WO2011110518A1 - Procédé de fabrication de polymères styrène expansibles - Google Patents

Procédé de fabrication de polymères styrène expansibles Download PDF

Info

Publication number
WO2011110518A1
WO2011110518A1 PCT/EP2011/053374 EP2011053374W WO2011110518A1 WO 2011110518 A1 WO2011110518 A1 WO 2011110518A1 EP 2011053374 W EP2011053374 W EP 2011053374W WO 2011110518 A1 WO2011110518 A1 WO 2011110518A1
Authority
WO
WIPO (PCT)
Prior art keywords
styrene
conversion
addition
particle size
stabilizer
Prior art date
Application number
PCT/EP2011/053374
Other languages
German (de)
English (en)
Inventor
Wolfgang Ferstl
Jun Gao
Klaus Hahn
Pascal Hesse
Jan Holoch
Klaus-Dieter Hungenberg
Wolfram Husemann
Renata Jovanovic
Wolfgang Kasten
Olaf Kriha
Eckhard Neufeld
Michel Pepers
Birgit Reinhard
Bernhard Schmied
Rudolf SÜTTINGER
Ping Zhang
Original Assignee
Basf Se
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
Application filed by Basf Se filed Critical Basf Se
Priority to KR1020127023750A priority Critical patent/KR20130048198A/ko
Priority to CN201180013393.4A priority patent/CN102791781B/zh
Priority to MX2012009463A priority patent/MX2012009463A/es
Priority to BR112012021646A priority patent/BR112012021646A2/pt
Priority to EP11708023A priority patent/EP2545107A1/fr
Publication of WO2011110518A1 publication Critical patent/WO2011110518A1/fr

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
    • C08F12/00—Homopolymers and copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by an aromatic carbocyclic ring
    • C08F12/02—Monomers containing only one unsaturated aliphatic radical
    • C08F12/04—Monomers containing only one unsaturated aliphatic radical containing one ring
    • C08F12/06—Hydrocarbons
    • C08F12/08—Styrene
    • 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
    • C08F2/18—Suspension polymerisation
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J9/00—Working-up of macromolecular substances to porous or cellular articles or materials; After-treatment thereof
    • C08J9/04—Working-up of macromolecular substances to porous or cellular articles or materials; After-treatment thereof using blowing gases generated by a previously added blowing agent
    • C08J9/12—Working-up of macromolecular substances to porous or cellular articles or materials; After-treatment thereof using blowing gases generated by a previously added blowing agent by a physical blowing agent
    • C08J9/14—Working-up of macromolecular substances to porous or cellular articles or materials; After-treatment thereof using blowing gases generated by a previously added blowing agent by a physical blowing agent organic
    • C08J9/141—Hydrocarbons
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J9/00—Working-up of macromolecular substances to porous or cellular articles or materials; After-treatment thereof
    • C08J9/16—Making expandable particles
    • C08J9/20—Making expandable particles by suspension polymerisation in the presence of the blowing agent
    • 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
    • C08F212/00—Copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by an aromatic carbocyclic ring
    • C08F212/02—Monomers containing only one unsaturated aliphatic radical
    • C08F212/04—Monomers containing only one unsaturated aliphatic radical containing one ring
    • C08F212/06—Hydrocarbons
    • C08F212/12—Monomers containing a branched unsaturated aliphatic radical or a ring substituted by an alkyl radical
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J2325/00—Characterised by the use of homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by an aromatic carbocyclic ring; Derivatives of such polymers
    • C08J2325/02—Homopolymers or copolymers of hydrocarbons
    • C08J2325/04—Homopolymers or copolymers of styrene
    • C08J2325/06—Polystyrene

