WO2004037894A1 - Herstellung von besonders wenig durch sauerstoff geschädigtem polycarbonat - Google Patents
Herstellung von besonders wenig durch sauerstoff geschädigtem polycarbonat Download PDFInfo
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- WO2004037894A1 WO2004037894A1 PCT/EP2003/011451 EP0311451W WO2004037894A1 WO 2004037894 A1 WO2004037894 A1 WO 2004037894A1 EP 0311451 W EP0311451 W EP 0311451W WO 2004037894 A1 WO2004037894 A1 WO 2004037894A1
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- polycarbonate
- hydroxyphenyl
- bis
- carbonate
- melt
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/002—Avoiding undesirable reactions or side-effects, e.g. avoiding explosions, or improving the yield by suppressing side-reactions
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G64/00—Macromolecular compounds obtained by reactions forming a carbonic ester link in the main chain of the macromolecule
- C08G64/20—General preparatory processes
- C08G64/205—General preparatory processes characterised by the apparatus used
Definitions
- the invention relates to a process for the production or processing of polycarbonate using apparatus or systems whose leak rate is ⁇ 10 "3 liters He x mbar / s and the polycarbonates obtainable therewith.
- Polycarbonate which is manufactured according to the phase boundary process, is exposed to extreme temperatures (> 200 ° C) to evaporate the solvent as a melt. The presence of oxygen leads to permanent damage to the polycarbonate.
- Polycarbonate which is manufactured according to the melt transesterification process, is exposed as a melt to extreme temperatures (> 270 ° C) at absolute pressures of up to 0.01 mbar during the course of the reaction.
- extreme temperatures > 270 ° C
- absolute pressures up to 0.01 mbar during the course of the reaction.
- the presence of oxygen also leads to permanent damage to the polycarbonate.
- EP-A 708 128 describes a melt transesterification process for polycarbonate in an inert, low-oxygen gas atmosphere.
- the first half of the reaction is preferably carried out without vacuum, with the elimination of phenol, in a reactor space which is permanently flushed with an inert, possibly pretreated, gas with a low oxygen content (at least ⁇ 2 ppm).
- the final phase of the reaction takes place while increasing the vacuum.
- a cycle mode of the inert gas streams is advantageous for the economy of a continuous process. However, these have to be freed from phenol in an extremely complex manner for recycling.
- a preferred one further pretreatment of the inert gas to further reduce the oxygen content also makes the method even more expensive.
- the aim was to provide a process which enables the largely damage-free production or processing of polycarbonate with comparatively simple and inexpensive process control.
- the invention therefore relates to a process for the production or processing of polycarbonate using systems and apparatus whose leak rate is ⁇ 10 "3 liters He x mbar / s, preferably ⁇ 10 " 4 liters He x mbar / s, particularly preferably ⁇ 10 " 5 liters He x mbar / s, very particularly preferably ⁇ 10 "6 liters He x mbar / s.
- the leak rates are measured, for example, in such a way that, for example, a helium gas measuring device from Leybold type 100, 100 plus or 200 or comparable devices is connected to the vapor lines of a system for the production or processing of polycarbonate, if necessary with an intermediate backing pump, which may only be used leads a partial flow of the gas volume to the measuring device.
- the flanges of the entire system which is under negative pressure, are coated with helium gas from a gas bottle over a gas lance. The meter measures the amount of helium drawn in by the flanges and reports a leak rate.
- a leak rate of ⁇ 10 "3 liters He x mbar / s is considered to be tight and a leak rate> 10 " 3 liters He x mbar / s is considered to be a leak.
- measurements can be carried out on a test leak before the measurement is carried out. It is also recommended to determine the basic level of helium in the environment using the measuring device. This concentration is then used as a zero or reference value. Ultrasound and leak spray can also be used to find leaks in flange connections, however the detection limit here is 10 "2 liters He x mbar / s and is therefore less sensitive than the helium leak test described.
- the helium leak test is first carried out in a cold system. The system is then heated to the desired operating temperatures, all flanges retightened, in order to then carry out the leak test again. The system only fulfills the requirements if this leak test has a positive result.
- the polycarbonate thus produced is distinguished by an improved color quality and is also the subject of the present application.
- the particular advantage of this method is that the tightness of the devices can be easily checked using a helium leak test and thus surprisingly displacement gases for oxygen, e.g. Nitrogen, and their installation becomes unnecessary.
- oxygen e.g. Nitrogen
- the polycarbonate is produced using the phase interface process.
- This process for polycarbonate synthesis has been described in many different ways in the literature, including in
- the disodium salt of a bisphenol which is initially introduced in an aqueous alkaline solution (or suspension), is phosgenated in the presence of an inert organic solvent or solvent mixture which forms a second phase.
- the resulting oligocarbonates which are mainly present in the organic phase, are converted into high molecular weight with the help of suitable catalysts the organic phase dissolved, polycarbonates condensed.
- the organic phase is finally separated off and the polycarbonate is isolated therefrom by various workup steps.
- an aqueous phase of NaOH, one or more bisphenols and water is used, the concentration of this aqueous solution, based on the sum of the bisphenols, not calculated as the sodium salt but as the free bisphenol, between 1 and 30% by weight, preferably between 3 and 25% by weight, particularly preferably between 3 and 8% by weight for polycarbonates with an Mw> 45000 and 12 to 22% by weight for polycarbonates with an Mw ⁇ 45000, can vary. At higher concentrations, it may be necessary to temper the solutions.
- the sodium hydroxide used to dissolve the bisphenols can be used in solid form or as an aqueous sodium hydroxide solution.
- the concentration of the sodium hydroxide solution depends on the target concentration of the desired bisphenolate solution, but is generally between 5 and 25% by weight, preferably 5 and 10% by weight, or is chosen to be more concentrated and then diluted with water. In the process with subsequent dilution, sodium hydroxide solutions with concentrations between 15 and 75% by weight, preferably 25 and 55% by weight, if appropriate at a temperature, are used.
- the alkali content per mol of bisphenol is very dependent on the structure of the bisphenol, but usually ranges between 0.25 mol alkali / mol bisphenol and 5.00 mol alkali / mol bisphenol, preferably 1.5-2.5 mol alkali / mol of bisphenol and, if bisphenol A is used as the sole bisphenol, 1.85 - 2.15 mol of alkali. If more than one bisphenol is used, these can be dissolved together. However, it can be advantageous to dissolve the bisphenols separately in the optimal alkaline phase and to meter the solutions separately or to supply the reaction in a combined manner. Furthermore, it can be advantageous not to dissolve the bisphenol (s) in sodium hydroxide solution but in dilute bisphenolate solution provided with additional alkali.
