WO2011094333A1 - Miniemulsion polymerization to prepare drag reducers - Google Patents

Miniemulsion polymerization to prepare drag reducers Download PDF

Info

Publication number
WO2011094333A1
WO2011094333A1 PCT/US2011/022602 US2011022602W WO2011094333A1 WO 2011094333 A1 WO2011094333 A1 WO 2011094333A1 US 2011022602 W US2011022602 W US 2011022602W WO 2011094333 A1 WO2011094333 A1 WO 2011094333A1
Authority
WO
WIPO (PCT)
Prior art keywords
miniemulsion
drag
solution
aqueous solution
reducer
Prior art date
Application number
PCT/US2011/022602
Other languages
French (fr)
Inventor
Zhiyi Bao
Kenneth W. Smith
Original Assignee
Conocophillips Company
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Family has litigation
First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=44309443&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=WO2011094333(A1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Priority to CA2788092A priority Critical patent/CA2788092C/en
Priority to NO11737595A priority patent/NO2528951T3/no
Priority to BR122020003462-9A priority patent/BR122020003462B1/en
Priority to PL17209731T priority patent/PL3323835T3/en
Priority to EA201290707A priority patent/EA025537B1/en
Priority to IN5189DEN2012 priority patent/IN2012DN05189A/en
Priority to BR112012019704-5A priority patent/BR112012019704B1/en
Application filed by Conocophillips Company filed Critical Conocophillips Company
Priority to DK11737595.6T priority patent/DK2528951T3/en
Priority to ES11737595.6T priority patent/ES2667330T3/en
Priority to CN201180007467.3A priority patent/CN102803301B/en
Priority to MX2012008779A priority patent/MX339756B/en
Priority to EP17209731.3A priority patent/EP3323835B1/en
Priority to EP11737595.6A priority patent/EP2528951B1/en
Priority to PL11737595T priority patent/PL2528951T3/en
Publication of WO2011094333A1 publication Critical patent/WO2011094333A1/en

Links

Classifications

    • 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
    • C08F2/00—Processes of polymerisation
    • C08F2/12—Polymerisation in non-solvents
    • C08F2/16—Aqueous medium
    • C08F2/22—Emulsion polymerisation

