EP3976688A1 - Procédé de production de mélanges de polyoxyalkylène polyols - Google Patents

Procédé de production de mélanges de polyoxyalkylène polyols

Info

Publication number
EP3976688A1
EP3976688A1 EP20725571.2A EP20725571A EP3976688A1 EP 3976688 A1 EP3976688 A1 EP 3976688A1 EP 20725571 A EP20725571 A EP 20725571A EP 3976688 A1 EP3976688 A1 EP 3976688A1
Authority
EP
European Patent Office
Prior art keywords
polyoxyalkylene polyol
koh
autoclave
starter substance
mixture
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
EP20725571.2A
Other languages
German (de)
English (en)
Inventor
Klaus Lorenz
Elena ROJO-WIECHEL
Elena FRICK-DELAITTRE
Martin MARAZITA
Reinhard Albers
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 Intellectual Property GmbH and Co KG
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 Intellectual Property GmbH and Co KG filed Critical Covestro Intellectual Property GmbH and Co KG
Publication of EP3976688A1 publication Critical patent/EP3976688A1/fr
Pending legal-status Critical Current

Links

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
    • C08G65/00—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule
    • C08G65/02—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring
    • C08G65/26—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
    • C08L71/00—Compositions of polyethers obtained by reactions forming an ether link in the main chain; Compositions of derivatives of such polymers
    • C08L71/02—Polyalkylene oxides
    • 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
    • C08G18/00—Polymeric products of isocyanates or isothiocyanates
    • C08G18/06—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen
    • C08G18/28—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen characterised by the compounds used containing active hydrogen
    • C08G18/40—High-molecular-weight compounds
    • C08G18/48—Polyethers
    • C08G18/4804—Two or more polyethers of different physical or chemical nature
    • 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
    • C08G18/00—Polymeric products of isocyanates or isothiocyanates
    • C08G18/06—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen
    • C08G18/70—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen characterised by the isocyanates or isothiocyanates used
    • C08G18/72—Polyisocyanates or polyisothiocyanates
    • 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
    • C08G65/00—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule
    • C08G65/02—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring
    • C08G65/32—Polymers modified by chemical after-treatment
    • C08G65/329—Polymers modified by chemical after-treatment with organic compounds
    • C08G65/331—Polymers modified by chemical after-treatment with organic compounds containing oxygen
    • C08G65/332—Polymers modified by chemical after-treatment with organic compounds containing oxygen containing carboxyl groups, or halides, or esters thereof

Definitions

  • the present invention relates to a process for the direct production of mixtures of short-chain, high-functionality polyoxyalkylene polyols and long-chain, low-functionality polyoxyalkylene polyols.
  • the short-chain, high-functionality polyoxyalkylene polyol component is obtained by alkylene oxide addition onto high-functionality H-functional starter compounds, while the long-chain, low-functionality polyoxyalkylene polyol component is correspondingly obtained by alkylene oxide addition onto low-functionality H-functional starter compounds.
  • Highly functional H -functional starter compounds in the context of the invention are understood to mean compounds which have on average at least three Zerewitinoff-active hydrogen atoms (i.e., for example, via hydroxyl and / or amine functionality).
  • Low-functional H-functional starter compounds in the context of the invention are understood to mean compounds which on average have a maximum of 3 Zerewitinoff-active hydrogen atoms (i.e., for example, via hydroxyl and / or amine functionality
  • a hydrogen bonded to N, O, or S is referred to as Zerewitinoff-active hydrogen if it produces methane by reacting with methyl magnesium iodide according to a process discovered by Zerewitinoff.
  • Typical examples of compounds with Zerewitinoff-active hydrogen are compounds which contain carboxyl, hydroxyl, amino, imino or thiol groups as functional groups.
  • Polyol formulations that contain polyether polyols produced on the basis of highly functional starter compounds such as sugar, oligo- and polysaccharides, sugar alcohols (such as mannitol or sorbitol) and pentaerythritol are generally used in polyurethane applications, in particular for the production of rigid polyurethane foams that are used for the insulation of Refrigeration devices, refrigerated containers, pipes or even for building insulation.
  • highly functional starter compounds such as sugar, oligo- and polysaccharides, sugar alcohols (such as mannitol or sorbitol) and pentaerythritol
  • Polyol formulations based on such polyoxyalkylene polyols produced on the basis of highly functional starter compounds can be processed with polyisocyanates to form rigid foams, whereby insulating elements made from them (such as refrigerator housings or insulating panels) can be quickly removed from the foam molds without any significant deformation of the insulating elements.
  • rigid foams obtained on the basis of such polyol formulations should have sufficient adhesion to all types of outer layers and should also be able to dissolve the amount of physical blowing agent (alkanes, cycloalkanes, fluorocarbons, partially fluorinated olefins and the like) necessary to achieve the desired bulk density.
  • the individual components of such formulations have a sufficiently low viscosity, this facilitates the handling of the substances for example in the production of the formulations which usually contain several individual polyol components.
  • These components have average functionalities of more than 3.5, preferably more than 4, particularly preferably 5 or higher, and their molar mass equivalents are below 190 g / mol, preferably below 160 g / mol.
  • These highly functional and short-chain components are usually obtained by reacting melts of highly functional starter compounds such as sorbitol or mixtures of such highly functional components with reactive co-starters such as glycerol or glycols with alkylene oxides.
  • highly functional starter compounds such as sorbitol or mixtures of such highly functional components with reactive co-starters such as glycerol or glycols with alkylene oxides.
  • sugars e.g. octafunctional sucrose
  • sucrose A disadvantage of the use of sucrose is that it can only be melted with decomposition.
  • No. 4,332,936 proposes the use of solvents to suspend the solid starters.
  • aromatic hydrocarbons are used for the same purpose.
  • a disadvantage in both cases is that valuable reactor volume for the Solvents must be made available and for reasons of sustainability and product hygiene the use of organic solvents is generally undesirable.
  • DE 1 276 622 B1 uses very short-chain adducts of starter compounds with alkylene oxides as suspending agents or solvents for the production of alkylene oxide adducts of high-melting / high-functionality starter compounds.
  • the lack of a polyoxyalkylene polyol with a low OH number results in products with very high viscosities according to the method of DE 1 276 622 B1.
  • DD 147469 other low molecular weight but more easily meltable costarters such as TMP or glycerine are also used in the addition of alkylene oxide to sucrose.
  • sucrose is reacted with alkylene oxides in the presence of other OH- or NH-functional co-starters, possibly together with starch or cellulose.
  • costarters can also have "very different" molar masses, but these costarters are not discussed in greater detail.
  • DD 219204 only low molecular weight costarters are used.
  • alcohol condensates are used as co-starters / solvents for solid or very highly viscous starter compounds which have been obtained by acid-catalyzed reactions, i.e. essentially oligomeric polyethers obtained via acid catalysis.
  • the problem to be solved in DE 4209358 was to deal with side reactions which, when using high-functionality starter compounds which are solid or highly viscous at room temperature, can occur in alkylene oxide addition reactions and lead, for example, to discoloration or difficulties in the work-up of the polyoxyalkylene polyol (high residual potassium content with KOH catalysis) suppress.
  • the object is achieved by using small amounts (0.51-5%, based on the total batch) of alkoxylatable aliphatic amines in addition to the actual starters. It is true that other liquid, low-molecular co-starters can also be used, but nothing is said about their structure.
  • the state of the art therefore does not have a production process which enables a homogeneous, single-phase mixture of one or more low-functional long-chain polyoxyalkylene polyol components and short-chain, higher-functional polyoxyalkylene polyol components to be obtained directly, with the resulting polyoxyalkylene polyol mixtures having technically manageable viscosities that are immediate Allow further processing into secondary products such as polyurethanes.
  • the direct production of such a mixture involves combining the two polyoxyalkylene polyol components, i.e.
  • first building block consisting of one or more low-functional long-chain polyoxyalkylene polyols and a second building block consisting of one or more short-chain, higher-functional polyoxyalkylene polyols building block in situ during the addition of the alkylene oxide (s) to the short-chain ( n) highly functional starter component (s) understood.
  • the object of the present invention was therefore to provide a direct, simplified process for the production of a single-phase, homogeneous mixture of one or more low-functional long-chain polyoxyalkylene polyol component (s) and at least two short-chain, higher-functional polyoxyalkylene polyol components with technically for immediate further sale work on secondary products, such as polyurethanes, to provide manageable viscosities.