- the dissolving processes can start from solid bisphenol, usually in flakes or prill form, or else from molten bisphenol.
- the sodium hydroxide used or the sodium hydroxide solution can have been produced by the amalgam process or the so-called membrane process. Both methods have been used for a long time and are familiar to the person skilled in the art.
- Sodium hydroxide solution from the membrane process is preferably used.
- aqueous phase thus prepared is phosgenated together with an organic phase consisting of solvents for polycarbonate which are inert to the reactants and form a second phase.
- the optionally practiced dosing of bisphenol after or during the introduction of phosgene can be carried out as long as phosgene or its immediate secondary products, the chlorocarbonic acid esters are present in the reaction solution.
- the synthesis of polycarbonates from bisphenols and phosgene in an alkaline medium is an exothermic reaction and is carried out in a temperature range from -5 ° C to 100 ° C, preferably 15 ° C to 80 ° C, very particularly preferably 25-65 ° C, where depending on the solvent or solvent mixture, it may be necessary to work under excess pressure.
- Diphenols suitable for the preparation of the polycarbonates to be used according to the invention are, for example, hydroquinone, resorcinol, dihydroxydiphenyl, bis (hydroxyphenyl) alkanes, bis (hydroxyphenyl) cycloalkanes, bis (hydroxyphenyl) sulfides, bis (hydroxyphenyl) ethers , Bis (hydroxyphenyl) ketones, bis (hydroxyphenyl) sulfones, bis (hydroxyphenyl) sulfoxides, ( ⁇ , ⁇ '-bis (hydroxyphenyl) diisopropylbenzenes, and their alkylated, corealkylated and nuclear halogenated compounds.
- hydroquinone resorcinol, dihydroxydiphenyl
- bis (hydroxyphenyl) alkanes bis (hydroxyphenyl) cycloalkanes
- bis (hydroxyphenyl) sulfides bis (hydroxyphenyl) ethers
- Preferred diphenols are 4,4'-dihydroxydiphenyl, 2,2-bis (4-hydroxyphenyl) -l-phenyl-propane, 1,1-bis (4-hydroxyphenyl) phenylethane, 2,2-bis- (4-hydroxyphenyl) propane, 2,4-bis (4-hydroxyphenyl) -2-methylbutane, l, l-bis (4-hydroxyphenyl) -m / p diisopropylbenzene, 2,2-bis- (3rd -methyl-4-hydroxyphenyl) propane, bis (3,5-dimethyl-4-hydroxyphenyl) methane, 2,2-bis (3,5-dimethyl-4-hydroxyphenyl) propane, bis- (3,5-dimethyl-4-hydroxyphenyl) sulfone, 2,4-bis- (3,5-dimethyl-4-hydroxyphenyl) -2-methylbutane, 1, 1 -B is- (3, 5- dimethyl-4-hydroxyphenyl) -m / p-
- diphenols are 4,4'-dihydroxydiphenyl, l, l-bis (4-hydroxyphenyl) phenylethane, 2,2-bis (4-hydroxyphenyl) propane, 2,2-bis (3,5 -dimethyl-4-hydroxyphenyl) propane, 1,1-bis (4-hydroxyphenyl) cyclohexane and l, l-bis (4-hydroxyphenyl) -3,3,5-trimethylcyclohexane.
- the organic 'phase can consist of one or mixtures of several solvents. Suitable solvents are chlorinated hydrocarbons (aliphatic and / or aromatic), preferably dichloromethane, trichlorethylene, 1,1,1-trichloroethane, 1,1,2-trichloroethane and chlorobenzene and mixtures thereof.
- aromatic hydrocarbons such as benzene, toluene, m / p / o-xylene or aromatic ethers such as anisole can also be used alone, in a mixture or in addition or in a mixture with chlorinated hydrocarbons.
- Another embodiment of the synthesis uses solvents which do not dissolve polycarbonate but only swell. Precipitants for polycarbonate can therefore also be used in combination with solvents.
- solvents which can be used in the aqueous phase such as tetrahydrofuran, 1,3 / 1,4-dioxane or 1,3-dioxolane, can also be used as the solvent if the solvent part forms the second organic phase.
- the two phases that make up the reaction mixture are mixed to accelerate the reaction. This is done by introducing energy via shear, i.e. Pumps or stirrers or by static mixers or by generating turbulent flow using nozzles and / or orifices. Combinations of these measures are also used, often repeatedly in chronological or apparatus sequence.
- Anchor, propeller, MIG stirrers etc. are preferably used as stirrers, such as those e.g. in Ullmann, "Encyclopedia of Industrial Chemistry", 5th edition, Vol B2, p. 251 ff.
- Centrifugal pumps often multi-stage, with 2 to 9 stages being preferred, are used as pumps.
- Perforated orifices or tapered pipe sections or Venturi or Lefos nozzles are used as nozzles and / or orifices.
- the phosgene can be introduced in gaseous or liquid form or dissolved in solvent.
- the excess phosgene used based on the sum of the bisphenols used, is between 3 and 100 mol%, preferably between 5 and 50 mol%.
- the pH of the aqueous phase is kept in the alkaline range, preferably between 8.5 and 12, during and after the phosgene metering, by means of single or multiple metering in of sodium hydroxide solution or corresponding metering in of bisphenolate solution, while it is kept at 10 to 14 after the addition of catalyst should be.
- the temperature during the phosgenation is 25 to 85 ° C., preferably 35 to 65 ° C., depending on the solvent used, it is also possible to work under excess pressure.
- the dosage of phosgene can take place directly in the mixture of the organic and aqueous phase described, or else entirely or partially, before the phases are mixed, in one of the two phases, which is then mixed with the corresponding other phase. Furthermore, all or part of the phosgene can be metered into a recycled partial stream of the synthesis mixture from both phases, this partial stream preferably before the addition of catalyst is returned.
- the described aqueous phase is mixed with the organic phase containing the phosgene and then after a dwell time of 1 second to 5 minutes, preferably 3 seconds to 2 minutes, is added to the recirculated partial stream mentioned above, or else the two phases, the aqueous phase described Phase with the organic phase containing the phosgene are mixed directly in the recirculated partial stream mentioned above.
- the pH value ranges described above are to be observed and, if necessary, to be observed by single or multiple replenishment of sodium hydroxide solution or corresponding replenishment of bisphenolate solution.
- the temperature range may have to be maintained by cooling or diluting the reaction mixture.
