• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    The subject of the invention is a process for the production of a polyester containing at least one 1,4: 3,6-dianhydrohexitol unit comprising: • a step of introduction into a monomer reactor comprising at least one monomer (A) which is a diacid or a diester and at least one monomer (B) which is a 1,4: 3,6-dianhydrohexitol; A step of introducing into the reactor a catalytic system comprising either a catalyst comprising the germanium element and a catalyst comprising the aluminum element, or a catalyst comprising the germanium and aluminum elements or a mixture of these catalysts; A step of polymerizing said monomers to form the polyester; A step of recovering a polyester composition comprising the polyester and the catalytic system. The invention also relates to a polyester composition containing a catalyst system comprising either a catalyst comprising the germanium element and a catalyst comprising the aluminum element, or a catalyst comprising the elements germanium and aluminum or a mixture of these catalysts and its use to reduce the color of the polyester.
    公开号:FR3027906A1
    申请号:FR1460403
    申请日:2014-10-29
    公开日:2016-05-06
    发明作者:Nicolas Jacquel；Loup Rene Saint；Rimlinger Francoise Fenouillot；Jean-Pierre Pascault；Alain Rousseau
    申请人:Roquette Freres SA；
    IPC主号:
    专利说明:

    [0001] FIELD OF THE INVENTION The present invention relates to a process for the manufacture of polyester comprising at least one 1,4: 3,6-dianhydrohexitol unit, by means of a catalytic system making it possible to reduce the coloration of the polyester thus formed. . The invention also relates to a polyester composition comprising said catalytic system. BACKGROUND OF THE INVENTION Because of their many advantages, plastics have become essential for the mass production of objects. Indeed, because of their thermoplastic nature, one can manufacture at high rates any kind of objects from these plastics. Some aromatic polyesters are thermoplastic and have thermal properties allowing them to be used directly for the manufacture of materials. They include aliphatic diol and aromatic diacid units. Among these aromatic polyesters, mention may be made of polyethylene terephthalate (PET), which is a polyester comprising ethylene glycol and terephthalic acid units, used for example for the manufacture of containers, packaging or textile fibers. PET can be a transparent polymer and thus be useful for making objects whose optical properties are important. It can also be opaque and white in the case where this polymer is semi-crystalline, if the crystallinity and the size of the crystallites are important. It is therefore necessary in both cases that the PET has the lowest color possible. "Monomeric units" means, according to the invention, units included in the polyester which can be obtained after polymerization of a monomer. As regards the ethylene glycol and terephthalic acid units included in the PET, they may be obtained by esterification reaction of ethylene glycol and terephthalic acid, or by a trans-esterification reaction of ethylene glycol and terephthalic acid ester.
    [0002] The development of polyesters from short-term renewable resources has become an ecological and economic imperative in the face of the depletion and rising prices of fossil fuels such as oil. One of the important concerns today in the field of polyesters is therefore to provide polyesters of natural origin (biosourcés). This is particularly true for polyesters comprising aliphatic diol and aromatic acid units. Thus, groups such as Danone or Coca-Cola are now marketing partially biobased PET drink bottles, this PET being made from bio-sourced ethylene glycol. A disadvantage of this PET is that it is only partially biobased, since terephthalic acid is generally derived from fossil resources. However, processes for the synthesis of biobased terephthalic acid and biobased terephthalic acid ester have recently been developed, which allows the manufacture of fully biobased PET. It is thus possible to cite the application WO 2013/034743 A1 which describes in particular such PETs. However, for certain applications or under certain conditions of use, these polyesters do not have all the required properties. Thus, PET modified glycols (PETg) have been developed. These are generally polyesters comprising, in addition to ethylene glycol and terephthalic acid units, cyclohexanedimethanol (CHDM) units. The introduction of this diol in the PET allows it to adapt the properties to the intended application, for example to improve its impact resistance or its optical properties, especially when the PETg is amorphous. Other modified PETs have also been developed by introducing 1,4: 3,6-dianhydrohexitol units into the polyester, in particular isosorbide (PEIT).
    [0003] These modified polyesters have higher glass transition temperatures than unmodified PETs or PETgs comprising CHDM. In addition, 1,4: 3,6-dianhydrohexitols have the advantage that they can be obtained from renewable resources such as starch. These modified polyesters are particularly useful for the manufacture of bottles, films, thick sheets, fibers or articles requiring high optical properties. However, a problem of these PEITs is that they can have a generally important coloration, generally greater than that of PETg or PET, and this even when the amounts of isosorbide used in the manufacture of polyester are very low.
    [0004] In order to solve this problem of high coloration, a process for the preparation of PEIT by melt polymerization has already been described in patent application US 2006/0173154 A1. This process comprises a first esterification step and a second polycondensation step. wherein is used in the esterification step a primary antioxidant and a secondary antioxidant in the polycondensation step. In the examples, a catalyst system comprising germanium and cobalt based catalysts are used. In the patent applications WO2013 / 183873 and WO2013 / 183874 are described processes for the manufacture of polyesters comprising a step of esterification of monomers comprising terephthalic acid, CHDM, isosorbide and additional diol compound in the presence of an esterification catalyst which is a zinc-based compound. This catalyst makes it possible to improve the polymerization reaction kinetics and / or to increase the viscosity of the polymer obtained from this process. In the processes which are exemplified in these two applications, a germanium catalyst is introduced during the polycondensation step. The Applicant has found by carrying out studies on the polymerization catalysts for the production of polyesters containing 1,4: 3,6-dianhydrohexitol units (see examples below), that the polyesters obtained from these processes are not not fully satisfactory, especially in terms of coloring.
    [0005] This coloration may be either very yellow as is the case when using exclusively a germanium-based polycondensation catalyst, or gray when using a catalytic system comprising catalysts based on germanium and based on cobalt . There remains therefore a need to find new processes for the manufacture of polyesters containing 1,4: 3,6-dianhydrohexitol units whose coloration is improved. SUMMARY OF THE INVENTION The subject of the invention is thus a process for producing a polyester containing at least one 1,4: 3,6-dianhydrohexitol unit comprising at least: a step of introduction into a monomer reactor comprising at least one monomer (A) which is a diacid or a diester and at least one monomer (B) which is a 1,4: 3,6-dianhydrohexitol; a step of introducing into the reactor a catalytic system comprising either a catalyst comprising the germanium element and a catalyst comprising the aluminum element, or a catalyst comprising the germanium and aluminum elements or a mixture of these catalysts; a step of polymerizing said monomers to form the polyester; a step of recovering a polyester composition comprising the polyester and the catalytic system. Catalyst systems combining a germanium catalyst with an aluminum-based catalyst have already been described for the manufacture of PET-type polyesters in the application WO 2004/048437. In this application are compared the colors of a polyester obtained from a germanium catalyst with a polyester obtained from a catalyst system comprising a germanium catalyst, an aluminum catalyst and a lithium-based catalyst. If the polycondensation time is significantly reduced, the coloration of the polyester is not improved. On the contrary, the polyester obtained is even more yellow or, in the case where a cobalt-based catalyst is added in the catalytic system, darker. Surprisingly, as demonstrated in the examples, the polyester recovered at the end of the process according to the invention has a lower coloration than that of a polyester obtained from a similar process which differs in the catalytic system used. DETAILED DESCRIPTION OF THE INVENTION The invention relates to a process for producing a polyester containing at least one 1,4: 3,6-dianhydrohexitol unit. This process comprises a step of introducing into a monomer reactor. The monomers introduced into the reactor comprise at least one monomer (A) which is a diacid or a diester and at least one monomer (B) which is a 1,4: 3,6-dianhydrohexitol.
