EP4355808A1 - Oligoesters comprenant du résorcinol et de l'acide iso-et/ou téréphtalique, carbonates de polyester correspondants et leur préparation - Google Patents

Oligoesters comprenant du résorcinol et de l'acide iso-et/ou téréphtalique, carbonates de polyester correspondants et leur préparation

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Publication number
EP4355808A1
EP4355808A1 EP22727952.8A EP22727952A EP4355808A1 EP 4355808 A1 EP4355808 A1 EP 4355808A1 EP 22727952 A EP22727952 A EP 22727952A EP 4355808 A1 EP4355808 A1 EP 4355808A1
Authority
EP
European Patent Office
Prior art keywords
formula
mixture
polyester carbonate
carbonate
hydrogen
Prior art date
Legal status (The legal status 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 status listed.)
Pending
Application number
EP22727952.8A
Other languages
German (de)
English (en)
Inventor
Alexander Meyer
Lukas Fabian SCHULZ
Thomas Pfingst
Ulrich Liesenfelder
Dirk Hinzmann
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Covestro Deutschland AG
Original Assignee
Covestro Deutschland AG
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 Covestro Deutschland AG filed Critical Covestro Deutschland AG
Publication of EP4355808A1 publication Critical patent/EP4355808A1/fr
Pending legal-status Critical Current

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Classifications

    • 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
    • C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
    • C08G63/02—Polyesters derived from hydroxycarboxylic acids or from polycarboxylic acids and polyhydroxy compounds
    • C08G63/12—Polyesters derived from hydroxycarboxylic acids or from polycarboxylic acids and polyhydroxy compounds derived from polycarboxylic acids and polyhydroxy compounds
    • C08G63/16—Dicarboxylic acids and dihydroxy compounds
    • C08G63/18—Dicarboxylic acids and dihydroxy compounds the acids or hydroxy compounds containing carbocyclic rings
    • C08G63/181—Acids containing aromatic rings
    • C08G63/183—Terephthalic acids
    • 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
    • C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
    • C08G63/64—Polyesters containing both carboxylic ester groups and carbonate groups
    • 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
    • C08G64/30—General preparatory processes using carbonates
    • 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
    • C08G64/30—General preparatory processes using carbonates
    • C08G64/307—General preparatory processes using carbonates and phenols

Definitions

  • the present invention relates to a mixture containing oligoesters, polyester carbonates comprising an ester block and a process for the production of polyester carbonates with an ester block.
  • aromatic polyester carbonates have good mechanical properties and heat resistance. Furthermore, it is known that special polyester carbonates, especially if they contain ester blocks from aromatic diacids and resorcinol, have a high resistance to weathering.
  • polyester carbonates which contain ester blocks of iso- and/or terephthalic acid and resorcinol have good weathering resistance. These materials are particularly interesting because they do not require painting to protect them from the elements, particularly UV rays.
  • the ester structures of resorcinol and iso- and/or terephthalic acid can undergo what are known as photo-Fries rearrangements when they come into contact with UV light. This results in hydroxybenzophenone structures that are built into the polymer chain. Hydroxybenzophenones are known to have UV absorbing properties. This explains the good weather resistance. This situation is described in US20030050400 A1, for example.
  • UV absorbers on the other hand, is far less effective since most of the UV absorber accumulates in the mass.
  • concentration of UV absorbers on the surface which must be protected against UV light in particular, is relatively low. If the person skilled in the art wants to use higher concentrations of UV absorber, he is confronted with further disadvantages. Low-molecular compounds reduce the mechanical properties, especially in higher concentrations. This is undesirable.
  • UV-sensitive materials such as polycarbonate with layers of lacquer which have high concentrations of UV absorbers.
  • painting is an additional step that causes costs and is not always the preferred solution for reasons of sustainability. Especially in the area of automotive exterior applications, it is advantageous if materials are intrinsically weather-resistant and costly painting can be dispensed with.
  • polyester carbonates described are produced in the prior art using a phase interface process.
  • aromatic diols and OH-terminated ester blocks are condensed using phosgene.
  • the OH-terminated ester blocks can also be prepared by condensation with phosgene starting from aromatic diacids and aromatic diols in solution.
  • Such a process for preparing the oligoesters and the corresponding polyester carbonates is described in WO0026275 A1.
  • polyester carbonates from bisphenol A containing ester blocks from Tcrcphtha1/1sophtha1 acid are described as preferred polymers.
  • the ester blocks are produced in a dichloromethane/water mixture using aqueous NaOH solution starting from the acid chlorides of the aromatic diacid and resorcinol.
  • the polyester solution containing hydroxy-terminated ester blocks is transferred to a phosgenation reactor.
  • alkaline bisphenol A solution is introduced and the reactants are reacted with phosgene.
  • melt transesterification processes which are based on the melt transesterification process known for polycarbonate are known and have the advantage that starting materials which are difficult to handle, such as phosgene, for example, can be used. They also have the great advantage of being able to do without solvents. Therefore, it would be industrially advantageous to produce polyester carbonates by the melt transesterification process.
  • this process also presents challenges.
  • the highly reactive acid chlorides are difficult to replace with other starting materials.
  • Transesterification processes often have long residence times in the appropriate reactors. Due to the high temperatures, decomposition products are often formed, which have a negative impact on the product quality. Since melt transesterification processes usually do not require complex work-up steps, impurities and catalyst residues remain in the product. These can degrade the product quality.
  • polycarbonates that are produced in the melt transesterification process have a significantly higher content of hydroxy-terminated end groups (content of phenolic OH groups) compared to corresponding products from the phase interface process.