  • this object was achieved by a process for the production of a polyoxyalkylene polyol mixture comprising at least 3 polyoxyalkylene polyols (a) (b) and (c), the mean OH number of the polyoxyalkylene polyol mixture being 290-560 mg KOH / g and the OH number has been determined in accordance with DIN 53240, the calculated mean OH number of the polyoxyalkylene polyols (b) and (c) being at least 360 mg KOH / g and the polyoxyalkylene polyol mixture by reacting a mixture comprising at least one polyoxyalkylene polyol (a), at least one H-functional starter substance (b ') and at least one H-functional starter substance (c') with an OH-reactive compound is optionally obtained in the presence of a catalyst, the process comprising the following steps i) providing a mixture (i) comprising the polyoxyalkylene polyol (a), the H-functional starter substance (b '), and the
  • the mixture (i) is reacted with the OH-reactive compound in step (ii) in the presence of a catalyst, this being a basic, a Brönsted acidic, a Lewis acidic and / or a double metal cyanide catalyst, preferably a basic one Catalyst is.
  • a catalyst this being a basic, a Brönsted acidic, a Lewis acidic and / or a double metal cyanide catalyst, preferably a basic one Catalyst is.
  • the functionality F (a) of 2 to 3 of the polyoxyalkylene polyol (a) is a hydroxyl functionality (OH functionality).
  • Suitable polyoxyalkylene polyols (a) have average starter functionalities between 2 and 3.
  • suitable polyoxyalkylene polyols (a) can be prepared by adding alkylene oxides to hydroxyl-containing starter compounds (a ') such as, for example, ethylene glycol, 1,2-propylene glycol, 1,3-propylene glycol, the various isomers of butanediol, the various isomers of hexanediol, or even cyclic diols how the various isomers of cyclohexanediol are obtained.
  • hydroxyl-containing starter compounds (a ') such as, for example, ethylene glycol, 1,2-propylene glycol, 1,3-propylene glycol, the various isomers of butanediol, the various isomers of hexanediol, or even cyclic diols how the various isomers of cyclohexanediol are obtained.
  • Trifunctional or mixed-functional starter compounds are, for example, trimethylolpropane, glycerol and castor oil.
  • Suitable starter compounds for obtaining polyoxyalkylene polyols (a) are also starter compounds containing amine groups such as triethanolamine, diethanolamine and ethanolamine, as well as N-methylethanolamine, N-methyldiethanolamine, N-alkylamines or N-alkylamines, which in turn carry further tertiary amino groups in the alkyl residue, such as, for example N, N-dimethylaminopropylamine.
  • An average starter functionality between 2 and 3 can also be set, for example, by using mixtures of di- and trifunctional starter compounds (a ‘).
  • Such medium starter functionalities by mixing bifunctional starter compounds with starter compounds which have a functionality of greater than 3.
  • Such starter compounds are, for example, pentaerythritol, sorbitol or ethylenediamine.
  • Suitable starter substances (b ') and (c') have functionalities of 3 to 8.
  • compounds selected from the group consisting of glycerol, trimethylolpropane (TMP), triethanolamine, mono-, oligo- and polysaccharides, pentaerythritol, dipentaerythritol, tripentaerythritol, sorbitol, cyclic polyols such as inositol, polyamines, such as, for example, compounds based on highly functional compounds are suitable polynuclear aniline / formaldehyde condensation products (“polymeric MDA”), isomers or isomer mixtures of toluenediamine (in particular 2,4-TDA, 2,6-TDA, 2,3-TDA, 3,4-TDA) and aliphatic amines such as ethylenediamine .
  • polymeric MDA polynuclear aniline / formaldehyde condensation products
  • Short-chain alkylene oxide adducts of such starter compounds can also be used, albeit less preferably.
  • Sucrose, sorbitol, glycerol, TMP, the isomers of tolylenediamine and / or ethylenediamine are preferably used as starter substances (b ') and (c'), very particularly preferably sucrose, sorbitol, glycerol and TMP. It is particularly preferred that one of the starter substances (b ') or (c') is sucrose.
  • the calculated number-average functionality of the mixture of the H-functional starter substances (b ') and (c') is at least 4.5 and preferably at least 5.
  • At least one of the starter substances (b ') and (c') has a melting point of less than 150 ° C.
  • the H-functional starter substances (b ') and (c') preferably have OH and / or NH numbers of greater than 800 mg KOH / g.
  • the at least one starter compound (b ‘) and the at least one starter compound (c‘) are suspended, dispersed or dissolved in the at least one polyoxyalkylene polyol (a) in a reactor system suitable for carrying out alkylene oxide addition reactions.
  • the ratio between the two starter compounds on the one hand and the at least one polyoxyalkylene polyol (a) can of course be varied.
  • the ratio chosen depends on the one hand on the desired product mix, on the other hand, of course, sufficient stirrability of the suspension, dispersion or the solution of the starter compounds in the at least one polyoxyalkylene polyol (a) must be ensured, so that i) uniform conversion of the starter compounds (b ') and (c') takes place with the alkylene oxides and thus ii) the heat of reaction that occurs can be dissipated sufficiently effectively.
  • the procedure is preferably such that the proportion of the at least one polyoxyalkylene polyol (a) in the finished product, i.e.
  • the mixture of the at least one polyolxyalkylene polyol (a), the at least one polyoxyalkylene polyol (b) and the at least one polyoxyalkylene polyol (c) is 2 to 30 wt .% is.
  • the arithmetic mean functionality of the mixture of the at least one starter compound (b) and the at least one starter compound (c ‘) is between 4.5 and 7.5, preferably between 5.0 and 7.5.
  • a catalyst is added to the suspension, dispersion or solution of the at least one starter compound (b ') and the at least one starter compound (c') in the at least one polyoxyalkylene polyol (a).
  • DMC compounds double metal cyanide compounds
  • DMC catalysts for example in US 5,470,813, US 6,696,383, EP-A 0 700 949, EP-A 0 743 093, EP-A 0 761 708, WO-A 97/40086, WO-A 98/16310 and WO -A 00/47649, have a high activity in alkylene oxide addition reactions on starter compounds with Zerewitinoff-active hydrogen atoms and allow the production of polyether polyols at very low catalyst concentrations (100 ppm or less), so that the separation of the DMC catalyst from the polyether polyol before its processing into polyurethanes, e.g. B. polyurethane foams, is no longer required. This significantly increases the profitability of technical polyether polyol production.
  • the process according to the invention can also be catalyzed by Lewis acids such as, for example, boron trifluoride etherate.
  • Lewis acids such as, for example, boron trifluoride etherate.
  • the basic catalyst is an alkali metal hydroxide, alkaline earth metal hydroxide and / or amine, preferably an amine.
  • Basic catalysts such as alkali metal hydrides, alkali metal carboxylates (for example those of monofunctional carboxylic acids), alkali metal hydroxides, alkali metal alkoxides (for example those of monofunctional alcohols) or amines are preferably used in the process according to the invention.
  • An overview of amines suitable for the process according to the invention is given by M. Ionescu et al. in "Advances in Urethanes Science and Technology", 1998, 14, pp. 151-218.
  • Alkali metal hydroxides such as sodium hydroxide, potassium hydroxide or cesium hydroxide
  • amines are particularly preferably used as basic catalysts in the process according to the invention.
  • the alkali metal hydroxides can be used as a solid or as highly concentrated aqueous solutions.
  • Amines are very particularly preferably used as catalysts in the process according to the invention, among these in turn preferably imidazole or alkyl-substituted imidazole derivatives (such as, for example, N-methylimidazole).
  • the basic catalysts are generally preferred in an amount of 0.004 to 0.8% by weight, based on the amount of end product (ie the polyoxyalkylene polyol mixture to be prepared comprising at least 3 polyoxyalkylene polyols (a) (b) and (c)) 0.004 to 0.2 wt .-% used.
  • end product ie the polyoxyalkylene polyol mixture to be prepared comprising at least 3 polyoxyalkylene polyols (a) (b) and (c)) 0.004 to 0.2 wt .-% used.
  • catalysts based on alkali metal hydroxide or when using N-methyldiethanolamine it should be noted that small amounts of dihydroxy-functional polyether molecules can arise during the alkylene oxide addition reaction.
