Patent Application
20230399446
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.
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 step of subjecting the monomer composition is performed under controlled adiabatic conditions. These polymer dispersions are designated as water-in-water (w/w) polymer dispersions.
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 radical polymerization is performed in presence of a metal scavenger system comprising a metal scavenger and an acid. These polymer dispersions are designated as water-in-water (w/w) polymer dispersions.
The foremost objective is to unlock the potential of water and renewable resources to find safer, healthier, more sustainable solutions. Numberless industrial processes are water-based processes. The replacement of environmental harmful substances or their volume reduction in water-based processes form the basis towards more sustainable solutions. The present disclosure aims at this foremost objective in the field of water-in-water polymer dispersions (w/w polymer dispersions). The improvements of w/w polymer dispersions directly correlate with the sustainability in downstream applications, as e.g. in the paper making process. The better such w/w polymer dispersion work as additives in water-based processes, like in the paper making process, the less of such process additives are to be used. Furthermore, the substitution of hydrocarbons supports the foremost objective.
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. There has been observed a target conflict with regard to an optimal resp. reduced reaction time versus physical properties of the product, in particular the viscosity of the dispersion. Further, it was observed that the products show instabilities 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. The underlaying problem further relates to the provision of a method for manufacturing a polymeric dispersion produced in a reduced time while keeping beneficial properties, i.e. with regard to the viscosity of the product.
BRIEF SUMMARY
Polymer dispersions and methods for manufacturing polymer dispersions are provided herein. In an embodiment, a method for manufacturing a polymer dispersion comprises the steps of
In another embodiment, a polymer dispersion comprises
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 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 found that a metal scavenger in an acidic medium prevents the polymer dispersion from destruction such that the product is kept stable and shelf-life is increased. Further, it was found that the reaction time is reduced while keeping the physical properties on a high level. In particular, the viscosity is in a range ensuring a beneficial handling of the product.
In a preferred embodiment, the method comprises the step C) of stabilizing the polymer dispersion being performed by adding the second carboxylic acid at a temperature of less than 40° C. The addition of the second carboxylic acid below 40° C. results surprisingly in an increased stabilization of the polymer dispersion.
In a preferred embodiment, the metal scavenger is a first carboxylic acid comprising 2, 3, 4, or 5 carboxylic acid groups and at least one nitrogen atom and/or a salt thereof. In a further preferred embodiment, the acid is an inorganic acid.
According to a preferred method, step B is performed in presence of a metal scavenger system comprising a metal scavenger and an acid such that the pH at the beginning of step B is from 4.7 to 5.1. In embodiments, the metal scavenger system consists of the metal scavenger and the acid. In accordance with this method, the copolymerization is started in a composition which pH is adjusted by adding the metal scavenger being preferably the first carboxylic acid and an inorganic acid. If the pH is too low, the reaction time increases, and retardation of the polymerization is observed. If the pH is in the right range, the viscosity, in particular the salt viscosity is higher. The salt viscosity is a dimension of molecular weight. A higher Mw results in general to a better performance, retention and dewatering during the paper making process.
For stabilizing the polymeric dispersion, it is preferred that the polymeric dispersion is subjected to the addition of a second carboxylic acid which is found to stabilize the product. Therefore, the polymer dispersion is after performing step B stabilized by a second carboxylic acid, preferably by a second carboxylic acid comprising 1, 2, or 3 carboxylic acid and having no nitrogen atom. A preferred second carboxylic acid is citric acid.
The second carboxylic acid is preferably added in an amount of 0.1 to 2 wt-%, 0.2 to 1.5 wt-%, even more preferred 0.5 to 1 wt-%, based on the total of the polymer dispersion.
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. By agitation, the components are well distributed in the reaction mixture. When the viscosity is monitored, the degree of stability can be observed. If the viscosity is outside the above ranges, in particular if the viscosity is higher, a gelling is observed resulting in a final product which does not provide the required properties as a flocculant.
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 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.
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. is 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 are beneficial for solving the above problems.
In a preferred embodiment, the monomer composition 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:
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-l-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 tetraallylammonium 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), an 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 (e) 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 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.
Preferably, the polymeric dispersant is derived from one or more cationic monomers, more preferably from a single cationic monomer.
In a preferred embodiment, the polymeric dispersant is derived from one or more radically polymerizable, ethylenically unsaturated monomers.
In a further preferred embodiment, the polymeric dispersant is a homopolymer made of the cationic monomer of formula (II)
where
where
According to a preferred embodiment, the polymeric dispersant is essentially a homopolymer. The term “essentially” in this regard means that the polymeric dispersant is made by polymerizing one monomer, whereupon minor amounts of further comonomers may be present, however, no second comonomer is purposely added.
Preferably, Y1, Y2 and Y3 are identical, preferably methyl. In a preferred embodiment, Z1 is 0 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 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 40,000 to less than 150,000 g/mol, preferred 50,000 to 140,000 g/mol, more preferred 60,000 to 130,000, most preferred 85,000 to 120,000 g/mol.
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.
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 10 to 28 wt.-%, preferred 12 to 26 wt. %, more preferred 13 to 23 wt.-%, even more preferred 14 to 20 wt.-%.
According to a further embodiment, the total weight of the dispersed polymer based on the total weight of the polymer dispersion is between 18 and 26 wt.-%, preferred 19 to 25 wt.-%.
In a preferred embodiment, the method is performed in that step B) is conducted by sequentially or simultaneously adding to the reaction mixture redox initiator system comprising an oxidizing agent and a reducing agent.
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.
Method step D) may be performed after method step C). In an alternative embodiment, method step C) may be performed after method step D).
According to a preferred embodiment, the ratio of the polymeric dispersant to the dispersed polymer in the polymer dispersion is in the range of 0.45:1 to 1:0.9, preferred in the range of 0.5:1 to 1:1, more preferred in the range of 0.55:1 to less than 1:1, even more preferred in the range of 0.6:1 to 0.99: 1, in particular in the range of 0.65:1 to 0.9:1.
According to a further preferred embodiment, the total weight of the polymeric dispersant based on the total weight of the polymer dispersion is in the range of 10 to 24 wt.-%, preferred 12 to 23 wt. %, more preferred 13 to 22 wt.-%, even more preferred 14 to wt.-%.
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 second 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 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 (F) 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
B) subjecting the monomer composition to a radical polymerization to synthesize a dispersed polymer and to form the polymer dispersion, wherein step B is performed in presence of a metal scavenger system comprising an acid and a metal scavenger, which metal scavenger is a first carboxylic acid comprising 2, 3, 4, or 5 carboxylic acid groups and at least one nitrogen atom, and wherein the pH at the beginning of step B is from 4.5 to 5.3; and
where
where
where
Method for manufacturing a polymer dispersion comprising the steps of
where
where
where
Polymer dispersion comprising
A polymer dispersion obtained by a method for manufacturing the polymer dispersion according to any one of the above items (A) to (D).
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±0.1 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:
Used Parameters:
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 30 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:
The effect of the citric acid addition for buffering the aqueous solution is shown in the following:
Citric acid acts as buffer in make-down solution. If no citric acid is added the polymer solution, the viscosity decreases (much faster at higher temperature) because of the hydrolyses of the cationic ADAME-Q units (ester bond).
When citric acid is added to the aqueous dispersion, the pH of the water drops to <5 after dilution of the polymer (cf.
The addition of a mineral acid is necessary to adjust the pH of the monomer solution (cf.
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 |
