WO2003048218A1 - Procedimiento para la produccion de microemulsiones inversas de polimeros no ionicos o de copolimeros ionicos - Google Patents
Procedimiento para la produccion de microemulsiones inversas de polimeros no ionicos o de copolimeros ionicos Download PDFInfo
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- C09K—MATERIALS FOR MISCELLANEOUS APPLICATIONS, NOT PROVIDED FOR ELSEWHERE
- C09K23/00—Use of substances as emulsifying, wetting, dispersing, or foam-producing agents
- C09K23/017—Mixtures of compounds
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F20/00—Homopolymers and copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and only one being terminated by only one carboxyl radical or a salt, anhydride, ester, amide, imide or nitrile thereof
- C08F20/02—Monocarboxylic acids having less than ten carbon atoms, Derivatives thereof
- C08F20/52—Amides or imides
- C08F20/54—Amides, e.g. N,N-dimethylacrylamide or N-isopropylacrylamide
- C08F20/56—Acrylamide; Methacrylamide
Definitions
- the invention relates to obtaining non-ionic polymers and high molecular weight ionic copolymers, obtained by polymerization in reverse microemulsion in the presence of a self-inverting surfactant system in contact with an aqueous solution or suspension, capable of thermodynamically stabilizing the system, the polymer consisting of acrylamide and copoly ero acrylamide and acid
- (meth) acrylic or one of its salts in a weight ratio of acrylamide to (meth) acrylic acid or one of its salts between 100: 0 and 40:60.
- Inverse microemulsions are stable and transparent or translucent water-in-oil systems, stabilized by surfactants.
- said surfactant system may also optionally contain one or more non-ionic HLB surfactants greater than or equal to 13 and / or an anionic surfactant.
- Desirable characteristic of a reverse microesion for use as a flocculant is that it autoinvest in contact with the aqueous solution or suspension in which it should accelerate the sedimentation of suspended solids.
- self-investment means that when the microemulsion comes into contact with an aqueous solution or suspension (for example, a waste water) a direct emulsion is formed, that is, oil in water, without the need to add a high HLB inverting surfactant, such that the flocculant polymer of the microemulsion dissolves in said aqueous solution or suspension and results in the formation of flocs.
- a Polymeric microemulsion for use as a flocculant maintains its stability and its ability to be vehiculable (necessary to facilitate its dosing by conventional means such as, for example, pumps) over a wide range of temperatures that corresponds to the temperatures in winter and summer in different geographical locations, typically between 0 ° C and 40 ° C.
- a fluidizer and / or an antifreeze such as polyethylene glycol.
- the present invention relates to non-ionic polymers and high molecular weight ionic copolymers, desirably above 3.10 6 g / mol, obtained by inverse microemulsion polymerization in the presence of a self-reversible surfactant system in contact with an aqueous solution or suspension, capable of thermodynamically stabilizing the microemulsion, the polymer consisting of acrylamide and the copolymer of acrylamide and (meth) acrylic acid or one of its salts in a weight ratio of acrylamide to acrylic acid or one of its salts between 100: 0 and 40:60.
- the present invention also relates to a process for obtaining inverse microemulsions of acrylamide polymers or acrylamide and acid copolymers.
- aqueous phase comprising:
- a monomer to be polymerized selected from acrylamide and a mixture of monomers comprising, at least, acrylamide and, at least, (meth) acrylic acid or one of its salts, in a total concentration of monomer (s) comprised between 20% and 40% by weight with respect to the total microemulsion, and in a weight ratio of acrylamide to (meth) acrylic acid or a salt thereof between 100: 0 and 40:60;
- a surfactant system whose HLB is comprised between 8 and 10, comprising one or more non-ionic surfactants, each of said non-ionic surfactants comprising at least one hydrophobic chain containing more of 16 carbon atoms and at least one double bond;
- (meth) acrylic acid or one of its salts includes both acrylic acid and methacrylic acid and any of its salts.
- a reverse microemulsion depends on the proper selection of the surfactant system, its concentration and HLB as well as the temperature, nature of the oil phase and composition of the aqueous phase.
- any surfactant system is not suitable for achieving stable polyether microemulsions, although microemulsions formed by the monomers are pre-polymerized.
- the inventors of the present invention have shown that, surprisingly, in addition to the HLB of the surfactant system being between 8 and 10, as indicated by the state of the art, the surfactant system proposed by this invention (sometimes identified in this description as a surfactant system of the invention) must contain at least one or more non-ionic surfactants, each containing at least one hydrophobic chain with a number of carbon atoms greater than 16, preferably between 18 and 20, and, in addition, at least a double link.
- the appropriate HLB of a surfactant system to form a reverse microemulsion according to the present invention, before polymerization, must be between 8 and 11, preferably, between 8 and 10.5. However, for the microemulsion to remain stable after polymerization it is necessary that the HLB be between 8 and 10, preferably between 9.2 and 9.6. Values greater than 9, 6 can cause self-investment during polymerization so that the polymers and copolymers object of the present invention are not obtained in microemulsion, but in the form of an unmanageable mass. Values below 9.2 hinder the self-investment of the microemulsion when, to act as a flocculant, it comes into contact with an aqueous solution or suspension.