    [0006] By diacid or diester is meant according to the invention a dicarboxylic acid or diester of carboxylic acid. According to a preferred embodiment, the monomer (A) is a diacid or a mixture of diacids. Some diacids, such as phthalic acid or maleic acid, may also be in anhydride form.
    [0007] The diacid may be an aromatic diacid, an aliphatic diacid or a mixture of these diacids.
    [0008] Preferably, the diacid is aromatic. It may be selected from terephthalic acid, isophthalic acid, phthalic acid, 2,6-naphthalene dicarboxylic acid, 1,4-naphthalene dicarboxylic acid, furanedicarboxylic acid, and a mixture of these diacids . Preferably, the aromatic acid is terephthalic acid. The monomer (A) may also be an aliphatic diacid or a mixture of these diacids. The aliphatic diacid may be a saturated or unsaturated aliphatic diacid. The saturated aliphatic diacid can be linear, branched or cyclic. As regards the linear saturated aliphatic diacid, it may be chosen from succinic acid, glutaric acid, adipic acid, pimelic acid, suberic acid, azelaic acid, sebacic acid and their mixtures. Preferably, the linear saturated aliphatic diacid is chosen from succinic acid, adipic acid and their mixture, most preferably succinic acid. As saturated cyclic aliphatic diacid, there may be mentioned 1,4-cyclohexanedioic acid.
    [0009] The monomer (A) may also be an unsaturated aliphatic diacid such as fumaric acid or maleic acid or itaconic acid or a mixture of these diacids. In the case where the monomer (A) is a diester (or a mixture of diesters), the diester is preferably a methyl and / or ethyl diester. The diester may be chosen from the diesters of the diacids mentioned above. Preferably, the diester is an aromatic diacid diester, preferably a diester of terephthalic acid, isophthalic acid, phthalic acid, 2,6-naphthalene dicarboxylic acid, 1,4-naphthalene dicarboxylic acid , furanedicarboxylic acid, or a mixture of these diesters, most preferably a diester of terephthalic acid.
    [0010] According to the invention, it is also possible to use as monomers (A) a mixture of diacid (s) and diester (s). The monomer (B) is a 1,4: 3,6-dianhydrohexitol. As explained above, the 1,4: 3,6-dianhydrohexitols have the disadvantage of causing the coloration of the polyester when using the monomers and manufacturing processes conventionally used for their manufacture. The 1,4: 3,6-dianhydrohexitol may be isosorbide, isomannide, isoidide, or a mixture thereof, preferably isosorbide. Isosorbide, isomannide and isoidide can be obtained respectively by dehydration of sorbitol, mannitol and iditol. With regard to isosorbide, it is marketed by the Applicant under the brand name POLYSORBe P. Preferably, the monomers introduced into the reactor further comprise a diol (C), other than 1,4: 3,6- dianhydrohexitols.
    [0011] The diol (C) may be: an aliphatic diol, especially a linear aliphatic diol (Cl), a cycloaliphatic diol (O 2), a branched aliphatic diol (O 3) or; an aromatic diol (04); or a mixture of these diols.
    [0012] The diol (Cl) is advantageously chosen from ethylene glycol, 1,3-propanediol, 1,4-butanediol, 1,5-pentanediol, 1,6-hexanediol, 1,8-octanediol, 1,10-decanediol, or a mixture of these diols, preferably ethylene glycol, 1,4-butanediol and a mixture of these diols, very preferably ethylene glycol. The diol (O 2) may be cyclobutanediol, for example tetramethylcyclobutanediol, bis-hydroxymethyltricyclodecane or cyclohexanedimethanol, in particular 1,4-cyclohexanedimethanol, 1,2-cyclohexanedimethanol or 1,3-cyclohexanedimethanol, or a mixture thereof. diols or isomers of these diols. Indeed, these diols can be in cis or trans configuration. When different isomers exist for the same monomer, unless explicitly specified, when speaking of this monomer, it may be an isomer of this monomer or a mixture of isomers. The diol (03) can be 2-methyl-1,3-propanediol, 2,2,4-trimethyl-1,3-pentanediol, 2-ethyl-2-butyl-1,3-propanediol , propylene glycol, neopentyl glycol or a mixture of these diols.
    [0013] The diol (C) is advantageously chosen from aliphatic diols, preferentially chosen from ethylene glycol, 1,3-propanediol, 1,4-butanediol, 1,5-pentanediol, 1,6-hexanediol, 1,8-octanediol, 1,10-decanediol, 1,4-cyclohexanedimethanol, 1,2-cyclohexanedimethanol, 1,3-cyclohexanedimethanol and mixtures of these diols, most preferably ethylene glycol, 1, 4-butanediol, 1,4-cyclohexanedimethanol and mixtures of these diols, most preferably ethylene glycol, 1,4-cyclohexanedimethanol and the mixture of these diols.
    [0014] According to a first advantageous variant in which the diol (C) is introduced into the reactor, the monomer (A) is terephthalic acid, the monomer (B) is isosorbide and the monomer (C) is ethylene glycol. According to a second advantageous variant in which the diol (C) is introduced into the reactor, the monomer (A) is terephthalic acid, the monomer (B) is isosorbide and the diol (C) is a mixture of ethylene glycol and 1,4-cyclohexanedimethanol. Advantageously, the molar percentage of monomers (A) relative to the total number of moles of monomers (A), (B) and optionally (C) ranges from 25 to 50%, preferably from 33 to 49%, most preferably from 40 to 48%. Preferably, when monomers (C) are introduced into the reactor, the molar percentage of (B), relative to the total number of moles of monomers (B) and (C), ranges from 1 to 50%, preferably from 2 to 30%, most preferably 5 to 20%. The monomers (B) and (C) can be introduced into the reactor in the form of an aqueous solution. Monomers other than the monomers (A), (B) and optionally (C), so-called "additional monomers" may also be added. It may be hydroxy acid monomers bearing a hydroxide function and a carboxylic acid function. By way of example, the hydroxy acid may be glycolic acid, lactic acid, hydroxybutyric acid, hydroxycaproic acid, hydroxyvaleric acid, 7-hydroxyheptanoic acid or 8-hydroxyoctanoic acid, 9-hydroxynonanoic acid, hydroxymethylfurancarboxylic acid, hydroxybenzoic acid or a mixture of these hydroxy acids. Additional monomers that may be used include dilactones such as glycolide or lactide. Preferably, the amount of hydroxy acid monomer is, based on the total sum of the monomers, less than 10 mol%. The monomers introduced into the reactor may be free of hydroxy acid monomers. The additional monomers may also comprise chain-lengthening monomers, which in turn are generally introduced into the reactor before or during the formation of the polyester produced during the polymerization stage, or before a second stage called the "post-stage" stage. polymerization "of reacting the polyester formed in the polymerization step with the chain extender monomer. This post-polymerization step may in particular be a reactive extrusion step of the chain-extending monomer with the polyester recovered after the polymerization step.