  • phenolic OH groups can be damaged by oxidative processes, which impairs the product quality.
  • the optical properties unfortunately below.
  • the prior art exclusively relates to the production of the polyester carbonates by means of phase interface reactions.
  • polyester carbonates with a low OH end group content can be produced in the melt transesterification process. Since the reactivity of the reactants is lower for the reasons mentioned above - compared to the Rrinsatz für in the phase interface process - it is also unknown how the above-mentioned polyester carbonates with high viscosity resp. Molecular weight can be produced.
  • WO2005021616 A1 describes the preparation of hydroxy-terminated oligoester blocks in the melt. Here it was investigated how a content of OH end groups in the oligoesters can be achieved which is comparable to oligoesters which can be achieved in a process using a solvent. Different catalytic converters and the influence of the driving style (e.g.
  • oligoesters with phenoxy end groups are described here, WO2005021616 A1 does not describe any molecular weight distribution of the oligomers of the oligoester.
  • the oligoesters are then condensed into a polyester carbonate using phase boundary processes.
  • this document cannot contain any teaching as to how end groups and/or oligomer distributions affect the production of a polyester carbonate by means of melt transesterification.
  • WO2006057810 A1 describes oligoesters according to the melt transesterification process, which are characterized in that they have a high proportion of carboxyl end groups.
  • US20030050400 A1 describes the production of oligomers from aromatic diacids and resorcinol.
  • US20030050400 A1 is based on the object of providing OH-terminated building blocks which can then be converted to polyester carbonates by means of phase interface processes. Similar to WO2005021616 A1, neither an oligomer distribution, the end group ratio nor their influence on a melt transesterification of the oligoesters is discussed here.
  • the present invention was based on the object of overcoming at least one disadvantage of the prior art.
  • the object of the present invention was to provide a polyester carbonate comprising ester blocks Based on isophthalic acid and/or terephthalic acid and resorcinol, which can be obtained by a melt transesterification process.
  • the aim here is preferably to obtain polyester carbonates which have good processability and at the same time have the lowest possible phenolic OH end group content.
  • the polyester carbonates should therefore preferably be stable to weathering and/or also essentially stable to yellowing and/or essentially not to polymer degradation, for example due to oxidative degradation. It is also preferred that no raw materials that pose challenges in handling, such as phosgene, are used in the production of the polyester carbonate.
  • a polyester carbonate can be obtained by means of melt transesterification which has a high (but not too high) molecular weight and at the same time has a content of phenolic OH end groups which is so low that the polyester carbonate has a high stability against degradation, for example.
  • the use of the special oligoester carbonates results in a new polyester carbonate being obtained in which a high proportion of the isophthalic acid and/or terephthalic acid groups are directly connected to the carbonate blocks.
  • the oligoesters are used with the highest possible OH end group content. This automatically leads to the diol used (e.g. resorcinol) forming the end group of these oligoesters. These then bind to the carbonate blocks, whereby z. B. carbonate-resorcinol linkages arise.
  • the oligoesters of the present invention are essentially terminated by specific aromatic esters of isophthalic acid and/or terephthalic acid.
  • the polyester carbonates have novel linkages via isophthalic acid and/or terephthalic acid.
  • the provision of the special oligoesters made it possible to obtain a polyester carbonate from an oligocarbonate and an oligoester block by means of melt transesterification, which polyester carbonate has good properties with regard to the objectives required above.
  • each q is independently 0 or 1
  • each Z is independently -H or an aromatic radical of formula (2a), where R2' is hydrogen or -COOCH 3 and indicates the position at which formula (2a) is attached to the oxygen atom of formula (1)
  • each Z independently represents an aromatic radical of the formula (2)
  • R 2 is hydrogen or -COOCH 3 and indicates the position at which formula (2) is attached to the oxygen atom of formula (1)
  • p indicates the number of repeating units, characterized in that at most 0.5 % by weight of the radicals Z in relation to the mixture for hydrogen and that the percentage of oligomers with a molecular weight of less than 1000 g/mol in the mixture is less than 12%, preferably less than 10%, the percentage of oligomers being determined is determined by the ratio of the area under a molecular weight distribution curve of the mixture in relation to the refractive index signal (from gel permeation chromatography) in a range below 1000
  • the term “mixture containing oligoesters of the formula (1)” is to be understood as meaning that this mixture consists essentially of the oligoesters of the formula (1). This means preferably at least 80% by weight, particularly preferably at least 90% by weight, very particularly preferably at least 95% by weight, of the mixture consists of the oligoesters of the formula (1).
  • Ri and p have the meanings given above.
  • the oligoester is terminated at least on one side with an isophthalic acid/terephthalic acid (-COOH as end group).
  • these go OH end groups (-COOH end groups) are not included in the defined % by weight of OH end groups (via Z in formula (1)) of the mixture according to the invention.
  • Those skilled in the art know how to determine these -COOH end groups.
  • deuterated DMSO is particularly suitable as a solvent.
  • the mixture contains a total of at most 0.5% by weight, preferably at most 0.45% by weight, particularly preferably at most 0.4% by weight, very particularly preferably at most 0.35% by weight. of OH end groups in relation to the total weight of the mixture (preferably detected via 1 1 l-NMR).
  • Ri in formula (1) is preferably hydrogen.
  • the ring substituted by the Ri is preferably derived from resorcinol.
  • R2 in formula (2) is preferably hydrogen.
  • the groups on which the R2 is present in formula (2) in combination with formula (1) are preferably phenyl isophthalate and/or terephthalate.
  • R2 ' in formula (2a) is also preferably hydrogen.