- HLB can be achieved using a single nonionic surfactant or a mixture of nonionic surfactants. However, it is preferable to use a mixture of two or more non-ionic surfactants such that the HLB of at least one of them is between 3 and 8, while the HLB of at least one of them is between 9, 5 and 14 , preferably between 9, 8 and 11, 5.
- the concentration of the surfactant system of the invention should be sufficient to stabilize the microemulsion obtained after polymerization. Generally, the concentration should be between 8% and 20% by weight, preferably between 10% and 15% by weight, based on the total weight of the microemulsion. Lower values do not allow stabilizing the polymeric microemulsion, while higher values do not provide any technical advantage and imply an economic penalty.
- surfactant or surfactants that form the surfactant system of the invention is critical for the purposes of the present invention.
- Such surfactants are of the non-ionic type, and must have, at least, a hydrophobic chain with a number of carbon atoms greater than 16, preferably between 18 and 20, and, in addition, at least, a double bond (sometimes these surfactants Non-ionic are identified in this description as non-ionic surfactants "A"). If the non-ionic surfactant "A" has more than one hydrophobic chain, they may be the same or different, usually the same.
- non-ionic surfactants "" may be mentioned, by way of example, and only for illustrative and non-limiting purposes, the following: sorbitol and sorbitan esters such as polyethoxylated sorbitol hexaoleate, polyethoxylated sorbitan trioleate, polyethoxylated sorbitan sesquioleate, sorbitol monooleate and polyethoxylated sorbitan monooleate, polyethylene glycol esters such as monooleate and polyethylene glycol dioleate; ethoxylated fatty alcohols, such as polyethoxylated oleic and ricinoleic alcohol; polyethoxylated xylitol esters, such as polyethoxylated xylitol pentaoleate; polyethoxylated glycerin esters, such as polyethoxylated glycerin trioleate; and polyethoxylated tri
- the surfactant system of the invention whose HLB must being between 8 and 10 comprises, in addition to one or more of said surfactants not ionic "A", at least one non-ionic surfactant (non-ionic surfactant "B") in which all its hydrophobic chains are saturated and HLB greater than 12, preferably equal to or greater than 13, in an amount between 2% and 20 % by weight with respect to the total surfactant system used in the microemulsion, preferably between 5% and 15% by weight of the total surfactant system.
- non-ionic surfactant "B" of HLB greater than 12 nonionic surfactants of the ethoxylated fatty alcohols type HLB between 13 and 18 are preferred.
- the surfactant system may contain, in addition, an anionic surfactant, in an amount comprised between 0.1% and 10%, preferably between 0.1% and 2%, by weight with respect to the total surfactant system used in the microemulsion. Any anionic surfactant can be used in the present invention.
- the oily or organic phase of the microemulsion is formed by the surfactant system and an organic solvent.
- the selection of the organic solvent in the microemulsion significantly influences the minimum amount of surfactant system needed to stabilize it and the optimal HLB to form it.
- This solvent may be an aliphatic or aromatic hydrocarbon or a mixture of aromatic and / or aliphatic hydrocarbons.
- the number of carbon atoms in the hydrocarbons may be between 6 and 18, preferably between 10 and 14.
- the aqueous phase of the microemulsion is composed of water, the monomers to be polymerized, and, optionally, (i) an additive necessary for prevent the inactivation of the polymerization due to the presence of metals, such as a metal chelating agent, for example EDTA (ethylenediaminetetraacetic acid) and / or NTA (nitrilotriacetic acid), and (ii) a polymerization initiator or a member of a redox polymerization initiator pair.
- a metal chelating agent for example EDTA (ethylenediaminetetraacetic acid) and / or NTA (nitrilotriacetic acid
- a polymerization initiator or a member of a redox polymerization initiator pair In case the polymerization initiation is carried out by a redox pair, said aqueous phase will preferably comprise the oxidizing agent of the redox pair.
- the aqueous phase monomers consist either of a single non-ionic vinyl monomer such as acrylamide, or of a mixture of non-ionic and ionic vinyl monomers such as acrylamide and (meth) acrylic acid or one of its salts, preferably sodium or potassium, in a total concentration of monomers with respect to the total weight of the microemulsion between 20% and 40% by weight and in a weight ratio of acrylamide to (meth) acrylic acid or its salts between 100: 0 and 40:60 .
- the preferred monomer concentration is, where appropriate, 50% by weight.
- the pH of the aqueous phase is between 6 and 8, preferably between 7.3 and 7.5.
- the ratio of the organic phase to the aqueous phase is such that the total concentration of active material (polymer or copolymer) of the microemulsion, once the polymerization is carried out, is between 20 and 35%, preferably between 25% and 30%, in weight with respect to the total of the microemulsion.
