Method for manufacturing a polymer dispersion comprising the steps of
Method for manufacturing a polymer dispersion comprising the steps of
Method for manufacturing a polymer dispersion comprising the steps of
Method for manufacturing a polymer dispersion comprising the steps of
In the following, the applied test methods are described in detail.
The product viscosity is measured as follows.
Use the product directly for the measurement. The spindle No. 5 is slowly immersed into the product and the viscosity determined with a Brookfield RVT viscometer at 10 rpm. The measurement is terminated when the reading remains constant for a period of sec.
The solution viscosity is measured in DI Water and determined as follows:
In a 400 ml beaker 323.0±0.1 g demineralised water is weighed. Then 17.0±g of the product are added (22±3° C.) under stirring at 300 rpm. The dissolving time amounts to 60 min. at 300±10 rpm. Thereafter, the solution has to rest for 5 min. Now the spindle No. 2 is slowly immersed, and the viscosity determined with a Brookfield RFT viscometer at 10 rpm. The measurement is terminated when the reading remains constant for a period of 30 sec.
The salt viscosity is measured in a 10% NaCl solution and determined as follows:
In a 400 ml beaker 289.0±0.1 g demineralized water is weighed. Then 17.0±0.1 g of the product are added (22±3° C.) under stirring at 300 rpm. The dissolving time amounts to 45 min. at 300±10 rpm and then 34.0±0.1 g NaCl is added. The solution is stirred for further 15 min. After this the solution has to rest for 5 min. Now the spindle No. 1 is slowly immersed, and the viscosity determined with a Brookfield RVT viscometer at 10 rpm. The measurement is terminated when the reading remains constant for a period of 30 sec.
The stability is determined via two distinguishing methods: (a) centrifugation and (b) oven test. The tests are performed as follows:
The molar mass is measured via Size Exclusion Chromatography (SEC). The measurement is in particular performed for the determination of the molecular weight of the dispersant.
The molecular weights are determined via aqueous SEC using Pullulan standards for the calibration.
Sample Preparation:
The following examples further illustrate the present disclosure but are not to be construed as limiting its scope.
At first, 294.06 g water, 666.7 g acryloyl amidopropyl trimethylammonium chloride (DIMAPA quat.) (60wt %) and sulfuric acid (50wt %) to adjust the pH to 5.0±0.2 were weighed in a 2 L vessel. Then the monomer solution was sparged with nitrogen for min by stirring. Subsequently, the aqueous solution was heated up to 60° C. and 2-mercaptoethanol and V-50 (2,2′-Azobis(2-amidinopropane) dihydrochloride) were added to the solution. After reaching Tmax, two additional portions of initiator (V-50) were given to the product in between 10 min for residual monomer burn out. The product was stirred for 2 h at 85° C. Then, the final aqueous product was cooled down to 30° C. The dispersants were provided in 40 wt.-% aqueous solutions.
Specifications:
The Mw is adjusted via variation of the chain transfer agent 2-mercaptoethanol (2-ME).
In a discontinuous process (batch size 1,000 kg), acrylamide and acryloyl oxyethyl trimethylammonium chloride (ADAME quat.) were polymerized in an aqueous solution in the presence of homopoly acryloyl amidopropyl trimethylammonium chloride (polymeric dispersant). The water-phase was prepared at 200 rpm.
Firstly, 206.90 kg soft water, 261.80 kg Bio-acryl amide (49 wt.-%), 77.20 kg acryloyl oxyethyl trimethylammonium chloride (ADAME quat) (80 wt %), 412.50 kg polymeric dispersant of Example 1, 10.00 kg ammonium sulphate and 0.20 kg Triton C were loaded into the reaction vessel. The pH value was adjusted to pH 5.0±0.2 with approximately 0.10 kg of sulphuric acid (50%). The vessel was heated up to 30° C. and was evacuated five times before being aerated with nitrogen. The initiator composition was added at a negative pressure of 0.5 bar and maximum agitator speed. Initiating started at 22±1° C. with the addition of 0.34 kg V-50 in 3.05 kg soft water, 0.025 kg sodium persulfate in 0.47 kg soft water, 0.014 kg sodium bisulfite in 0.27 kg soft water, and 0.003 kg t-butylhydroperoxide (70%) in 1 kg soft water. Afterwards the vessel was aerated again with nitrogen. After reaching the maximum temperature, a solution of 0.17 kg V-50 in 1.53 kg soft water was added to reduce the monomer content. After a one-hour post reaction time, the product was cooled down to a temperature below 40° C. Then, 8.30 kg citric acid and 0.82 kg of the biocide Acticide SPX were added and the product was cooled down to a temperature below 30° C.
Specifications:
In the following, the effect of the ratio dispersant to dispersed phase is analyzed:
The ratio dispersant to dispersed phase is adjusted in the way that the resulting aqueous dispersion shows a low viscosity and good stability. In addition, the ratio is also very important for the polymerization itself. If the ratio of dispersant and dispersed phase does not fit to each other, the torque during the reaction is extremely high. The extreme high viscosity can yield in an interruption of the agitator/stirrer.
High Viscosity/Torque During the Polymerization:
The process profile depends on recipe and other parameters. In particular, the ratio dispersant to dispersed phase represents an important parameter.
The stability of the dispersion is also dependent on the ratio dispersant to dispersed phase. The most important factor in terms of stability is the viscosity parameter. If the dispersion is made by using an inappropriate ratio of dispersant and dispersed phase, the viscosity is significantly increased up to gelation.
The following Tab. 2 shows the outcome of physical parameters depending on the ratio of dispersant to dispersed phase. Some dispersion batches of the dispersion according to the present disclosure were prepared with different ratios—below 0.6, in between 0.6 and 1 and above 1. The table summarizes the outcome. There is only a small window of a useful ratio of dispersant to dispersed phase. As a further parameter, the charge density may play a role with regard to the physical parameters of the dispersion.
a20° C., spindle 4, speed 10
bTorque @ lab mixer IKA Power Control, max. 65 N/cm
c20° C., lab centrifuge Hermle Z300, 1 h @ 4000 rpm
d poly acryloylamidopropyltrimethylammonium chloride
While at least one exemplary embodiment has been presented in the foregoing detailed description, it should be appreciated that a vast number of variations exist. It should also be appreciated that the exemplary embodiment or exemplary embodiments are only examples, and are not intended to limit the scope, applicability, or configuration of the present disclosure in any way. Rather, the foregoing detailed description will provide those skilled in the art with a convenient road map for implementing an exemplary embodiment of the present disclosure. It being understood that various changes may be made in the function and arrangement of elements described in an exemplary embodiment without departing from the scope of the present disclosure as set forth in the appended claims.
| Number | Date | Country | Kind |
|---|---|---|---|
| 102022114638.3 | Jun 2022 | DE | national |
| 102022114640.5 | Jun 2022 | DE | national |
| 102022114641.3 | Jun 2022 | DE | national |
| 102022114642.1 | Jun 2022 | DE | national |
| 102022114644.8 | Jun 2022 | DE | national |
This application claims the benefit of German Patent Application No. 10 2022 114 638.3, filed Jun. 10, 2022; German Patent Application No. 10 2022 114 641.3, filed Jun. 10, 2022; German Patent Application No. 10 2022 114 640.5, filed Jun. 10, 2022; German Patent Application No.10 2022 114 642.1, filed Jun. 10, 2022; and German Patent Application No. 10 2022 114 644.8, filed Jun. 10, 2022.