Definitions

  • the invention relates to a process for the preparation of expandable styrene polymers having a narrow bead size distribution with high specific reactor yield by polymerization of the monomers in aqueous suspension in the presence of a volatile blowing agent.
  • Foams based on styrene polymers have gained great technical importance as thermal insulation and packaging material. They are generally produced on an industrial scale by first producing expandable styrene polymers by suspension polymerization of styrene in the presence of a blowing agent, foaming them by heating to give foam particles and then sealing them in molds to form parts.
  • suspension polymerization takes place here in the presence of suspension stabilizers and customary styrene-soluble polymerization initiators.
  • molecular colloids such as polyvinyl alcohol (PVA) and polyvinylpyrrolidone (PVP)
  • sparingly soluble salts such as Ca 3 (PO 4 ) 2 (so-called Pickering salts) are usually used as suspension stabilizers in combination with alkali metal or alkaline earth alkyl sulfonates.
  • Pickering salts are usually used as suspension stabilizers in combination with alkali metal or alkaline earth alkyl sulfonates.
  • a suspension stabilizer system for example, a mixture of magnesium pyrophosphate, sodium alkyl sulfonates and sodium acrylate is used.
  • the disadvantage of the method is that a comparatively wide bead size distribution is obtained. This has the consequence that the desired bead fractions can not be produced without simultaneous formation of so-called edge fractions.
  • a process for the preparation of expandable styrene polymers having a relatively narrow bead size distribution by polymerization of styrene in aqueous suspension is known from EP-A 304 582.
  • the stabilizer system used is a mixture of an organic protective colloid, for example polyvinylpyrrolidone or hydroxyethylcellulose, and an inorganic stabilizer, for example a calcium or barium phosphate or sulfate, as stabilizer system.
  • an organic protective colloid for example polyvinylpyrrolidone or hydroxyethylcellulose
  • an inorganic stabilizer for example a calcium or barium phosphate or sulfate
  • the measurement of the conversion of monomers can be carried out, for example, using Raman spectroscopy. This is described, for example, in J.C. Santos et al., On-line Monitoring of Suspension Polymerization Reactions using a Raman Spectroscopy, Ind. Eng. Chem. Res., 2004, 43, pages 7282-7289. It is also known from EP-B 1 442 284 to use Raman spectroscopy to determine the progress of the reaction of graft polymerizations. The use of Raman spectroscopy serves to monitor a process. Influence on the bead size distribution is not taken by Raman spectroscopy.
  • the object of the present invention is to provide an improved process for the preparation of expandable styrene polymers in which the bead size distribution of the expandable styrene polymers has only slight fluctuations with a well-adjustable average diameter and which permits a high specific reactor yield.
  • the object is achieved by a process for the preparation of expandable styrene polymers, which comprises the following steps: (a) adding a suspension stabilizer-containing aqueous phase and a styrene and initiator-containing organic phase to a reactor,
  • bead size distributions can be achieved with fewer fluctuations than in the known processes, in particular also compared to the processes in which the dosage is time-based.
  • Impurities in this context are, in particular, inhibiting impurities, for example phenols.
  • a further advantage of the sales-based addition of the individual components is that coagulation of the organic phase in the suspension becomes less likely because process irregularities are compensated.
  • incipient coagulations are detected and it can be taken in time countermeasures, for example, a metered addition of the stabilizer to stabilize the bead size distribution.
  • the addition of the suspension stabilizer-containing aqueous phase and the styrene and initiator-containing organic phase in a reactor over a period of 5 to 60 minutes. Furthermore, it is preferred that the start of dosing of the styrene and initiator-containing organic phase begin after the dosing of the suspension stabilizer-containing aqueous phase has started, with a short time lag. This ensures that the filling of the reactor begins in excess water.
  • the parallel dosing of both phases shortens the reactor cycle time by the time of the dosing of the aqueous phase and less the time offset.
  • the Dosing of the styrene and initiator-containing organic phase 1 to 20 minutes, particularly preferably 2 to 5 minutes after the beginning of the metering of the aqueous phase and lasts 1 to 20 minutes, more preferably 2 to 5 minutes, after completion of the metering of the aqueous phase.
  • the pure water content of the suspension phase-containing aqueous phase can either be preheated in a feed vessel and / or heated during the filling.
  • a higher temperature is reached after the end of the reactor filling. This shortens the reactor cycle time by the time required to heat the reactors to the now attainable temperature after filling.
  • the reactor contents are preferably brought to an internal temperature in the range from 30 to 90 ° C., particularly preferably in the range from 35 to 75 ° C., until the end of the metering of both phases.
  • the aqueous phase preferably contains magnesium pyrophosphate, tricalcium phosphate and / or magnesium sulfate.
  • the organic phase contains, in addition to the styrene as an initiator, preferably organic peroxides.
  • the volume ratio of the organic phase containing styrene and initiator to the aqueous phase containing the suspension stabilizer is generally 2: 1 to 1: 2, more preferably 1: 6: 1 to 1: 1, 6 and in particular 3: 2 to 1: 1.
  • a hydroxyalkylamine can be added.
  • the addition of the hydroxyalkylamine positively influences the foam structure of moldings made from the styrene polymer.