Definitions

  • a method of producing a polymer latex drag reducer from a miniemulsion [0003] A method of producing a polymer latex drag reducer from a miniemulsion.
  • a drag reducer is a composition capable of substantially reducing friction loss associated with the turbulent flow of a fluid through a conduit. Where fluids are transported over long distances, such as in oil and other hydrocarbon liquid pipelines, these friction losses result in inefficiencies that increase equipment and operations costs.
  • Ultra-high molecular weight polymers are known to function well as drag reducers, particularly in hydrocarbon liquids. In general, drag reduction depends in part upon the molecular weight of the polymer additive and its ability to dissolve in the hydrocarbon under turbulent flow. Effective drag-reducing polymers typically have molecular weights in excess of five million.
  • drag reducers comprising polymeric latex emulsions can be used to reduce friction loss associated with turbulent fluid flow througlLa ⁇ coiiduit.
  • hydrocarbon streams e.g., crude oil, gasoline, diesel fuel, etc.
  • the drag reducer must be dissolved in the hydrocarbon stream.
  • Currently, a number of different commercial approaches are being taken to address the problem of preparing, dissolving, transporting and using such drag reducing polymers.
  • a common commercial method is to prepare the polymer in dilute solutions in an inert solvent such as kerosene or other solvating material.
  • This method utilizes a solution of high molecular weight polymer suitable for use as a drag reducing agent when produced by polymerization of alpha olefins in a hydrocarbon solvent.
  • the entire mixture, containing polyolefin, solvent, and catalyst particles is used without separation to form dilute solutions of the polymer in crude oil or finished hydrocarbons.
  • Yet another method is to polymerize monomers with slight water solubility using emulsion polymerization.
  • This method has the advantage that suspensions containing high levels of active drag reduction polymer (up to 45%) can be prepared.
  • the types of monomers that can be used in emulsion polymerization are not always the best choices for making drag reducing polymers for use in hydrocarbon fluids (crude oil, gasoline, and diesel fuel).
  • a method of producing a polymer latex drag reducer begins by forming an aqueous solution comprising a surfactant, a buffer and water. The method then forms an organic solution comprising a monomer and a co-stabilizer. The aqueous solution and the organic solution are mixed to form an emulsion. The emulsion is then subjected to a high shear device to produce a miniemulsion, wherein the monomers are broken into small droplets followed by polymerizing the miniemulsion with the addition of an initiator, wherein a nucleation occurs in the small monomer droplets.
  • the present method provides a method to produce a polymer latex drag reducer.
  • the method begins with forming an aqueous solution with a surfactant, a buffer and water in addition to forming an organic solution from a monomer and a co-stabilizer.
  • the aqueous solution and the organic solution are mixed to form an emulsion.
  • the emulsion is then subjected to a sonifier to produce a miniemulsion, wherein the monomers are broken into small droplets.
  • the miniemulsion is then polymerized with the addition of an initiator, wherein the nucleation occurs in the small droplets.
  • the initiator can be either water soluble or oil soluble.
  • the initiator can also be produced by mixing an oxidizer and a reducer or even, a secondary buffer, an oxidizer and a reducer.
  • the polymerization process produces a polymer latex drag reducer.
  • a second benefit is increased drag reducing properties.
  • the drag reducing properties can improve 5, 10, 15, 20, 25, 30 35, 40, or even 50% by using the miniemulsion process.
  • the drag reducing properties of the polymer do not affect the viscosity of the crude oil, more specifically heavy crude oil that it is placed into. Instead the drag reducing polymers are able to break up the turbulent flow in the pipelines that the heavy crude oil flows in, thereby improving the flow of the oil in the pipeline.
  • miniemulsion polymerization is that water insoluble monomer do not need to transfer from monomer droplets to micelles to start polymerization as in conventional emulsion polymerization. The step of monomer diffusion is eliminated.
  • Suitable examples of heavy crude oils include, but are not limited to, Merey heavy crude, Petrozuata heavy crude, Corocoro heavy crude, Albian heavy crude, Bow River heavy crude, Maya heavy crude, and San Joaquin Valley heavy crude. Additionally, the crude oil can be a blend of heavy crude oil with lighter hydrocarbons or diluents. Suitable examples of blended crude oils include, but are not limited to, Western Canadian Select and Marlim Blend. [0014]
  • the aqueous solution contains a surfactant, a buffer and water which are stirred together. The resultant homogeneous aqueous solution can have the following properties.
  • the surfactant used can include at least one high HLB anionic or nonionic surfactant.
  • HLB number refers to the hydrophile-lipophile balance of a surfactant in an emulsion. The HLB number is determined by the methods described by W.C. Griffin in J Soc. Cosmet. Chem., 1, 311 (1949) and J Soc. Cosmet. Chem., 5, 249 (1954), which are incorporated herein by reference. As used herein, the term "high HLB” shall denote an HLB number of 7 or more.
  • the HLB number of surfactants for use with forming the reaction mixture can be at least about 8, at least about 10, or at least 12.
  • Exemplary high HLB anionic surfactants include, but are not limited to, high HLB alkyl sulfates, alkyl ether sulfates, dialkyl sulfosuccinates, alkyl phosphates, alkyl aryl sulfonates, and sarcosinates.
  • Suitable examples of commercially available high HLB anionic surfactants include, but are not limited to, sodium lauryl sulfate (available as RHODAPON LSB from Rhodia Incorporated, Cranbury, NJ), dioctyl sodium sulfosuccinate (available as AEROSOL OT from Cytec Industries, Inc., West Paterson, NJ), 2-ethylhexyl polyphosphate sodium salt (available from Jarchem Industries Inc., Newark, NJ), sodium dodecylbenzene sulfonate (available as NORFOX 40 from Norman, Fox & Co., Vernon, CA), and sodium lauroylsarcosinic (available as HAMPOSYL L-30 from Hampshire Chemical Corp., Lexington, MA).
  • Exemplary high HLB nonionic surfactants include, but are not limited to, high HLB sorbitan esters, PEG fatty acid esters, ethoxylated glycerine esters, ethoxylated fatty amines, ethoxylated sorbitan esters, block ethylene oxide/propylene oxide surfactants, alcohol/fatty acid esters, ethoxylated alcohols, ethoxylated fatty acids, alkoxylated castor oils, glycerine esters, linear alcohol ethoxylates, and alkyl phenol ethoxylates.
  • Suitable examples of commercially available high HLB nonionic surfactants include, but are not limited to, nonylphenoxy and octylphenoxy poly(ethyleneoxy) ethanols (available as the IGEPAL CA and CO series, respectively from Rhodia, Cranbury, NJ), C8 to CI 8 ethoxylated primary alcohols (such as RHODASURF LA-9 from Rhodia Inc., Cranbury, NJ), CI 1 to CI 5 secondary-alcohol ethoxylates (available as the TERGITOL 15-S series, including 15-S-7, 15-S-9, 15-S-12, from Dow Chemical Company, Midland, MI), polyoxyethylene sorbitan fatty acid esters (available as the TWEEN series of surfactants from Uniquema, Wilmington, DE), polyethylene oxide (25) oleyl ether (available as SIPONIC Y-500-70 from Americal Alcolac Chemical Co., Baltimore, MD), alkylaryl polyether alcohols (available as the TRITON X series, including X-
  • the buffer can comprise any known buffer that is compatible with the initiation system such as, for example, carbonate, phosphate, and/or borate buffers.
  • Specific buffers that can be used include potassium dihydrogen phosphate and dipotassium hydrogen phosphate.
  • the organic solution contains a monomer and a co-stabilizer which are stirred together.
  • the resultant homogeneous organic solution have the following properties costabilizer are totally dissolved in the monomer
  • the drag reducing polymer can comprise a plurality of repeating units of the residues of one or more of the monomers selected from the group consisting of:
  • Ri is H or a C1-C10 alkyl radical
  • R 2 is H, a C1-C30 alkyl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, a C6-C20 substituted or unsubstituted aryl radical, an aryl-substituted C1-C10 alkyl radical, a -(CH2CH20) X -R A or -(CH2CH(CH3)0) X -R A radical wherein x is in the range of from 1 to 50 and R A is H, a C1-C30 alkyl radical, or a C6-C30 alkylaryl radical;