  • the water which is introduced when the aqueous catalyst solution is added and the water formed during the reaction of the Zerewitinoff-active hydrogens with the alkali metal hydroxide can also be separated off by a (possibly vacuum-assisted) distillation step before the addition of the alkylene oxide. If there is an amine under the at least one starter compound (b ‘) or the at least one starter compound (c‘), the addition of the catalyst to the reaction mixture can also be delayed, ie. H. only after a certain amount of alkylene oxide has been added to the catalyst-free reaction mixture.
  • an OH-reactive compound preferably an alkylene oxide, preferably under inert gas atmosphere, dosed.
  • the alkylene oxide is preferably at least one selected from the group consisting of ethylene oxide, propylene oxide, 1,2-butylene oxide, 2,3-butylene oxide and styrene oxide. Ethylene oxide, propylene oxide or a mixture of propylene oxide and ethylene oxide are particularly preferred.
  • the alkylene oxides can be added to the reaction mixture individually, as a mixture or in succession.
  • the polyoxyalkylene polyol mixtures produced contain polyether chains with block structures. Products with ethylene oxide end blocks are characterized, for example, by an increased proportion of primary end groups, which give the polyoxyalkylene polyol mixture increased reactivity towards isocyanates.
  • the choice of the alkylene oxide used in each case and the decision about its arrangement within the polyether chains are made with regard to the desired properties of the polyoxyalkylene polyol mixture. It is very particularly preferred to use propylene oxide exclusively for the preparation of the polyoxyalkylene polyol mixtures.
  • the polyoxyalkylene polyols (a) are produced in situ directly before the addition of the at least one starter compound (b ') and the at least one starter compound (c') in the same reactor in which the production of the Polyoxyalkylene polyol mixtures according to the invention takes place.
  • suitable starter compounds (a ') which have already been mentioned by way of example, are initially reacted with alkylene oxides at least partially in the presence of catalysts in the reactor system suitable for carrying out alkylene oxide addition reactions, in the absence of starter compounds (b') and (c '), until the desired molecular weight of the polyoxyalkylene polyol (a) is reached.
  • the at least one starter compound (b ‘) and the at least one starter compound (c‘) are added and the alkylene oxide addition, optionally with the addition of further catalyst, is continued until the desired polyoxyalkylene polyol mixture is obtained.
  • triglycerides such as soybean oil, rapeseed oil, palm kernel oil, palm oil, linseed oil, sunflower oil, herring oil, sardine oil, lesquerella oil and castor oil or other fatty acid esters according to EP 1923417 can be added to the process in amounts of 10-50% by weight, based on the final product amount, can be added.
  • triglycerides or fatty acid esters without hydroxyl groups are used here, the amount corresponding to the triglyceride or fatty acid ester can be used with the OH number remaining the same Save alkylene oxide.
  • Polyoxyalkylene polyester polyol mixtures are obtained in whose structure the oils are completely incorporated by transesterification reactions running parallel to the alkylene oxide addition, so that they can no longer be detected in the end product, or only in very small amounts.
  • the OH-reactive compounds in particular alkylene oxides
  • the OH-reactive compounds are fed continuously to the reactor in the usual manner in such a way that the safety-related pressure limits of the reactor system used are not exceeded.
  • care must be taken that a sufficient inert gas partial pressure is maintained in the reactor during the start-up and metering phase. This can be set, for example, using noble gases or nitrogen.
  • the alkylene oxides can be fed into the reactor in different ways: Dosing into the gas phase or directly into the liquid phase is possible, e.g. B. via a dip tube or a distribution ring located near the reactor bottom in a well-mixed zone.
  • the metering units When metering into the liquid phase, the metering units should be designed to be self-draining, for example by making the metering bores on the underside of the distributor ring.
  • a backflow of reaction medium into the lines and metering units carrying alkylene oxide or into the alkylene oxide storage containers can be prevented by means of apparatus, for example by installing non-return valves.
  • the reaction with the OH-reactive compounds, preferably the alkoxylation is preferably carried out at a temperature of 70 to 170.degree. C., particularly preferably at a temperature of 100 to 150.degree.
  • the temperature can be varied within the limits described during the alkylene oxide metering phase: In order to achieve an optimal balance between high alkylene oxide conversion and low by-product formation when using sensitive starter compounds (such as sucrose), initially at low reaction temperatures (for example at 70 to 110 ° C) are alkoxylated, and only when there is sufficient starter conversion (ie as soon as at least 50% by weight of the starter compounds used have reacted with alkylene oxide on at least one Zerewitinoff-active hydrogen atom) are transferred to higher reaction temperatures (for example to 110 to 130 ° C). Post-reactions can optionally be carried out at higher temperatures (ie after the temperature has been raised to 100 to 170 ° C., preferably 100 to 150 ° C.).
  • the temperature of the exothermic alkylene oxide addition reaction is kept at the desired level by cooling.
  • cooling generally takes place via the reactor wall (e.g. double jacket , Half-pipe coil) as well as by means of further internal im Reactor and / or heat exchanger surfaces arranged externally in the pumping circuit, for example on cooling coils, cooling plugs, plate, tube bundle or mixer heat exchangers.
  • agitators should ensure thorough mixing of the reactor contents in all reaction phases, with stirrers arranged in one or more stages or stirrer types operating over a large area being particularly suitable (see, for example, Apparatus Manual; Vulkan-Verlag Essen, 1st edition (1990), pp. 188-208).
  • Technically particularly relevant here is a mixing power entered on average over the entire reactor content, which is generally in the range from 0.2 to 5 W / 1, with correspondingly higher local power inputs in the area of the stirring elements themselves and possibly at lower fill levels.
  • baffles e.g.
  • the stirring power of the mixing unit can also be varied depending on the level during the dosing phase in order to ensure a particularly high energy input in critical reaction phases. For example, it can be advantageous to mix particularly vigorously dispersions containing solids, which may be present at the start of the reaction, for example when using sucrose. In addition, especially when using solid H-functional starter compounds, the choice of the agitator should ensure that the solid is adequately dispersed in the reaction mixture. Bottom-going agitator stages and agitator elements particularly suitable for suspension are preferably used here.
  • stirrer geometry should contribute to reducing the foaming of reaction products.
  • the foaming of reaction mixtures can be observed, for example, after the end of the metering and post-reaction phase when residual alkylene oxides are additionally removed in vacuo at absolute pressures in the range from 1 to 500 mbar.
  • agitators have proven to be suitable, which achieve continuous mixing of the liquid surface.
  • the agitator shaft has a bottom bearing and, if necessary, further support bearings in the container.
  • the stirrer shaft can be driven from above or below (with a central or eccentric arrangement of the shaft).
  • a pumped circulation circuit guided by a heat exchanger or this in addition to the agitator unit operate as a further mixing component, the reactor contents being pumped around as required (typically 1 to 50 times per hour).
  • the specific mixing power entered by means of pumping for example via an external heat exchanger via this or when returning to the reactor via a nozzle or injector, also amounts to values of on average 0.2 to 5 W / L, this being based on that in the reactor and the pumping circuit at the end of the reaction phase is based on the volume of liquid.
  • reactor bottoms are suitable for carrying out the process according to the invention.
  • cylindrical containers are used which have a height / diameter ratio of 1: 1 to 10: 1.
  • spherical, dished, flat, or conical bottoms can be used as reactor bottoms.
  • reaction mixture can be completely freed from small amounts of unreacted alkylene oxides in vacuo, for example at an absolute pressure of 1 to 500 mbar, or by stripping after the end of the last post-reaction phase.
  • Volatile constituents such as (residual) alkylene oxides, for example, are removed by stripping while introducing inert gases and / or water vapor into the liquid phase while simultaneously applying a vacuum (for example by passing inert gas through at an absolute pressure of 5 to 500 mbar).
  • the removal of volatile constituents is generally carried out at temperatures from 20 to 200 ° C., preferably from 50 to 160 ° C. and preferably at the reaction temperature with stirring.
  • Such stripping processes can also be carried out in so-called stripping columns in which a stream of inert gas or water vapor is passed against the product stream.
  • stripping columns with random packings or internals are preferably used.
  • Such stripping processes can also be carried out continuously, for example by collecting the non-stripped material in a buffer tank and continuously feeding it from this to the stripping column. After constant pressure has been reached in the post-reaction phase and, if necessary, after volatile constituents have been removed by vacuum and / or stripping, the product can be drained from the reactor or post-treatment steps, in particular work-up steps, can be carried out.