- the polycarbonate synthesis can be carried out continuously or batchwise.
- the reaction can therefore be carried out in stirred tanks, tubular reactors, pump-around reactors or stirred tank cascades or their combinations, it being necessary to ensure by using the mixing elements already mentioned that the aqueous and organic phases only separate if possible when the synthesis mixture has fully reacted, i.e. no longer contains saponifiable chlorine from phosgene or chlorocarbonic acid esters.
- the monofunctional chain terminators required to regulate the molecular weight such as phenol or alkylphenols, in particular phenol, p-tert-butylphenol, isooctylphenol, cumylphenol, their chlorocarbonic acid esters or acid chlorides of monocarboxylic acids or mixtures of these chain terminators, are either mixed with the bisphenolate or fed to the bisphenolates in the reaction or added at any point in the synthesis as long as phosgene or chlorocarbonic acid end groups are still present in the reaction mixture, or in the case of acid chlorides and chlorocarbonic acid esters as chain terminators, as long as sufficient phenolic end groups of the polymer formed are available.
- phenol or alkylphenols in particular phenol, p-tert-butylphenol, isooctylphenol, cumylphenol, their chlorocarbonic acid esters or acid chlorides of monocarboxylic acids or mixtures of these chain terminators
- the chain terminator (s) are added after the phosgenation at one place or at a time when there is no more phosgene but the catalyst has not yet been metered in, or they are metered in before or in parallel with the catalyst.
- any branches or branchings to be used are added to the synthesis; usually before the chain terminators.
- Trisphenols, quarterphenols or acid chlorides of tri- or tetracarboxylic acids are usually used, or else mixtures of the polyphenols or the acid chlorides.
- Some of the compounds that can be used with three or more than three phenolic hydroxyl groups are, for example phloroglucinol,
- trifunctional compounds are 2,4-dihydroxybenzoic acid, trimesic acid, cyanuric chloride and 3,3-bis (3-methyl-4-hydroxyphenyl) -2-oxo-2,3-dihydroindole.
- Preferred branching agents are 3,3-bis- (3-methyl-4-hydroxyphenyl) -2-oxo-2,3-dihydroindole and
- the catalysts used in interfacial synthesis are tert.
- Amines especially triethylamine, tributylamine, trioctylamine, N-ethylpiperidine, N-methylpiperidine, N-i / n-propylpiperidine; quaternary ammonium salts such as tetrabutylammonium / tributylbenzylammonium / tetraethylammonium hydroxide / chloride / bromide / hydrogen sulfate / tetrafluoroborate; and the phosphonium compounds corresponding to the ammonium compounds.
- ammonium and phosphonium compounds are also referred to collectively as onium compounds.
- phase interface catalysts These compounds are described in the literature as typical phase interface catalysts, are commercially available and are familiar to the person skilled in the art.
- the catalysts can be added individually, in a mixture or also side by side and in succession to the synthesis, if appropriate also before the phosgenation, but doses after the phosgene introduction are preferred, unless an onium compound or mixtures of onium compounds are used as catalysts, then an addition before the phosgene is preferred.
- the metering of the catalyst or catalysts can be carried out in bulk, in an inert solvent, preferably that of polycarbonate synthesis, or as an aqueous solution, in the case of the tert. Amines then take place as their ammonium salts with acids, preferably mineral acids, especially hydrochloric acid. If several catalysts are used or partial amounts of the total amount of catalyst are metered, different metering methods can of course also be carried out at different locations or at different times.
- the total amount of the catalysts used is between 0.001 to 10 mol%, based on moles of bisphenols used, preferably 0.01 to 8 mol%, particularly preferably 0.05 to 5 mol%.
- the fully reacted, at most traces, preferably ⁇ 2 ppm, at least two-phase reaction mixture containing chlorocarbonic acid esters are allowed to settle for phase separation.
- the aqueous alkaline phase may be wholly or partly fed back into the polycarbonate synthesis as an aqueous phase or may be sent to the wastewater treatment, where solvent and catalyst components are separated and recycled.
- the organic impurities, in particular the solvent and polymer residues are separated off and, if appropriate, after the pH has been adjusted, e.g. by adding sodium hydroxide solution, the salt separated, which, for. B. the chlor-alkali electrolysis can be supplied, while the aqueous phase is optionally fed back to the synthesis.
- the organic phase containing the polymer must now be cleaned of all contaminations of an alkaline, ionic or catalytic type. It also contains portions after one or more settling processes, if necessary supported by runs through the settling tank, stirred tank, coalescer or separators or combinations of these measures - whereby water can optionally be metered in in each or a few separation steps, if necessary using active or passive mixing elements the aqueous alkaline phase in fine droplets and the catalyst, usually a tert. Amine.
- aqueous phase the organic phase is washed one or more times with dilute acids, mineral, carbon-hydroxycarbonic and / or sulfonic acids.
- Aqueous mineral acids are preferred, in particular hydrochloric acid, phosphorous acid and phosphoric acid or mixtures of these acids.
- the concentration of these acids should be in the range 0.001 to 50% by weight, preferably 0.01 to 5% by weight.
- the organic phase is washed repeatedly with deionized or distilled water.
- the organic phase which may be dispersed with parts of the aqueous phase, is separated off after the individual washing steps by means of a settling tank, stirred tank, Coalescers or separators or combinations of these measures, it being possible for the washing water to be metered in between the washing steps, if appropriate using active or passive mixing elements.
- acids preferably dissolved in the solvent on which the polymer solution is based, can optionally be added.
- Hydrogen chloride gas and phosphoric acid or phosphorous acid are preferably used here, which can optionally also be used as mixtures.
- the purified polymer solution thus obtained should not contain more than 5% by weight, preferably less than 1% by weight, very particularly preferably less than 0.5% by weight of water after the last separation process.
- the polymer can be isolated from the solution by evaporating the solvent by means of temperature, vacuum or a heated entraining gas. Other isolation methods are crystallization and precipitation.
- the residues of the solvent can either be obtained directly from the melt with evaporation extruders (BE-A 866 991, EP-A 0 411 510, US-A 4 980 105, DE-A 33 32 065), thin-film evaporators (EP -A 0 267 025), Falling film evaporators, strand evaporators or by friction compaction (EP-A 0 460 450), optionally also with the addition of an entrainer such as nitrogen or carbon dioxide or using a vacuum (EP-A 003 996, EP-A 0 256 003, US-A 4 ' 423 207) can be removed, alternatively also by subsequent crystallization (DE-A 3 429 960) and heating of the residues of the solvent in the solid phase (US-A 3 986 269, DE-A 2 053 876).