    [0015] By "chain-extending monomers" is meant a monomer comprising two functions other than the hydroxyl, carboxylic acid and carboxylic acid ester functions, and capable of reacting with these same functions. The functions may be isocyanate, isocyanurate, lactam, lactone, carbonate, epoxy, oxazoline and imide functions, said functions possibly being identical or different. As chain-extending monomers which can be used in the present invention, mention may be made of: diisocyanates, preferably methylenediphenyl diisocyanate (MDI), isophorone diisocyanate (IPDI), dicyclohexylmethane diisocyanate (H12MDI), toluene diisocyanate (TDI), naphthalene diisocyanate (NDI), hexamethylene diisocyanate (HMDI) or lysine diisocyanate (LDI), aliphatic diisocyanate of molar mass 600 g / mol obtained from di-fatty acid dimers (DD101410 Diisocyanate), dimers, trimers and tetramers of diisocyanates, the so-called "isocyanate-free" prepolymers resulting from a reaction of a diol or an amine on a diisocyanate under conditions such that the prepolymer contains an isocyanate function at each of its ends (α, f functional or telechelic polymer) without the free diisocyanate being detectable, the dialkylcarbonates, especially the dialkylcarbonates of dianhydrohexitols, and especially isosorbide dialkylcarbonates, dicarbamoylcaprolactams, preferably 1,1'-carbonyl-bis-caprolactam, dicarbamoylcaprolactones, diepoxides, compounds having an epoxide function and a halide function, preferably epichlorohydrin, heterocyclic compounds. preferably bis-oxazolines, bisoxazolin-5-ones and bis-azalactones, methylenic or ethylenic diester derivatives, preferably methyl or ethyl carbonate derivatives, any mixtures of any two or more the aforesaid goods.
    [0016] Preferably, the amount of chain-lengthening monomers is, based on the sum total of the monomers introduced, less than 10 mol%. The monomers introduced into the reactor may be free of chain extender monomer. The additional monomers may also be polyfunctional monomers. By "polyfunctional monomers" is meant a monomer capable of reacting with the hydroxide and / or carboxylic acid and / or carboxylic acid ester functions and whose functionality is greater than 2. The polyfunctional monomers may be introduced into the reactor before the reaction. polymerization or post-polymerization step as described above (the polyfunctional monomer then replacing the chain-extending monomer), preferably before the polymerization step. The reactive functions of these branching agents may be hydroxide, carboxylic acid, anhydride, isocyanate, isocyanurea, caprolactam, caprolactone, carbonate, epoxy, oxazoline and imide functions, said functions possibly being identical or different, preferably carboxylic acid, hydroxide epoxide or isocyanate, most preferably carboxylic acid or hydroxide. The functionality of these branching agents can be from 3 to 6, preferably from 3 to 4. Among the branching agents conventionally used, mention may be made of: malic acid, citric or isocitric acid, tartaric acid, trimesic acid, tricarballylic acid, cyclopentane tetracarboxylic acid, trimellitic anhydride, pyromellitic mono or dianhydride, glycerol, pentaerythritol, dipentaerythritol, monoanhydrosorbitol, monoanhydromannitol, epoxidized oils, dihydroxystearic acid, trimethylolpropane, ethers of these polyols, for example glycerol propoxylate (marketed under the name Voranol 450 by Dow Chemical), polymers having lateral epoxide functional groups, triisocyanates, tetraisocyanates and the respective homopolymers of di-, existing tri- and tetraisocyanates, polyanhydrides, alkoxysilanes, preferably tetraethoxysilane.
    [0017] Preferably, the amount of polyfunctional monomers is, based on the total sum of the monomers, less than 10 mol%. The monomers introduced into the reactor may be free of polyfunctional monomers. Advantageously, with respect to all the monomers introduced into the reactor, the molar amount of additional monomer is less than 20%, preferably less than 10%, or even less than 5%. The monomers introduced into the reactor may be free of additional monomers.
    [0018] The process according to the invention also comprises a step of introducing into the reactor a catalytic system comprising: either a catalyst comprising the germanium element and a catalyst comprising the aluminum element; or a catalyst comprising the elements germanium and aluminum; or a mixture of these catalysts. According to the first variant, as regards the catalyst comprising the germanium element, it may be chosen from the following compounds: the aliphatic carboxylic acid salts such as formate, acetate, propionate, butyrate, oxalate, acrylate, methacrylate, the salts of aromatic carboxylic acids such as benzoate, halogenated carboxylic acid salts such as trichloroacetate, trifluoroacetate, hydroxycarbonate salts such as lactate, citrate, oxalate, mineral salts such as carbonate, sulfate, nitrate, phosphate, phosphonate, phosphinate , hydrogen sulphate, hydrogencarbonate, hydrogen phosphate, sulphite, thiosulfate, hydrochloride, hydrobromide, chloride, chlorate, bromide, bromate, organosulfonates such as 1-propane sulphonate, 1-pentane sulphonate, naphthalene sulphonate, organic sulphates such as lauryl sulphate, alkoxides such as methoxy, ethoxy, propoxy, iso-propoxy, butoxy, acetylacetonates, oxides, mixed oxides comprising other metals or hydroxides, preferably germanium dioxide. The catalyst comprising the aluminum element may be chosen from the following compounds: aliphatic carboxylic acid salts such as formate, acetate, propionate, butyrate, oxalate, acrylate, methacrylate, salts of aromatic carboxylic acids such as benzoate, salts of halogenated carboxylic acids such as trichloroacetate, trifluoroacetate, hydroxycarbonate salts such as lactate, citrate, oxalate, mineral salts such as carbonate, sulfate, nitrate, phosphate, phosphonate, phosphinate, hydrogen sulfate, hydrogencarbonate, hydrogen phosphate, sulfite, thiosulfate, hydrochloride, hydrobromide, chloride, chlorate, bromide, bromate, organosulfonates such as 1-propane sulfonate, 1-pentane sulfonate, naphthalene sulfonate, organic sulfates such as lauryl sulfate, alkoxides such as methoxy, ethoxy, propoxy , iso-propoxy, butoxy, acetylacetonates, oxides, mixed oxides including other metals or hydroxides, preferably aluminum triethoxide.
    [0019] According to the second variant, the catalytic system comprises a catalyst comprising the elements germanium and aluminum, for example comprises a mixed oxide of aluminum and germanium. According to a third variant, the catalytic system comprises a mixture of the catalysts described in the two previous variants. The catalytic system may be chosen so that the molar element ratio Ge: Al is from 0.05: 1 to 500: 1, advantageously from 0.2 to 300: 1, preferably from 0.33: 1 to 1 , 25: 1. It is stated that this elemental ratio only takes into consideration the metals included in the catalytic system.
    [0020] According to the first and third variants, the catalysts may be selected and present in amounts such that the molar element ratio Ge: Al is that described above. According to the second variant, the catalyst comprising the germanium and aluminum element is chosen such that the molar element ratio Ge: Al is that described above. The catalyst system may further include additional metals. According to an advantageous embodiment of the invention, the catalytic system comprises the cobalt element, that is to say that: the catalytic system further comprises an additional catalyst comprising the cobalt element; or at least one of the catalysts comprising the germanium element and / or the aluminum element further comprises the cobalt element. The use of a catalytic system comprising the cobalt element makes it possible in particular to obtain polyester compositions having improved b * coloring.
    [0021] By way of example of additional catalyst comprising the cobalt element, mention may be made of the following compounds: aliphatic carboxylic acid salts such as formate, acetate, propionate, butyrate, oxalate, acrylate, methacrylate, carboxylic acid salts aromatics such as benzoate, halogenated carboxylic acid salts such as trichloroacetate, trifluoroacetate, hydroxycarbonate salts such as lactate, citrate, oxalate, mineral salts such as carbonate, sulfate, nitrate, phosphate, phosphonate, phosphinate, hydrogen sulfate, hydrogencarbonate, hydrogenphosphate, sulfite, thiosulfate, hydrochloride, hydrobromide, chloride, chlorate, bromide, bromate, organosulfonates such as 1-propane sulfonate, 1-pentane sulfonate, naphthalene sulfonate, organic sulfates such as lauryl sulfate, alkoxides such as methoxy , ethoxy, propoxy, iso-propoxy, butoxy, acetylacetonates, oxides, mixed oxides including other metals or hydroxides, preferably cobalt acetate. When at least one of the catalysts comprising the germanium element and / or the aluminum element further comprises the cobalt element, this catalyst may be a mixed oxide of aluminum, germanium and cobalt; a mixed oxide of aluminum and cobalt; or a mixed oxide of germanium and cobalt.