  • the groups on which the R2' is present in formula (2a) in combination with formula (1) are preferably resorcinol phenyl carbonate.
  • Ri in formula (1) is particularly preferably hydrogen
  • R2 in formula (2) is hydrogen
  • R2′ in formula (2a) is hydrogen
  • p in formula (1) indicates the number of repeating units of the oligoester.
  • P is preferably on average at least 4. More preferably p in formula (1) is on average at least 4 and at most 30, more preferably at least 5 and at most 27, most preferably at least 5 and at most 24.
  • the mixture of oligoesters has a number average molecular mass in the range from 1300 g/mol to 6000 g/mol, more preferably 1400 g/mol to 5500 g/mol and most preferably 1500 g/mol to 5000 g/mol.
  • This M n is preferably determined via gel permeation chromatography in dichloromethane using a bisphenol A polycarbonate as the standard.
  • the molecular weights Mw (weight average) and Mn (number average) according to the invention of the oligoesters or polyester carbonates used were - unless otherwise stated - by means of size exclusion chromatography (gel permeation chromatography GPC; based on DIN 55672-1: 2007-08 using a BPA polycarbonate calibration ) definitely.
  • the calibration was carried out with linear polycarbonates of known molar mass distribution (e.g. from PSS Polymer Standards Service GmbH, Germany). Method 2301-0257502-09D (from 2009 in German) from Currenta GmbH & Co. OHG, Feverkusen was used.
  • the column combination consisted of crosslinked styrene-divinylbenzene resins.
  • the GPC can include one or more series-connected commercially available GPC columns for size exclusion chromatography, which are selected such that a sufficient separation of the molar masses of polymers, in particular of aromatic polycarbonates with weight-average molar masses M w of 2000 to 100 000 g/mol is possible .
  • the analytical columns have a diameter of 7.5 mm and a length of 300 mm.
  • the particle sizes of the column material are in the range from 3 pm to 20 pm.
  • the mixture according to the invention is preferably characterized in that Ri in formula (1) is hydrogen, at most 0.4% by weight of the radicals Z in relation to the mixture are hydrogen and the percentage of oligomers with a molecular weight of less than 1000 g /mol is less than 10%.
  • the mixture according to the invention has at most 0.5% by weight, preferably at most 0.45% by weight, particularly preferably at most 0.4% by weight, very particularly preferably at most 0.35% by weight
  • This OH end group content can be determined in a manner known to those skilled in the art.
  • the OH end group content is preferably determined by means of 111 -NMR. This can be done, for example, in dichloromethane with tetramethylsiloxane as an internal standard.
  • the area under the signal of the OH groups (this is usually at 5.3 to 5.6 ppm) can be set in relation to the area of the other signals of the oligomer.
  • polyester carbonates are obtained by means of melt transesterification, which have a relative Have a solution viscosity that is no longer workable (i.e. usually above an eta rel of 1.35). Polyester carbonates are thus obtained which are difficult to process into molded parts, for example by means of injection molding. At the same time, many of the polyester carbonates obtained in this way also have a high phenolic OH content. This usually leads to an unstable polymer that tends to degrade due to temperature and/or light. If the OH end group content of the mixture according to the invention is at most 0.5 wt processable (e.g. by means of injection molding) and are also very stable against degradation.
  • This ratio of the end groups can be determined in a manner known to those skilled in the art. In particular, this ratio can be determined by 111 -NMR, preferably at at least 700 MHz. This can be done, for example, in dichloromethane with tetramethylsiloxane as an internal standard.
  • the area under the signal of the OH groups (this is usually at 5.3 to 5.6 ppm) can be set in relation to the area of the other signals of the oligomer.
  • the area of the peak at about 7.4 ppm, which should correspond to a phenyl end group (2 protons), in relation to the area of the peaks between 6 .6 and 6.8 ppm, which should correspond to a resorcinol end group (3 protons).
  • the proportion of oligomers with a molecular weight of less than 1000 g/mol in the mixture according to the invention is preferably less than 12% must be less than 11%, particularly preferably less than 10%, so that there is a sufficient increase in the molecular weight of the polyester carbonate by means of melt transesterification. If the proportion is greater than 12%, the mixture of oligoesters is not reactive enough for a sufficient increase in molecular weight to occur. This means that the resulting polyester carbonate does not have the desired processability, mechanical and optical properties.
  • the proportion of oligomers with a molecular weight of less than 1000 g/mol is determined by the ratio of the area under a molecular weight distribution curve of the mixture in relation to the refractive index signal (from gel permeation chromatography) in a range below 1000 g/mol and the total area under this molecular weight distribution curve definitely.
  • gel permeation chromatography is carried out in dichloromethane using a bisphenol A polycarbonate standard (see also the detailed description of gel permeation chromatography above).
  • the curve of refractive index signal versus molecular weight can be integrated in a manner known to those skilled in the art, in particular using the GPC software.
  • the area under the curve below 1000 g/mol is related to the total area.
  • the Mn of the mixture of oligoesters has an influence on the amount of oligomers with a molecular weight below 1000 g/mol.
  • mixture according to the invention containing oligoesters of the formula (1) is prepared in all preferences and combinations of preferences described above via a process in which
  • At least isophthalic acid and/or terephthalic acid are mixed with a diol of formula (3) and at least one diaryl carbonate of formula (4), where in which Ri represents a hydrogen atom, a halogen or an alkyl group having 1 to 4 carbon atoms, preferably hydrogen, and where in which R2 each independently represents hydrogen or -COOCH 3 , preferably hydrogen,
  • this mixture from step (i) is heated in the presence of at least one catalyst and
  • step (iii) applying vacuum to the mixture from step (ii) to obtain the mixture containing oligoester.