- evaporation extruders BE-A 866 991, EP-A 0 411 510, US-A 4 980 105, DE-A
- Granules are preferably obtained by directly spinning off the melt and subsequent granulation, or else by using discharge extruders from which spinning is carried out in air or under liquid, usually water. If extruders are used, additives can be added to the melt before this extruder, if necessary using static mixers or by side extruders in the extruder. '
- the polymer solution is either sprayed into a vessel under reduced pressure after heating or by means of a nozzle with a heated carrier gas, e.g. Inject nitrogen, argon or water vapor into a vessel with normal pressure.
- a heated carrier gas e.g. Inject nitrogen, argon or water vapor into a vessel with normal pressure.
- powder (diluted) or flakes (concentrated) of the polymer are obtained, from which the last residues of the solvent may also have to be removed as above.
- Granules can then be obtained using a compounding extruder and subsequent spinning.
- Additives, as described above, can also be added here in the periphery or in the extruder itself.
- a compacting step for the polymer powder often has to be used before extrusion due to the low bulk density of the powders and flakes:
- the polymer can be largely precipitated in crystalline form from the washed and possibly still concentrated solution of the polycarbonate by adding a precipitant for polycarbonate. It is advantageous to add a small amount of the precipitant first and, if necessary, also to insert waiting times between the additions of the batches of precipitant. It can also be advantageous to use different precipitants.
- a precipitant here e.g. Hydrocarbons, especially heptane, i-octane, cyclohexane and alcohols such as methanol, ethanol, i-propanol.
- the polymer solution is slowly added to a precipitant during the precipitation.
- Alcohols such as methanol, ethanol, i-propanol, but also cyclohexane or ketones such as acetone are usually used as the precipitant.
- the materials thus obtained are processed into granules as described in the spray evaporation and optionally additized.
- precipitation and crystallization products or amorphously solidified products in fine-grained form are crystallized by passing vapors of one or more precipitants for polycarbonate, with simultaneous heating below the glass transition temperature, and further condensed to higher molecular weights. If these are oligomers, possibly with different end groups (phenolic and chain terminators), one speaks of solid phase condensation.
- the polycarbonate according to the invention is also produced by the melt transesterification process.
- the production of aromatic oligo- or polycarbonates by the melt transesterification process is known from the literature and is described, for example, in the Encyclopedia of Polymer Science, Vol. 10 (1969), Chemistry and Physics of Polycarbonates, Polymer Reviews, H. Schnell, Vol. 9, John Wiley and Sons, Inc. (1964) and in DE-C 10 31 512, US-B 3,022,272, US-B 5,340,905 and US-B 5,399,659.
- aromatic dihydroxy compounds are transesterified in the melt with carbonic acid diesters with the aid of suitable catalysts and optionally other additives.
- Dihydroxyaryl compounds suitable for the process according to the invention are those of the formula (I)
- Z is an aromatic radical with 6 to 30 C atoms, which may contain one or more aromatic nuclei, may be substituted and may contain aliphatic or cycloaliphatic radicals or alkylaryls or heteroatoms as bridge members.
- dihydroxyaryl compounds of the formula (I) are 4,4'-dihydroxydiphenyl, 2,2-bis (4-hydroxyphenyl) -1-phenyl-propane, 1,1-bis (4-hydroxyphenyl) phenyl-ethane, 2,2-B is- (4-hydroxyphenyl) propane, 2,4-bis (4-hydroxyphenyl) -2-methylbutane, 1,3-bis- [2- (4-hydroxyphenyl) -2-pro - pyl] benzene (bisphenol M), 2,2-bis (3-methyl-4-hydroxyphenyl) propane, bis (3,5-dimethyl-4-hydroxyphenyl) methane, 2,2-bis ( 3,5-dimethyl-4-hydroxyphenyl) propane, bis (3,5-dimethyl-4-hydroxyphenyl) sulfone, 2,4-bis (3,5-dimethyl-4-hydroxyphenyl) -2 -methylbutane, 1,3-bis- [2- (3,5-dimethyl-4-hydroxyphenyl)
- diphenols are 4,4'-dihydroxydiphenyl, l, l-bis (4-hydroxyphenyl) phenylethane, 2,2-bis (4-hydroxyphenyl) propane, 2,2-bis (3,5 -dimethyl-4-hydroxyphenyl) propane, 1,1-bis. (4-hydroxyphenyl) cyclohexane and l, l-bis (4-hydroxyphenyl) -3,3,5-methylcyclohexane (bisphenol TMC).
- the dihydroxyaryl compounds can also be used with residual contents of the monohydroxyaryl compounds from which they were produced.
- the contents can be up to 20%, preferably 10%, particularly preferably up to 5% and very particularly preferably up to 2% (see e.g. EP-A 1 240 232).
- Carbonic acid diesters for the purposes of the invention are those of the formulas (II) and (III)
- R, R 'and R "are independently H C ⁇ -C 6 -C 34 -aryl may represent optionally branched 34 -AlkyI / CycIoalkyl, C 7 -C 3 -A__kylaryl or C
- Diphenyl carbonate for example Diphenyl carbonate, butylphenyl phenyl carbonate, di-butylphenyl carbonate, isobutylphenyl phenyl carbonate, di-isobutylphenyl carbonate, tert-butylphenyl phenyl carbonate, di-tert-butylphenyl carbonate, n-pentylphenyl phenyl carbonate, di- (n-pentylphenyl) carbonate, n -Hexylphenyl phenyl carbonate,
- the diaryl carbonates can also be used with residual contents of the monohydroxyaryl compounds from which they were produced.
- the contents can be up to 20%, preferably 10%, particularly preferably up to 5% and very particularly preferably up to 2%.
- the phenolic compounds used as carbonates can also be used directly as a monohydroxyaryl compound in addition to one of the carbonates mentioned, in order to influence the end groups of the polycarbonate.
- a monohydroxyaryl compound should be selected whose boiling point is above that of the monohydroxyaryl compound from which the diaryl carbonate was formed. Preferred mixtures are those with diphenyl carbonate.
- the inventive method there is the possibility of adding the monohydroxyaryl compound at any time in the reaction, preferably at the start of the reaction, and the addition can be divided into several portions.
- the proportion of free monohydroxyaryl compound can be 0.4-17 mol%, preferably 1.3-8.6 mol% (based on the dihydroxyaryl compound). The addition can take place either before the reaction or in whole or in part during the reaction.