- the polymerization of the monomers is carried out by free radicals until the conversion of the monomers is equal to or greater than 60%, preferably, equal to or greater than 80%, more preferably, equal to or greater than 95%, and preferably, 100% substantially.
- the polymerization initiation can be carried out at a temperature between 10 ° C and 40 ° C, preferably between 25 ° C and 35 ° C. If the polymerization is carried out discontinuously, in a single stage, during the course of the polymerization the heat released is such that, taking into account the high polymerization rate, it is practically impossible to keep the temperature constant, which can be increased up to values between 60 ° C and 92 ° C without altering the quality of the product obtained.
- a wide variety of free radical polymerization initiators can be used for the implementation of the present invention.
- thermal initiators it is possible to mention 2,2'- azobisisobutyronitrile (AIBN), 2,2'-azobis (2- aminopropane) dihydrochloride (V-50), peroxides, such as terebutyl peroxide, and inorganic compounds, such as sodium persulfate.
- AIBN 2,2'- azobisisobutyronitrile
- V-50 2,2'-azobis (2- aminopropane) dihydrochloride
- peroxides such as terebutyl peroxide
- inorganic compounds such as sodium persulfate.
- a thermal initiator it can be added initially to the aqueous phase or subsequently to the final microemulsion after degassing. In the first case it is necessary to perform degassing at a temperature between 20 ° C and 30 ° C.
- the ammonium ferrous sulfate / ammonium persulfate and sodium disulfite / ammonium persulfate pairs can be mentioned.
- the aqueous phase will preferably comprise the oxidizing agent of the redox pair.
- sodium disulfite Na 2 S 2 ⁇ 5
- the polymerization is initiated by the exclusive use of sodium disulfite as initiator, adding it continuously and in the form of an aqueous solution on the deoxygenated microemulsion at a given temperature.
- concentration of the reducing agent present, where appropriate, in the aqueous solution to be added on the deoxygenated microemulsion is between 0.10 g / 1 and 400 g / 1, preferably between 0.25 g / 1 and 5 g / 1 , more preferably, between 0.5 g / 1 and 3 g / 1.
- the rate of addition of the reducing agent solution depends on the concentration of reducing agent therein.
- the flow rate may vary between 20 and 110 ml / h / kg of aqueous phase, preferably between 70 and 95 ml / h / kg of aqueous phase.
- the inverse microemulsion polymerization reaction can be carried out both discontinuously (in a single stage or in several sequential steps of adding the aqueous phase) or continuous or semi-continuous.
- the preferred mode of operation is the discontinuous mode on a single charge. which, preferably, is performed as follows:
- aqueous phase comprising:
- a monomer to be polymerized selected from acrylamide and a mixture of acrylamide and (meth) acrylic acid or a salt thereof, in a total concentration of monomer comprised between 20% and 40% by weight with respect to the total microemulsion, and in a weight ratio of acrylamide to (meth) acrylic acid or its salts between 100: 0 and 40:60;
- a metal chelating agent such as EDTA
- Y optionally, a metal chelating agent, such as EDTA
- an oxidizing agent member of a redox pair initiating free radical polymerization such as ammonium or potassium persulfate;
- a surfactant system whose HLB is comprised between 8 and 10, preferably between 9.2 and 9.6, comprising one or more non-ionic surfactants, each of said surfactants comprising at least one hydrophobic chain containing more of 16 carbon atoms and at least one double bond;
- the polymeric microemulsions obtained according to the process of the present invention can have various applications.
- One of the main applications is its use as a flocculant since they have notable advantages compared to flocculants that are currently sold in solid state or in emulsion. Among these advantages are: a) higher performance; b) stability in the typical application temperature range; c) ease of dosing by conventional dosing devices; and d) self-investment capacity in contact with an aqueous solution or suspension.
- the microemulsion flocculants obtained according to the process of the present invention have, at equal dosing, a performance as a flocculant equal to or greater than the emulsions of the same ionic charge currently marketed, while They lack the disadvantages of these mentioned above.
- Example 1 In an jacketed reactor an aqueous phase is prepared by adding 90 g of a 50% by weight aqueous acrylamide solution 0.2 g of the disodium salt of ethylenediaminetetraacetic acid and 0.135 g of ammonium persulfate. This aqueous phase is deoxygenated by bubbling nitrogen for 15 minutes.
- an oil phase is prepared by adding 30 g of a HLB 8.68 surfactant system, formed by 21 g of a polyethoxylated secondary linear fatty alcohol of HLB 7.9 and 9 g of a surfactant of the same type but of HLB 10.5, both with an average number of carbon atoms in their hydrophobic chain of 13, at 30 g of a paraffinic oil formed by a mixture of n-decane and tetradecane in a weight ratio of 40:60.
- This oil phase is deoxygenated by bubbling nitrogen for 15 minutes.
- the oil phase is slowly added to the aqueous phase under a nitrogen atmosphere and with stirring.
- the mixture returns to deoxygenate bubbling nitrogen for 15 minutes.