  • R 4 is H, a C1-C30 alkyl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, CI, S0 3 , OR B , or COORc
  • R B is H, a C1-C30 alkyl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, a C6-C20 substituted or unsubstituted aryl radical, or an aryl-substituted CI -CIO alkyl radical
  • Rc is H, a C1-C30 alkyl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, a C6-C20 substituted or
  • R 5 is H, a C1-C30 alkyl radical, or a C6-C20 substituted or unsubstituted aryl radical;
  • R 6 is H, a C1-C30 alkyl radical, or a C6-C20 substituted or unsubstituted aryl radical;
  • R 7 is H or a CI -CI 8 alkyl radical
  • R 8 is H, a C1-C18 alkyl radical, or CI
  • R 9 and R 10 are independently H, a C1-C30 alkyl radical, a C6-C20 substituted or unsubstituted aryl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, or heterocyclic radicals;
  • R n and R 12 are independently H, a C1-C30 alkyl radical, a C6-C20 substituted or unsubstituted aryl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, or heterocyclic radicals;
  • R 13 and R 14 are independently H, a C1-C30 alkyl radical, a C6-C20 substituted or unsubstituted aryl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, or heterocyclic radicals;
  • R 15 is H, a C1-C30 alkyl radical, a C6-C20 substituted or unsubstituted aryl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, or heterocyclic radicals;
  • R 16 is H, a C1-C30 alkyl radical, or a C6-C20 aryl radical;
  • R 17 and R 18 are independently H, a C1-C30 alkyl radical, a C6-C20 substituted or unsubstituted aryl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, or heterocyclic radicals;
  • R 19 and R 20 are independently H, a C1-C30 alkyl radical, a C6-C20 substituted or unsubstituted aryl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, or heterocyclic radicals.
  • the drag reducing polymer can comprise repeating units of the residues of C4-C20 alkyl, C6-C20 substituted or unsubstituted aryl, or aryl-substituted CI -CIO alkyl ester derivatives of methacrylic acid or acrylic acid.
  • the drag reducing polymer can be a copolymer comprising repeating units of the residues of 2-ethylhexyl methacrylate and the residues of at least one other monomer.
  • the drag reducing polymer can be a copolymer comprising repeating units of the residues of 2-ethylhexyl methacrylate monomers and butyl acrylate monomers. In still another embodiment, the drag reducing polymer can be a homopolymer comprising repeating units of the residues of 2-ethylhexyl methacrylate.
  • the drag reducing polymer can comprise the residues of at least one monomer having a heteroatom.
  • heteroatom includes any atom that is not a carbon or hydrogen atom. Specific examples of heteroatoms include, but are not limited to, oxygen, nitrogen, sulfur, phosphorous, and/or chlorine atoms.
  • the drag reducing polymer can comprise at least about 10 percent, at least about 25 percent, or at least 50 percent of the residues of monomers having at least one heteroatom.
  • the heteroatom can have a partial charge.
  • partial charge is defined as an electric charge, either positive or negative, having a value of less than 1.
  • the co-stabilizer can be any highly water insoluble small molecules that are presently known in the art.
  • co-stabilizers that can be used include fatty alcohols (C 12 -C 2 o), hexadecane, isohexadecane and hydrophobic oligomers such as styrene.
  • Some of the most widely used co-stabilizers include cetyl alcohol and hexadecane.
  • the co-stabilizer is required in to effectively stabilize the high shearing that is required to form the miniemulsion. Due to the high solubility of co-stabilizer in water insoluble monomer, so-stabilizer prevents monomer particles from coagulation and stabilizes the monomer particles after shearing.
  • the organic solution and aqueous solution are then mixed together to form an emulsion.
  • the emulsion is then subjected to a high-shear device.
  • High shear devices can be any commonly known device in the art such as sonifier, microfluidizers, static mixer or homogenizers.
  • the high shear devices should be able to produce submicron dispersions of monomer droplets whose droplet sizes can range from 20 to 1000 nm or even 50 to 500 nm. By reducing the droplet sizes the primary loci of nucleation would occur in the droplets rather than the micelles. This increases the possibility that polymerization of the hydrophobic monomers would take place in the monomer droplets, which in turn allows the miniemulsion to prepare oil-soluble polymers as drag reducer products.
  • the miniemulsion is then polymerized with the addition of an initiator.
  • the initiator can comprise of only an oxidizer and a reducer or it can contain a secondary buffer, an oxidizer and a reducer.
  • the initiator can also be aqueous.
  • the secondary buffer can be any commonly used buffer. Ideal buffers are those used described above that were used in production of the homogeneous aqueous solution.
  • the oxidizer solution can be any commonly used oxidizer solution.
  • the oxidizing solution are persulfates, peroxides or azonitrile initiators.
  • Possible persulfate oxidizers that can be used include ammonium persulfate, sodium persulfate and potassium persulfate.
  • Possible peroxides that can be used include hydrogen peroxide and organic peroxides.
  • the reducer is selected to reduce the oxidizer.
  • the reducer is a salt.
  • the reducer can be sulfites such as bisulfite or hydrosulfite, acids such as ascorbic acid or erythrobic acid, iron based reducers or even sodium formaldehyde sulfoxylate.
  • One example of a reducer that is frequently used is ferrous ammonium sulfate, hexahydrate, Fe(NH 4 ) 2 (S0 4 ) 2 -6H 2 0).
  • One optional component is a secondary surfactant.
  • the secondary surfactant can be any commonly used surfactant. Ideal surfactants are those used described above that were used in production of the homogeneous aqueous solution.
  • %DR ((APbase - ⁇ - APtreated) / APbase) x 100%
  • T e emuls on was done in a reactor for four hours under nitrogen at a temperature set around 2.0°C.
  • the agitator was set at 400 rpm.
  • a catalyst solution was then added to the emulsion when the temperature was 5 °C.
  • the catalyst solution was injected over 21 hours at 188 ⁇ with a total volume injected of 3.18 mL.
  • the final product weight of the polymer was 200.92 grams with the following characteristics.
  • the aqueous solution and the organic solution where then mixed together and subjected to a high shear device.
  • the jacket temperature set to around 2.0°C and the agitator at 400 rpm.
  • the emulsion was sheared under nitrogen for 1 hour.
  • the oxidizer solution was injected into the miniemulsion at 0.10 mL/minute over 40 minutes while still under nitrogen.
  • the catalyst (iron) solution was injected into the miniemulsion when the miniemulsion was 5°C.
  • the syringe pump was programmed to deliver at 188 ⁇ for 21 hours a total of 2.91 mL of the catalyst.
  • the final product weight of the polymer was 187.52 grams with the following
  • the reactor was purged for four hours under nitrogen at a temperature set around 5.0°C before starting polymerization.
  • the agitator was set at 400 rpm.
  • a catalyst solution was then added to the emulsion when the temperature was 5 °C.
  • the catalyst solution was injected over 24 hours at 330 ⁇ ⁇ with a total volume injected of 4.92mL.
  • the final product weight of the polymer was 197.97 grams with the following
  • Phosphate buffer (87.0 g potassium dihydrogen phosphate
  • the aqueous solution and the organic solution where then mixed together for 10 minutes and subjected to a high shear device.
  • the high shear device used was a Branson sonifier at the output power setting of eight and a duty cycle of 50%. After sonification the solution was cooled down to around 5.0°C placed under nitrogen for 1 hour
  • the oxidizer solution was injected into the miniemulsion at 0.10 mL/minute over 40 minutes while still under nitrogen.
  • the catalyst (iron) solution was injected into the miniemulsion when the miniemulsion was 5°C.
  • the syringe pump was programmed to deliver at 330 ⁇ ,/hr for 24 hours a total of 7.71 mL of the catalyst.
  • the final product weight of the polymer was 196.60 grams with the following characteristics.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Organic Chemistry (AREA)
  • Polymerisation Methods In General (AREA)
  • Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)