- the diaryl carbonates are mixed with 1.02 to 1.30 mol, preferably with 1.04 to 1.26 mol, particularly preferably with 1.06 to 1.22 mol per mol of dihydroxyaryl. connection used. Mixtures of the above-mentioned diaryl carbonates can also be used.
- onium salts As catalysts in the context of the invention, basic catalysts such as, for example, alkali metal and alkaline earth metal hydroxides and oxides, but also ammonium or phosphonium salts, hereinafter referred to as onium salts, are used in the melt transesterification process as described in the literature mentioned. Onium salts are preferably used, particularly preferably phosphonium salts. Phosphonium salts for the purposes of the invention are those of the formula (IV)
- R M have the same or different C ⁇ -C ⁇ 0 alkyls, C 6 -C ⁇ o-aryls, C 7 -C ⁇ o-aralkyls or C 5 -C 6 - can be cycloalkyls, preferably methyl or C 6 -C ⁇ aryls, more preferably methyl or Phenyl, and
- X can be an anion such as hydroxide, sulfate, hydrogen sulfate, bicarbonate, carbonate, a halide, preferably chloride, or an alcoholate of the formula OR, where RC 6 - C ⁇ aryl or C 7 -C aralkyl, preferably phenyl, can be Preferred catalysts are
- Additional catalysts can be used alone or optionally in addition to the onium salt to increase the rate of polymerization.
- These include salts of alkali metals and alkaline earth metals, such as hydroxides, alkoxides and aryl oxides of lithium, sodium and potassium, preferably hydroxides, alkoxides or aryl oxides of sodium. Most preferred are sodium hydroxide and sodium phenolate.
- the amounts of the cocatalyst can range from 1 to 500 ppb, preferably 5 to 300 ppb and most preferably 5 to 200 ppb, each calculated as sodium.
- the catalysts are added in solution in order to avoid harmful excess concentrations during metering.
- the solvents are system and process inherent compounds such as dihydroxyaryl compounds, diaryl carbonates or monohydroxyaryl compounds.
- Monohydroxyaryl compounds are particularly preferred because those skilled in the art are familiar with the fact that the dihydroxyaryl compounds and diaryl carbonates easily change and decompose at temperatures which are already slightly elevated, in particular under the action of a catalyst.
- the resulting connections reduce the polycarbonate quality.
- the preferred compound is phenol. Phenol is also an obvious choice because the preferred catalyst, tetraphenylphosphonium phenate, is isolated as a mixed crystal with phenol during manufacture.
- the temperatures over the entire process are between 180 and 330 ° C, the pressures between 15 bar absolute and 0.01 mbar. '
- the continuous process for the production of polycarbonates by transesterification of diaryl carbonates with dihydroxyaryl compounds is preferably characterized in that, using catalysts, after precondensation without removal of the monohydroxyaryl compound formed, in subsequent subsequent flash / evaporator stages at gradually increasing temperatures , and gradually falling prints an oligocarbonate is produced, which is then condensed in one or more basket reactors one after the other, with further rising temperatures and further falling prints to the finished polycarbonate.
- the reactants can either be melted together or the solid dihydroxyaryl compound can be dissolved in the diaryl carbonate melt or the solid diaryl carbonate can be dissolved in the melt of the dihydroxyaryl compound, or both raw materials are brought together as a melt, preferably directly from the preparation.
- the residence times of the separate melting of the raw materials, in particular that of the melt of the dihydroxyaryl compound, are set as short as possible.
- the melt mixture can remain longer without damage because of the lower melting point of the raw material mixture compared to the individual raw materials at correspondingly lower temperatures.
- the catalyst preferably dissolved in phenol, is then mixed in and the melt is heated to the reaction temperature.
- the melt mixture is expanded in a first vacuum chamber, the pressure of which is set to 100 to 400 mbar, preferably 150 to 300 mbar, and immediately afterwards heated again to the inlet temperature in a suitable device at the same pressure.
- the hydroxyaryl compound formed during the relaxation process is still present
- the reaction mixture is expanded in a second vacuum chamber, the pressure of which is 50 to 200 mbar, preferably 80 to 150 mbar, and immediately afterwards in a suitable device heated at the same pressure to a temperature of 190 to 250 ° C, preferably 210 to 240 ° C, particularly preferably 210 to 230 ° C.
- a suitable device heated at the same pressure to a temperature of 190 to 250 ° C, preferably 210 to 240 ° C, particularly preferably 210 to 230 ° C.
- the hydroxyaryl compound formed is evaporated with monomers still present.
- the reaction mixture is depressurized in a third vacuum chamber, the pressure of which is 30 to 150 mbar, preferably 50 to 120 mbar, and immediately thereafter in a suitable device at the same pressure to a temperature of 220 to 280 ° C, preferably 240 to 270 ° C, particularly preferably 240 to 260 ° C, heated.
- a third vacuum chamber the pressure of which is 30 to 150 mbar, preferably 50 to 120 mbar
- a suitable device at the same pressure to a temperature of 220 to 280 ° C, preferably 240 to 270 ° C, particularly preferably 240 to 260 ° C, heated.
- the hydroxyaryl compound formed is evaporated with monomers still present.
- the reaction mixture is passed into a further vacuum chamber, the pressure of which is 5 to 100 mbar, preferably 15 to 100 mbar, particularly preferably 20 to 80 mbar, relaxed and immediately afterwards heated in a suitable device at the same pressure to a temperature of 250 to 300 ° C, preferably 260 to 290 ° C, particularly preferably 260 to 280 ° C.
- a suitable device at the same pressure to a temperature of 250 to 300 ° C, preferably 260 to 290 ° C, particularly preferably 260 to 280 ° C.
- the hydroxyaryl compound formed is evaporated with monomers still present.
- the number of these stages, here 4 by way of example, can vary between 2 and 6. The rel.
- Viscosity of the oligomer is between 1.04 and 1.20, preferably between 1.05 and 1.15, particularly preferably between 1.06 and 1.10.
- the relative viscosity is determined as the quotient of the viscosity of the solvent and the viscosity of the polymer dissolved in this solvent. It was determined in dichloromethane at a concentration of 5 g / 1 at 25 ° C.
- the oligomer produced in this way is, after a dwell time of 5 to 20 min, in a sump receiver, optionally with pumping at the same pressure and the same temperature as in the last flash / evaporator stage, into a basket reactor and at 250 to 310 ° C., preferably 250 to 290 ° C. C, particularly preferably 250 to 280 ° C, further condensed at pressures of 2 to 15 mbar, preferably 4 to 10 mbar, with residence times of 30 to 90 min, preferably 30 to 60 min.