- a completely transparent microemulsion is formed. Its temperature is adjusted to 40 ° C by recirculating water at 41 ° C through the reactor jacket.
- Polymerization is initiated by adding an aqueous solution of sodium disulfite (45 g / 1) at a flow rate such that the polymerization temperature does not exceed 52 ° C.
- the reaction mass separates in phases during polymerization.
- Example 3 The procedure of example 1 is repeated, but adjusting the relative amounts of the surfactants so that the HLB is 9.
- the reaction mass separates in phases during polymerization.
- Example 4 The procedure of example 1 is repeated, but the initial polymerization temperature is set at 25 ° C.
- the reaction mass separates in phases during polymerization.
- Example 5 The procedure of example 1 is repeated, but the initial polymerization temperature is set at 30 ° C. The reaction mass separates into phases during polymerization.
- Example 6 The procedure of example 1 is repeated, but the initial polymerization temperature is adjusted to 35 ° C.
- the reaction mass separates in phases during polymerization.
- Example 7 In an jacketed reactor an aqueous phase is prepared by adding 52.74 g of a 50% by weight aqueous acrylamide solution, 13.99 g of demineralized water, 13,585 g of acrylic acid, and 7.626 g of sodium hydroxide in lentils The addition of sodium hydroxide is carried out under conditions such that the temperature of the solution does not exceed 35 ° C at any time. Then, 0.442 g of ammonium persulfate and 0.152 g of the disodium salt of ethylenediaminetetraacetic acid are added with stirring. The pH is measured and if it is outside the range 7.3-7.5 it is adjusted to said range by adding either sodium hydroxide or acrylic acid. This aqueous phase is deoxygenated by bubbling nitrogen for 15 minutes. The proportion of the monomers is such that after polymerization the ionic charge of the copolymer is 40%.
- an oil phase is prepared by adding 30 g of a HLB 8.68 surfactant system, formed by 21 g of a polyethoxylated secondary linear fatty alcohol of HLB 7.9 and 9 g of a surfactant of the same type but of HLB 10.5, both with an average number of carbon atoms in their hydrophobic chain of 13, to 41,479 g of a paraffinic oil formed by a mixture of n-decane and tetradecane in a weight ratio of 40:60.
- This oil phase is deoxygenated by bubbling nitrogen for 15 minutes.
- the oil phase is slowly added to the aqueous phase under a nitrogen atmosphere and with stirring.
- the mixture is deoxygenated again by bubbling nitrogen for 15 minutes. It forms a completely transparent microemulsion. Its temperature is adjusted to 25 ° C.
- Polymerization is initiated by adding an aqueous solution of sodium disulfite (45 g / 1) with a flow rate of 88.88 ml / h / kg of aqueous phase.
- the reaction mass separates in phases during polymerization.
- Example 7 is repeated, but in this case the surfactant system consists of 19.5 g of a mixture of an ethoxylated oleic alcohol (HLB 4.9), polyethylene glycol 400 dilaurate (HLB 10.2) and an ethoxylated secondary alcohol (HLB 13.3) with 13 carbon atoms in its hydrophobic chain.
- the proportions between the surfactants are such that the HLB of the surfactant system is 9.6 and the percentage of ethoxylated secondary alcohol (HLB 13.3) is 10% of the total weight of surfactants.
- the reaction mass separates in phases during polymerization.
- Example 9 Example 8 is repeated, but in this case the surfactant system consists of 19.5 g (13% by weight of the total microemulsion weight) of a mixture of an ethoxylated oleic alcohol (HLB 4.9), and polyethylene glycol 400 dilaurate (HLB 10.2) in proportions such that the HLB of the surfactant system is 9.2.
- HLB ethoxylated oleic alcohol
- the reaction mass separates in phases during polymerization.
- Example 8 is repeated, but in this case the surfactant system is constituted by 22.5 g (15% by weight of the total microemulsion weight) of a mixture of an ethoxylated oleic alcohol (HLB 4.9), and dilaurate of polyethylene glycol 400 (HLB 10.2) in proportions such that the HLB of the surfactant system is 9.2.
- HLB ethoxylated oleic alcohol
- the reaction mass separates in phases during polymerization.
- Example 11 Example 10 is repeated, but in this case the surfactant system consists of 22.5 g (15% by weight of the total microemulsion weight) of a mixture of an ethoxylated oleic alcohol (HLB 4.9), and polyethylene glycol dilaurate 400 (HLB 10.2) in proportions such that the HLB of the surfactant system is 8, 9.
- HLB ethoxylated oleic alcohol
- the reaction mass separates in phases during polymerization.
- Example 12 Example 8 is repeated, but polymerization is started at 35 ° C.
- the reaction mass separates in phases during polymerization.
- Example 13 In an jacketed reactor an aqueous phase is prepared by adding 52.74 g of a 50% by weight aqueous acrylamide solution, 13.996 g of demineralized water, 13.585 g of acrylic acid, and 7.626 g of sodium hydroxide in lentils .