  • the hydroxyalkylamine is particularly preferably initially charged in the organic phase containing styrene and initiator.
  • hydroxyalkylamines are preferably alkyl-di (2-hydroxyethyl) amines, more preferably Ci 2 / Ci4-alkyl-di (2-hydroxyethyl) amine, which is commercially available under the name Armostat® 400 Akzo, used.
  • the hydroxyalkylamine is usually initially charged or at a temperature of less than 100 ° C, that is, at a conversion of less than 20% added. Preference is given to the hydroxyalkylamine.
  • Styrene polymers in the context of the present invention are polystyrene and copolymers of styrene with other ⁇ , ⁇ -olefinically unsaturated compounds which contain at least 50 parts by weight of styrene in copolymerized form.
  • suitable comonomers are, for example: a-methylstyrene, ring-halogenated styrenes, ring-alkylated styrenes, acrylonitrile, esters of acrylic or methacrylic acid of alcohols having 1 to 8 carbon atoms, N-vinyl compounds, such as Vinylcarbazole or even small amounts of compounds containing two polymerizable double bonds, for example, butadiene, divinylbenzene or butanediol diacrylate.
  • preferred volatile blowing agents are 1 to 10% by weight, preferably 3 to 8% by weight, of a C 3 to C 7 hydrocarbon, for example propane, butane, isobutane, n-pentane, i-pentane, Neopentane and / or hexane used. In principle, however, other volatile substances can be used. Particular preference is given to using n-pentane and i-pentane, usually as a mixture.
  • the polymerization is triggered by conventional styrene-soluble initiators.
  • Suitable initiators are, for example, dibenzoyl peroxide, tert-butyl perbenzoate, dicumyl peroxide, di-tert-butyl peroxide and mixtures thereof, preferably in amounts of from 0.2 to 1% by weight, in particular in amounts of from 0.3 to 0.7% by weight. % based on the monomers.
  • the styrene polymers may also contain conventional additives to other substances which impart certain properties to the expandable products.
  • Can be added for example, flame retardants based on organic bromine or chlorine compounds, for example Trisdibrompropylphosphat, Hexabromcyclododecan, tetrabromobisphenol A derivatives, brominated diphenylethanes, chlorinated paraffin and synergists for flame retardants such as dicumyl and highly decomposable, organic peroxides;
  • antistatic agents, stabilizers, lubricants, fillers and antifoaming substances during Vorschaeu- men for example, zinc stearate, Melaminformalde- hydkondensate or silica and agents for shortening the demolding time during foaming, for example, glycerol esters or hydroxycarboxylic acid esters.
  • the additives can be homogeneously distributed in the particles or present as a surface coating
  • Suitable additives for lowering the thermal conductivity are carbon particles such as carbon black and graphite. Suitable are all customary carbon blacks, with flame black having a particle size of 80 to 120 nm being preferred. Carbon black is preferably used in amounts of from 2 to 10% by weight. However, graphite is particularly well suited, with an average particle size of 0.5 to 200 ⁇ m, preferably of 1 to 25 ⁇ m and in particular of 2 to 20 ⁇ m, a bulk density of 100 to 500 g / l and a specific surface area of 5 to 20 m 2 / g are preferred. It can be used natural graphite or ground synthetic graphite.
  • the graphite particles are present in the styrene polymer in amounts of from 0.1 to 25% by weight, in particular from 0.5 to 8% by weight.
  • the additives can be added in the process according to the invention or subsequently applied to the expandable styrene polymers prepared according to the invention.
  • the suspension polymerization of styrene is known per se. It is described, for example, in the Kunststoff-Handbuch, Vol. V, "Polystyrene", Karl Hanser Verlag, 1969, pages 679-688, wherein in general styrene, optionally together with the abovementioned comonomers, is suspended in water and in the presence of organic or inorganic suspension stabilizers.
  • peripiform, expandable styrene polymers are prepared by polymerization of styrene, optionally together with up to 50% by weight of the abovementioned comonomers, in aqueous suspension, before, during or after the polymerization the blowing agents described above and, if appropriate, conventional additives in effective Quantities are added.
  • the polymerization can also be carried out in the presence of a conventional chain transfer agent which controls the molecular weight.
  • a conventional chain transfer agent which controls the molecular weight.
  • tert-dodecylmercaptan or DMS dimeric ⁇ -methylstyrene
  • the regulator is generally used in an amount of 0.001 to 0.5% by weight based on monomers.
  • diphosphates or phosphates particularly preferably magnesium pyrophosphate or tricalcium phosphate.
  • a mixture of magnesium pyrophosphate, a secondary alkali metal or alkaline earth metal alkylsulfonate and optionally a carboxylate bearing a double bond as suspension stabilizer system.
  • the carboxylate improves the stabilizing ability and prevents deposits on the reactor walls.
  • the product properties such as expandability and electrostatic chargeability are favorably influenced.
  • Magnesium pyrophosphate is generally in a concentration between 0.03 and 2.0 wt .-%, preferably between 0.05 and 1, 0 wt .-% and particularly preferably between 0.1 and 0.5 wt .-% based the aqueous phase used.
  • the magnesium pyrophosphate is preferably prepared immediately prior to the polymerization by combining highly concentrated solutions of pyrophosphate and magnesium ions, wherein the stoichiometric amount of a magnesium salt which is at least necessary for the precipitation of magnesium pyrophosphate is used.
  • the magnesium salt may be in solid form or in aqueous solution.
  • the magnesium pyrophosphate is prepared by combining aqueous solutions of sodium pyrophosphate (Na 4 P 2 O 7 ) and magnesium sulfate (MgS0 4 -7H 2 O).
  • the magnesium salt is added in at least the stoichiometrically required amount, preferably in a stoichiometric amount. It is favorable for the process according to the invention if there is no excess of alkali pyrophosphate.