  • the crude polyoxyalkylene polyol mixture resulting from step ii) can optionally be subjected to work-up steps in order to remove any traces of catalyst.
  • work-up steps in order to remove any traces of catalyst.
  • post-treatment steps are generally not required.
  • the optional removal of the catalyst from the crude polyoxyalkylene polyol mixture resulting from step ii) can take place in various ways:
  • the basic catalyst can be neutralized with dilute mineral acids such as sulfuric acid or phosphoric acid.
  • the salts formed during the neutralization are separated off, for example by filtration.
  • the polyether polyol manufacturing processes described in EP-A 2028211 and WO-A 2009106244 are exceptions.
  • the neutralization with hydroxycarboxylic acids can be carried out.
  • Carboxylic acids such as, for example, formic acid (cf. US Pat. No. 4,521,548) are also suitable for neutralization.
  • the metal carboxylates formed after neutralization with carboxylic acids are clearly soluble in the polyether polyols, so that the salts do not have to be separated off here.
  • the neutralization can also be carried out, for example, by adding cyclic dicarboxylic anhydrides, such as phthalic anhydride, maleic anhydride, tetrahydrophthalic anhydride or succinic anhydride, salts which are also soluble in the polyoxyalkylene polyol mixtures according to the invention are obtained.
  • cyclic dicarboxylic anhydrides such as phthalic anhydride, maleic anhydride, tetrahydrophthalic anhydride or succinic anhydride
  • salts which are also soluble in the polyoxyalkylene polyol mixtures according to the invention are obtained.
  • ring-opening products of cyclic carboxylic acid anhydrides with polyols, that is to say of dicarboxylic acid half-esters, as neutralizing agents is also possible.
  • the incompletely alkoxylated oxo acids of phosphorus are also suitable as neutralization acids.
  • the use of acidic cation exchangers, as described, for example, in DE-A 100 24 313, is also possible to remove the catalyst.
  • the catalysts can also be separated using adsorbents such as sheet silicates (bentonite, attapulgite), diatomaceous earth or synthetic magnesium silicates (such as AMBOSOL ® or BriteSorb ® ).
  • sheet silicates bentonite, attapulgite
  • diatomaceous earth such as AMBOSOL ® or BriteSorb ®
  • synthetic magnesium silicates such as AMBOSOL ® or BriteSorb ®
  • Phase separation processes are also possible in principle, but the water solubilities of the highly functional constituents of the reaction mixture are generally too high for phase separation processes to be carried out effectively.
  • Phase separation processes are described, for example, in WO-A 0114456, JP-A 6-157743, WO-A 9620972 and US-A 3823145.
  • the polyoxyalkylene polyol mixtures according to the invention be prepared with the exclusion of oxygen. Handling and storage in the absence of oxygen are also recommended for completely processed, salt-free and stabilized polyoxyalkylene polyol mixtures according to the invention.
  • Inert gases suitable for this are, for example, noble gases, or nitrogen or carbon dioxide, noble gases or nitrogen are particularly suitable.
  • reaction of the mixture (i) with the OH-reactive compound, in particular with the alkylene oxide (s), which takes place in step ii), is in fact carried out in such a way that the alkylene oxide preferably reacts with the Zerewitinoff-active hydrogens of the starter compounds (b ' ) and (c ') react and practically not react with the hydroxyl groups of the polyoxyalkylene compound (a), see Fig. 1.
  • this i) is due to the number of polyoxyalkylene compounds ( a) bound hydroxyl groups can be attributed to a significantly higher number of Zerewitinoff-active hydrogen atoms bound to the starter compounds (b ') and (c'), and / or that at the beginning of the metering in of the alkylene oxide (s) the mixture of the at least one starter compound ( b '), the at least one starter compound (c') and the catalyst in the relatively nonpolar polyoxyalkylene polyol (a) is given, so that the starter compounds (b '), (c ‘) and the catalyst form a separate reaction system in which the reaction with the alkylene oxide or oxides takes place almost exclusively.
  • Antioxidants for example based on phenol derivatives and / or based on amines
  • Antioxidants can be added to the polyoxyalkylene polyol mixtures according to the invention. If an alkali metal hydroxide is used to catalyze the addition of alkylene oxide to the starter compounds used, it is advisable to add such antioxidants only after these traces of catalyst have been neutralized or separated off, since discoloration of the polyoxyalkylene polyol mixtures can be avoided in this way.
  • the polyoxyalkylene polyol mixtures obtainable by the process according to the invention can be used as starting components for the production of solid or foamed polyurethane materials and, less preferably, also for obtaining polyurethane elastomers.
  • the polyurethane materials and elastomers can also contain isocyanurate, allophanate and biuret structural units.
  • polyetherester polyols according to the invention optionally mixed with other isocyanate-reactive components and with
  • Polyoxyalkylene polyols polyester polyols, polycarbonate polyols, polyether carbonate polyols, polyester carbonate polyols, polyether ester carbonate polyols and / or low molecular weight chain extenders and / or crosslinking agents with OH numbers or NH numbers of 6 to 1870 mg KOH / g can optionally be added to the polyoxyalkylene polyol mixtures according to the invention as further isocyanate-reactive components will.
  • Polyoxyalkylene polyols suitable for this purpose can, for example, by anionic polymerization of alkylene oxides in the presence of alkali hydroxides or alkali alcoholates as catalysts and with the addition of at least one starter molecule containing 2 to 8 Zerewitinoff-active hydrogen atoms bonded, or by cationic polymerization of alkylene oxides in the presence of Brpnstedt or Lewis Acids such as trifluoromethanesulfonic acid, perchloric acid, antimony pentachloride, boron trifluoride etherate, or tris (pentafluorophenyl) borane can be obtained.
  • Lewis Acids such as trifluoromethanesulfonic acid, perchloric acid, antimony pentachloride, boron trifluoride etherate, or tris (pentafluorophenyl) borane can be obtained.
  • Suitable catalysts are, of course, those of the double metal cyanide complex type, as described, for example, in US-A 3,404,109, US-A 3 829 505, US-A 3 941 849, US-A 5 158 922, US-A 5 470 813, EP A 700 949, EP-A 743 093, EP-A 761 708, WO 97/40086, WO 98/16310 and WO 00/47649 are described.
  • Suitable alkylene oxides and some suitable starter compounds have already been described in the previous sections. Additionally to be mentioned are, for example, tetrahydrofuran as a Lewis acidic polymerizable cyclic ether and water as a starter molecule.
  • the polyoxyalkylene polyols preferably polyoxypropylene-polyoxyethylene-polyols, preferably have number average molecular weights of 200 to 8000 Da.
  • polyoxyalkylene polyols are also suitable as polyoxyalkylene polyols, preferably graft polyoxyalkylene polyols, in particular those based on styrene and / or acrylonitrile, which are obtained by in-situ polymerization of acrylonitrile, styrene or preferably mixtures of styrene and acrylonitrile, for example in a weight ratio of 90:10 to 10:90.
  • polyoxyalkylene polyols expediently in the aforementioned polyoxyalkylene polyols, as well as polyoxyalkylene polyol dispersions, which as a disperse phase, usually in a Amount of 1 to 50% by weight, preferably 2 to 25% by weight, of inorganic fillers, polyureas, polyhydrazides, polyurethanes containing bound tert-amino groups and / or melamine.
  • Suitable polyester polyols can, for example, be prepared from organic dicarboxylic acids having 2 to 12 carbon atoms and polyhydric alcohols, preferably diols, having 2 to 12 carbon atoms, preferably 2 to 6 carbon atoms.
  • Suitable dicarboxylic acids are, for example: succinic acid, glutaric acid, adipic acid, suberic acid, azelaic acid, sebacic acid, decanedicarboxylic acid, dodecanedicarboxylic acid, maleic acid, fumaric acid, phthalic acid, isophthalic acid and terephthalic acid.
  • the dicarboxylic acids can be used either individually or as a mixture with one another.
  • dicarboxylic acid derivatives such as. B. dicarboxylic acid mono- and / or diesters of alcohols having 1 to 4 carbon atoms or dicarboxylic anhydrides can be used.