Abstract

A method of producing a polymer latex drag reducer. The method begins by forming an aqueous solution comprising a surfactant, a buffer and water. The method then forms an organic solution comprising a monomer and a co-stabilizer. The aqueous solution and the organic solution are mixed to form an emulsion. The emulsion is then subjecting to a high shear device to produce a miniemulsion, wherein the monomers are broken into small droplets followed by polymerizing the miniemulsion with the addition of an initiator, wherein a nucleation occurs in the small monomer droplets.

Description

MINIEMULSION POLYMERIZATION TO PREPARE DRAG
REDUCERS
CROSS-REFERENCE TO RELATED APPLICATIONS
[0001] This application is a non-provisional application which claims the benefit of and priority to U.S. Provisional Application Serial No. 61/299,200 filed January 28, 2010, entitled "Miniemulsion Polymerization to Prepare Drag Reducers," which is hereby incorporated by reference in its entirety.
STATEMENT REGARDING FEDERALLY SPONSORED RESEARCH OR
DEVELOPMENT
[0002] None
FIELD OF THE INVENTION
[0003] A method of producing a polymer latex drag reducer from a miniemulsion.
BACKGROUND OF THE INVENTION
[0004] A drag reducer is a composition capable of substantially reducing friction loss associated with the turbulent flow of a fluid through a conduit. Where fluids are transported over long distances, such as in oil and other hydrocarbon liquid pipelines, these friction losses result in inefficiencies that increase equipment and operations costs. Ultra-high molecular weight polymers are known to function well as drag reducers, particularly in hydrocarbon liquids. In general, drag reduction depends in part upon the molecular weight of the polymer additive and its ability to dissolve in the hydrocarbon under turbulent flow. Effective drag-reducing polymers typically have molecular weights in excess of five million.
[0005] In the past, it has been proposed that drag reducers comprising polymeric latex emulsions can be used to reduce friction loss associated with turbulent fluid flow througlLa^coiiduit. The use ofLpoIy eric 1 atejLemulsioi^d ag^educejs^as^mQst commonly been proposed for application to the flow of hydrocarbon streams (e.g., crude oil, gasoline, diesel fuel, etc.) through pipelines. In order to be most effective, the drag reducer must be dissolved in the hydrocarbon stream. [0006] Currently, a number of different commercial approaches are being taken to address the problem of preparing, dissolving, transporting and using such drag reducing polymers. A common commercial method is to prepare the polymer in dilute solutions in an inert solvent such as kerosene or other solvating material. This method utilizes a solution of high molecular weight polymer suitable for use as a drag reducing agent when produced by polymerization of alpha olefins in a hydrocarbon solvent. The entire mixture, containing polyolefin, solvent, and catalyst particles is used without separation to form dilute solutions of the polymer in crude oil or finished hydrocarbons.
[0007] Another current commercial approach to drag reduction is to polymerize alpha olefins in bulk form, mill the bulk polymer into small (50μ to 500μ) particles, and then suspend the particles in an aqueous or other (non-solvent) liquid medium. This method allows for much higher levels of active drag reducing polymer in the final product (up to about 25%).
[0008] Yet another method is to polymerize monomers with slight water solubility using emulsion polymerization. This method has the advantage that suspensions containing high levels of active drag reduction polymer (up to 45%) can be prepared. Unfortunately, the types of monomers that can be used in emulsion polymerization are not always the best choices for making drag reducing polymers for use in hydrocarbon fluids (crude oil, gasoline, and diesel fuel).
[0009] The use of miniemulsion polymerization techniques for the production of drag recuing polymer prepared with very water insoluble monomers solves the problem of using the best, water insoluble monomers for the production of drag reducers for use in hydrocarbon liquids.
SUMMARY OF THE INVENTION
[0010] A method of producing a polymer latex drag reducer. The method begins by forming an aqueous solution comprising a surfactant, a buffer and water. The method then forms an organic solution comprising a monomer and a co-stabilizer. The aqueous solution and the organic solution are mixed to form an emulsion. The emulsion is then subjected to a high shear device to produce a miniemulsion, wherein the monomers are broken into small droplets followed by polymerizing the miniemulsion with the addition of an initiator, wherein a nucleation occurs in the small monomer droplets. DETAILED DESCRIPTION OF THE INVENTION
[0011] The present method provides a method to produce a polymer latex drag reducer. The method begins with forming an aqueous solution with a surfactant, a buffer and water in addition to forming an organic solution from a monomer and a co-stabilizer. The aqueous solution and the organic solution are mixed to form an emulsion. The emulsion is then subjected to a sonifier to produce a miniemulsion, wherein the monomers are broken into small droplets. The miniemulsion is then polymerized with the addition of an initiator, wherein the nucleation occurs in the small droplets. The initiator can be either water soluble or oil soluble. The initiator can also be produced by mixing an oxidizer and a reducer or even, a secondary buffer, an oxidizer and a reducer. The polymerization process produces a polymer latex drag reducer.
[0012] There are many benefits that can be attributed to using a miniemulsion to produce a drag reducing product. One benefit is the enhanced ability to mix water insoluble monomers together. Since nucleation occurs in small monomer droplets it is possible for the monomers to be more thoroughly mixed together. A second benefit is increased drag reducing properties. The drag reducing properties can improve 5, 10, 15, 20, 25, 30 35, 40, or even 50% by using the miniemulsion process. The drag reducing properties of the polymer do not affect the viscosity of the crude oil, more specifically heavy crude oil that it is placed into. Instead the drag reducing polymers are able to break up the turbulent flow in the pipelines that the heavy crude oil flows in, thereby improving the flow of the oil in the pipeline. Another benefit that miniemulsion polymerization provide is that water insoluble monomer do not need to transfer from monomer droplets to micelles to start polymerization as in conventional emulsion polymerization. The step of monomer diffusion is eliminated.
[0013] Suitable examples of heavy crude oils include, but are not limited to, Merey heavy crude, Petrozuata heavy crude, Corocoro heavy crude, Albian heavy crude, Bow River heavy crude, Maya heavy crude, and San Joaquin Valley heavy crude. Additionally, the crude oil can be a blend of heavy crude oil with lighter hydrocarbons or diluents. Suitable examples of blended crude oils include, but are not limited to, Western Canadian Select and Marlim Blend. [0014] The aqueous solution contains a surfactant, a buffer and water which are stirred together. The resultant homogeneous aqueous solution can have the following properties.
Figure imgf000005_0001
[0015] The surfactant used can include at least one high HLB anionic or nonionic surfactant. The term "HLB number" refers to the hydrophile-lipophile balance of a surfactant in an emulsion. The HLB number is determined by the methods described by W.C. Griffin in J Soc. Cosmet. Chem., 1, 311 (1949) and J Soc. Cosmet. Chem., 5, 249 (1954), which are incorporated herein by reference. As used herein, the term "high HLB" shall denote an HLB number of 7 or more. The HLB number of surfactants for use with forming the reaction mixture can be at least about 8, at least about 10, or at least 12.