  • extenders include, for example, sodium dodecyl benzene sulfonate, long chain alkyl sulfonates, vinyl sulfonate, and di-isobutylnaphthalenesulfonate.
  • the extenders used are preferably alkali metal salts of dodecylbenzenesulfonic acid and / or alkali metal salts of a mixture of d 2 - to C 7 -alkylsulfonic acids.
  • a particularly suitable mixture of C 12 - to C 7 -alkyl sulfonates consists predominantly of secondary sodium alkylsulfonates having the mean chain length Ci 5 .
  • Such a mixture is marketed under the name "Mersolat® K30" by Bayer AG
  • the extenders increase the ability of the poorly soluble inorganic compounds to stabilize the suspension
  • the extenders are generally used in amounts of between 0.5 and 15% by weight. -%, preferably in amounts of between 2 and 10 wt .-%, each based on magnesium pyrophosphate used.
  • the desired bead diameter d can be set in a targeted manner over a wide range, for example in the range from 0.5 to 3 mm.
  • the addition of the extender is preferably carried out in the process according to the invention at a conversion of styrene in the range of 20 to 50%.
  • the extender is preferably added in the form of an extender solution. Particularly preferably, the addition of the extender solution takes place at a conversion of styrene in a range from 25 to 45%.
  • the bead size distribution can be particularly preferably influenced by the addition of carbonate and / or bicarbonate.
  • 1 to 1000 ppm, preferably 50 to 500 ppm, based on the aqueous phase, of a water-soluble carbonate and / or bicarbonate are preferably added.
  • Suitable carbonates or bicarbonates are those of sodium, potassium and ammonium. It is advantageous to add the carbonates or bicarbonates in the course of the polymerization at a conversion of styrene in the range of 10 to 40%. The addition of the carbonate and / or bicarbonate is preferably carried out in the form of a solution.
  • edge fractions are used, which are screened out as too large or too small particles in the separation of the resulting in the production of expandable polystyrene Perl spectrum.
  • the expandable styrene polymer particles produced according to the invention preferably have a diameter in the range from 0.2 to 4 mm. They can be prefoamed by conventional methods, for example with steam, into foam particles with a diameter between 0.1 and 2 cm and a bulk density between 5 and 100 kg / m 3 . The prefoamed particles can then be foamed by conventional methods to foam moldings having a density of 5 to 100 kg / m 3 .
  • the inventive method in which the individual components are added depending on the conversion of styrene, the particle diameter of the expandable, peribular styrene polymers can be controlled well and precisely.
  • the blowing agent-containing, expandable styrene polymers have low internal water contents, a high expansion capacity and good and constant processing properties. Moreover, the tendency for electrostatic charging is low.
  • the reactor After completion of the polymerization cycle time, the reactor is usually cooled via a jacket to a temperature between 60 and 30 ° C and the contents transferred via a bottom valve and a downstream transfer pump in a suspension tank.
  • Chromatographic methods are, for example, HPLC (High Performance Liquid Chromatography), GC (Gas Chromatography) and SEC (Size Exclusion Chromatography).
  • HPLC High Performance Liquid Chromatography
  • GC Gas Chromatography
  • SEC Size Exclusion Chromatography
  • a spectroscopic determination of sales can be done for example via IR spectroscopy, N IR spectroscopy or Raman spectroscopy. Furthermore, the use is also of UV measurements or fluorescence measurements possible. NMR spectroscopic methods can also be used.
  • spectroscopic measuring methods is preferred for determining the conversion of styrene. Very particular preference is given to using Raman spectroscopy as the spectroscopic measurement method.
  • Raman spectroscopy light is used in the near infrared range and in the visible range for excitation and detection.
  • Advantage of the Raman spectroscopy for determining the conversion of styrene in the present invention is that water has only a weak Raman scattering.
  • the particle size is also an important unit.
  • the particle size of the expandable styrene polymer is also measured and the addition of at least one component takes place only when a predetermined particle size is reached.
  • the particle size for the addition of the components is also taken into account, and a further influence on the setting of the particle size is thus possible. This makes it possible to achieve an even narrower particle size distribution.
  • Another advantage is that the size of the particles to be produced can be adjusted in a simple manner.
  • the addition of the stabilizer to stabilize the bead size distribution takes place only when a predetermined particle size is reached.
  • a stabilizer for stabilizing the bead size distribution preference is given to using a sulfate, in particular an alkaline earth metal sulfate and, preferably, magnesium sulfate thereof.
  • the addition of the stabilizer to stabilize the bead size distribution prevents coalescence of the individual styrene polymer particles.
  • the addition of the stabilizer to stabilize the bead size distribution therefore preferably takes place upon reaching a predetermined particle size, wherein the predetermined particle size is preferably the desired particle size for the styrene polymer produced.
  • the particle size-dependent addition of components is particularly relevant when the desired average particle diameter is almost reached, it is generally sufficient to take into account the measurement of the particle size of the expandable styrene polymer only from a conversion of styrene of at least 50%. Usually, the determination of the particle size is carried out during the entire manufacturing process, but the results take meaningful values only at high conversions.