- the addition of sodium hydroxide is carried out under conditions such that the temperature of the solution does not exceed 35 ° C at any time.
- 0.442 g of ammonium persulfate and 0.152 g of the disodium salt of ethylenediaminetetraacetic acid are added with stirring.
- the pH is measured and if it is outside the range 7.3-7.5 it is adjusted to said range by adding either sodium hydroxide or acrylic acid.
- This aqueous phase is deoxygenated by bubbling nitrogen for 15 minutes.
- the proportion of the monomers is such that after polymerization
- the ionic charge of the copolymer is 40%.
- an oil phase is prepared by adding 23.85 g of a surfactant system of HLB 9.36, formed by 8.87 g of sorbitol hexalaurate with 7 moles of ethylene oxide (HLB 4.9) and 14, 98 g of sorbitol hexalaurate with 39 moles of ethylene oxide (HLB 12), to 37,129 g of a paraffinic oil formed by a mixture of n-decane and tetradecane in a weight ratio of 40:60.
- This oil phase is deoxygenated by bubbling nitrogen for 15 minutes.
- the oil phase is slowly added to the aqueous phase under a nitrogen atmosphere and with stirring.
- the mixture is deoxygenated again by bubbling nitrogen for 15 minutes.
- a completely transparent microemulsion is formed. Its temperature is adjusted to 35 ° C. Polymerization is initiated by adding an aqueous solution of sodium disulfite (45 g / 1) with a flow rate of 88.88 ml / h / kg of aqueous phase. The polymerization begins almost instantaneously and during it the reaction mass separates into phases.
- Example 14 The experiment of example 13 is repeated, but using as a surfactant system a mixture of xylitol pentalaurate with 9 moles of ethylene oxide (HLB 4.9) and xylitol pentalaurate with 33 moles of ethylene oxide (HLB 12).
- reaction mass separates into phases.
- Examples 1 to 14 demonstrate that the use of a surfactant system in which at least one of the major constituents has a hydrophobic chain with a number of low carbon atoms less than 13, does not allow obtaining stable microemulsions after polymerization, independently that the number of hydrophobic chains per surfactant molecule is one or more.
- E emplo 15 In an jacketed reactor an aqueous phase is prepared by adding 52.74 g of a 50% by weight aqueous acrylamide solution, 13.996 g of demineralized water, 13.585 g of acrylic acid, and 7.626 g of sodium hydroxide in lentils The addition of sodium hydroxide is carried out under conditions such that the temperature of the solution does not exceed 35 ° C at any time.
- an oil phase is prepared by adding 19.982 g of a surfactant system of HLB 9.6, formed by 5.406 g of an ethoxylated oleic alcohol of HLB 4.9, 12.579 g of an ethoxylated ricinoleic alcohol of HLB 11 and 1,997 g of a linear secondary fatty alcohol with 13 carbon atoms in its hydrophobic chain (HLB 13.3), to 41,479 g of a paraffinic oil formed by a mixture of n-decane and tetradecane in a weight ratio of 40:60.
- This oil phase is deoxygenated by bubbling nitrogen for 15 minutes.
- the oil phase is slowly added to the aqueous phase under a nitrogen atmosphere and with stirring.
- the mixture is deoxygenated again by bubbling nitrogen for 15 minutes.
- a completely transparent microemulsion is formed. Its temperature is adjusted to 30 ° C.
- Polymerization is initiated by adding an aqueous solution of sodium disulfite (45 g / 1) with a flow rate of 88.88 ml / h / kg of aqueous phase.
- the polymerization starts almost instantaneously and during it the temperature rises to 90-92 ° C in less than a minute.
- the polymerization is given by finished when the temperature returns to its initial value.
- a microemulsion flocculant with an active matter content of 30% by weight is obtained.
- microemulsion is translucent, stable and easily vehiculable. By adding 4 g of it to 250 g of water under stirring, its inversion takes place in less than 1 hour, as is shown by monitoring the increase in viscosity of the solution as a function of time.
- Example 15 is repeated, but polymerization starts at 35 ° C.
- the microemulsion obtained after polymerization is translucent, stable and easily transportable.
- Example 17 Example 15 is repeated, but polymerization starts at 25 ° C.
- the microemulsion obtained after polymerization is translucent, stable and easily transportable.
- Example 15 is repeated, but the proportions of the surfactants are adjusted so that the HLB of the surfactant mixture is 8.9.
- the polymerization starts at 35 ° C.
- the microemulsion obtained after polymerization is translucent, stable and easily transportable. By adding 4 g of it to 250 g of water under stirring, its investment takes place in less than 1 hour, as shown by monitoring the increase in viscosity of the solution as a function of time.
- Example 15 is repeated, except that the polymerization is started at 35 ° C, and the oil phase is constituted by a mixture of a surfactant system of HLB 9.36 formed by a mixture of 8.87 g of xylitol pentaoleate with 9 moles of ethylene oxide (HLB 4.9) and 14.98 g of xylitol pentaoleate with 47 moles of ethylene oxide (HLB 12), and 37.129 g of a paraffinic oil consisting of a mixture of n-decane and tetradecane at a weight ratio of 40:60.