    [0022] For the sake of simplicity and availability of the catalysts, it is preferred to use a catalytic system of a catalyst system comprising a catalyst comprising the germanium element and a catalyst comprising the aluminum element. Advantageously, the total mass quantity of metal included in the catalytic system introduced into the reactor, relative to the total mass quantity of polymer obtained, ranges from 50 to 500 ppm. The catalyst system may be introduced into the reactor before or during the polymerization step, preferably before the polymerization step. It can be introduced by different stages of introduction, for example by introducing different catalysts at different times. Preferably, when the catalyst system comprises different catalysts, they are introduced simultaneously into the reactor, most preferably simultaneously and before the polymerization step. The catalyst or catalysts may be used in the state or in the form of solution (s), in particular aqueous or alcoholic solution, preferably in the form of a solution in a monomer such as ethylene glycol, in which is (are) diluted (s). or dispersed (s) the catalyst (s). The process according to the invention also comprises a step of polymerizing the monomers to form the polyester. Advantageously, this polymerization step is carried out by molten means, that is to say by keeping the reaction medium in the molten state in the reactor, in the absence of solvent. This polymerization step can be done by supplying heat of heat. This polymerization step can also be done under vacuum. Preferably, the polymerization step of the monomers comprises: a first stage during which the reaction medium is stirred at a temperature ranging from 220 to 310 ° C in order to form oligomers, advantageously from 245 to 275 ° C .; a second stage during which the oligomers formed are stirred under vacuum at a temperature ranging from 240 ° to 330 ° C. in order to form the polyester, advantageously from 255 ° to 275 ° C. The reaction medium may be stirred with any type of stirrer conventionally used for the synthesis of polyesters. The stirring rate can be kept constant during the polymerization step or the stirring rate can be reduced during the reaction, as the viscosity of the polyester increases. The first stage can be carried out at atmospheric pressure or under pressure, generally at a pressure ranging from 1.1 to 10 bar. Oligomers formed in the first stage generally have a number average molecular weight of less than 5000 g / mol, often less than 4000 g / mol. They generally have a viscosity index of less than 20 ml / g. The monitoring of this first stage can be done by controlling the evolution of the quantity of distillates extracted from the reactor. As regards the second stage of the polymerization step, it is carried out under vacuum, preferably at a pressure of less than 10 mbar, most preferably less than 1 mbar. The monitoring of the polymerization reaction can be done by controlling the evolution of the amount of torque measured on the stirrer or by any other system for evaluating the viscosity of the molten reaction medium. Advantageously, the catalytic system, comprising the catalyst or catalysts described above, is introduced into the reactor before the first stage of the polymerization stage. Preferably, the process comprises a reactor deoxygenation step carried out prior to the monomer polymerization step, and in particular before the first oligomer formation stage, advantageously by placing the reactor under an inert gas such as nitrogen. This deoxygenation step is generally carried out at low temperature, that is to say often at a temperature below 100 ° C. This can be done by performing at least once a sequence of a vacuum stage, for example between 100 and 700 mbar in the reactor followed by a stage of introduction of an inert gas into the reactor, for example between 1 , 2 and 2 bars. This empty cycle-introduction of inert gas can be done for example from 3 to 5 times. Preferably, this vacuum-nitrogen cycle is carried out at a temperature between 60 and 80 ° C so that the reagents, and especially the monomers (B), are completely melted. This deoxygenation step has the advantage of further improving the coloring properties of the polyester obtained at the end of the process. When the reactor is evacuated, especially during the second stage of oligomer polymerization, it should be noted that a small portion of the monomers can be extracted from the reactor and thus be lost. It is in particular a small part of the most volatile monomers and in excess. This loss of monomers can also result in the entrainment of a slight loss of catalyst. In addition, it is also possible to introduce into the reactor before the polymerization stage additives known as "polymerization additives".
    [0023] Among the polymerization additives, mention may be made of antioxidants which make it possible to further reduce the coloring of the polyester obtained. The antioxidants may be primary and / or secondary antioxidants. The primary antioxidant can be a sterically hindered phenol such as the compounds Hostanox® 0 3, Hostanox® 010, Hostanox® 016, Ultranox® 210, Ultranox®276, Dovernox® 10, Dovernox® 76, Dovernox® 3114 Irganox® 1010, Irganox® 1076 or a phosphonate such as Irgamod® 195. The secondary antioxidant may be trivalent phosphorus compounds such as Ultranox® 626, Doverphos® S-9228, Hostanox® P-EPQ, or Irgafos 168. It is also possible to introduce as polymerization additive into the reactor at least one compound capable of limiting spurious etherification reactions, such as sodium acetate, tetramethylammonium hydroxide, or tetraethylammonium hydroxide. The method according to the invention also comprises a step of recovering a polyester composition comprising the polyester and the catalytic system. This composition can be recovered by extracting it from the reactor in the form of a melted polymer rod. After cooling, this rod can be converted into granules using conventional granulation techniques.
    [0024] The polyester obtained at the end of the polycondensation step may, after cooling, be semi-crystalline or amorphous. The method according to the invention may also comprise, after the step of recovering the polyester composition, a solid state polycondensation step (PCS). Those skilled in the art can easily perform this PCS step from semicrystalline polyesters. The subject of the invention is also the polyester composition obtainable according to the process of the invention, in which the polyester contains at least one 1,4: 3,6-dianhydrohexitol unit, the composition further comprising a catalyst system comprising either a catalyst comprising the germanium element and a catalyst comprising the aluminum element, or a catalyst comprising the elements germanium and aluminum or a mixture of these catalysts The catalyst system included in the polyester composition, is identical to that described above for the process according to the invention. Thus, in the polyester composition according to the invention, the metals included in the catalytic system may have a molar element ratio Ge: Al which ranges from 0.05: 1 to 500: 1, advantageously from 0.2 to 300: 1 preferably, from 0.33: 1 to 1.25: 1. The amounts of catalyst in the polyester composition are also close but may be slightly lower than those introduced into the reactor, due to the possible loss in entrainment of catalyst described above. However, these losses can be considered relatively small. The total mass of metal included in the catalytic system of the polyester composition, based on the total mass quantity of polyester, is generally from 30 to 500 ppm.
    [0025] The metal amounts of the catalysts included in the polyester can be determined by elemental analysis. "Monomeric units" means, according to the invention, units included in the polyester which can be obtained after polymerization of a monomer. By way of example, with regard to the ethylene glycol and terephthalic acid units included in a PET, they may be obtained by esterification reaction of ethylene glycol and terephthalic acid, or by a transesterification reaction of ethylene glycol and terephthalic acid ester.
    [0026] The polyester included in the composition according to the invention may comprise, relative to all the diol units (B) and optionally (C) of the polyester, from 0.1 to 100% of 1,4: 3 units, 6-dianhydrohexitol (100% is the case where no monomer (C) is used in the process), advantageously from 1 to 50%, preferably from 2 to 30%, most preferably from 5 to 20%. According to a first most preferred variant, the polyester included in the composition comprises, with respect to the sum of the monomeric units: 45 to 55% of terephthalic acid units; from 1 to 25% of isosorbide; from 20 to 54% of ethylene glycol. According to a second most preferred variant, the polyester included in the composition comprises, relative to the sum of the monomeric units: 45 to 55% of terephthalic acid units; from 1 to 25%) isosorbide units; from 1 to 53% of ethylene glycol units; from 1 to 53% of 1,4-cyclohexanedimethanol units. The number of diacid units and the number of diol units are generally substantially identical. The ratio of diol units / diacid units included in the polyester can range from 1.15 / 1 to 0.85 / 1, often from 1.08 / 1 to 0.92 / 1.