  • the particle size of the expandable styrene polymer from a styrene conversion of at least 50% lower styrene conversions do not require multiple process parameters to be monitored and the process can be made simpler in this manner.
  • An advantage of the particle size-dependent metering of components, in particular of the stabilizer for stabilizing the bead size distribution, is that this makes it easier to convert to other particle sizes in the production from one batch to the next.
  • the addition of components which are added at a low conversion of styrene, depending on the conversion of styrene and components which are added at a high conversion of styrene, depending on the conversion of styrene or depending on the particle size wherein, for example, the stabilizer for stabilizing the bead size distribution, for example magnesium sulfate, is usually added only as a function of the particle size and the volatile blowing agent as a function of the conversion.
  • a low conversion of styrene means a conversion of styrene of at most 50% and a high conversion of styrene means a conversion of styrene of at least 50%.
  • the stirred tank is closed, a nitrogen pressure of 0.5 bar set. Subsequently, the stirred tank at a heating rate of 0.833 ° C / min is heated to 95 ° C. Thereafter, the mixture is heated to 137 ° C at a constant heating rate. The temperature of 137 ° C is reached at a monomer conversion in the reactor of 95.8%. The mixture is then stirred for a further 138 minutes at 137 ° C.
  • the conversion of styrene is determined using a dispersive Raman spectrometer (Kaiser Optical Systems SARL).
  • a dispersive Raman spectrometer Karl Optical Systems SARL.
  • the radiation of a wavelength of 785 nm which was generated by a semiconductor laser, coupled via fiber optic cable and a submersible probe in the reactor.
  • Part of the scattered radiation was recaptured via the probe and returned to the central spectrometer unit using fiber optic cables.
  • the elastic scattered Rayleigh radiation was separated by a Notch filter and the individual wavelengths of light were spatially split by a transmission grating.
  • the intensities of the inelastically scattered light were measured by means of a CCD (Charge-Coupled Device) detector with corresponding local resolution.
  • the spectra were calculated using a separate computer. The recording frequency of the spectra and the number of accumulations were chosen so that the highest possible signal-to-noise ratio was ensured at the same time high time resolution. Revenue calculation spectra were obtained at intervals of 7 to a maximum of 18 seconds.
  • the sales values were transferred to the process control system in real time and then used for the sales-based dosing of the sodium carbonate / bicarbonate solution, the extender solution, the pentane and the epsom salt.
  • the addition of the epsom salt was initiated by achieving a desired average bead size.
  • the particle size is also determined by Raman spectroscopy.
  • the corresponding band maximum is at about 1630 cm '1.
  • the absolute Raman intensities depend on various factors. Of these, some, such as temperature, particle size, density and solvent concentration in the course of a suspension change greatly. For this reason, it is necessary to have a To use additional bands in the spectrum as an internal reference, the Raman band of the ring respiration vibration of the aryl ring around 1000 cm -1 was used. Although their intensity is different for monomeric and polymeric styrene, but since the extent of the intensity decrease is known, this effect can be compensated by an appropriate correction factor.
  • Example 2 It was prepared in a pressure-resistant stirred tank, a styrene polymer according to Example 1, but the addition of magnesium sulfate did not occur when a predetermined particle diameter but sales-based when reaching a conversion of 88.4%.
  • the following table shows the mean bead size d 'and the measure of the bead size distribution ⁇ for each of the 25 tests carried out according to Example 1, Example 2 and Comparative Example 1. From the respective experiments the mean value of the bead size and the standard deviation were determined.
  • the mean bead size d 'and the measure of the bead size distribution ⁇ were determined according to Rosin-Rammler-Sperling-Bennett.
  • the bead size distribution corresponds to the total distribution, where ⁇ is a measure of the width and d 'means that 63.2% of the beads have a diameter that is less than or equal to d'.
  • the bead size distributions of the bead polymers obtained from Comparative Example 1 were determined by sieving and the results for the average bead size d 'were correlated with the Raman intensities of the spectra at high reaction times, ie at approximately complete monomer conversion.
  • the results for the average bead size d 'in this absolute method are heavily dependent on instrumental influences such as the condition of the optical fiber cable, the laser and the lens.
  • the ⁇ values are a measure of the width of the bead size distribution; high ⁇ values correspond to a large proportion of marginal fractions.
  • the transition from a time-based to a particle-size-based dosage shows a reduction in the ⁇ -values. This means that not only the variability of the average particle diameter can be reduced by the Raman spectroscopic process control, but also the fraction of the edge fractions. Although a reliable determination of the mean particle diameter via Raman spectroscopy is only possible with high conversions, process irregularities that lead to coagulation of the approach can already be recognized from low conversions. The detection of incipient coagulation is usually earlier possible than for example in the tracking of the stirrer torque.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Manufacture Of Porous Articles, And Recovery And Treatment Of Waste Products (AREA)
  • Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
  • Polymerisation Methods In General (AREA)