- the product reaches a rel. Viscosity from 1.12 to 1.25, preferably 1.13 to 1.22, particularly preferably 1.13 to 1.20.
- the melt leaving this reactor is brought to the desired final viscosity in a further basket reactor.
- the temperatures are 270 to 330 ° C, preferably 280 to 320 ° C, particularly preferably 280 to 310 ° C, the pressure 0.01 to 3 mbar, preferably 0.2 to 2 mbar, with residence times of 60 to 180 min, preferably 75 to 150 min.
- the rel. Viscosities are set to the level required for the intended application and are 1.18 to 1.40, preferably 1.18 to 1.36, particularly preferably 1.18 to 1.34.
- the function of the two basket reactors can also be summarized in one basket reactor.
- the vapors are derived directly from all stages of the process and processed, for example, in accordance with German patent application No. 1 01 00 404 (e.g. column 3 sections 14-22 and the examples).
- the apparatuses and reactors suitable for the individual process steps are heat exchangers, apparatuses or stirred tanks which provide the necessary residence time at constant temperature, depending on the course of the process; Relaxation devices such as large-volume containers, separators or cyclones; Stirred tanks, circulation evaporators, falling film evaporators or other commercially available apparatus that enable the necessary heat input; Containers which ensure the required retention times after heating; single- or twin-shaft basket or disc reactors with the necessary volumes and film formation areas as well as a design that meets the growing melt viscosities.
- the pipes between the devices should of course be as short as possible and the curvature of the pipes should be kept as small as possible.
- the external framework conditions for assembling chemical plants must be taken into account.
- a conventional heat exchanger is used to heat the raw material melt.
- a perforated plate column is used as the retention tank for the reaction equilibrium.
- the expansion processes, ie the flash evaporation, are carried out in centrifugal separators, preferably cyclones, or in deflection separators.
- the heating of the melt flowing out of the centrifugal separators, preferably cyclones, or deflection separators, is carried out in falling film evaporators, which
- the containers are provided with a pump 1 , the liquids from the falling film evaporator and the pump flowing over t built-in grid or perforated sheet metal constructions or packed beds into the sump and collected.
- the condensation to a medium-viscosity product is carried out in a disc or basket reactor.
- the polycondensation is also in one
- Disc or basket reactor which provides a very large, constantly renewing surface at the vacuum during the long dwell times.
- the disc or basket reactors are geometrically designed in accordance with the increase in melt viscosity. In a special arrangement, a disk or basket reactor can also be sufficient.
- Reactors such as those described in DE 44 47 422 C2 and EP A 1 253 163, or twin-shaft reactors such as those described in WO A 99/28 370 are suitable, for example.
- Particularly suitable materials for the manufacture of the apparatus, reactors, pipelines, pumps and fittings are stainless steels of the type Cr Ni (Mo) 18/10, such as, for. B. 1.4571 or 1. 4541 (Stahlkey 2001, publisher: Stahlkey Wegst GmbH, Th-Heuss-Strasse 36, D-71672 Marbach) and Ni-based alloys of type C, such as. B. 2.4605 or 2.4610 (Stahlkey 2001, 5 publisher: StahlKey Wegst GmbH, Th-Heuss-Strasse 36, D-71672 Marbach).
- the stainless steels are used up to process temperatures of around 290 ° C and the Ni-based alloys at process temperatures above around 290 ° C.
- thermoplastic polycarbonates obtainable by the melt transesterification process according to the invention likewise form part of the present invention. They have an extremely low content of cations and anions of less than 60 ppb, preferably ⁇ 40 ppb and particularly preferably ⁇ 20 ppb (calculated as Na cation), the cations being those of alkali and alkaline earth metals which are present, for example, as Contamination can come from the raw materials used and the phosphonium and ammonium salts.
- Other ions such as Fe, Ni, Cr, Zn, Sn, Mo, AI ions and their homologues can be found in the raw materials be contained or come from the materials of the system used due to abrasion or corrosion.
- the total content of these ions is less than 2 ppm, preferably less than 1 ppm and particularly preferably less than 0.5 ppm.
- the aim is to achieve the smallest quantities that can only be achieved 5 using the purest raw materials.
- Such pure raw materials are e.g. B. only after cleaning processes such as recrystallization, distillation, tumbling with washing u. available.
- Anions are those of inorganic acids and of organic acids in equivalent amounts (e.g. chloride, sulfate, carbonate, phosphate, phosphite, oxalate, etc.)
- the polycarbonates are also distinguished by the fact that they do not contain any detectable amounts of incorporated cleavage or decomposition products with reactive end groups which are formed during the transesterification process.
- cleavage or decomposition products are, for example, isopropenylmonohydroxyaryls or their dimers.
- the average weight molecular weights obtained are 15,000 to 40,000, preferably 17,000 to 36,000, particularly preferably 17,000 to 34,000, the average weight ole- 15 molecular weight over the relative viscosity according to the Mark-Houwing correlation (JMG Cowie, chemistry and physics of synthetic polymers, Vieweg Textbook, Braunschweig / Wiesbaden, 1997, page 235) was determined.
- the polycarbonates can be branched in a targeted manner and can therefore contain small amounts of branching agents of 0.02 to 3.6 mol% (based on the dihydroxyaryl compound).
- Suitable branching agents are the compounds having three or more functional groups, preferably those having three or more than three phenolic OH groups, which are suitable for the production of polycarbonates.
- Some of the compounds that can be used with three or more than three phenolic hydroxyl groups are, for example
- trifunctional compounds are 2,4-dihydroxybenzoic acid, trimesic acid, cyanuric chloride and 3,3-bis (3-methyl-4-hydroxyphenyl) -2-oxo-2,3-dihydroindole.
- Preferred branching agents are 3,3-bis (3-methyl-4-hydroxyphenyl) -2-oxo-2,3-dihydroindole and 1,1,1-tri- (4-hydroxyphenyl) ethane.
- Residual monomers due to the chemical equilibrium and given by process parameters such as temperature, pressure and residence time can be further reduced if necessary by suitable evaporation processes.
- Granules are obtained by spinning the melt out of the reactor using a gear pump, cooling the strands in air or water, followed by granulation.
- Additives, auxiliaries and reinforcing materials can be added to the polycarbonates produced according to the invention, regardless of the production process, before spinning.