    [0027] The amounts of different units in the polyester can be determined by 1 H NMR. Those skilled in the art can easily find the conditions of analysis to determine the amounts in each of the patterns of the polyester. For example, from an NMR spectrum of a poly (ethylene-co-isosorbide terephthalate), the chemical shifts relative to ethylene glycol are between 4.4 and 5.0 ppm, the chemical shifts relating to the cycle terephthalate are between 7.8 and 8.4 ppm and chemical shifts relative to isosorbide are between 4.1 ppm and 5.8 ppm. The integration of each signal makes it possible to determine the quantity of each pattern of the polyester. Preferably, the polyester composition has a clarity L * greater than 45, preferably greater than 55. In the case where a solid state polycondensation step is carried out, the clarity L * can reach or even exceed 65.
    [0028] Preferably, the polyester composition has a color b * of between -10 and 10, preferably between -6 and 6. This parameter makes it possible to quantify the color ranging from blue (if b * is negative) to yellow (if b * is positive). The parameters L * and b * can be determined using a spectrophotometer, using the CIE Lab model. The polyester composition may have a relative viscosity greater than 35 mL / g, preferably greater than 50 mL / g. The viscosity number can be determined according to the method described in the Examples section. The number-average molecular weight of the polyester included in the polyester composition according to the invention may range from 5000 to 50000 g / mol. The molar mass of the polyester can be determined by conventional methods, for example by steric exclusion chromatography (SEC) in a mixture of chloroform and 1,1,1,3,3,3-Hexafluoro-2-propanol. in a 98/2 volume ratio. The signal detection can then be performed by a differential refractometer calibrated with methyl polymethacrylate standards. Preferably, the glass transition temperature of the polyester is greater than or equal to 80 ° C. The glass transition temperature of the polyester can be measured by conventional methods, especially using differential scanning calorimetry (DSC) using a heating rate of 10 K / min. The experimental protocol is detailed in the examples section below. Advantageously, the polyester has a glass transition temperature ranging from 80 to 190 ° C. The invention also relates to a composition comprising the polyester according to the invention and at least one additive or at least one additional polymer or at least one mixture thereof.
    [0029] The polyester composition according to the invention may comprise the polymerization additives possibly used during the process. It may also comprise other additives and / or additional polymers which are generally added during a subsequent thermomechanical mixing step. As an example of an additive, there may be mentioned charges or fibers of organic or inorganic nature, nanometric or non-functional, functionalized or not. It can be silicas, zeolites, fibers or glass beads, clays, mica, titanates, silicates, graphite, calcium carbonate, carbon nanotubes, wood fibers, of carbon fibers, polymer fibers, proteins, cellulosic fibers, lignocellulosic fibers and non-destructured granular starch. These fillers or fibers can improve the hardness, rigidity or permeability to water or gases. The composition may comprise from 0.1 to 75% by weight filler and / or fibers relative to the total weight of the composition, for example from 0.5 to 50%. The additive useful for the composition according to the invention may also comprise opacifying agents, dyes and pigments. They can be selected from cobalt acetate and the following compounds: HS-325 Sandoplast® RED BB (which is a compound carrying an azo function also known as Solvent Red 195), HS-510 Sandoplast® Blue 2B which is an anthraquinone, Polysynthren® Blue R, and Clariant® RSB Violet. The composition may also include as an additive a process agent, or processing aid, to reduce the pressure in the processing tool. A release agent to reduce adhesion to polyester forming materials such as molds or calender rolls can also be used. These agents can be selected from esters and fatty acid amides, metal salts, soaps, paraffins or hydrocarbon waxes. Specific examples of these agents are zinc stearate, calcium stearate, aluminum stearate, stearamide, erucamide, behenamide, beeswax or candelilla waxes. The composition according to the invention may also comprise other additives such as stabilizing agents, for example light stabilizing agents, UV stabilizing agents and heat stabilizing agents, fluidifying agents, flame retardants and antistatic agents.
    [0030] The composition may further comprise an additional polymer, different from the polyester according to the invention. This polymer may be chosen from polyamides, polyesters other than the polyester according to the invention, polystyrene, styrene copolymers, styrene-acrylonitrile copolymers, styrene acrylonitrile-butadiene copolymers, polymethyl methacrylates, acrylic copolymers, poly (ether-imides), phenylene polyoxides such as (2,6-dimethylphenylene) polyoxide, phenylene polysulfate, poly (ester-carbonates), polycarbonates, polysulfones, polysulfone ethers, polyether ketones and mixtures of these polymers.
    [0031] The composition may also comprise, as additional polymer, a polymer making it possible to improve the impact properties of the polymer, in particular functional polyolefins such as functionalized ethylene or propylene polymers and copolymers, core-shell copolymers or block copolymers.
    [0032] The composition according to the invention may also comprise polymers of natural origin, such as starch, cellulose, chitosans, alginates, proteins such as gluten, pea proteins, casein, collagen, gelatin, lignin, these polymers of natural origin may or may not be physically or chemically modified. The starch can be used in destructured or plasticized form.
    [0033] In the latter case, the plasticizer may be water or a polyol, in particular glycerol, polyglycerol, isosorbide, sorbitans, sorbitol, mannitol or else urea. In order to prepare the composition, use may especially be made of the process described in document WO 2010/0102822 A1. The composition according to the invention may be manufactured by standard thermoplastic transformation methods. These conventional methods include at least one step of melt blending or softening of the polymers and a step of recovering the composition. This method can be carried out in internal mixers with blades or rotors, external mixers, co-rotating or counter-rotating twin screw extruders. However, it is preferred to carry out this mixture by extrusion, in particular by using a co-rotating extruder. The mixture of the constituents of the composition can be carried out under an inert atmosphere. In the case of an extruder, the various constituents of the composition can be introduced by means of introducing hoppers located along the extruder. The invention also relates to an article comprising the polyester or the composition according to the invention. This article can be of any type and be obtained using conventional transformation techniques. This may be, for example, fibers or yarns useful for the textile industry or other industries. These fibers or yarns can be woven to form fabrics or nonwovens.
    [0034] The article according to the invention can also be a film, a sheet. These films or sheets can be manufactured by calendering techniques, cast film extrusion, extrusion blow molding. The article according to the invention may also be a container for transporting gases, liquids and / or solids. It may be bottles, gourds, bottles, for example bottles of sparkling water or not, bottles of juice, bottles of soda, bottles, bottles of alcoholic beverages, vials, for example bottles of medicine, bottles of cosmetic products, dishes, for example for ready meals, microwave dishes or lids.
    [0035] These containers can be of any size. They can be manufactured by extrusion blow molding, thermoforming or injection blow molding. These articles can also be optical articles, that is to say articles requiring good optical properties such as lenses, disks, transparent or translucent panels, optical fibers, films for LCD screens or even windows. These optical articles have the advantage of being able to be placed near sources of light and therefore of heat, while maintaining excellent dimensional stability and good resistance to light. The articles may also be multilayer articles, at least one layer of which comprises the polymer or the composition according to the invention. These articles can be manufactured by a process comprising a coextrusion step in the case where the materials of the different layers are brought into contact in the molten state. By way of example, mention may be made of tube coextrusion techniques, coextrusion of profiles, coextrusion blow molding (in English "blowmolding") of bottles, flasks or tanks, generally grouped under the term coextrusion blow molding of hollow bodies, coextrusion inflation also called blowing of sheath (in English "film blowing") and co-extrusion flat ("in English" cast coextrusion "). They can also be manufactured by a process comprising a step of applying a polyester layer in the molten state to a layer based on organic polymer, metal or adhesive composition in the solid state. This step may be carried out by pressing, overmolding, lamination or lamination, extrusion-rolling, coating, extrusion-coating or coating.