Abstract

L'invention concerne un procédé de fabrication de polymères styrène expansibles, comprenant les étapes consistant à (a) ajouter une phase aqueuse contenant un stabilisateur de suspension et une phase organique contenant un styrène et un initiateur dans un réacteur, (b) commencer à ajouter un agent d'expansion lorsque la conversion en styrène se situe dans une plage comprise entre 40 et 70% et ajouter cet agent d'expansion pendant 30 à 60 minutes, et (c) ajouter un stabilisateur pour stabiliser la distribution granulométrique du polymère styrène expansible lorsque la conversion en styrène se situe dans une plage comprise entre 65 et 99%.
PCT/EP2011/053374 2010-03-12 2011-03-07 Procédé de fabrication de polymères styrène expansibles WO2011110518A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
KR1020127023750A KR20130048198A (ko) 2010-03-12 2011-03-07 팽창성 스티렌 중합체의 제조 방법
CN201180013393.4A CN102791781B (zh) 2010-03-12 2011-03-07 制备可发泡苯乙烯聚合物
MX2012009463A MX2012009463A (es) 2010-03-12 2011-03-07 Preparacion de polimeros de estireno expansible.
BR112012021646A BR112012021646A2 (pt) 2010-03-12 2011-03-07 processo para preparar polímeros de estireno expansíveis
EP11708023A EP2545107A1 (fr) 2010-03-12 2011-03-07 Procédé de fabrication de polymères styrène expansibles

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP10156440 2010-03-12
EP10156440.9 2010-03-12

Publications (1)

Publication Number Publication Date
WO2011110518A1 true WO2011110518A1 (fr) 2011-09-15

Family

ID=44279745

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2011/053374 WO2011110518A1 (fr) 2010-03-12 2011-03-07 Procédé de fabrication de polymères styrène expansibles

Country Status (7)

Country Link
EP (1) EP2545107A1 (fr)
KR (1) KR20130048198A (fr)
CN (1) CN102791781B (fr)
AR (1) AR080755A1 (fr)
BR (1) BR112012021646A2 (fr)
MX (1) MX2012009463A (fr)
WO (1) WO2011110518A1 (fr)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9453083B2 (en) * 2013-03-14 2016-09-27 Saudi Basic Industries Corporation Vinyl polymers prepared via suspension polymerization and methods thereof
CN103965502B (zh) * 2014-04-28 2016-08-24 新疆蓝山屯河新材料有限公司 一种高熔结性可发性聚苯乙烯颗粒的生产方法