  • this process according to the invention can also be supplemented by a step (iv), in which the mixture obtained, comprising oligoesters, from step (iii) is precipitated.
  • the mixture is preferably dissolved in dichloromethane. Also preferably, it can then be precipitated in a non-solvent such as methanol. After subsequent separation of the precipitated mixture containing oligoesters from the non-solvent and optional drying, the mixture according to the invention containing oligoesters is obtained.
  • Step (iv) can be used when the proportion of oligomers with a molecular weight of less than 1000 g/mol in the mixture is greater than 12%. The precipitation causes the low molecular weight oligomers to remain in solution. As a result, the proportion of oligomers with a molecular weight of less than 1000 g/mol in the mixture can be reduced.
  • step 1 The method according to the invention can also optionally also be used in addition to step
  • step (iv) have a further step (v) in which the mixture obtained from step (iii) or from step (iv), containing oligoester, is reacted with a diacid diphenyl ester, preferably isophthalic acid diphenyl ester and/or terephthalic acid diphenyl ester.
  • a diacid diphenyl ester preferably isophthalic acid diphenyl ester and/or terephthalic acid diphenyl ester.
  • Process step (v) can be used in particular when the OH end group content of the mixture containing oligoesters obtained from step (iii) or step (iv) is greater than 0.5% by weight, based on the mixture.
  • step (v) to reduce the OH end group content are also known to those skilled in the art. However, step (v) described is particularly preferred since the introduction of the end group described leads to reactivity in the subsequent melt transesterification process to give a polyester carbonate.
  • step (ii) by choosing the suitable parameters and in particular also the choice of the suitable catalyst in step (ii), a mixture containing oligoesters is obtained after step (iii) which has the characteristics of the OH required according to the invention -End group content and the proportion of oligomers with a molecular weight below 1000 g/mol. Neither step (iv) nor step (v) is then necessary.
  • the resulting end group ratio in the mixture containing oligoesters can be influenced, preferably by the ratio of isophthalic acid and/or terephthalic acid to the diol of the formula (3).
  • the ratio of isophthalic acid and/or terephthalic acid to the diol of the formula (3) is preferably from 1.00 to 1.15, particularly preferably from 1.03 to 1.13, very particularly preferably from 1.04 to 1.12. It has been found that at a ratio below 1.00, a high proportion of oligomers with a molecular weight below 1000 g/mol are formed. As already described, these can be removed from the mixture by means of step (iv). However, it is therefore preferred that the ratio is above 1.00. Conversely, too high a ratio leads to very high OH end group termination. Here, too, it has already been described that this can be reduced using step (v). However, it is preferred that the ratio is therefore at most 1.15.
  • Both isophthalic acid and terephthalic acid are preferably used in process step (i). If both diacids are used, then it is additionally preferred that the ratio of isophthalic acid to terephthalic acid is 0.25-4.0 to 1, more preferably 0.4-2.5 to 1 and most preferably 0.67-1. is 5 to 1. It is also preferred that the diol of formula (3) is resorcinol. Likewise, and preferably at the same time, it is preferred that the diaryl carbonate of formula (4) is diphenyl carbonate.
  • the mixture from process step (i) is heated in the presence of at least one catalyst.
  • the individual components from process step (i) are preferably melted.
  • terephthalic acid in particular is not soluble under the given conditions, at least initially. However, this can change in the course of process step (ii).
  • carbon dioxide is generally released. This procedure allows a quick reaction under low temperature stress.
  • Process step (ii) preferably takes place under a protective gas atmosphere, preferably under nitrogen and/or argon.
  • Step (ii) is preferably carried out in the absence of a solvent.
  • solvent is known to a person skilled in the art.
  • the term “solvent” is preferably understood to mean a compound which does not undergo a chemical reaction in any of process steps (i), (ii) and/or (iii). Excluded are those compounds which result from the reaction (e.g. phenol if diphenyl carbonate is used as the diaryl carbonate).
  • phenol if diphenyl carbonate is used as the diaryl carbonate
  • the starting compounds contain traces of solvents. This case should preferably be included according to the invention.
  • an active step of adding such a solvent is preferably avoided.
  • the heating in process step (ii) preferably takes place at temperatures from 180°C to 300°C, preferably from 190°C to 270°C and particularly preferably from 195°C to 250°C. Under these temperature conditions, the corresponding aryl alcohol of the diaryl carbonate, preferably phenol, may already be distilled off.
  • Process step (ii) preferably takes place under atmospheric pressure. The mixture is preferably stirred under atmospheric pressure until the evolution of gas essentially stops. Alternatively, the temperature can also be increased stepwise--depending on the reactivity observed--to 200.degree. C.-300.degree. C., preferably 210-260.degree. C., particularly preferably 215-240.degree. The reactivity can be estimated from the evolution of gas in a manner known to those skilled in the art. In principle, higher temperatures are also possible in this step, but side reactions (e.g. discoloration) can occur at higher temperatures. Therefore, higher temperatures are less preferred.
  • the at least one catalyst used in process step (ii) can influence the oligomer distribution of the mixture according to the invention containing oligoesters. It is possible to use a catalyst containing alkali metal ions, preferably sodium ions, in process step (ii) (with). However, the alkali metal ions remain in the mixture according to the invention. This should then be condensed using melt transesterification. However, since alkali metal ions, in particular sodium ions, can catalyze the melt transesterification, the amounts of sodium remaining in the mixture must be precisely known and, if necessary, determined. It is therefore advantageous if no catalyst which has an alkali metal ion is used in process step (ii).