  • Dicarboxylic acid mixtures of succinic, glutaric and adipic acid are preferably used in proportions of, for example, 20 to 35/40 to 60/20 to 36 parts by weight, and in particular adipic acid.
  • dihydric and polyhydric alcohols examples include ethanediol, diethylene glycol, 1,2- or 1,3-propanediol, dipropylene glycol, methyl 1,3-propanediol, 1,4-butanediol, 1,5-pentanediol, 3-methyl 1,5-pentanediol, 1,6-hexanediol, neopentyl glycol, 1,10-decanediol, 1,12-dodecanediol, glycerin, trimethylolpropane and pentaerythritol.
  • 1,2-ethanediol diethylene glycol, 1,4-butanediol, 1,6-hexanediol, glycerol, trimethylolpropane or mixtures of at least two of the polyhydric alcohols mentioned, in particular mixtures of ethanediol, 1,4-butanediol and 1,6 -Hexanediol, glycerine and / or tri methylolpropane. It is also possible to use polyester polyols made from lactones, e.g. s-caprolactone or hydroxycarboxylic acids, e.g. B. hydroxycaproic acid and hydroxyacetic acid.
  • the organic, aromatic or aliphatic polycarboxylic acids and / or polycarboxylic acid derivatives and polyhydric alcohols can be used without a catalyst or in the presence of esterification catalysts, expediently in an atmosphere of inert gases, e.g. Nitrogen, helium or argon and also in the melt at temperatures of 150 to 300 ° C., preferably 180 to 230 ° C., if appropriate under reduced pressure, to the desired acid and OH numbers, are polycondensed.
  • the acid number is advantageously less than 10, preferably less than 2.5.
  • the esterification mixture is polycondensed at the abovementioned temperatures up to an acid number of 80 to 30, preferably 40 to 30, under normal pressure and then under a pressure of less than 500 mbar, preferably 1 to 150 mbar.
  • the esterification catalysts are, for example, iron, cadmium, Cobalt, lead, zinc, antimony, magnesium, titanium and tin catalysts in the form of metals, metal oxides or metal salts are possible.
  • polycondensation of aromatic or aliphatic carboxylic acids with polyhydric alcohols can, however, also be carried out in the liquid phase in the presence of diluents and / or entrainers, such as benzene, toluene, xylene or chlorobenzene, for azeotropic distillation of the water of condensation.
  • diluents and / or entrainers such as benzene, toluene, xylene or chlorobenzene
  • the ratio of dicarboxylic acid (derivative) and polyhydric alcohol to be selected to obtain a desired OH number, functionality and viscosity and the alcohol functionality to be selected can be determined in a simple manner by the person skilled in the art.
  • Suitable polycarbonate polyols are those of the type known per se which, for example, by reacting diols such as 1,2-propanediol, 1,4-butanediol, 1,6-hexanediol, diethylene glycol, triethylene glycol, tetraethylene glycol, oligo-tetramethylene glycol and / or oligo-hexa - methylene glycol with diaryl carbonates and / or dialkyl carbonates, e.g. B. diphenyl carbonate, dimethyl carbonate and a-w bischloroformates or phosgene can be produced.
  • diols such as 1,2-propanediol, 1,4-butanediol, 1,6-hexanediol
  • diethylene glycol triethylene glycol, tetraethylene glycol, oligo-tetramethylene glycol and / or oligo-hexa - methylene glycol
  • the polyether carbonate polyols which are also suitable are obtained by copolymerizing cyclic epoxides and carbon dioxide; such copolymerizations are preferably carried out under high pressure and catalyzed by double metal cyanide (DMC) compounds.
  • DMC double metal cyanide
  • Low molecular weight, preferably trifunctional or tetrafunctional crosslinking agents or difunctional chain extenders can be added to the polyoxyalkylene polyol mixtures to be used according to the invention in order to modify the mechanical properties, in particular the hardness, of the PUR materials.
  • Suitable crosslinking agents e.g. B. 3- or 4-valent alcohols and oligomeric polyoxyalkylene polyols with a functionality of 3 to 4, usually have molecular weights of 90 to 300 Da.
  • Suitable crosslinking agents are, for example, glycerol, trimethylolpropane or pentaerythritol.
  • Alkanediols having 2 to 12 carbon atoms for example ethanediol, 1,3-propanediol, 1,5-pentanediol, 1,6-hexanediol, 1,7-heptanediol, 1,8-octanediol, 1,9-nonanediol, are preferably used as chain extenders , 1,10-decanediol and in particular 1,4-butanediol and dialkylene glycols with 4 to 8 carbon atoms, for example diethylene glycol and dipropylene glycol.
  • branched-chain and / or unsaturated alkanediols with usually not more than 12 carbon atoms, such as 1,2-propanediol, 2-methyl-1,3-propanediol, 3-methyl-1,5-pentanediol, 2,2-dimethyl -l, 3-propanediol, 2-butyl-2-ethyl-l, 3-propanediol, 2-butene-1,4-diol and 2-butyne-1,4-diol, diesters of terephthalic acid with glycols with 2 up to 4 carbon atoms, such as bis-ethylene glycol terephthalate or bis-1,4-butylene glycol terephthalate and hydroxyalkylene ethers of hydroquinone or resorcinol, eg 1,4-di- (ß-hydroxyethylj-hydroquinone or 1,3- (ß-hydroxyethyl) )
  • Alkanolamines with 2 to 12 carbon atoms such as ethanolamine, 2-aminopropanol and 3-amino-2,2-dimethylpro- panol, N-alkyldialkanolamines, e.g. N-methyl- and N-ethyl-diethanolamine, (cyclo) aliphatic diamines with 2 to 15 carbon atoms, such as 1,2-ethylenediamine, 1,3-propylenediamine,
  • Q is an aliphatic hydrocarbon radical with 2-18 , preferably 6-10 carbon atoms, a cycloaliphatic hydrocarbon radical with 4-15, preferably 5-10 carbon atoms, an aromatic hydrocarbon radical with 6-15, preferably 6-13 carbon atoms, or an aralip
  • 1,4-diisocyanate and any mixtures of these isomers 1-isocyanato-3,3,5-tri-methyl-5-isocyanatomethyl-cyclohexane (DE-B 1 202 785, US-A 3 401 190), 2,4- and 2 , 6—
  • 1,4-phenylene diisocyanate, Pcihydro-2,4'- and -4,4'-diphenylmethane diisocyanate, 1,3- and 1,4-phenylene diisocyanate (DE-A 196 27 907), 1,4-durene diisocyanate (DDI), 4,4'-stilbene diisocyanate (DE-A 196 28 145), 3,3'-dimethyl-4,4'-biphenylene diisocyanate (DIBDI) (DE-A 195 09 819) 2,4- and 2, 6-tolylene diisocyanate (TDI) and any mixtures of these isomers, diphenylmethane-2,4'-diisocyanate and / or diphenylmethane-4,4'-diisocyanate (MDI) or naphthylene-1,5-diisocyanate (NDI).
  • triphenylmethane-4,4 ', 4 "-triisocyanate polyphenyl-polymethylene-polyisocyanates, as obtained by aniline-formaldehyde condensation and subsequent phosgenation and, for example, in GB-A 874 430 and GB-A 848 671 m- and p-isocyanatophenylsulfonyl isocyanates according to US Pat. No. 3,454,606, perchlorinated aryl polyisocyanates as described in US Pat. No. 3,277,138, polyisocyanates containing carbodiimide groups, as described in US Pat. No.
  • polyisocyanates containing acylated urea groups according to DE-C 1 230 778 polyisocyanates containing biuret groups, as described in US Pat 3,124,605, 3,201,372 and 3,124,605 and in GB-B 889 050, by Telome Polyisocyanates prepared by reactions, as described in US Pat. No. 3,654,106, and polyisocyanates containing ester groups, such as those mentioned in GB-B 965 474 and 1,072,956, in US Pat. No.
  • isocyanate group-containing distillation residues obtained during the industrial production of isocyanates optionally dissolved in one or more of the aforementioned polyisocyanates. It is also possible to use any mixtures of the aforementioned polyisocyanates.