- the concentration of surfactant system is 15.9% by weight with respect to the total weight of the microemulsion.
- the microemulsion obtained after polymerization is translucent, stable and easily transportable.
- Example 20 The experiment of example 15 is repeated, except that the polymerization is started at 35 ° C and the surfactant system consists of a mixture of sorbitol penta stearate with 9 moles of ethylene oxide (HLB 4.9) and sorbitol pentaestearate with 47 moles of ethylene oxide (HLB 12), in a proportion such that the HLB of the mixture is 9.2.
- the surfactant system consists of a mixture of sorbitol penta stearate with 9 moles of ethylene oxide (HLB 4.9) and sorbitol pentaestearate with 47 moles of ethylene oxide (HLB 12), in a proportion such that the HLB of the mixture is 9.2.
- Example 20 is repeated, with the exception that the surfactant system consists of a mixture of sorbitol hexaestearate with 11 moles of ethylene oxide (HLB 4.9) and sorbitol hexaestearate with 56 moles of ethylene oxide (HLB 12) , in a proportion such that the HLB of the mixture is 9.2.
- HLB ethylene oxide
- the maximum temperature reached is 64 ° C and the polymerization is terminated when the temperature drops to the initial temperature. A stable microemulsion is obtained which, after standing overnight, separates into phases.
- Examples 20 and 21 demonstrate that neither stable microemulsions of anionic and non-ionic flocculants can be obtained after polymerization using surfactants with a high number of carbon atoms (18) in their hydrophobic chain or in each of their hydrophobic chains. For this, it is necessary that there is at least a double bond in the hydrophobic chain or chains of the surfactant, as evidenced by examples 15 to 19.
- An aqueous phase is prepared in a jacketed reactor by adding 54 g of a 50% by weight aqueous acrylamide solution, 14,516 g of demineralized water, 13,739 g of acrylic acid, and 7,545 g of sodium hydroxide in lentils.
- the addition of sodium hydroxide is carried out under conditions such that the temperature of the solution does not exceed 35 ° C at any time.
- 0.150 g of the disodium salt of ethylenediaminetetraacetic acid is added with stirring.
- the pH is measured and if it is outside the range 7.3-7.5 it is adjusted to said range by adding either sodium hydroxide or acrylic acid.
- an oil phase is prepared by adding
- Polymerization is initiated at 35 ° C by adding an aqueous solution of sodium disulfite (5 g / 1) with a flow rate of 88.89 ml / h / kg of aqueous phase.
- the polymerization starts within a few seconds and during it the temperature rises to 79 ° C.
- the polymerization is terminated when the temperature returns to its initial value.
- a microemulsion flocculant with an active matter content of 30% by weight is obtained.
- the microemulsion is translucent, stable and easily vehiculable.
- the polymerization was repeated under the same conditions as in Example 22, except that the concentration of the aqueous sodium disulfite solution was 3 g / 1. The temperature rose to 77.5 ° C. The microemulsion was translucent, stable and easily vehicular.
- the polymerization was repeated under the same conditions as in Example 22, except that the concentration of the aqueous sodium disulfite solution was 1 g / 1. The temperature rose to 66.4 ° C. The microemulsion was translucent, stable and easily vehicular.
- Example 25 Polymerization was repeated under the same conditions as in Example 22, except that the concentration of the aqueous sodium disulfite solution was 0.5 g / 1. The temperature rose to 61 ° C. The microemulsion was translucent, stable and easily vehicular. Ex emplo 26
- the polymerization was repeated under the same conditions as in Example 22, except that the concentration of the aqueous disulfite solution was 0.1 g / 1. The temperature rose to 53 ° C. The microemulsion was translucent, stable and easily vehicular.
- the microemulsion was translucent, stable and easily vehicular.
- the polymerization was repeated under the same conditions as in Example 25, except that the initial polymerization temperature was 30 ° C. The temperature rose to 58 ° C. The microemulsion was translucent, stable and easily vehicular.
- the polymerization was repeated under the same conditions as in Example 25, except that the initial polymerization temperature was 25 ° C. The temperature rose to 52 ° C. The microemulsion was translucent, stable and easily vehicular.
- the polymerization was repeated under the same conditions as in Example 25, except that the initial polymerization temperature was 20 ° C. The temperature rose to 47 ° C. The microemulsion was translucent, stable and easily vehicular.
- Example 31 Polymerization was repeated under the same conditions as in Example 25, except that the initial temperature of polymerization was 15 ° C. The temperature rose to 56.5 ° C. The microemulsion was translucent, stable and easily vehicular.
- Example 32 (Comparative)
- the yields as dehydration agents of the microemulsions obtained according to examples 22 to 31 of the present invention are compared with two commercial dehydration agents in emulsion: Superfloc A-1883 and Superfloc A-1820, of Cytec Technology Corp., Wil ington, DE, both with a 40% anionic charge and the same active matter content as the microemulsions of this invention tested in this example.