- additives serves to extend the useful life of the consumer goods made from the polycarbonate or to improve the color (stabilizers), to simplify processing (e.g. mold release agents, flow aids, antistatic agents) or to adapt the polymer properties to specific loads (impact modifiers such as rubbers; Flame retardants, colorants, glass fibers).
- additives can be added individually or in any mixtures or several different mixtures to the polymer melt, directly during the isolation of the polymer or after melting of the granulate in a so-called compounding step.
- the additives or their mixtures can be added to the polymer melt as a solid, ie as a powder, or as a melt.
- Another type of metering is the use of masterbatches or mixtures of masterbatches of the additives or additive mixtures.
- Suitable additives are described, for example, in “Additives for Plastics Handbook, John Murphy, Elsevier, Oxford 1999", and in “Plastics Additives Handbook, Hans Doubt, Hanser, Kunststoff 2001”.
- Suitable antioxidants or thermal stabilizers are, for example:
- Alkylated monophenols alkylthiomethylphenols, Hydroquinones and alkylated hydroquinones,
- Aromatic hydroxybenzyl compounds
- Organic phosphites, phosphonates and phosphanes are preferred, mostly those in which the organic radicals consist wholly or partly of optionally substituted aromatic radicals.
- Suitable complexing agents for heavy metals and for neutralizing traces of alkali are ortho- and meta-phosphoric acids, fully or partially esterified phosphates or phosphites,
- UV absorbers Suitable as light stabilizers (UV absorbers)
- Oxamides 2.8. 2- (2-hydroxyphenyl) -l, 3,5-triazines, substituted benzotriazoles are preferred.
- Polypropylene glycols alone or in combination with, for example, sulfones or sulfonamides as stabilizers can be used against damage by gamma rays.
- stabilizers can be used individually or in combinations and can be added to the polymer in the stated forms.
- Processing aids such as mold release agents, usually derivatives of long-chain fatty acids, can also be added.
- Preferred are e.g. Pentaerythritol tetrastearate and glycerol monostearate. They are used alone or in a mixture, preferably in an amount of 0.02 to 1% by weight, based on the mass of the composition.
- Suitable flame retardant additives are phosphate esters, i.e. Triphenyl phosphate, resorcinodi- phosphoric acid esters, bromine-containing compounds such as brominated phosphoric acid esters, brominated oligocarbonates and polycarbonates, and preferably salts of fluorinated organic sulfonic acids.
- Suitable impact modifiers are butadiene rubber with grafted styrene-acrylonitrile or methyl methacrylate, ethylene-propylene rubbers with grafted maleic anhydride, ethyl and butyl acrylate rubbers with grafted methyl methacrylate or styrene-acrylonitrile, interpenetrating siloxane-acrylate-acrylate or acrylate-nitrate networks with acrylate-methacrylate and acrylate-acrylate-acrylate-acrylate or acrylate-nitrate networks with acrylate or acrylate-acrylate.
- colorants such as organic dyes or pigments or inorganic pigments, IR absorbers, individually, in a mixture or in combination with stabilizers, glass fibers, glass (hollow) spheres, inorganic fillers can be added.
- the present application also relates to the polycarbonates as obtained by the process according to the invention and their use for the production of extrudates and moldings, in particular those for use in the transparent area, very particularly in the area of optical applications such as, for example, Plates, multi-wall sheets, glazing, diffusing screens, lamp covers or optical data storage media, such as audio CDs, CD-R (W), DVD, DVD-R (W), mini discs in their various readable or writable versions, which can also be described repeatedly.
- optical applications such as, for example, Plates, multi-wall sheets, glazing, diffusing screens, lamp covers or optical data storage media, such as audio CDs, CD-R (W), DVD, DVD-R (W), mini discs in their various readable or writable versions, which can also be described repeatedly.
- extrudates and moldings from the polymer according to the invention are also the subject of the present application.
- Safety panes which are known to be required in many areas of buildings, vehicles and aircraft, and as shields for helmets.
- Translucent panels such as solid panels or in particular hollow chamber panels, for example for covering buildings such as train stations, greenhouses and lighting systems.
- Optical data storage such as audio CDs, CD-R (W) 's, DCD's, DVD-R (W)' s, mini discs and the subsequent developments.
- Traffic light housing or traffic signs.
- Translucent formulations containing barium sulfate and or titanium dioxide and or zirconium oxide or organic polymeric acrylate rubbers (EP-A 0 634 445, EP-A 0 269 324) for the production of translucent and light-scattering moldings.
- Precision injection molded parts such as brackets, e.g. Lens holders; here polycarbonates with glass fibers and an additional content of 1-10% by weight of molybdenum disulfide (based on the total molding composition) are used where appropriate.
- Optical device parts in particular lenses for photo and film cameras (DE-A 27 01 173).
- Light transmission carrier in particular light guide cable (EP-A '0 089 801) and lighting strips.
- Food applications such as bottles, dishes and chocolate molds.
- Sporting goods such as slalom poles, ski shoe buckles.
- Household items such as kitchen sinks, sinks, letter boxes.
- Housings such as electrical distribution boxes.
- Housings for electrical devices such as toothbrushes, hair dryers, coffee machines, machine tools, such as drilling, milling, planing machines and saws.
- Chip boxes, chip carriers, boxes for Si wafers 30. Chip boxes, chip carriers, boxes for Si wafers.
- the leak detector / helium detector (device from Leybold Type 200) was connected in front of the vacuum pump and the extruder, side extruder, separator, sight glasses and screw housing 5 and all flange connections in this area were checked.
- the test device has a response time of ⁇ 5 seconds.
- the basic level of the system was determined to be ⁇ 10 "5 liters He x mbar / s.
- the screw housing was tight with 8x10 " 5 liters He x mbar / s, whereas a sight glass with a leak rate of 10 "3 liters of He x mbar / s was identified as a leak.
- the relative solution viscosity was determined in dichloromethane at a concentration of 5 g / 1 at 25 ° C. 10,
- Spray temperature was 300 ° C.
- the color number was determined as the difference in absorbance at 420 nm and 700 nm in dichloromethane at a concentration of 2.4 g / 50 ml and a layer thickness of 10 cm.
- the samples were weighed in gas-tight closed rim vials and sealed gas-tight in an air atmosphere. These samples were then annealed at temperatures of 320, 350 and 380 ° C. for 10, 20 and 30 minutes. After cooling, the oxygen content in the gas space of the ampoules was determined by means of GC. The oxygen uptake of the polymer is determined from the difference from the initial sample. Samples with comparable weights of about 500 mg were compared. The analyzes were carried out as triple determinations to estimate the error limits of the method. The measurements have an error range of approximately +/- 10%. The oxygen contents, measured in vol%, were converted into ppm or mmol / g polymer, assuming the validity of the ideal gas law.