    [0036] The invention also relates to the use of the catalytic system previously described in a polymerization process for reducing the coloration of a polyester containing at least one 1,4: 3,6-dianhydrohexitol unit. It is specified that all the embodiments described above, which concern the process and the polyester composition according to the invention, are applicable to the use according to the invention. The invention will now be illustrated in the examples below. It is specified that these examples do not limit the present invention.
    [0037] EXAMPLES The properties of the polymers were studied with the following techniques: The reduced viscosity in solution is evaluated using a Ubbelohlde capillary viscometer at 25 ° C. in an equimassic mixture of phenol and orthodichlorobenzene after dissolution of the polymer. at 130 ° C with stirring. For these measurements, the polymer concentration introduced is 5 g / l. The color of the polymer was measured on the granules using a Konica Minolta CM-2300d spectrophotometer.
    [0038] For the illustrative examples presented below the following reagents were used: Monomer Monomers (A): Terephthalic acid (purity 99 +%) of Accros Monomer (B): Isosorbide (purity> 99.5%) Polysorb® P de Roquette Brothers Monomer (C): Ethylene Glycol (purity> 99.8%) of Sigma-Aldrich Catalysts Titanium butoxide (> 97%) from Sigma Aldrich Germanium dioxide (> 99.99%) from Sigma Aldrich Aluminum triethoxide ( > 97%) Sigma Aldrich n-Butyltin oxide hydroxide (95%) from ABCR GmbH Molybdenum trioxide (> 99.5%) from Sigma Aldrich Cobalt acetate tetrahydrate (99.999%) from Sigma Aldrich35 Irgamode 195 polymerization additives from BASF SE: BASF SE lrganox 1010 Antioxidant: Clariant Hostanox PEPQ Antioxidant: Antioxidant Sigma Aldrich Phosphoric Acid (99.999 +%): Antioxidant Sodium Acetate Trihydrate (Purity> 99.0%): Additive of polymerization limiting the etherification reactions Tetraethylammonium hydroxide solution 40% in water of Sigma Aldrich: polymerization additive limiting the etherification reactions Preparation of the polyesters: Example 1: In a 7.5L reactor are added 893.8 g (14.4 mol) of ethylene glycol, 701.1 g (4.8 mol) of isosorbide, 2656.1 g (16.0 mol) of terephthalic acid, 0.181 g of sodium acetate and 0.707 g of Irgamod 195. 0.394 g of germanium dioxide (Ge = 80ppm) and 1.216g of aluminum triethoxide (ie Al = 6Oppm) are also introduced as catalysts.
    [0039] To extract the residual oxygen from the isosorbide crystals, 4 vacuum-nitrogen cycles are carried out at 60 to 80 ° C. The reaction mixture is then heated to 260 ° C (4 ° C / min) under 5.7 bar pressure and with constant stirring (150 rpm). The esterification rate is estimated from the amount of distillate collected. Then, the pressure is reduced to 0.7 mbar in 90 minutes and the temperature brought to 270 ° C. These conditions of vacuum and temperature were maintained until a torque increase of 15 nm with respect to the initial torque. The necessary polycondensation time is reported in the Table below. Finally, a polymer rod is poured through the bottom valve of the reactor, cooled in a thermo-regulated water tank and cut into granules of about 15 mg.
    [0040] The thus obtained poly (ethylelene-co-isosorbide) terephthalate resin has a reduced solution viscosity of 55.8 ml / g and a molar mass of 10 300 g.mol -1. The resulting polymer granules are pale yellow and have the following staining characteristics: L * = 56.7, a * = 0.0 and b * = 9.4.35 Example 2-6 and Counter-Examples 1-7: For the Example series 2 to 13, identical synthesis conditions were used except for the nature and proportions of catalysts. These conditions are given in Table 1.
    [0041] Table 1: Summary of manufacturing tests for poly (ethylene-co-isosorbide) terephthalate. TI red Color (min) (mL / g) M-1 (ppm) M2 (ppm) M3 (ppm) L * a * b * CExl Ge 80 - - - - 288 56.2 Yellow 52.3 0.7 12 , 6 Exl Ge 80 Al 60 - - 260 55.8 Pale yellow 56.7 0.0 9.4 Ex2 Ge 120 Al 45 - - 240 54.9 Pale yellow 60.9 0.2 9.8 CEx2 Ge 200 - - - - 223 54.6 Yellow 59.0 0.4 11.2 Ex3 Ge 200 Al 60 - - 207 54.8 Pale yellow 61.0 0.0 9.4 Ex4 Ge 200 Al 150 - - 213 53.4 Pale Yellow 60.8 0.1 7.4 CEx3 Ge 80 Co 30 - - 287 56.2 Gray 45.2 0.3 3.9 CEx4 Ge 200 Co 30 - - 222 54.1 Gray 44.9 0.3 3.8 CEx5 Ge 80 MB 106 - - 200 52.2 Black 37.5 0.2 -0.5 CEx6 Ti 8 Al 60 - - 310 53.8 Orange 54.3 1.8 13.6 ECx7 Sn 120 Al 60 - - 173 55.9 Dark orange 49.1 2.9 11.2 Ex5 Ge 80 Al 60 Co 15 256 55.5 Gray 45.9 0.5 5.7 Ex6 Ge 80 Al 60 Co 30 254 51.8 Gray 46.8 0.5 2.0 Example 7: In a 7.5L reactor are added 422.1 g (6.8 mol) of ethylene glycol, 418.2 g (2.9 mol) of isosorbide 1143.6 g (7.9 mol) of 1,4-cyclohexanedimethanol, 2656.0 g (16.0 mol) of terephthalic acid, 0.60 g of tetraethylammonium hydroxide and 1.94 g of 1010. 0.703 g of germanium dioxide (ie Ge = 126 ppm) and 0.538 g of cobalt acetate tetrahydrate (33 ppm) are also introduced as catalysts. To extract the residual oxygen from the isosorbide crystals, 4 vacuum-nitrogen cycles are carried out at 60 to 80 ° C. The reaction mixture is then heated at 250 ° C (4 ° C / min) under 2.5 bar pressure and with constant stirring (150 rpm). The esterification rate is estimated from the amount of distillate collected. Then the pressure is reduced to atmospheric pressure in 30min. At atmospheric pressure, 0.71 g of aluminum triethoxide (ie Al = 30 ppm), 0.42 g of phosphoric acid and 1.95 g of Hostanox PEPQ are added to the reactor. The pressure is then reduced to 0.7 mbar in 30 minutes and the temperature brought to 265 ° C. These conditions of vacuum and temperature were maintained for 220min until a torque increase of 12Nm compared to the initial torque. Finally, a polymer rod is poured through the bottom valve of the reactor, cooled in a thermo-regulated water tank and cut into granules of about 15 mg. The resin thus obtained has a reduced solution viscosity of 61.5 ml / g. The polymer granules obtained are gray and have the following color characteristics: L * = 48.8 a * = -0.4 and b * = 0.3.