  • the at least one catalyst is particularly preferably an organic base, preferably alkylamines, imidazole (derivatives), guanidine bases such as triazabicyclodecene, DMAP and corresponding derivatives, l,5-diazabicyclo[4.3.0]non-5-ene (DBN ) and diazabicycloundecene (DBU), most preferably DMAP.
  • organic base preferably alkylamines, imidazole (derivatives), guanidine bases such as triazabicyclodecene, DMAP and corresponding derivatives, l,5-diazabicyclo[4.3.0]non-5-ene (DBN ) and diazabicycloundecene (DBU), most preferably DMAP.
  • DBN l,5-diazabicyclo[4.3.0]non-5-ene
  • DBU diazabicycloundecene
  • a mixture of at least one organic base such as, for example, alkylamines, imidazole (derivatives), guanidine bases such as triazabicyclodecene, DMAP and corresponding derivatives, DBN or DBU is preferably used together with a phosphonium catalyst of the formula (VIII) (see below).
  • a mixture of 4-(dimethylamino)pyridine (DMAP) and tetrabutylphosphonium acetate is very particularly preferably used as the catalyst in process step (ii).
  • the at least one catalyst is preferably used in amounts of 1 to 5000 ppm, preferably 5 to 1000 ppm and particularly preferably 20 to 500 ppm, based on the sum of the masses of isophthalic acid and/or terephthalic acid, the diol of the formula (3) and the diaryl carbonate of formula (4) used. If more than one catalyst is used in the reaction, these catalysts are preferably used in total in amounts of 1 to 5000 ppm, preferably 5 to 1000 ppm and particularly preferably 300 to 700 ppm.
  • vacuum is applied to the mixture obtained from process step (ii).
  • the corresponding aryl alcohol of the diaryl carbonate used preferably phenol, is distilled off and the equilibrium of the reaction is shifted towards oligoesters.
  • the aryl alcohol is the chemical compound split off by the condensation reaction.
  • condensation is known to those skilled in the art. This is preferably understood to mean a reaction in which two molecules (of the same substance or different substances) combine to form a larger molecule, with one molecule of a chemically simple substance being split off.
  • This compound split off during the condensation is removed in process step (iii) by means of a vacuum.
  • the process according to the invention is characterized in that during process step (iii) the volatile components which have a boiling point below the mixture of oligoesters formed in process step (ii) are separated off, optionally with stepwise reduction of the pressure.
  • a gradual removal is preferably chosen when different volatile components are removed. Stepwise removal is also preferably selected in order to ensure that the volatile component(s) is/are removed as completely as possible.
  • the volatile constituents are the chemical compound or compounds split off during the condensation, preferably phenol.
  • the pressure can be lowered step by step, for example in such a way that as soon as the head temperature falls, the pressure is lowered in order to ensure continuous removal of the chemical compound split off during the condensation.
  • the condensation product is separated off in process step (iii) preferably at temperatures of from 200.degree. C. to 280.degree. C., more preferably from 210.degree. C. to 270.degree. C. and particularly preferably from 220.degree. C. to 265.degree.
  • the vacuum during the separation is also preferably from 500 mbar to 0.01 mbar. In particular, it is preferred that the separation takes place gradually by reducing the vacuum.
  • the vacuum in the last stage is very particularly preferably 10 mbar to 0.01 mbar.
  • a polyester carbonate comprising
  • each Y independently represents a structure of formula (III), (IV), (V) or (VI), wherein in the R6 and R7 each independently represent hydrogen, Ci-Cix-alkyl, Ci-Cis-alkoxy, halogen or each optionally substituted aryl or aralkyl, preferably hydrogen, and
  • X for a single bond, -CO-, -O-, -S-, Ci- to C7, -alkylene, C2- to CVAlkylidcn, Cg to Cio-cycloalkylidene or for Cg- to Ci2-arylene, which optionally with further
  • Aromatic rings containing heteroatoms may be condensed, preferably for a single bond, C2- to CV-alkylidcn or Cg to Cio-cycloalkylidene, particularly preferably isopropylidene, where in these formulas (IV) to (VI) R 3 is in each case Ci-Ci-alkyl, aralkyl or aryl, preferably methyl or phenyl, very particularly preferably methyl, and which each indicate the positions with which the formulas ( 111), (IV), (V) or (VI) bind to the carbonate group in formula (11), m is at least 5, preferably 8 to 300, more preferably 10 to 250 and most preferably 50 to 200 and each of the Specify positions with which the carbonate groups are bound into the polyester carbonate, characterized in that at least some of the ester groups (A) are directly linked to at least some of the carbonate groups (B) via the formula (VII), where
  • a structure of formula (VII) can be determined by NMR. This is described by way of example using a direct linkage of bisphenol units to form isophthalic acid and/or terephthalic acid units. The linkage is an ester linkage. The presence of this linkage can be determined via 13 C-NMR spectroscopy by determining the chemical shift of the carbonyl carbon atom marked with an arrow in formula (VIIa).
  • Polyester carbonates produced in the phase interface process which comprise the ester groups (A) and (B), do not have the structural formula (VII) (see FIG. 1).
  • an OH-terminated oligoester reacts with a bisphenol (usually bisphenol A) or a corresponding oligocarbonate by reacting with phosgene to form a carbonate.
  • a resorcinol unit for example, is always bound directly to a BPA unit via a carbonate group.