- the annealed polymers were then dissolved and the color numbers of the solutions were determined
- 1. FS 20 SO natur is a linear melt polycarbonate with a relative solution viscosity of 1.201 and a color number of 0.11.
- the phenolic OH value is 540 5 ppm.
- FS 26 SO natur is a linear melt polycarbonate with a relative solution viscosity of 1.275 and a color number of 0.14.
- the phenolic OH value is 250 ppm.
- the samples were annealed for 10, 20 and 30 min at temperatures of 320, 350 and 380 ° C in an air atmosphere in gas-tight closed rim vials.
- the oxygen and CO 2 content in the gas space of the ampoules was then determined by means of GC.
- the samples marked with x contained insoluble / insoluble dark brown particles, so that deviations can be expected in these samples.
- Fig. 1 shows the relationship between the color number and the C0 2 release (ppm) as a function of the 0 2 uptake (pm).
- the example clearly demonstrates the harmful influence of air or oxygen at elevated temperatures and mean periods of time on the color quality of the melt polycarbonate.
Abstract
Description
Claims
Priority Applications (3)
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JP2005501519A JP2006504860A (ja) | 2002-10-21 | 2003-10-16 | 酸素によって特に小範囲にダメージを受けるポリカーボネートの調製 |
EP03769397A EP1565510A1 (de) | 2002-10-21 | 2003-10-16 | Herstellung von besonders wenig durch sauerstoff geschädigtem polycarbonat |
AU2003278087A AU2003278087A1 (en) | 2002-10-21 | 2003-10-16 | Production of polycarbonate with particularly little damage due to oxygen |
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DE2002148950 DE10248950A1 (de) | 2002-10-21 | 2002-10-21 | Herstellung von besonders wenig durch Sauerstoff geschädigtem Polycarbonat |
DE10248950.5 | 2002-10-21 | ||
DE10314609 | 2003-04-01 | ||
DE10314609.1 | 2003-04-01 |
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WO2004037894A1 true WO2004037894A1 (de) | 2004-05-06 |
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PCT/EP2003/011451 WO2004037894A1 (de) | 2002-10-21 | 2003-10-16 | Herstellung von besonders wenig durch sauerstoff geschädigtem polycarbonat |
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US (1) | US20040103717A1 (de) |
EP (1) | EP1565510A1 (de) |
JP (2) | JP2006504860A (de) |
AU (1) | AU2003278087A1 (de) |
TW (1) | TW200415173A (de) |
WO (1) | WO2004037894A1 (de) |
Cited By (1)
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EP1865027B2 (de) † | 2005-03-28 | 2017-07-12 | Mitsubishi Engineering-Plastics Corporation | Polycarbonatharzzusammensetzung und formprodukt zum schutz gegen heisse strahlung |
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US8478238B2 (en) | 2005-04-29 | 2013-07-02 | Jasper Wireless, Inc. | Global platform for managing subscriber identity modules |
US7309755B2 (en) * | 2005-08-24 | 2007-12-18 | General Electric Company | Method of producing polycarbonate articles by rotation molding and rotation molded articles made by the method |
JP7167569B2 (ja) * | 2018-09-12 | 2022-11-09 | 三菱エンジニアリングプラスチックス株式会社 | 金属膜付樹脂成形品 |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
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DE2441123A1 (de) * | 1974-08-28 | 1976-03-11 | Leybold Heraeus Gmbh & Co Kg | Verfahren zur dichtigkeitspruefung von gegenstaenden |
US5345814A (en) * | 1990-12-28 | 1994-09-13 | Whirlpool Corporation | Method and apparatus for testing vacuum insulation panel quality |
EP0976773A2 (de) * | 1998-06-04 | 2000-02-02 | Teijin Limited | Verfahren zur Herstellung von Polycarbonatharz |
Family Cites Families (4)
Publication number | Priority date | Publication date | Assignee | Title |
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DE3346946A1 (de) * | 1983-12-24 | 1985-07-04 | Bayer Ag, 5090 Leverkusen | Verfahren zur herstellung von farblosen aromatischen polyestern und polyestercarbonaten |
JP2863386B2 (ja) * | 1992-04-20 | 1999-03-03 | 新日鐵化学株式会社 | 熱安定性の優れたビスフェノールaの製造方法 |
US5317900A (en) * | 1992-10-02 | 1994-06-07 | The Lyle E. & Barbara L. Bergquist Trust | Ultrasensitive helium leak detector for large systems |
DE19860144C1 (de) * | 1998-12-24 | 2000-09-14 | Bayer Ag | Verfahren zur Herstellung von Bisphenol A |
-
2003
- 2003-10-16 WO PCT/EP2003/011451 patent/WO2004037894A1/de not_active Application Discontinuation
- 2003-10-16 JP JP2005501519A patent/JP2006504860A/ja active Pending
- 2003-10-16 EP EP03769397A patent/EP1565510A1/de not_active Withdrawn
- 2003-10-16 AU AU2003278087A patent/AU2003278087A1/en not_active Abandoned
- 2003-10-17 US US10/688,104 patent/US20040103717A1/en not_active Abandoned
- 2003-10-20 TW TW092128995A patent/TW200415173A/zh unknown
- 2003-10-21 JP JP2003360981A patent/JP2004277703A/ja not_active Withdrawn
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2441123A1 (de) * | 1974-08-28 | 1976-03-11 | Leybold Heraeus Gmbh & Co Kg | Verfahren zur dichtigkeitspruefung von gegenstaenden |
US5345814A (en) * | 1990-12-28 | 1994-09-13 | Whirlpool Corporation | Method and apparatus for testing vacuum insulation panel quality |
EP0976773A2 (de) * | 1998-06-04 | 2000-02-02 | Teijin Limited | Verfahren zur Herstellung von Polycarbonatharz |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
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EP1865027B2 (de) † | 2005-03-28 | 2017-07-12 | Mitsubishi Engineering-Plastics Corporation | Polycarbonatharzzusammensetzung und formprodukt zum schutz gegen heisse strahlung |
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US20040103717A1 (en) | 2004-06-03 |
JP2004277703A (ja) | 2004-10-07 |
JP2006504860A (ja) | 2006-02-09 |
EP1565510A1 (de) | 2005-08-24 |
AU2003278087A1 (en) | 2004-05-13 |
TW200415173A (en) | 2004-08-16 |
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