[0016] Exemplary high HLB anionic surfactants include, but are not limited to, high HLB alkyl sulfates, alkyl ether sulfates, dialkyl sulfosuccinates, alkyl phosphates, alkyl aryl sulfonates, and sarcosinates. Suitable examples of commercially available high HLB anionic surfactants include, but are not limited to, sodium lauryl sulfate (available as RHODAPON LSB from Rhodia Incorporated, Cranbury, NJ), dioctyl sodium sulfosuccinate (available as AEROSOL OT from Cytec Industries, Inc., West Paterson, NJ), 2-ethylhexyl polyphosphate sodium salt (available from Jarchem Industries Inc., Newark, NJ), sodium dodecylbenzene sulfonate (available as NORFOX 40 from Norman, Fox & Co., Vernon, CA), and sodium lauroylsarcosinic (available as HAMPOSYL L-30 from Hampshire Chemical Corp., Lexington, MA).
[0017] Exemplary high HLB nonionic surfactants include, but are not limited to, high HLB sorbitan esters, PEG fatty acid esters, ethoxylated glycerine esters, ethoxylated fatty amines, ethoxylated sorbitan esters, block ethylene oxide/propylene oxide surfactants, alcohol/fatty acid esters, ethoxylated alcohols, ethoxylated fatty acids, alkoxylated castor oils, glycerine esters, linear alcohol ethoxylates, and alkyl phenol ethoxylates. Suitable examples of commercially available high HLB nonionic surfactants include, but are not limited to, nonylphenoxy and octylphenoxy poly(ethyleneoxy) ethanols (available as the IGEPAL CA and CO series, respectively from Rhodia, Cranbury, NJ), C8 to CI 8 ethoxylated primary alcohols (such as RHODASURF LA-9 from Rhodia Inc., Cranbury, NJ), CI 1 to CI 5 secondary-alcohol ethoxylates (available as the TERGITOL 15-S series, including 15-S-7, 15-S-9, 15-S-12, from Dow Chemical Company, Midland, MI), polyoxyethylene sorbitan fatty acid esters (available as the TWEEN series of surfactants from Uniquema, Wilmington, DE), polyethylene oxide (25) oleyl ether (available as SIPONIC Y-500-70 from Americal Alcolac Chemical Co., Baltimore, MD), alkylaryl polyether alcohols (available as the TRITON X series, including X-100, X-165, X-305, and X-405, from Dow Chemical Company, Midland, MI).
[0018] The buffer can comprise any known buffer that is compatible with the initiation system such as, for example, carbonate, phosphate, and/or borate buffers. Specific buffers that can be used include potassium dihydrogen phosphate and dipotassium hydrogen phosphate.
[0019] The organic solution contains a monomer and a co-stabilizer which are stirred together. The resultant homogeneous organic solution have the following properties costabilizer are totally dissolved in the monomer
Figure imgf000006_0002
[0020] In one embodiment of the present invention, the drag reducing polymer can comprise a plurality of repeating units of the residues of one or more of the monomers selected from the group consisting of:
(A)
Figure imgf000006_0001
[0021] wherein Ri is H or a C1-C10 alkyl radical, and R2 is H, a C1-C30 alkyl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, a C6-C20 substituted or unsubstituted aryl radical, an aryl-substituted C1-C10 alkyl radical, a -(CH2CH20)X-RA or -(CH2CH(CH3)0)X-RA radical wherein x is in the range of from 1 to 50 and RA is H, a C1-C30 alkyl radical, or a C6-C30 alkylaryl radical;
(B)
R3-arene-R4
[0022] wherein arene is a phenyl, naphthyl, anthracenyl, or phenanthrenyl, R3 is CH=CH2 or CH3-C=CH2, and R4 is H, a C1-C30 alkyl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, CI, S03, ORB, or COORc, wherein RB is H, a C1-C30 alkyl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, a C6-C20 substituted or unsubstituted aryl radical, or an aryl-substituted CI -CIO alkyl radical, and wherein Rc is H, a C1-C30 alkyl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, a C6-C20 substituted or unsubstituted aryl radical, or an aryl- substituted CI -CIO alkyl radical;
(C)
Figure imgf000007_0001
[0023] wherein R5 is H, a C1-C30 alkyl radical, or a C6-C20 substituted or unsubstituted aryl radical;
CD)
Figure imgf000007_0002
[0024] wherein R6 is H, a C1-C30 alkyl radical, or a C6-C20 substituted or unsubstituted aryl radical;
(E)
Figure imgf000008_0001
[0025] wherein R7 is H or a CI -CI 8 alkyl radical, and R8 is H, a C1-C18 alkyl radical, or CI;
Figure imgf000008_0002
[0026] wherein R9 and R10 are independently H, a C1-C30 alkyl radical, a C6-C20 substituted or unsubstituted aryl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, or heterocyclic radicals;
Figure imgf000008_0003
[0027] wherein Rn and R12 are independently H, a C1-C30 alkyl radical, a C6-C20 substituted or unsubstituted aryl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, or heterocyclic radicals;
(H)
Figure imgf000008_0004
[0028] wherein R13 and R14 are independently H, a C1-C30 alkyl radical, a C6-C20 substituted or unsubstituted aryl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, or heterocyclic radicals;
(I)
Figure imgf000009_0001
[0029] wherein R15 is H, a C1-C30 alkyl radical, a C6-C20 substituted or unsubstituted aryl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, or heterocyclic radicals;
(J)
Figure imgf000009_0002
[0030] wherein R16 is H, a C1-C30 alkyl radical, or a C6-C20 aryl radical;
(L)
Figure imgf000010_0001
(M)
Figure imgf000010_0002
(N)
Figure imgf000010_0003
(O)
Figure imgf000010_0004
[0031] wherein R17 and R18 are independently H, a C1-C30 alkyl radical, a C6-C20 substituted or unsubstituted aryl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, or heterocyclic radicals;
(P)
Figure imgf000011_0001
[0032] wherein R19 and R20 are independently H, a C1-C30 alkyl radical, a C6-C20 substituted or unsubstituted aryl radical, a C5-C30 substituted or unsubstituted cycloalkyl radical, or heterocyclic radicals.
[0033] In one embodiment of the present invention, the drag reducing polymer can comprise repeating units of the residues of C4-C20 alkyl, C6-C20 substituted or unsubstituted aryl, or aryl-substituted CI -CIO alkyl ester derivatives of methacrylic acid or acrylic acid. In another embodiment, the drag reducing polymer can be a copolymer comprising repeating units of the residues of 2-ethylhexyl methacrylate and the residues of at least one other monomer. In yet another embodiment, the drag reducing polymer can be a copolymer comprising repeating units of the residues of 2-ethylhexyl methacrylate monomers and butyl acrylate monomers. In still another embodiment, the drag reducing polymer can be a homopolymer comprising repeating units of the residues of 2-ethylhexyl methacrylate.
[0034] In one embodiment of the present invention, the drag reducing polymer can comprise the residues of at least one monomer having a heteroatom. As stated above, the term "heteroatom" includes any atom that is not a carbon or hydrogen atom. Specific examples of heteroatoms include, but are not limited to, oxygen, nitrogen, sulfur, phosphorous, and/or chlorine atoms. In one embodiment, the drag reducing polymer can comprise at least about 10 percent, at least about 25 percent, or at least 50 percent of the residues of monomers having at least one heteroatom. Additionally, the heteroatom can have a partial charge. As used herein, the term "partial charge" is defined as an electric charge, either positive or negative, having a value of less than 1.
[0035] The co-stabilizer can be any highly water insoluble small molecules that are presently known in the art. Examples of co-stabilizers that can be used include fatty alcohols (C12-C2o), hexadecane, isohexadecane and hydrophobic oligomers such as styrene. Some of the most widely used co-stabilizers include cetyl alcohol and hexadecane. The co-stabilizer is required in to effectively stabilize the high shearing that is required to form the miniemulsion. Due to the high solubility of co-stabilizer in water insoluble monomer, so-stabilizer prevents monomer particles from coagulation and stabilizes the monomer particles after shearing.