    [0042] The examples show that the use of aluminum in addition to germanium makes it possible to significantly reduce the color of the final polymer nred constant). This is remarkable by comparing the CEX1 tests with Ex1 for which there is an increase in the L * parameter and a decrease in the parameters a * and b *. The same observations made with higher levels of catalysts 200ppm Ge (Cex2, Ex3, Ex4) or with Co in addition to Ge and Al (Ex6 and CEx3) lead to similar observations in terms of color. Tests CEx 5, Cex6 and Cex7 show the interest of the Ge / Al mixture compared with other metal mixtures: - The Ge / Mo mixture (CEx.5) which is another catalytic system used in WO 2004/048437 leads to a black polymer. In the ECx6 example, the addition of aluminum to titanium does not make it possible to obtain a catalytic synergy comparable to the Ge / Al pair, the polymerization is much longer and the final polymer is very colored. It is specified that 8 ppm Ti is a customary amount used for PET synthesis. Finally, the ECx 7 test shows that the use of tin in combination with aluminum also does not make it possible to obtain a polymer with a weak coloration. Example 7 shows another way of conducting the invention this time using a mixture of diols including ethylene glycol, isosorbide and cyclohexanedimethanol.
    权利要求:
    Claims (18)
    [0001]
    REVENDICATIONS1. A method of manufacturing a polyester containing at least one 1,4: 3,6-dianhydrohexitol unit comprising at least: - a step of introducing into a monomer reactor comprising at least one monomer (A) which is a diacid or a diester and at least one monomer (B) which is a 1,4: 3,6-dianhydrohexitol; a step of introducing into the reactor a catalytic system comprising either a catalyst comprising the germanium element and a catalyst comprising the aluminum element, or a catalyst comprising the germanium and aluminum elements or a mixture of these catalysts; a step of polymerizing said monomers to form the polyester; a step of recovering a polyester composition comprising the polyester and the catalytic system. 15
    [0002]
    2. The manufacturing method according to claim 1, characterized in that the monomer (A) is an aromatic monomer, preferably selected from terephthalic acid, isophthalic acid, phthalic acid, 2,6-naphthalene acid. dicarboxylic acid, 1,4-naphthalene dicarboxylic acid, a furanedicarboxylic acid, a mixture of these diacids, a diester of these diacids and a mixture of these diesters.
    [0003]
    3. The manufacturing method according to claim 2, characterized in that the monomer (A) is terephthalic acid or a terephthalic acid diester. 25
    [0004]
    4. Manufacturing process according to any one of claims 1 to 3, characterized in that said monomers further comprise at least one diol (C), other than 1,4: 3,6-dianhydrohexitols, especially a diol selected from aliphatic diols, preferably one selected from ethylene glycol, 1,3-propanediol, 1,4-butanediol, 1,5-pentanediol, 1,6-hexanediol, 1,8-octanediol, 1,10-decanediol, 1,4-cyclohexanedimethanol, 1,2-cyclohexanedimethanol, 1,3-cyclohexanedimethanol and a mixture of these diols, most preferably ethylene glycol, 1,4-butanediol, 1,4-cyclohexanedimethanol and a mixture of of these diols, most preferably ethylene glycol, 1,4-cyclohexanedimethanol and a mixture of these diols.
    [0005]
    5. Manufacturing process according to any one of claims 1 to 4, characterized in that the step of polymerization of said monomers comprises: - a first stage during which the reaction medium is stirred at a temperature ranging from 220 to 310 ° C to form oligomers, preferably 245 to 275 ° C; a second stage during which the oligomers formed are stirred under vacuum at a temperature ranging from 240 ° to 330 ° C. in order to form the polyester, advantageously from 255 ° to 275 ° C.
    [0006]
    6. Method according to any one of claims 1 to 5, characterized in that the catalytic system is introduced into the reactor before the polymerization step.
    [0007]
    7. Manufacturing process according to any one of claims 1 to 6, characterized in that the catalytic system is chosen so that the molar element ratio Ge: Al is from 0.05: 1 to 500: 1, advantageously from 0.2 to 300: 1, preferably from 0.33: 1 to 1.25: 1.
    [0008]
    8. Manufacturing process according to any one of claims 1 to 7, characterized in that the catalytic system further comprises an additional catalyst comprising the cobalt element or at least one of the catalysts comprising the germanium element and / or the aluminum element further comprises the cobalt element.
    [0009]
    9. Manufacturing process according to any one of claims 1 to 8, characterized in that the total mass of metal included in the catalyst system, based on the total mass of polymer obtained, ranges from 50 to 500 ppm.
    [0010]
    10. Process according to any one of claims 1 to 9, characterized in that a deoxygenation step of the reactor is carried out prior to the polymerization step of the monomers, preferably by placing the reactor under an inert gas such as nitrogen, for example by conducting at least once a sequence of a vacuum stage in the reactor followed by a stage of introduction of an inert gas into the reactor.
    [0011]
    11. Method according to any one of claims 1 to 10, characterized in that the molar percentage of monomer (A) relative to the total number of moles of monomers (A), (B) and where appropriate (C) is from 25 to 50%, preferably from 33 to 49%, most preferably from 40 to 48%.
    [0012]
    12. Method according to any one of claims 1 to 11, characterized in that the 1,4: 3,6-dianhydrohexitol is isosorbide.
    [0013]
    A polyester composition comprising: - a polyester containing at least one 1,4: 3,6-dianhydrohexitol unit and - a catalytic system comprising either a catalyst comprising the germanium element and a catalyst comprising the aluminum element, or a catalyst comprising germanium and aluminum elements or a mixture of these catalysts.
    [0014]
    14. The polyester composition according to claim 13, characterized in that it has a clarity L * greater than 45, preferably greater than 55.
    [0015]
    15. A polyester composition according to claim 13 or 14, characterized in that it has a color b * between -10 and 10, preferably between -6 and 6.
    [0016]
    16. Polyester composition according to any one of claims 13 to 15, characterized in that it has a reduced viscosity greater than 35 mL / g, preferably greater than 50 mL / g.
    [0017]
    An article comprising the polyester composition of any one of claims 13 to 16.
    [0018]
    18. Use of a catalyst system comprising a catalyst comprising the germanium element and a catalyst comprising the aluminum element, a catalyst comprising the elements germanium and aluminum or a mixture of these catalysts to reduce the color of a polyester containing at least one 1,4: 3,6-dianhydrohexitol unit.