- the tests were performed by previously inverting both the microemulsions of this invention and the commercial emulsions mentioned to give a concentration of 2 g / 1 emulsion or microemulsion. Then, and from this solution, different doses of the inverted solution were added to the sludge used to determine the optimum dose as flocculant of each product.
- the microemulsions of examples 22 to 26 of this invention were evaluated with a sludge from the physical-chemical treatment of a drinking water treatment plant by means of the CST ("Capillary Suction Time") method, with a stirring time of 10 seconds. The concentration of sludge solids was 10 g / 1.
- the yield of the microemulsions of Examples 23 to 26 of this invention was similar and equal to that of the Superfloc A-1883 emulsion, the optimum dose being 100 ppm emulsion or microemulsion, and much higher than that of the Superfloc A-1820 emulsion. whose optimal dose was 140 ppm.
- the microemulsion yield of example 22 of this invention (optimum dose 120 ppm) was lower than that of the Superfloc A-1883 emulsion and superior to that of the Superfloc A-1820 emulsion.
- microemulsions of examples 27 to 31 of this invention were evaluated with a sludge from the physical-chemical treatment of a sewage treatment plant. industrial by the same criteria above.
- concentration of sludge solids was 50 g / 1.
- the yield of the microemulsions of this invention was similar and equal to that of the Superfloc A-1883 emulsion, the optimum dose being 80 ppm emulsion or microemulsion, and much higher than that of the Superfloc A-1820 emulsion whose optimal dose was 120 ppm.
- the quality of the ball formed by the microemulsions of this invention and the Superfloc A-1883 product measured as the size and consistency of the ball, was far superior to that of the Superfloc A-1820 product.
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- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
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Abstract
Description
Claims
Priority Applications (7)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP01274875A EP1462462B1 (en) | 2001-12-07 | 2001-12-07 | Method of producing reverse microemulsions from non-ionic polymers or ionic copolymers |
ES01274875T ES2250306T3 (es) | 2001-12-07 | 2001-12-07 | Procedimiento para la produccion de microemulsiones inversas de polimeros no ionicos o de copolimeros ionicos. |
PCT/ES2001/000481 WO2003048218A1 (es) | 2001-12-07 | 2001-12-07 | Procedimiento para la produccion de microemulsiones inversas de polimeros no ionicos o de copolimeros ionicos |
AT01274875T ATE304026T1 (de) | 2001-12-07 | 2001-12-07 | Verfahren zur herstellung von umgekehrten mikroemulsionen aus nichtionischen polymeren oder ionischen copolymeren |
DE60113307T DE60113307D1 (de) | 2001-12-07 | 2001-12-07 | Verfahren zur herstellung von umgekehrten mikroemulsionen aus nichtionischen polymeren oder ionischen copolymeren |
AU2002221975A AU2002221975A1 (en) | 2001-12-07 | 2001-12-07 | Method of producing reverse microemulsions from non-ionic polymers or ionic copolymers |
US10/497,922 US20050119405A1 (en) | 2001-12-07 | 2001-12-09 | Method of producing reverse microemulsions from non-ionic polymers or ionic copolymers |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/ES2001/000481 WO2003048218A1 (es) | 2001-12-07 | 2001-12-07 | Procedimiento para la produccion de microemulsiones inversas de polimeros no ionicos o de copolimeros ionicos |
Publications (1)
Publication Number | Publication Date |
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WO2003048218A1 true WO2003048218A1 (es) | 2003-06-12 |
Family
ID=8244409
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/ES2001/000481 WO2003048218A1 (es) | 2001-12-07 | 2001-12-07 | Procedimiento para la produccion de microemulsiones inversas de polimeros no ionicos o de copolimeros ionicos |
Country Status (7)
Country | Link |
---|---|
US (1) | US20050119405A1 (es) |
EP (1) | EP1462462B1 (es) |
AT (1) | ATE304026T1 (es) |
AU (1) | AU2002221975A1 (es) |
DE (1) | DE60113307D1 (es) |
ES (1) | ES2250306T3 (es) |
WO (1) | WO2003048218A1 (es) |
Families Citing this family (5)
Publication number | Priority date | Publication date | Assignee | Title |
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DE60112338T2 (de) * | 2001-12-31 | 2006-06-01 | Acideka, S.A., Bilbao | Verfahren zur herstellung von umgekehrten mikroemulsionen aus kationischen copolymeren |
GT200600405A (es) * | 2005-09-07 | 2007-04-16 | Formula de microemulsión | |