[0036] The organic solution and aqueous solution are then mixed together to form an emulsion. The emulsion is then subjected to a high-shear device. High shear devices can be any commonly known device in the art such as sonifier, microfluidizers, static mixer or homogenizers. The high shear devices should be able to produce submicron dispersions of monomer droplets whose droplet sizes can range from 20 to 1000 nm or even 50 to 500 nm. By reducing the droplet sizes the primary loci of nucleation would occur in the droplets rather than the micelles. This increases the possibility that polymerization of the hydrophobic monomers would take place in the monomer droplets, which in turn allows the miniemulsion to prepare oil-soluble polymers as drag reducer products.
[0037] The miniemulsion is then polymerized with the addition of an initiator. The initiator can comprise of only an oxidizer and a reducer or it can contain a secondary buffer, an oxidizer and a reducer. The initiator can also be aqueous.
Figure imgf000012_0001
[0038] The secondary buffer can be any commonly used buffer. Ideal buffers are those used described above that were used in production of the homogeneous aqueous solution.
[0039] The oxidizer solution can be any commonly used oxidizer solution. In one embodiment the oxidizing solution are persulfates, peroxides or azonitrile initiators. Possible persulfate oxidizers that can be used include ammonium persulfate, sodium persulfate and potassium persulfate. Possible peroxides that can be used include hydrogen peroxide and organic peroxides. [0040] The reducer is selected to reduce the oxidizer. In one embodiment the reducer is a salt. The reducer can be sulfites such as bisulfite or hydrosulfite, acids such as ascorbic acid or erythrobic acid, iron based reducers or even sodium formaldehyde sulfoxylate. One example of a reducer that is frequently used is ferrous ammonium sulfate, hexahydrate, Fe(NH4)2(S04)2-6H20).
[0041] One optional component is a secondary surfactant. The secondary surfactant can be any commonly used surfactant. Ideal surfactants are those used described above that were used in production of the homogeneous aqueous solution.
Examples
[0042] Calculation of drag reduction properties. Pipeline field testing was performed with various diameter pipelines, and various crude oils. For each of the tests the percent drag reduction (%DR) was determined by measuring the pressure drop in the segment of pipe being tested prior to addition of drag reducing agent (APbase) and measuring the pressure drop in the segment of pipe being tested after addition of drag reducing agent (AP-'-'treated). The percent drag reduction was then determined according to the following formula:
%DR = ((APbase -■- APtreated) / APbase) x 100%
Example 1
[0043] Batch Polymerization - 300-mL Reactor
[0044] Pol mer reactants
Figure imgf000013_0001
[0045] Oxidizer solution
Figure imgf000014_0001
[0046] T e emuls on was done in a reactor for four hours under nitrogen at a temperature set around 2.0°C. The agitator was set at 400 rpm. A catalyst solution was then added to the emulsion when the temperature was 5 °C.
[0047] Catalyst (Iron) solution:
Figure imgf000014_0002
[0048] The catalyst solution was injected over 21 hours at 188 μΙΤητ with a total volume injected of 3.18 mL.
[0049] The final product weight of the polymer was 200.92 grams with the following characteristics.
Figure imgf000014_0003
Figure imgf000014_0004
[0050] The drag reduction property of the polymer was tested at 28.8% at 2 ppm.
Example 2
[0051] Batch Polymerization - 300-mL Reactor
[0052] Aqueous solution
Figure imgf000014_0005
Polystep B-5 4.32 0.02 4.33
Tergitol 15-S-7 8.00 0.02 8.00
Phosphate buffer (87.0 g potassium dihydrogen
phosphate 68.0 g potassium hydrogen phosphate in 2.60 0.02 2.61 1000 mL DI water)
[0053] Organic solution
Recipe
Component ± Actual
(grams)
Ethylhexyl methacrylate 80.00 0.50 80.05
Cetyl alcohol 3.20 0.02 3.21
[0054] The aqueous solution and the organic solution where then mixed together and subjected to a high shear device. The jacket temperature set to around 2.0°C and the agitator at 400 rpm. The emulsion was sheared under nitrogen for 1 hour.
[0055] Oxidizer solution
Figure imgf000015_0001
[0056] The oxidizer solution was injected into the miniemulsion at 0.10 mL/minute over 40 minutes while still under nitrogen.
[0057] Catalyst (Iron) solution:
Figure imgf000015_0002
[0058] The catalyst (iron) solution was injected into the miniemulsion when the miniemulsion was 5°C. The syringe pump was programmed to deliver at 188 μΙΤΙιτ for 21 hours a total of 2.91 mL of the catalyst.
The final product weight of the polymer was 187.52 grams with the following
Figure imgf000016_0001
Figure imgf000016_0002
[0060] The drag reduction property of the polymer was tested at 36.4% at 2 ppm.
Example 3
[0061] Batch Polymerization - 300-mL Reactor
[0062] Polymer reactants
Figure imgf000016_0003
[0063] Oxidizer solution
Figure imgf000016_0004
Deionized Water 40.00 0.05 40.00
[0064] The reactor was purged for four hours under nitrogen at a temperature set around 5.0°C before starting polymerization. The agitator was set at 400 rpm. A catalyst solution was then added to the emulsion when the temperature was 5 °C.
[0065] Catalyst (Iron) solution:
Figure imgf000017_0001
[0066] The catalyst solution was injected over 24 hours at 330 μΙ τ with a total volume injected of 4.92mL.
The final product weight of the polymer was 197.97 grams with the following
Figure imgf000017_0002
Figure imgf000017_0003
[0068] The drag reduction property of the polymer was tested at 0% at 2 ppm.
Example 4
[0069] Batch Polymerization - 300-mL Reactor
[0070] Aqueous solution Recipe
Component ± Actual
(grams)
Deionized Water 97.90 0.50 97.90
Polystep B-5 4.30 0.02 4.30
Phosphate buffer (87.0 g potassium dihydrogen phosphate
2.60 0.02 2.61 68.0 g potassium hydrogen phosphate in 1000 mL DI water)
[0071] Organic solution
Figure imgf000018_0001
[0072] The aqueous solution and the organic solution where then mixed together for 10 minutes and subjected to a high shear device. The high shear device used was a Branson sonifier at the output power setting of eight and a duty cycle of 50%. After sonification the solution was cooled down to around 5.0°C placed under nitrogen for 1 hour
[0073] Oxidizer solution
Figure imgf000018_0002
[0074] The oxidizer solution was injected into the miniemulsion at 0.10 mL/minute over 40 minutes while still under nitrogen.
[0075] Catalyst (Iron) solution:
Figure imgf000018_0003
[0076] The catalyst (iron) solution was injected into the miniemulsion when the miniemulsion was 5°C. The syringe pump was programmed to deliver at 330 μΐ,/hr for 24 hours a total of 7.71 mL of the catalyst.
[0077] The final product weight of the polymer was 196.60 grams with the following characteristics.
Figure imgf000019_0001
Figure imgf000019_0002
[0078] The drag reduction property of the polymer was tested at 19.25% at 2 ppm.
[0079] Accordingly, the scope of protection is not limited by the description set out above, but is only limited by the claims which follow, that scope including all equivalents of the subject matter of the claims. Each and every claim is incorporated into the specification as an embodiment of the present invention. Thus the claims are a further description and are an addition to the preferred embodiments of the present invention. The discussion of any reference is not an admission that it is prior art to the present invention, especially any reference that may have a publication date after the priority date of this application.