  • ester groups (A) and the carbonate groups (B) can each occur more than once in a polyester carbonate. It is also evident that n and m and the number of ester groups (A) and/or carbonate groups (B) must be chosen such that the corresponding solution viscosity of the polyester carbonate results. It is preferred that the polyester carbonate according to the invention has a ratio of 5 to 90% by weight, particularly preferably 8 to 30% by weight and very particularly preferably 9 to 25% by weight of ester groups (A) based on the total weight the ester groups (A) and the carbonate groups (B). Likewise, it is preferred that the polyester carbonate according to the invention consists of at least 80% by weight, particularly preferably at least 90% by weight and very particularly preferably at least 95% by weight, of the units of the formula (1) and (11).
  • the polyester carbonate according to the invention is characterized in that the polyester carbonate has a relative solution viscosity of at least 1.26 to at most 1.34. As already described above, this relative solution viscosity ensures good processability of the polyester carbonate, for example by injection molding. This relative solution viscosity also makes it possible to show the good mechanical properties for interesting areas of application such as in the automotive exterior sector.
  • the polyester carbonate has a high stability and is intrinsically weather-stable.
  • the relative solution viscosity (prel; also referred to as eta rel) is preferably determined in dichloromethane at a concentration of 5 g/l at 25° C. using an Ubbelohde viscometer.
  • eta rel the relative solution viscosity
  • dichloromethane at a concentration of 5 g/l at 25° C.
  • Ubbelohde viscometer The person skilled in the art is familiar with the determination of the relative solution viscosity using an Ubbelohde viscometer. According to the invention, this is preferably according to DIN 51562-3; conducted 1985-05.
  • the flow times of the polyester carbonate to be measured are measured by the Ubbelohde viscometer in order to then determine the viscosity difference between the polymer solution and its solvent.
  • the Ubbelohde viscometer is first calibrated by measuring the pure solvents dichloromethane, trichlorethylene and tetrachlorethylene (at least 3 measurements and a maximum of 9 measurements are always carried out). The actual calibration then takes place with the solvent dichloromethane. The polymer sample is then weighed, dissolved in dichloromethane and the flow time for this solution is then determined three times. The mean value of the flow times is corrected using the Hagenbach correction and the relative solution viscosity is calculated.
  • the polyester carbonate according to the invention has a content of phenolic OH groups in the range of greater than 50 ppm and less than or equal to 400 ppm, particularly preferably greater than 80 ppm and less than or equal to 350 ppm.
  • This content of phenolic OH groups is preferably determined via infrared spectroscopy. As described above in relation to the OH end groups of the mixture according to the invention, it can also be determined via 111 -NMR. However, the signals may overlap here. It is therefore preferred that the content of phenolic OH groups is determined by means of infrared spectroscopy.
  • the polyester carbonate is preferably dissolved in dichloromethane (2 g / 50 ml) and evaluated by the Band determined at a wave number of 3583 cm 1 .
  • the calibration of the infrared device required for this is known to the person skilled in the art.
  • Ri in formula (1) is hydrogen. It is also preferred that Y in formula (11) is a structure of formula (111).
  • R6 and R7 in formula (111) each independently represent hydrogen or Ci-Ci2-alkyl, particularly preferably hydrogen or Ci-Cx-alkyl and very particularly preferably hydrogen or methyl.
  • Y is introduced into the carbonate group (B) via diphenols which are selected from the group consisting of 4'-dihydroxydiphenyl, 2,2-bis-(4-hydroxyphenyl)propane (bisphenol A) , 2,4-bis(4-hydroxyphenyl)-2-methylbutane, 1,1-bis(4-hydroxyphenyl)-p-diisopropylbenzene, 2,2-bis(3-methyl-4-hydroxyphenyl)-propane , dimethyl bisphenol A, 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, l,l-bis(3,5-dimethyl-4-hydroxyphenyl)-p- diisopropylbenzene and
  • the polyester carbonate according to the invention can be processed as such to form all types of molded parts. It can also be processed with other thermoplastics and/or polymer additives to form thermoplastic molding compounds.
  • the molding compounds and moldings are further subjects of the present invention.
  • the polymer additives are preferably from the group consisting of flame retardants, anti-dripping agents, flame retardant synergists, smoke inhibitors, lubricants and mold release agents, nucleating agents, antistatic agents, conductivity additives, stabilizers (e.g. hydrolysis, heat aging and UV stabilizers and transesterification inhibitors), flow promoters, phase compatibility mediators, dyes and pigments, impact modifiers, fillers and reinforcing materials.
  • thermoplastic molding compositions can be produced, for example, by mixing the polyester carbonate and the other constituents in a known manner and melt-compounding and melt-extruding at temperatures of preferably 200° C. to 320° C. in customary units such as internal kneaders, extruders and twin-shaft screws. In the context of this application, this process is generally referred to as compounding. Thus, by molding compound is meant the product obtained when the ingredients of the composition are melt compounded and melt extruded.
  • the moldings made from the polyester carbonate according to the invention or from the thermoplastic molding compositions containing the polyester carbonate can be produced, for example, by injection molding, extrusion and blow molding processes.
  • Another form of processing is the production of molded parts by deep drawing from previously produced sheets or foils.
  • a process for producing the polyester carbonate according to the invention characterized in that the mixture according to the invention, containing oligoesters, is reacted with a mixture of oligocarbonates by means of melt transesterification.
  • melt transesterification is known per se to a person skilled in the art.
  • Schnell, “Chemistry and Physics of Polycarbonates”, Polymer Reviews, Volume 9, Interscience Publishers, New York, London, Sydney 1964 can be referred to here.
  • this is a process which can be carried out without solvents and/or phosgene.
  • This requires that the mixture containing oligoesters and also the mixture of oligocarbonates are melted.
  • temperatures of 280° C. to 400° C. preferably 300° C. to 390° C., particularly preferably 305° C. to 350 °C and more preferably 310 °C to 340 °C.