CN101235111B (zh) * | 2007-01-29 | 2010-04-21 | 中南大学 | 高固含、低油水比水溶性聚合物反相微乳液制备方法 |
US7816305B2 (en) * | 2008-05-15 | 2010-10-19 | Halliburton Energy Services, Inc. | Reversible surfactants and methods of use in subterranean formations |
CA2985806C (en) | 2015-05-19 | 2023-09-19 | The Mosaic Company | Reverse emulsions for cavity control |
Citations (6)
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GB2150579A (en) * | 1983-12-01 | 1985-07-03 | Pennwalt Corp | Process for preparing high molecular weight acrylamide polymers |
FR2565592A1 (fr) * | 1984-06-07 | 1985-12-13 | Inst Francais Du Petrole | Procede de preparation de microlatex inverses et les microlatex inverses obtenus |
US4656222A (en) * | 1985-05-16 | 1987-04-07 | Celanese Corporation | Preparation of high molecular weight polyacrylates by inverse emulsion polymerization |
US4672090A (en) * | 1984-04-04 | 1987-06-09 | Calgon Corporation | Surfactant system for emulsion polymers |
US5290479A (en) * | 1986-12-09 | 1994-03-01 | Phillips Petroleum Company | Surfactant system of polyethoxylated compounds and glyceride compounds |
EP1059305A1 (en) * | 1999-06-09 | 2000-12-13 | Calgon Corporation | Inverse emulsion polymer and production thereof |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6130303A (en) * | 1988-12-19 | 2000-10-10 | Cytec Technology Corp. | Water-soluble, highly branched polymeric microparticles |
US5914366A (en) * | 1993-11-24 | 1999-06-22 | Cytec Technology Corp. | Multimodal emulsions and processes for preparing multimodal emulsions |
DE60112338T2 (de) * | 2001-12-31 | 2006-06-01 | Acideka, S.A., Bilbao | Verfahren zur herstellung von umgekehrten mikroemulsionen aus kationischen copolymeren |
-
2001
- 2001-12-07 AU AU2002221975A patent/AU2002221975A1/en not_active Abandoned
- 2001-12-07 AT AT01274875T patent/ATE304026T1/de not_active IP Right Cessation
- 2001-12-07 WO PCT/ES2001/000481 patent/WO2003048218A1/es not_active Application Discontinuation
- 2001-12-07 DE DE60113307T patent/DE60113307D1/de not_active Expired - Lifetime
- 2001-12-07 ES ES01274875T patent/ES2250306T3/es not_active Expired - Lifetime
- 2001-12-07 EP EP01274875A patent/EP1462462B1/en not_active Expired - Lifetime
- 2001-12-09 US US10/497,922 patent/US20050119405A1/en not_active Abandoned
Patent Citations (6)
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---|---|---|---|---|
GB2150579A (en) * | 1983-12-01 | 1985-07-03 | Pennwalt Corp | Process for preparing high molecular weight acrylamide polymers |
US4672090A (en) * | 1984-04-04 | 1987-06-09 | Calgon Corporation | Surfactant system for emulsion polymers |
FR2565592A1 (fr) * | 1984-06-07 | 1985-12-13 | Inst Francais Du Petrole | Procede de preparation de microlatex inverses et les microlatex inverses obtenus |
US4656222A (en) * | 1985-05-16 | 1987-04-07 | Celanese Corporation | Preparation of high molecular weight polyacrylates by inverse emulsion polymerization |
US5290479A (en) * | 1986-12-09 | 1994-03-01 | Phillips Petroleum Company | Surfactant system of polyethoxylated compounds and glyceride compounds |
EP1059305A1 (en) * | 1999-06-09 | 2000-12-13 | Calgon Corporation | Inverse emulsion polymer and production thereof |
Non-Patent Citations (4)
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HERNANDEZ-BARAJAS J. ET AL: "Reaction engineering of acrylic water-soluble polymers", DECHEMA MONOGRAPHS (6TH INTERNATIONAL WORKSHOP ON POLYMER REACTION ENGINEERING), vol. 134, 1998, pages 523 - 543, XP002968788 * |
HUNKELER D., HERNANDEZ-BARAJAS J.: "Heterophase water-in-oil polymerization of acrylamide by a hybrid inverse-emulsion/inverse-microemulsion process", POLYMER, vol. 38, no. 22, 1997, pages 5623 - 5641, XP004090228 * |
KATIME I. ET AL: "Synthesis and characterization of polyacrylamides in inverse-emulsions with an isoparaffinic solvent", MACROMOL. CHEM. PHYS., vol. 202, no. 9, June 2001 (2001-06-01), pages 1837 - 1843, XP002968789 * |
REKEN A. ET AL: "Effect of the surfactant blend compositon on the properties of polymerizing acrlamide-based inverse-emulsions: characterization by small-angle neutron scattering and quasi-elastic light scattering", POLYMER, vol. 40, 1999, pages 3545 - 3554, XP002968229 * |
Also Published As
Publication number | Publication date |
---|---|
AU2002221975A1 (en) | 2003-06-17 |
US20050119405A1 (en) | 2005-06-02 |
ATE304026T1 (de) | 2005-09-15 |
DE60113307D1 (de) | 2005-10-13 |
ES2250306T3 (es) | 2006-04-16 |
EP1462462A1 (en) | 2004-09-29 |
EP1462462B1 (en) | 2005-09-07 |
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