Claims

1. A method comprising:
forming an aqueous solution comprising a surfactant, a buffer and water;
forming an organic solution comprising a monomer and a co-stabilizer;
mixing the aqueous solution and the organic solution to form an emulsion;
subjecting the emulsion to a high shear device to produce a miniemulsion, wherein the monomers are broken into small droplets; and
polymerizing the miniemulsion with the addition of an initiator, wherein a nucleation occurs in the small monomer droplets;
wherein the polymerization produces a polymer latex drag reducer.
2. The method of claim 1, wherein the co-stabilizer is a water insoluble small
molecule.
3. The method of claim 1, wherein the co-stabilizer are selected from the group consisting of cetyl alcohol, hexadecane and combinations thereof.
4. The method of claim 1, wherein the high shear device is used to produce droplets ranging from 50-500 nm.
5. The method of claim 1, wherein the high shear device comprises a sonifier, a microfluidizer, a static mixer or a homogenizer.
6. The method of claim 1 , wherein the drag reduction properties are improved by at least 20% compared to drag reducers not produced through a miniemulsion.
7. The method of claim 1 , wherein the initiator is aqueous.
8. The method of claim 1, wherein the initiator comprises an oxidizer and a reducer. The method of claim 1 , wherein the initiator comprises a secondary buffer, an oxidizer and a reducer.
The method of claim 1, wherein the aqueous solution and the organic solution homogeneous.
PCT/US2011/022602 2010-01-28 2011-01-26 Miniemulsion polymerization to prepare drag reducers WO2011094333A1 (en)

Priority Applications (14)

Application Number Priority Date Filing Date Title
PL11737595T PL2528951T3 (en) 2010-01-28 2011-01-26 Miniemulsion polymerization to prepare drag reducers
BR112012019704-5A BR112012019704B1 (en) 2010-01-28 2011-01-26 METHOD OF PRODUCTION OF A LATEX TRAIL REDUCING POLYMER
BR122020003462-9A BR122020003462B1 (en) 2010-01-28 2011-01-26 METHOD FOR FORMING A LATEX DRAG REDUCING POLYMER
PL17209731T PL3323835T3 (en) 2010-01-28 2011-01-26 Miniemulsion polymerization to prepare drag reducers
DK11737595.6T DK2528951T3 (en) 2010-01-28 2011-01-26 MINI MULSION POLYMERIZATION FOR THE PREPARATION OF RESISTANT REDUCTIONS
IN5189DEN2012 IN2012DN05189A (en) 2010-01-28 2011-01-26
NO11737595A NO2528951T3 (en) 2010-01-28 2011-01-26
CA2788092A CA2788092C (en) 2010-01-28 2011-01-26 Miniemulsion polymerization to prepare drag reducers
EA201290707A EA025537B1 (en) 2010-01-28 2011-01-26 Method of producing a drag reducer
ES11737595.6T ES2667330T3 (en) 2010-01-28 2011-01-26 Mini-emulsion polymerization to prepare feed resistance reducers
CN201180007467.3A CN102803301B (en) 2010-01-28 2011-01-26 Miniemulsion polymerization to prepare drag reducers
MX2012008779A MX339756B (en) 2010-01-28 2011-01-26 Miniemulsion polymerization to prepare drag reducers.
EP17209731.3A EP3323835B1 (en) 2010-01-28 2011-01-26 Miniemulsion polymerization to prepare drag reducers
EP11737595.6A EP2528951B1 (en) 2010-01-28 2011-01-26 Miniemulsion polymerization to prepare drag reducers

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US29920010P 2010-01-28 2010-01-28
US61/299,200 2010-01-28

Publications (1)

Publication Number Publication Date
WO2011094333A1 true WO2011094333A1 (en) 2011-08-04

Family

ID=44309443

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2011/022602 WO2011094333A1 (en) 2010-01-28 2011-01-26 Miniemulsion polymerization to prepare drag reducers

Country Status (18)

Country Link
US (1) US9951151B2 (en)
EP (2) EP3323835B1 (en)
CN (1) CN102803301B (en)
AR (1) AR080045A1 (en)
BR (2) BR122020003462B1 (en)
CA (1) CA2788092C (en)
DK (2) DK3323835T3 (en)
EA (1) EA025537B1 (en)
EC (1) ECSP12012063A (en)
ES (2) ES2764671T3 (en)
HU (2) HUE048380T2 (en)
IN (1) IN2012DN05189A (en)
MX (1) MX339756B (en)
NO (1) NO2528951T3 (en)
PE (1) PE20110689A1 (en)
PL (2) PL2528951T3 (en)
TR (1) TR201806914T4 (en)
WO (1) WO2011094333A1 (en)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AU2015374408B2 (en) * 2014-12-31 2020-01-02 Kemira Oyj Emulsions, treatment fluids and methods for treating subterranean formations
US20180312693A1 (en) * 2015-10-28 2018-11-01 Umg Abs, Ltd. Graft copolymer, crosslinked particles, graft crosslinked particles, rubbery polymer, and thermoplastic resin composition using same
MX2020002740A (en) 2017-09-11 2020-07-21 Basf Corp Aqueous polymer dispersions, a method for their preparation and the use thereof as pour-point depressants for crude oil, petroleum, and petroleum products.
US11767487B2 (en) 2020-07-13 2023-09-26 Baker Hughes Oilfield Operations Llc Inverting aids for latex-based drag reducing agents