    类似技术:
    公开号 | 公开日 | 专利标题
    EP3212692A1|2017-09-06|Method for producing a polyester containing at least one 1,4:3,6-dianhydrohexitol unit with improved colouring
    EP3298064A1|2018-03-28|High-viscosity polyester with improved impact properties
    EP3119831B1|2019-10-02|Polyesters comprising 2,5-furandicarboxylate and saturated diol units having a high glass transition temperature
    EP3143068B1|2018-05-02|Thermoplastic aromatic polyesters comprising tetrahydrofuran-dimethanol and furandicarboxylic acid motifs
    WO2017093684A1|2017-06-08|Thermoplastic copolyesters comprising 1,4 : 3,6-dianhydrohexitol and various aromatic diacids
    EP3861050A1|2021-08-11|Method for preparing a polyester of the poly| type
    FR3105232A1|2021-06-25|Process for the manufacture of a polyester containing at least one 1,4: 3,6-dianhydrohexitol unit with reduced coloration and the rate of incorporation of said unit improved
    WO2019073169A1|2019-04-18|Thermoplastic polyester with high incorporation of 1,4:3,6-dianhydro-l-iditol units
    WO2019158885A1|2019-08-22|Thermoplastic polyester having improved resistance to the phenomenon of cracking
    EP3140339A1|2017-03-15|Thermoplastic aromatic polyesters comprising tetrahydrofuran-dimethanol motifs
    同族专利:
    公开号 | 公开日
    CN107148438B|2020-02-28|
    JP6688792B2|2020-04-28|
    FR3027906B1|2017-01-06|
    WO2016066956A1|2016-05-06|
    EP3212692A1|2017-09-06|
    MX369523B|2019-11-11|
    MX2017005664A|2017-07-26|
    US20170335055A1|2017-11-23|
    CA2965900A1|2016-05-06|
    CN107148438A|2017-09-08|
    SG11201703370TA|2017-05-30|
    KR20170076672A|2017-07-04|
    US10400062B2|2019-09-03|
    JP2017533320A|2017-11-09|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US6020421A|1998-09-01|2000-02-01|Unitika Ltd.|Polyester composition and method for producing the same|
    WO2006032022A1|2004-09-14|2006-03-23|E.I. Dupont De Nemours And Company|Processes for making low color poly terephthalate polymers|
    FR2888851A1|2005-07-25|2007-01-26|Tergal Fibres Sa|CATALYTIC SYSTEM FOR THE MANUFACTURE OF POLYESTER BY POLYCONDENSATION, PROCESS FOR THE MANUFACTURE OF POLYESTER|
    JP2013166874A|2012-02-16|2013-08-29|Toyobo Co Ltd|Copolymerized polyester resin, and coating, coating agent, and adhesive using the same|WO2018024993A1|2016-08-03|2018-02-08|Roquette Freres|Semi-crystalline thermoplastic polyester for producing bioriented films|
    CN110573558A|2017-05-05|2019-12-13|罗盖特公司|Method for producing composite material|US6063464A|1998-04-23|2000-05-16|Hna Holdings, Inc.|Isosorbide containing polyesters and methods for making same|
    JP2003306538A|2002-04-15|2003-10-31|Toyobo Co Ltd|Polyester, polyester molded article composed thereof and method for producing the same|
    US6953768B2|2002-11-26|2005-10-11|Teck Cominco Metals Ltd.|Multi-component catalyst system for the polycondensation manufacture of polyesters|
    JP5511129B2|2007-06-25|2014-06-04|三井化学株式会社|Production method of polyester resin|
    FR2934272B1|2008-07-24|2013-08-16|Roquette Freres|PROCESS FOR THE PREPARATION OF COMPOSITIONS BASED ON AMYLACEOUS MATERIAL AND SYNTHETIC POLYMER|
    FR2965814B1|2010-10-08|2012-11-16|Roquette Freres|PLASTIFICATION OF ALIPHATIC POLYESTERS BY ALKYLIC ESTERS OF DIANHYDROHEXITOLS|
    KR101769560B1|2011-03-29|2017-08-18|에스케이케미칼주식회사|Polyester resin copolymerized with lactic acid and isosorbide and preparing method thereof|
    JP5676533B2|2011-08-25|2015-02-25|富士フイルム株式会社|Biaxially stretched polyester film, method for producing the same, and solar cell module|
    WO2013034950A1|2011-09-08|2013-03-14|Société Anonyme Des Eaux Minerales D'evian|Method for producing a bio-pet polymer|
    KR101952941B1|2012-06-05|2019-02-27|에스케이케미칼 주식회사|Polyester resin and preparation method of the same|
    KR101969004B1|2012-06-05|2019-04-15|에스케이케미칼 주식회사|Polyester resin and preparation method of the same|
    CN105392816A|2013-05-21|2016-03-09|艾斯特工业有限公司|Heat resistant polyethylene terephthalate and a process for the preparation of the same|US10696778B1|2017-01-26|2020-06-30|Novol, Inc.|Methods of making polymers using isosorbide|
    US11168158B2|2017-03-06|2021-11-09|Braskem America, Inc.|Electron donors for ziegler-natta precatalyst preparation and catalyst system for olefin polymerization|
    FR3065957B1|2017-05-05|2019-07-12|Roquette Freres|THERMOPLASTIC COMPOSITE|
    FR3072094B1|2017-10-11|2020-09-04|Roquette Freres|HIGHLY INCORPORATED THERMOPLASTIC POLYESTER IN THE PATTERN 1,4: 3,6-DIANHYDRO-L-IDITOL|
    FR3078069B1|2018-02-19|2020-09-04|Roquette Freres|THERMOPLASTIC POLYESTER WITH IMPROVED RESISTANCE TO THE CRACKING PHENOMENON|
    EP3626759A1|2018-09-21|2020-03-25|Erfindergemeinschaft Lorenz + Grahneis GbR|High-temperature-up-resinsbased on cyclic and non-cyclic raw materials |
    KR20200036301A|2018-09-28|2020-04-07|에스케이케미칼 주식회사|Polymer resin composition|
    FR3105232B1|2019-12-20|2021-12-24|Roquette Freres|Method for manufacturing a polyester containing at least one 1,4: 3,6-dianhydrohexitol unit with reduced coloring and improved rate of incorporation of said unit|
    法律状态:
    2015-11-02| PLFP| Fee payment|Year of fee payment: 2 |
    2016-05-06| PLSC| Publication of the preliminary search report|Effective date: 20160506 |
    2016-10-28| PLFP| Fee payment|Year of fee payment: 3 |
    2017-10-31| PLFP| Fee payment|Year of fee payment: 4 |
    2018-10-30| PLFP| Fee payment|Year of fee payment: 5 |
    2019-10-31| PLFP| Fee payment|Year of fee payment: 6 |
    2020-10-30| PLFP| Fee payment|Year of fee payment: 7 |
    2021-10-29| PLFP| Fee payment|Year of fee payment: 8 |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1460403A|FR3027906B1|2014-10-29|2014-10-29|METHOD FOR MANUFACTURING POLYESTER CONTAINING AT LEAST ONE IMPROVED COLORATION 1,4: 3,6-DIANHYDROHEXITOL|FR1460403A| FR3027906B1|2014-10-29|2014-10-29|METHOD FOR MANUFACTURING POLYESTER CONTAINING AT LEAST ONE IMPROVED COLORATION 1,4: 3,6-DIANHYDROHEXITOL|
    CA2965900A| CA2965900A1|2014-10-29|2015-10-28|Method for producing a polyester containing at least one 1,4:3,6-dianhydrohexitol unit with improved colouring|
    KR1020177010817A| KR20170076672A|2014-10-29|2015-10-28|Method for producing a polyester containing at least one 1,4:3,6-dianhydrohexitol unit with improved colouring|
    US15/522,726| US10400062B2|2014-10-29|2015-10-28|Method for producing a polyester containing at least one 1,4:3,6-dianhydrohexitol unit with improved colouring|
    JP2017523298A| JP6688792B2|2014-10-29|2015-10-28|Process for producing a polyester containing at least one 1,4: 3,6-dianhydrohexitol unit with improved coloration|
    SG11201703370TA| SG11201703370TA|2014-10-29|2015-10-28|Method for producing a polyester containing at least one 1,4:3,6-dianhydrohexitol unit with improved colouring|
    CN201580058584.0A| CN107148438B|2014-10-29|2015-10-28|Process for producing polyesters containing at least one 1,4:3, 6-dianhydrohexitol unit with improved coloration|
    EP15797131.8A| EP3212692A1|2014-10-29|2015-10-28|Method for producing a polyester containing at least one 1,4:3,6-dianhydrohexitol unit with improved colouring|
    MX2017005664A| MX369523B|2014-10-29|2015-10-28|Method for producing a polyester containing at least one 1,4:3,6-dianhydrohexitol unit with improved colouring.|
    PCT/FR2015/052901| WO2016066956A1|2014-10-29|2015-10-28|Method for producing a polyester containing at least one 1,4:3,6-dianhydrohexitol unit with improved colouring|
    [返回顶部]