  • polyisocyanates e.g. the 2,4- and 2,6-tolylene diisocyanate and any mixtures of these isomers
  • TDI 2,4- and 2,6-tolylene diisocyanate and any mixtures of these isomers
  • CAde MDI aniline-formaldehyde condensation and subsequent phosgenation
  • carbodiimide groups Urethane groups, allophanate groups, isocyanurate groups, urea groups or biuret groups containing polyisocyanates
  • modified polyisocyanates in particular those modified polyisocyanates which are derived from 2,4- and / or 2,6-tolylene diisocyanate or from 4,4 "and / or Derive 2,4'-diphenylmethane diisocyanate.
  • Naphthylene-1,5-diisocyanate and mixtures of the polyisocyanates mentioned are also very suitable.
  • prepolymers containing isocyanate groups which are obtainable by reacting a portion or the total amount of the polyether ester polyols to be used according to the invention and / or a portion or the total amount of the above-described isocyanate-reactive components to be optionally mixed with the polyether ester polyols to be used according to the invention with at least one aromatic Di- or polyisocyanate from of the group TDI, MDI, DIBDI, NDI, DDI, preferably with 4,4'-MDI and / or 2,4-TDI and / or 1,5-NDI to form a polyadduct containing urethane groups, preferably urethane groups and isocyanate groups.
  • the prepolymers containing isocyanate groups are prepared by reacting exclusively higher molecular weight polyhydroxyl compounds, i.e. the polyoxyalkylene polyol mixtures to be used according to the invention, and / or polyetherester polyols, polyether polyols, polyester polyols or polycarbonate polyols with the polyisocyanates, preferably 4,4'-MDI , 2,4-TDI and / or 1,5-NDI.
  • the prepolymers containing isocyanate groups can be prepared in the presence of catalysts. However, it is also possible to produce the prepolymers containing isocyanate groups in the absence of catalysts and to add these to the reaction mixture for producing the PUR materials.
  • Water can be used as a blowing agent which can optionally be used, which reacts with the organic polyisocyanates or with the prepolymers containing isocyanate groups in situ to form carbon dioxide and amino groups, which in turn react with other isocyanate groups to form urea groups and act as chain extenders. If water is added to the polyurethane formulation in order to set the desired density, this is usually used in amounts of 0.001 to 6.0% by weight, based on the weight of components 1, 4 and 5.
  • gases or volatile inorganic or organic substances that evaporate under the influence of the exothermic polyaddition reaction and advantageously have a boiling point under normal pressure in the range from -40 to 120 ° C., preferably from 10 to 90 ° C, can be used as a physical blowing agent.
  • organic blowing agents examples include acetone, ethyl acetate, methyl acetate, halogen-substituted alkanes such as methylene chloride, chloroform, ethylidene chloride, vinylidene chloride, monofluorotrichloromethane, chlorodifluoromethane, dichlorodifluoromethane, HFCs such as R 134a, R 245fa and R 365mfc, or so-called HFOs such as HFOs trans-l, 3,3,3-tetrafluoropropene or trans-l-chloro-3,3,3-trifluoropropene, and also unsubstituted alkanes such as butane, n-pentane, isopentane, cyclopentane, hexane, heptane or diethyl ether can be used.
  • halogen-substituted alkanes such as methylene chloride
  • blowing agents can also be used as mixtures.
  • Inorganic blowing agents that can be used are, for example, air, CO2 or N2O.
  • a propellant effect can also be achieved by adding compounds which form at temperatures above room temperature with the elimination of gases, for example nitrogen and / or Carbon dioxide, such as azo compounds, such as azodicarbonamide or azoisobutyronitrile, or salts such as ammonium bicarbonate, ammonium carbamate or ammonium salts of organic carboxylic acids, such as the monoammonium salts of malonic acid, boric acid, formic acid or acetic acid, decompose.
  • azo compounds such as azodicarbonamide or azoisobutyronitrile
  • salts such as ammonium bicarbonate, ammonium carbamate or ammonium salts of organic carboxylic acids, such as the monoammonium salts of malonic acid, boric acid, formic acid or acetic acid, decompose.
  • the appropriate amount of solid propellants, low-boiling liquids or gases to be used, each individually or in Lorm of mixtures, eg. B. can be used as liquid or gas mixtures or as gas-liquid mixtures, depends on the desired PUR material density and the amount of water used. The required amounts can easily be determined experimentally. Satisfactory results usually give amounts of solids of 0.5 to 35 parts by weight, preferably 2 to 15 parts by weight, amounts of liquid of 1 to 30 parts by weight, preferably 3 to 18 parts by weight and / or amounts of gas of 0 , 01 to 80 parts by weight, preferably from 10 to 35 parts by weight, based in each case on the weight of the structural components 1 and 2.
  • B. air, carbon dioxide, nitrogen and / or helium can be carried out either via the formulation components 1, 4 and 5 or via the polyisocyanates 2 or via 1, 4, 5 on the one hand and 2 on the other.
  • Amine catalysts familiar to Lachmann can be used as component 4, e.g. tertiary amines such as triethylamine, tributylamine, N-methyl-morpholine, N-ethyl-morpholine, N, N, N ', N'-tetramethyl-ethylenediamine, pentamethyl-diethylenetriamine and higher homologues (DE OS 26 24 527 and 26 24 528), 1,4-diaza-bicyclo- (2,2,2) -octane, N-methyl-N'-dimethylaminoethyl-piperazine, bis- (dimethylaminoalkyl) -piperazine (DE-A 26 36 787), N, N-dimethylbenzylamine, N, N-dimethylcyclohexylamine, N, N-diethylbenzylamine, bis- (N, N-diethylaminoethyl) adipate, N, N, N '
  • Mannich bases known per se and composed of secondary amines, such as dimethylamine, and aldehydes, preferably formaldehyde, or ketones such as acetone, methyl ethyl ketone or cyclohexanone and phenols, such as phenol or alkyl-substituted phenols, can also be used as catalysts.
  • Tertiary amines containing hydrogen atoms active towards isocyanate groups as catalysts are, for example, triethanolamine, triisopropanolamine, N-methyl-diethanolamine, N-ethyl- diethanolamine, N, N-dimethylethanolamine, their reaction products with alkylene oxides such as propylene oxide and / or ethylene oxide and secondary-tertiary amines according to DE-A 27 32 292.
  • Silaamines with carbon-silicon bonds as described in US A 3,620,984, for example 2,2,4-trimethyl-2-silamorpholine and 1,3-diethyl-aminomethyl-tetramethyl-disiloxane, can be used.
  • nitrogen-containing bases such as tetraalkylammonium hydroxides and hexahydrotriazines are also suitable.
  • the reaction between NCO groups and Zerewitinoff-active hydrogen atoms is also greatly accelerated by lactams and azalactams, whereby an association is initially formed between the lactam and the compound with acidic hydrogen.
  • amines are used as catalysts for the catalysis of the polyurethane reaction, it must of course be noted that polyoxyalkylene-polyol mixtures prepared according to the invention with amine catalysis may already contain catalytically active amines. By means of a suitable series of experiments, however, it is easily possible for the person skilled in the art to determine the amounts of amine catalysts which may still be added.
  • organic metal compounds can be used as catalysts for this purpose, preferably organic tin compounds such as tin (II) salts of organic carboxylic acids, eg. B. tin (II) acetate, tin (II) octoate, tin (II) ethylhexoate and tin (II) taurate and, less preferred, the dialkyltin (IV) salts of mineral acids or organic Carboxylic acids, e.g. B. dibutyltin diacetate, dibutyltin dilaurate, dibutyltin maleate, dioctyltin diacetate and dibutyltin dichloride.
  • sulfur-containing compounds such as di-n-octyltin mercaptide (US Pat. No. 3,645,927) can also be used.
  • Catalysts which catalyze the trimerization of NCO groups in a special way, are used for the production of polyurethane materials with high proportions of so-called poly (isocyanurate) structures (“PIR foams”).
  • PIR foams are usually produced with indexes from 180 to 450, the index being defined as the ratio of isocyanate groups to hydroxyl groups multiplied by a factor of 100.
  • Catalysts which contribute to the development of isocyanurate structures are metal salts such as potassium or sodium acetate, sodium octoate and amino compounds such as 1,3,5-tris (3-dimethylaminopropyl) hexahydrotriazine.
  • the catalysts or catalyst combinations are generally used in an amount between about 0.001 and 10% by weight, in particular 0.01 to 4% by weight, based on the total amount Compounds with at least two isocyanate-reactive hydrogen atoms are used.
  • additives 5 can optionally be used.