  • temperatures of less than 320° C., preferably greater than 280° C. to 315° C. are advantageous with regard to the incorporation of the oligoester block into the polyester carbonate. This applies in particular when mixtures containing oligoesters are used which have a high OH end group content within the range defined according to the invention.
  • a vacuum is applied to shift the reaction equilibrium to the polyester carbonate side.
  • Pressures of 0.001 mbar to 50 mbar are preferably used for this purpose, particularly preferably from 0.005 to 40 mbar, very particularly preferably from 0.02 to 30 mbar and furthermore preferably from 0.03 to 5 mbar.
  • the mixture of oligocarbonates has a phenolic OH group content of from 250 ppm to 2500 ppm, preferably from 500 to 2400 ppm, and particularly preferably from 1000 to 2300 ppm.
  • the determination of the phenolic OH group content has already been described above.
  • the mixture of oligocarbonates has a relative solution viscosity of 1.08 to 1.22, preferably 1.11 to 1.22, particularly preferably 1.13 to 1.20.
  • the determination of the relative solution viscosity has also been described above.
  • the person skilled in the art is able to select the chemical nature of the oligocarbonates in such a way that the carbonate groups (B) of the polyester carbonate according to the invention result.
  • Bisphenol-A-based oligocarbonates are particularly preferred.
  • the process according to the invention is preferred in the absence of a catalyst. This has the advantage that the catalyst does not have to be separated from the polyester carbonate obtained or does not remain in it. Depending on the catalyst, this can affect the stability of the polyester carbonate.
  • the process according to the invention can also be carried out in the presence of a catalyst, particularly preferably in the presence of a basic catalyst.
  • inorganic or organic basic compounds for example lithium, sodium, potassium, cesium, calcium, barium, magnesium, hydroxides, carbonates, halides, phenolates, diphenolates, fluorides, -acetates, -phosphates, hydrogen phosphates, -boranates, nitrogen and phosphorus bases such as tetramethylammonium hydroxide, tetramethylammonium acetate, tetramethylammonium fluoride, tetramethylammoniumtetraphenylboronate, tetraphenylphosphonium fluoride, tetraphenylphosphoniumtetraphenyl borohydride, dimethyldiphenylammonium hydroxide, tetraethyl ammonium hydroxide, cethyltrimethylammonium tetraphenylboranate, cethyltrimethylammonium phenolate, l,8-diazabicyclo[5.4.0]undec-7-ene (
  • Phosphonium catalysts of the formula (VIII) are particularly suitable: where Ra, Rb, Re and Rd are the same or different C1-C10-alkyls, C6-C14-aryls, C7-C15-arylalkyls or C5-C6-cycloalkyls, preferably methyl or C6-C14-aryls, particularly preferred can be methyl or phenyl, and X- can be an anion such as hydroxide, sulfate, bisulfate, bicarbonate, carbonate or a halide, preferably chloride or an alkylate or arylate of the formula -OR, where R is a C6-C14 aryl, C7 -C15-arylalkyl or C5-C6-cycloalkyl, preferably phenyl.
  • catalysts are tetraphenylphosphonium chloride, tetraphenylphosphonium hydroxide and tetraphenylphosphonium phenolate; Tetraphenylphosphonium phenolate is very particularly preferred. Tetrabutylphosphonium acetate is also preferred.
  • These catalysts are preferably used in amounts of 10.sup.2 to 10.times.mol , based on 1 mol of the mixture of oligoesters.
  • the amounts of the alkaline salts used as cocatalyst can be in the range from 1 to 500 ppb, preferably 5 to 300 ppb and particularly preferably 5 to 200 ppb.
  • a polyestercarbonate obtained by the inventive method described above in all disclosed combinations and preferences.
  • FIG. 1 Excerpt from a 13 C-NMR spectrum of a commercial product containing isophthalic acid/terephthalic acid resorcinol ester blocks and BPA, produced by means of phase interface processes
  • Terephthalic acid for synthesis, CAS 100-21-0, Bernd Kraft Duisburg isophthalic acid: 99%, CAS 121-91-5, Sigma-Aldrich resorcinol: 99%, CAS 108-46-3, ABCR
  • Diphenyl carbonate Diphenyl carbonate, 99.5%, CAS 102-09-0; Acros Organics, Geel, Belgium, abbreviated as DPC
  • 4-dimethylaminopyridine 4-(dimethylaminopyridine; >98.0%; purum; CAS 1122-58-3; Sigma-Aldrich, Kunststoff Germany, abbreviated as DMAP
  • Tetrabutylphosphonium acetate CAS-34430-94-9, prepared according to Angewandte Chemie, International Edition, Vol. 48, Issue: 40, 7398-7401; 2009
  • Oligocarbonate Linear bisphenol A oligocarbonate containing phenyl end groups and phenolic OH end groups with a relative solution viscosity of 1.17 was used as the starting material for the production of the polyester carbonate. This oligocarbonate contained no additives such as UV stabilizers, mold release agents or heat stabilizers. The oligocarbonate was produced using a melt transesterification process as described in WO02085967A1 and was removed immediately at the outlet of the first horizontal reactor. The oligocarbonate has a phenolic end group content of 0.16%.
  • the relative solution viscosity (h rc 1; also referred to as eta rel) was determined in dichloromethane at a concentration of 5 g/l at 25 °C using an Ubbelohde viscometer.
  • the oligomer content was also determined via GPC.
  • the signal of the refractive index (R1D) was used.
  • the range of the molecular weight distribution with ⁇ 1000 g/mol was defined as the oligomer range.