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3657162A (en) * 1965-05-13 1972-04-18 Foster Grant Co Inc Process of making expandable polymeric styrene particles
DD129556A2 (de) * 1974-05-09 1978-01-25 Wolfgang Wagenknecht Verfahren zur herstellung von kohlenhydratmischestern,insbesondere von cellulose
EP0304582A1 (fr) 1987-08-22 1989-03-01 Hüls Aktiengesellschaft Procédé de préparation de polymères de styrène à répartition granulométrique étroite
EP0575872A1 (fr) 1992-06-20 1993-12-29 BASF Aktiengesellschaft Procédé de préparation de perles de polymères styréniques expansibles
DE19816469C1 (de) * 1998-04-14 1999-12-09 Buna Sow Leuna Olefinverb Gmbh Verfahren und Vorrichtung zur Herstellung von expandierbaren Styrolpolymerisaten
FR2790091A1 (fr) * 1999-02-18 2000-08-25 Rhodia Chimie Sa Procede de preparation de latex par (co)polymerisation en emulsion de monomeres ethyleniquement insatures, avec suivi direct en ligne par spectroscopie raman
JP2004315671A (ja) * 2003-04-16 2004-11-11 Kanegafuchi Chem Ind Co Ltd スチレン系樹脂粒子の製造方法、及び発泡性スチレン系樹脂粒子の製造方法
WO2007144273A1 (fr) 2006-06-13 2007-12-21 Basf Se Procédé de fabrication de polymères de styrène expansibles
EP1442284B1 (fr) 2001-10-30 2008-03-12 Lanxess Deutschland GmbH Determination de l'avancement de reactions de polymerisation par greffage

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3657162A (en) * 1965-05-13 1972-04-18 Foster Grant Co Inc Process of making expandable polymeric styrene particles
DD129556A2 (de) * 1974-05-09 1978-01-25 Wolfgang Wagenknecht Verfahren zur herstellung von kohlenhydratmischestern,insbesondere von cellulose
EP0304582A1 (fr) 1987-08-22 1989-03-01 Hüls Aktiengesellschaft Procédé de préparation de polymères de styrène à répartition granulométrique étroite
EP0575872A1 (fr) 1992-06-20 1993-12-29 BASF Aktiengesellschaft Procédé de préparation de perles de polymères styréniques expansibles
DE19816469C1 (de) * 1998-04-14 1999-12-09 Buna Sow Leuna Olefinverb Gmbh Verfahren und Vorrichtung zur Herstellung von expandierbaren Styrolpolymerisaten
FR2790091A1 (fr) * 1999-02-18 2000-08-25 Rhodia Chimie Sa Procede de preparation de latex par (co)polymerisation en emulsion de monomeres ethyleniquement insatures, avec suivi direct en ligne par spectroscopie raman
EP1442284B1 (fr) 2001-10-30 2008-03-12 Lanxess Deutschland GmbH Determination de l'avancement de reactions de polymerisation par greffage
JP2004315671A (ja) * 2003-04-16 2004-11-11 Kanegafuchi Chem Ind Co Ltd スチレン系樹脂粒子の製造方法、及び発泡性スチレン系樹脂粒子の製造方法
WO2007144273A1 (fr) 2006-06-13 2007-12-21 Basf Se Procédé de fabrication de polymères de styrène expansibles

Non-Patent Citations (9)

* Cited by examiner, † Cited by third party
Title
"Polystyrol", vol. V, 1969, KARL HANSER VERLAG, article "Kunststoff-Handbuch", pages: 679 - 688
AL-KHANBASHI A ET AL: "APPLICATION OF IN-LINE FIBER-OPTIC RAMAN SPECTROSCOPY TO MONITORINGEMULSION POLYMERIZATION REACTIONS", APPLIED SPECTROSCOPY REVIEWS, vol. 33, no. 1/02, 1 January 1998 (1998-01-01), NEW YORK, US, pages 115 - 131, XP001031059, ISSN: 0570-4928 *
DATABASE WPI Week 200480, Derwent World Patents Index; AN 2004-807228, XP002655023 *
J. C. SANTOS ET AL.: "Online Monitoring of Suspension Polymerization Reactions Using a Raman Spectroscopy", IND. ENG. CHEM. RES., vol. 43, 2004, pages 7282 - 7289, XP007920468, DOI: doi:10.1021/ie034278m
M. VAN DEN BRINK, J. APPL. POLYM. SCI., vol. 79, 2001, pages 426 - 436
REIS M M ET AL: "Evidences of correlation between polymer particle size and Raman scattering", POLYMER, vol. 44, no. 20, 1 September 2003 (2003-09-01), ELSEVIER SCIENCE PUBLISHERS B.V, GB, pages 6123 - 6128, XP004452527, ISSN: 0032-3861, DOI: 10.1016/S0032-3861(03)00669-4 *
REIS, M. M.; ARAÜJO, P. H. H.; SAYER, C.; GIUDICI, R., ANAL. CHIM. ACTA, vol. 595, 2007, pages 257 - 265
REIS, M. M.; ARAÜJO, P. H. H.; SAYER, C.; GIUDICI, R., POLYMER, vol. 44, 2003, pages 6123 - 6128
SANTOS, J. C.; REIS, M. M.; MACHADO, R. A. F.; BOLZAN, A.; SAYER, C.; GIUDICI, R.; ARAÜJO, P. H. H., IND. ENG. CHEM. RES., vol. 43, 2004, pages 7282 - 7289