  • Surface-active additives such as emulsifiers, foam stabilizers, cell regulators, flame retardants, nucleating agents, oxidation retarders, stabilizers, lubricants and mold release agents, dyes, dispersing aids and pigments may be mentioned, for example.
  • Suitable emulsifiers are, for example, the sodium salts of castor oil sulfonates or salts of fatty acids with amines such as oleic diethylamine or stearic acid diethanolamine.
  • Alkali or ammonium salts of sulfonic acids such as dodecylbenzenesulfonic acid or dinaphthylmethane disulfonic acid or of fatty acids such as ricinoleic acid or of polymeric fatty acids can also be used as surface-active additives.
  • Polyether siloxanes in particular are suitable as foam stabilizers. These compounds are generally structured in such a way that copolymers of ethylene oxide and propylene oxide are bonded to a polydimethylsiloxane radical. Such foam stabilizers can be reactive towards isocyanates or be unreactive towards isocyanates due to etherification of the terminal OH groups.
  • organopolysiloxanes oxyethylated alkylphenols, oxyethylated fatty alcohols and paraffin oils, and cell regulators such as paraffins, fatty alcohols and dimethylpolysiloxanes are also suitable.
  • cell regulators such as paraffins, fatty alcohols and dimethylpolysiloxanes.
  • oligomeric polyacrylates with polyoxyalkylene and fluoroalkane radicals as side groups are also suitable.
  • the surface-active substances are usually used in amounts of 0.01 to 5 parts by weight, based on 100 parts by weight of component 1.
  • Reaction retarders for example acidic substances such as hydrochloric acid, or organic acids and acid halides, as well as pigments or dyes and flame retardants known per se, e.g. tris (chloroethyl) phosphate, tricresyl phosphate or ammonium phosphate and polyphosphate, and also stabilizers against aging and aging, can also be added Weather conditions, plasticizers and fungicidal and bactericidal substances.
  • acidic substances such as hydrochloric acid, or organic acids and acid halides
  • pigments or dyes and flame retardants known per se, e.g. tris (chloroethyl) phosphate, tricresyl phosphate or ammonium phosphate and polyphosphate, and also stabilizers against aging and aging, can also be added Weather conditions, plasticizers and fungicidal and bactericidal substances.
  • the ratio of the isocyanate groups in the polyisocyanates 2. to the isocyanate-reactive hydrogens in components 1, 3, 4 and 5 can be varied widely. Ratios of 0.7: 1 to 5: 1 are common.
  • the PUR or PIR materials can be prepared using the methods described in the literature, e.g. the one-shot or the prepolymer process, with the aid of mixing devices known in principle to the person skilled in the art, are produced.
  • the highly functional polyoxyalkylene polyol mixtures which can be produced particularly advantageously by the process according to the invention can be processed with polyisocyanates and, if necessary, physical blowing agents, using the usual high-pressure or low-pressure processing machines, in particular to give rigid polyurethane insulating foams, which are used, for example, in the insulation of refrigerators or buildings will.
  • the polyoxyalkylene polyol mixtures according to the invention can be fed to the mechanical mixing unit either as an individual component or as part of a formulation prepared beforehand. Their low viscosity proves to be particularly advantageous for machine processing of the polyoxyalkylene polyol mixtures according to the invention.
  • a process for producing a polyoxyalkylene polyol mixture comprising at least 3 polyoxyalkylene polyols (a) (b) and (c), the mean OH number of the polyoxyalkylene polyol mixture being 290-560 mg KOH / g and the OH -Number has been determined according to the regulation of DIN 53240; where the calculated mean OH number of the polyoxyalkylene polyols (b) and (c) is at least 360 mg KOH / g and the polyoxyalkylene polyol mixture by reacting a mixture comprising at least one polyoxyalkylene polyol (a), at least one H-functional starter substance (b ' ) and at least one H-functional starter substance (c ') with an OH-reactive compound is optionally obtained in the presence of a catalyst, the process comprising the following steps i) providing a mixture (i) comprising the polyoxyalkylene polyol (a), the H- functional starter substance (b
  • the invention relates to a process according to the first embodiment, the reaction of the mixture (i) with the OH-reactive compound in step (ii) taking place in the presence of the catalyst.
  • the invention relates to a process according to the first or second embodiment, wherein the catalyst is a basic, a Brönsted acid, a Lewis acid and / or a double metal cyanide catalyst, preferably a basic catalyst.
  • the invention relates to a method according to the third embodiment, wherein the catalyst is a basic catalyst and the basic catalyst is an alkali metal hydroxide, alkaline earth metal hydroxide and / or amine.
  • the invention relates to a method according to the fourth embodiment, wherein the basic catalyst is an amine.
  • the invention relates to a method according to one of the first to fifth embodiments, the mass fraction of the at least one polyoxyalkylene polyol (a) being 2 to 30% by weight, preferably 5 to 30% by weight, based on the mass of the polyoxyalkylene polyol - Mixture is.
  • the invention relates to a method according to one of the first to sixth embodiments, wherein the starter substance (b ‘) has a functionality of 3 to 8 and the starter substance (c‘) has a functionality of 6 to 8.
  • the invention relates to a method of one of the first to seventh embodiments, wherein at least one of the starter substances (b ') or (c') has a melting point of greater than 150 ° C. and one of the starter substances (b ') or (c') has a melting point of less than 150 ° C, the melting points being determined using ASTM E324 (11/2016).
  • the invention relates to a method according to one of the first to eighth embodiment, wherein the mass fraction of the H-functional starter substance (b ') based on the total mass of the H-functional starter substance (b') and the H-functional starter substance (c ') Is 15% by weight to 40% by weight.
  • the invention relates to a method according to one of the first to ninth embodiments, the OH-reactive compound being an alkylene oxide and / or a fatty acid ester, preferably an alkylene oxide.
  • the invention relates to a method according to the tenth embodiment, the OH-reactive compound being an alkylene oxide.
  • the invention relates to a method according to the eleventh embodiment, the alkylene oxide being propylene oxide and / or ethylene oxide, preferably propylene oxide.
  • the invention relates to a polyoxyalkylene polyol mixture obtainable according to one of the first to twelfth embodiments.
  • the invention relates to a polyoxyalkylene polyol mixture according to the thirteenth embodiment with a viscosity of 5000-60,000 mPas at 25 ° C. determined by means of a rotary viscometer according to the specification of DIN 53018.
  • the invention relates to a process for producing polyurethanes by reacting the polyoxyalkylene polyol mixture according to the thirteenth or fourteenth embodiment with a polyisocyanate.
  • OH numbers were determined in accordance with the specification of DIN 53240. All calculated OH numbers relate to the salt-free alkylene oxide adducts.
  • the viscosities were determined using a rotary viscometer (Physica MCR 51, manufacturer: Anton Paar) in accordance with the DIN 53018 specification.
  • the molecular weight distribution was determined by means of size exclusion chromatography (SEC).
  • SEC size exclusion chromatography
  • the Agilent 1100 Series device from Agilent was used.
  • the polydispersity (PD) for the molecular weight distribution M n / M n is given , where M n stands for the weight average molar mass and M n for the number average molar mass. More information:
  • PSS is the manufacturer of the columns (Polymer Standard Solutions, Mainz)
  • the diol obtained (polyoxyalkylene polyol (a)) has a calculated OH number of 112.6 mg KOH / g. 169.1 g of a 70% strength solution of sorbitol (starter substance (b ')) in water, 3.339 g of a solution (44.89% by weight) of KOH in water and 219.6 g of sucrose were then added under nitrogen (Starter substance (c ')) added to the reactor.
  • the autoclave was closed, the temperature was increased to 110 ° C. with stirring (100 rpm) and the pressure was reduced to about 80 mbar. After 15 min.
  • the intermediate product obtained a diol with a calculated OH number of 100 mg KOH / g (polyoxyalkylene polyol (a)), was at 110 ° C. over a period of 0.51 h at a pressure of 15 baked out mbar and then cooled to 50 ° C. There were then 169.8 g of a 70% solution of sorbitol in water (starter substance (b ')), 223.1 g of sucrose (starter substance (c')) and 4.199 g of a solution (44.89 wt. -%) of KOH in water added to the reactor. The autoclave was closed, the temperature was increased to 110 ° C.
  • the difference between the mean OH number of the alkylene oxide adducts of the H-functional Starter substances (b ') and (c') and the OH number of the polyoxyalkylene polyol (a) was 300 mg KOH / g.