  • the range ⁇ 1000 g/mol was evaluated as an area percentage by integration in comparison to the total area of the distribution curve.
  • the ratio of the phenyl end groups to the OH end groups was determined by means of 111 NMR spectroscopy (Bruker, 700 MHz). The measurement was carried out in dichloromethane with tetramethylsiloxane as an internal standard. The area of the peak at approx. 7.4 ppm (2 protons) was related to the area of the peaks between 6.6 and 6.8 ppm (3 protons).
  • the carbonyl carbon shows a shift at 164-165 ppm whereas the isophthalic and/or terephthalic acid resorcinol ester shows a peak at ca. 163-164 ppm.
  • the measurement was carried out on a Bruker Avance 111 HD 600 MHz NMR spectrometer. The measurement was performed in CDCE with tetramethylsilane as the standard.
  • This compound was prepared to unequivocally identify the ester carbon atom signal that characterizes the ester of BPA and terephthalic acid or isophthalic acid. It could be shown that the corresponding signal is at 164.2 to 164.5 ppm.
  • the oligoester prepared with these modified preparation parameters had characteristics similar to the sodium counterpart.
  • the oligoester of Example 6 was dissolved in dichloromethane and then precipitated in methanol.
  • Example 9 The test was carried out analogously to Example 1. In contrast to Examples 2-7, the product had a significantly increased melt viscosity when it was removed. example 9
  • Tetrabutylphosphonium acetate 300ppm
  • Tetrabutylphosphonium acetate 300ppm
  • Example 11 (comparative example) The test was carried out as described in example 10. Notwithstanding, 36.0 g of oligocarbonate (90% by weight) and 4.0 g of oligoester (10% by weight) from Example 1 were used.
  • Example 16 The test was carried out as described in example 10. Notwithstanding, 36.0 g of oligocarbonate (90% by weight) and 4.0 g of oligoester (10% by weight) from example 4 were used.
  • Example 17
  • Example 18 The test was carried out as described in example 10. Notwithstanding, 36.0 g of oligocarbonate (90% by weight) and 4.0 g of oligoester (10% by weight) from example 5 were used.
  • Example 21 The experiment was carried out as described in example 10. Notwithstanding, the oligocarbonate from example 5 was used. Viscosity increase was less compared to the previous examples.
  • Example 24 The experiment was carried out as described in example 10. Notwithstanding, 36.0 g of oligocarbonate (90% by weight) and 4.0 g of oligoester (10% by weight) from Example 8 were used.
  • Example 25
  • Example 26 The test was carried out as described in example 10. Notwithstanding, 36.0 g of oligocarbonate (90% by weight) and 4.0 g of oligoester (10% by weight) from Example 9 were used.
  • Example 2 Experiments with Na-Kat In Example 1, a predominantly OH-terminated oligoester is obtained (0.6% by weight OH).
  • the GPC of the oligoester shows only a few oligomers in the ⁇ 1000 g/mol range.
  • This oligoester was used in Examples 1 and 2.
  • the respective end products show relatively high phenolic OH values - in example 1, 500 ppm are exceeded. This shows that this ester block is less suitable, since products below 500 ppm cannot always be obtained. Even if example 2 has an OH value of less than 500 ppm, the viscosity and thus the molecular weight are very high. It is therefore very likely that the limit of 500 ppm will be exceeded with correspondingly lower molecular weights.
  • Example 2 a low OH content oligoester was prepared (0.2% by weight). This block is predominantly phenyl terminated. However, this block contains significant amounts of oligomers in the ⁇ 1000 g/mol range. As example 13, in which the oligoester block from example 2 was used, shows, the increase in molecular weight is low compared to the other examples. This shows that the reactivity is lower in the case of phenyl-terminated blocks, which have a higher content of oligomers. It was surprising that the desired molecular weight could not be achieved despite the use of a catalyst. In example 3, an oligoester with a relatively high OH content (0.85% by weight) was prepared.
  • This product also has a relatively high oligomer content in the range of ⁇ 1000 g/mol.
  • Example 15 shows that the corresponding polyester carbonate has phenolic OH values of >500 ppm. It is therefore not possible to produce the full range of polyester carbonates with different ester contents.
  • Example 4 shows an oligoester which is predominantly OH-terminated (0.80% by weight OH).
  • Examples 16 and 17 have relatively high molecular weights (without having to use a catalyst) and thus show that OH-terminated blocks have high reactivity.
  • the corresponding end products show high levels of phenolic OH end groups (> 500 ppm) both with an ester block content of 10% and 20%.
  • the ester block obtained from example 4 is precipitated. This reduces the content of phenolic OH end groups from 0.8 to 0.7% by weight.
  • products with acceptable OH contents cannot be produced with this block either (see Examples 18 and 19).
  • an oligoester block with an acceptable OH content is used.
  • Examples 26 and 27 according to the invention also have low OH contents.
  • An oligoester block with 0.2% by weight of phenolic OH groups was used here.

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  • Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Organic Chemistry (AREA)
  • Polyesters Or Polycarbonates (AREA)

Abstract

L'invention concerne un mélange contenant de l'oligoester, des polyestercarbonates comprenant un bloc ester et un procédé de préparation de carbonates de polyester avec un bloc ester par transestérification à l'état fondu.
EP22727952.8A 2021-06-15 2022-06-10 Oligoesters comprenant du résorcinol et de l'acide iso-et/ou téréphtalique, carbonates de polyester correspondants et leur préparation Pending EP4355808A1 (fr)

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US20030139529A1 (en) * 2001-11-02 2003-07-24 General Electric Company Method of making block copolymers by solid state polymerization
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