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6369135B1 (en) * 1995-08-15 2002-04-09 Georgia Tech Research Corporation Water-borne alkyd coatings by miniemulsion polymerization
WO2005090851A1 (en) 2004-03-17 2005-09-29 Baker Hughes Incorporated Polymeric nanoemulsion as drag reducer for multiphase flow
US20060148928A1 (en) 2004-12-30 2006-07-06 Harris William F Modified latex drag reducer and processes therefor and therewith
WO2008083991A1 (en) * 2007-01-12 2008-07-17 Cytec Surface Specialties, S.A. Polymer composition and process

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4070323A (en) * 1976-03-26 1978-01-24 Vanderhoff John W Aqueous polyurethane emulsions
US4177177A (en) * 1976-03-26 1979-12-04 El Aasser Mohamed S Polymer emulsification process
US5686518A (en) * 1993-10-12 1997-11-11 Georgia Tech Miniemulsion polymerization process using polymeric co-surfactant
US5639841A (en) 1995-02-28 1997-06-17 Union Carbide Chemicals & Plastics Technology Corporation Polymers containing macromonomer mixtures
DE19750159A1 (en) * 1997-11-12 1999-05-20 Basf Ag Production of aqueous polymer dispersion
US6126872A (en) * 1998-01-27 2000-10-03 Baker Hughes Incorporated Microencapsulated drag reducing agents
US20070249764A1 (en) * 2006-04-21 2007-10-25 Glenn Lewis Shoaf Aqueous coatings with optical brighteners
DE102007014916A1 (en) * 2007-03-26 2008-10-02 Evonik Degussa Gmbh Method and apparatus for high pressure dispersion
DE102007058713A1 (en) * 2007-12-06 2009-06-10 Evonik Goldschmidt Gmbh Silicone (meth) acrylate particles, process for their preparation and their use

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6369135B1 (en) * 1995-08-15 2002-04-09 Georgia Tech Research Corporation Water-borne alkyd coatings by miniemulsion polymerization
WO2005090851A1 (en) 2004-03-17 2005-09-29 Baker Hughes Incorporated Polymeric nanoemulsion as drag reducer for multiphase flow
US20060148928A1 (en) 2004-12-30 2006-07-06 Harris William F Modified latex drag reducer and processes therefor and therewith
WO2008083991A1 (en) * 2007-01-12 2008-07-17 Cytec Surface Specialties, S.A. Polymer composition and process

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of EP2528951A4 *

Also Published As

Publication number Publication date
EP2528951A1 (en) 2012-12-05
CN102803301A (en) 2012-11-28
EP3323835B1 (en) 2019-11-13
PL3323835T3 (en) 2020-05-18
CN102803301B (en) 2015-06-10
PL2528951T3 (en) 2018-07-31
BR112012019704A8 (en) 2020-08-04
CA2788092C (en) 2018-08-07
MX2012008779A (en) 2012-09-07
EA025537B1 (en) 2017-01-30
MX339756B (en) 2016-06-08
PE20110689A1 (en) 2011-10-20
DK2528951T3 (en) 2018-05-28
BR122020003462B1 (en) 2021-05-04
ES2667330T3 (en) 2018-05-10
EP2528951B1 (en) 2018-03-21
EP3323835A1 (en) 2018-05-23
BR112012019704A2 (en) 2018-05-29
IN2012DN05189A (en) 2015-10-23
TR201806914T4 (en) 2018-06-21
HUE038360T2 (en) 2018-10-29
US20110184121A1 (en) 2011-07-28
AR080045A1 (en) 2012-03-07
US9951151B2 (en) 2018-04-24
HUE048380T2 (en) 2020-07-28
NO2528951T3 (en) 2018-08-18
EA201290707A1 (en) 2013-01-30
EP2528951A4 (en) 2013-07-31
CA2788092A1 (en) 2011-08-04
BR112012019704B1 (en) 2020-09-24
ES2764671T3 (en) 2020-06-04
ECSP12012063A (en) 2012-10-30
DK3323835T3 (en) 2020-01-27

Similar Documents

Publication Publication Date Title
US8022118B2 (en) Drag reduction of asphaltenic crude oils
DK2195377T3 (en) HYBRID RESISTANT REDUCING COMPOSITIONS WITH HIGH POLYMER CONTENT
US20210261707A1 (en) Core-shell flow improver
US20220099255A1 (en) Drag reduction of asphaltenic crude oils
EP2528951B1 (en) Miniemulsion polymerization to prepare drag reducers
US7884144B2 (en) Hydrate inhibited latex flow improver
US8656950B2 (en) Drag reduction of asphaltenic crude oils
US20120004343A1 (en) Drag reduction of asphaltenic crude oils
US20230287255A1 (en) Low glass transition temperature polymer latex drag reducing agent
EP3071645B1 (en) Additives for drag reducing polymers
US9676878B2 (en) Monomer selection to prepare ultra high molecular weight drag reducer polymer

Legal Events

Date Code Title Description
WWE Wipo information: entry into national phase

Ref document number: 201180007467.3

Country of ref document: CN

121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 11737595

Country of ref document: EP

Kind code of ref document: A1

WWE Wipo information: entry into national phase

Ref document number: 5189/DELNP/2012

Country of ref document: IN

WWE Wipo information: entry into national phase

Ref document number: 12105022

Country of ref document: CO

ENP Entry into the national phase

Ref document number: 2788092

Country of ref document: CA

WWE Wipo information: entry into national phase

Ref document number: MX/A/2012/008779

Country of ref document: MX

Ref document number: 2011737595

Country of ref document: EP

NENP Non-entry into the national phase

Ref country code: DE

WWE Wipo information: entry into national phase

Ref document number: 201290707

Country of ref document: EA

REG Reference to national code

Ref country code: BR

Ref legal event code: B01A

Ref document number: 112012019704

Country of ref document: BR

ENP Entry into the national phase

Ref document number: 112012019704

Country of ref document: BR

Kind code of ref document: A2

Effective date: 20120730