Also Published As

Publication number Publication date
KR20130048198A (ko) 2013-05-09
CN102791781A (zh) 2012-11-21
CN102791781B (zh) 2014-08-13
EP2545107A1 (fr) 2013-01-16
MX2012009463A (es) 2012-09-12
AR080755A1 (es) 2012-05-09
BR112012021646A2 (pt) 2016-09-20

Similar Documents

Publication Publication Date Title
US8455559B2 (en) Preparing expandable styrene polymers
EP2526143B1 (fr) Procédé de préparation de particules de polymérisat de styrène expansibles présentant une conductivité thermique réduite
EP0476256A1 (fr) Procédé pour régler la granulation lors de la préparation de polymères expansibles de styrène par polymérisation en suspension
EP0405325B1 (fr) Billes de polystyrène expansibles, à forte capacité d'expansion
EP2545107A1 (fr) Procédé de fabrication de polymères styrène expansibles
EP0106127B1 (fr) Particules en mousse de poly-p-méthylstyrène
EP0405324B1 (fr) Procédé de préparation de perles de polymères styréniques expansibles
DE883350C (de) Verfahren zur Polymerisation von polymerisierbaren Vinylaryl-Verbindungen, vorzugsweise Styrolen
EP0304582B1 (fr) Procédé de préparation de polymères de styrène à répartition granulométrique étroite
EP0143880B1 (fr) Procédé pour maîtriser les dimensions des perles pendant la préparation de polymères de styrène expansibles par polymérisation en suspension
DE2840355C2 (de) Feinteilige expandierbare Styrolpolymerisate zur Herstellung von Schaumstoffkörpern mit kurzen Mindestformverweilzeiten
EP2032609B1 (fr) Procédé de fabrication de polymères de styrène expansibles
DE60017548T2 (de) Verfahren zur herstellung von latex durch emulsions(co)polymerisation ethylenisch ungesättigter monomere mit direkter in-line-kontrolle durch raman-spektroskopie, und vorrichtung zur durchführung des verfahrens
DE60127205T2 (de) Gesteuertes Polymerisationsverfahren und Vorrichtung hierfür
EP1994085B1 (fr) Procede de fabrication de polymeres de styrene expansibles
EP0036136A1 (fr) Procédé pour la préparation de copolymères de styrène et/ou de ses dérivés
EP0254039A2 (fr) Polymères de styrène contenant des agents gonflants
DE4308636A1 (de) Verfahren zur Herstellung von perlförmigen expandierbaren Styrolpolymerisaten mit verbesserter Expandierbarkeit
EP0027609B1 (fr) Polymères de styrène contenant des agents d'expansion en forme de particules et leur utilisation
EP0068298B1 (fr) Procédé de préparation de polymères de styrène en suspension
EP0419966B1 (fr) Polymères styréniques expansibles, resistant à la chaleur, et à haute expansibilité
DE102007043351A1 (de) Verfahren zum Transferieren einer wässrigen Suspension von expandierbaren Styrolpolymerisaten
DE1301082C2 (de) Verfahren zur herstellung von blockpolymerisaten aus monovinylaromatischen monomeren
DE4420569A1 (de) Verfahren zum Recyclen von Polystyrolschaumstoffen
DE2431337A1 (de) Verfahren zur herstellung von selbstverloeschendem expandierbarem polystyrol

Legal Events

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

Ref document number: 201180013393.4

Country of ref document: CN

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

Ref document number: 11708023

Country of ref document: EP

Kind code of ref document: A1

WWE Wipo information: entry into national phase

Ref document number: MX/A/2012/009463

Country of ref document: MX

WWE Wipo information: entry into national phase

Ref document number: 7717/CHENP/2012

Country of ref document: IN

ENP Entry into the national phase

Ref document number: 20127023750

Country of ref document: KR

Kind code of ref document: A

NENP Non-entry into the national phase

Ref country code: DE

WWE Wipo information: entry into national phase

Ref document number: 2011708023

Country of ref document: EP

REG Reference to national code

Ref country code: BR

Ref legal event code: B01A

Ref document number: 112012021646

Country of ref document: BR

ENP Entry into the national phase

Ref document number: 112012021646

Country of ref document: BR

Kind code of ref document: A2

Effective date: 20120828