  • the contents of the autoclave were heated to 110 ° C. with stirring (cross-bar stirrer, 100 rpm) and the pressure was reduced to about 30 mbar. After a dewatering time of 3.5 h, the vacuum line was closed and the stirrer speed was increased to 800 rpm. Metering of a total of 927.9 g of propylene oxide into the head space of the reactor was started at 110 ° C. The propylene oxide metering phase lasted 10.7 h, the metering rate was gradually increased from 25 g / h to the final value of 115 g / h and the temperature was raised to 120 ° C. during the propylene oxide metering.
  • the contents of the autoclave were heated out at 120 ° C. over a period of 1.0 h in a vacuum (57 mbar). After cooling to 80 ° C., 4.579 g of an 85% strength by weight solution of lactic acid in water were added. After adding 0.780 g of IRGANOX ® 1076, an initial 30 min. stirred at 80 ° C. Finally, the product was heated in an oil pump vacuum (5 mbar) over a period of 3 h at 110 ° C. A homogeneous, clear end product was obtained with an OH number of 415 mg KOH / g and a viscosity (25 ° C.) of 37,900 mPas.
  • the intermediate product obtained a diol with a calculated OH number of 120.8 mg KOH / g (polyoxyalkylene polyol (a)), was at 130 ° C. over a period of 0.5 h one Baked out pressure of 38 mbar and then cooled to 40 ° C. 80 g of glycerol (starter substance (b ')), 315.1 g of sucrose (starter substance (c')) and 3.390 g of a solution (44.89% by weight) of KOH in water were then added to the reactor under nitrogen . The autoclave was closed, the temperature was increased to 110 ° C.
  • the contents of the autoclave were heated to 110 ° C. with stirring (cross-bar stirrer, 100 rpm) and the pressure was reduced to about 50 mbar. After a dewatering time of 3.5 h, the vacuum line was closed and the stirrer speed was increased to 800 rpm. Metering of a total of 855.6 g of propylene oxide into the head space of the reactor was started at 110 ° C. The propylene oxide metering phase lasted 10.0 h, the metering rate was increased successively from 25 g / h to the final value of 120 g / h and the temperature was raised to 120 ° C. during the propylene oxide metering.
  • a homogeneous, clear end product with an OH number of 441 mg KOH / g and a viscosity (25 ° C.) of 28300 mPas was obtained.
  • the difference between the mean OH number of the The alkylene oxide adduct of the H-functional starter substances (b ') and (c') and the OH number of the polyoxyalkylene polyol (a) was 383 mg KOH / g.
  • the contents of the autoclave were heated to 110 ° C. with stirring (cross-bar stirrer, 100 rpm) and the pressure was reduced to about 33 mbar. After a drainage time of 3.3 hours, the vacuum line was closed and the stirrer speed increased to 800 rpm. Metering of a total of 927.9 g of propylene oxide into the head space of the reactor was started at 110 ° C. The propylene oxide metering phase lasted 10.7 h, the metering rate was increased successively from 25 g / h to the final value of 120 g / h and the temperature was raised to 120 ° C. during the propylene oxide metering.
  • a homogeneous, clear end product with an OH number of 460 mg KOH / g and a viscosity (25 ° C.) of 39,850 mPas was obtained.
  • the difference between the mean OH number of the alkylene oxide adduct of the H-functional starter substances (b ') and (c') and the OH number of the polyoxyalkylene polyol (a) was 377 mg KOH / g.
  • the intended dosage was a total of 789.3 g of propylene oxide. After 265 g of propylene oxide had been fed in within 5 hours and the pressure had risen to 4.8 bar, the experiment was terminated due to the very slow absorption of epoxide.
  • the intermediate product obtained a diol with a calculated OH number of 160 mg KOH / g (polyoxyalkylene polyol (a))
  • the autoclave was closed, the temperature was increased to 110 ° C. with stirring (800 rpm) and the pressure was reduced to about 80 mbar.
  • the intermediate product obtained a diol with a calculated OH number of 100 mg KOH / g (polyoxyalkylene polyol (a)), was at 110 ° C. over a period of 0.51 hours at one pressure of 20 mbar and then cooled to 50 ° C. 216.6 g of a 70% strength solution of sorbitol in water (starter substance (b ')), 285.0 g of sucrose (starter substance (c')) and 4.153 g of a solution (44.89% by weight) were then added under nitrogen. -%) of KOH in water added to the reactor. The autoclave was closed, the temperature was increased to 110 ° C.
  • the intermediate product obtained a diol with a calculated OH number of 102 mg KOH / g (starter substance a ')
  • starter substance a ' was at 110 ° C. over a period of 1.7 h at a pressure of 22 mbar baked and then cooled to 50 ° C.
  • 201.5 g of a 70% strength solution of sorbitol in water starter substance b '
  • 265.1 g of sucrose were then added under nitrogen
  • Starter substance c ' 4.170 g of a solution (44.89% by weight) of KOH in water were added to the reactor.
  • the autoclave was closed, the temperature was increased to 110 ° C.
  • the contents of the autoclave were heated to 110 ° C. with stirring (cross-bar stirrer, 100 rpm) and the pressure was reduced to about 30 mbar. After a dewatering time of 3.7 h, the vacuum line was closed and the stirrer speed increased to 800 rpm. Metering of a total of 927.9 g of propylene oxide into the head space of the reactor was started at 110 ° C. The propylene oxide metering phase lasted 10.5 h, the metering rate was increased successively from 25 g / h to the final value of 120 g / h and the temperature was raised to 120 ° C. during the propylene oxide metering.
  • the contents of the autoclave were heated to 110 ° C. with stirring (cross-bar stirrer, 100 rpm) and the pressure was reduced to about 40 mbar. After a dewatering time of 3.5 h, the vacuum line was closed and the stirrer speed was increased to 800 rpm. Metering of a total of 975.8 g of propylene oxide into the head space of the reactor was started at 110 ° C. The propylene oxide metering phase lasted 10.9 h, the metering rate was gradually increased from 25 g / h to the final value of 120 g / h and the temperature was raised to 120 ° C. during the propylene oxide metering.
  • the contents of the autoclave were heated in vacuo (58 mbar) at 120 ° C. over a period of 3.0 hours. After cooling to 80 ° C., 5.160 g of an 85% strength by weight solution of lactic acid in water were added. After adding 0.785 g of IRGANOX ® 1076, an initial 30 min. stirred at 80 ° C. Finally, the product was heated in an oil pump vacuum (5 mbar) over a period of 3 h at 110 ° C. A cloudy end product was obtained, of which the OH number and viscosity were not determined. The difference between the mean OH number of the alkylene oxide adduct of the H-functional starter substances b 'and c' and the OH number of the polyoxyalkylene polyol (a) was 344 mg KOH / g.
  • Example 25 comparison (according to DE 102 37 910 A1 and DE 102 37 914 A1)
  • Table 1 Compilation of the functionality and OH number of the polyoxyalkylene polyol (a); Functionalities of the starter substances b‘and c ‘; Average functionality of the starter substances b ‘and c‘ and the presence of a starter substance b ‘or c‘ with a melting temperature of ⁇ 150 ° C and the resulting OH number, viscosities, OH number differences and the phase behavior of the polyoxyalkylene polyol mixtures (at room temperature).

Landscapes

  • Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Polyethers (AREA)

Abstract

La présente invention concerne un procédé de production directe de mélanges de polyoxyalkylène polyols à chaîne courte, à fonctionnalité élevée, et de polyoxyalkylène polyols à chaîne longue, à faible fonctionnalité. Le constituant polyoxyalkylène polyol à chaîne courte, à fonctionnalité élevée, est obtenu par addition d'oxyde d'alkylène à des composés de départ à fonction H à fonctionnalité élevée, tandis que, de façon correspondante, le constituant polyoxyalkylène polyol à chaîne longue, à faible fonctionnalité, est obtenu par addition d'oxyde d'alkylène à des composés de départ à fonction H à faible fonctionnalité. L'invention concern également les polyoxyalkylène polyols ainsi obtenus ainsi que leur utilisation pour produire des polyuréthanes.
EP20725571.2A 2019-05-24 2020-05-19 Procédé de production de mélanges de polyoxyalkylène polyols Pending EP3976688A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP19176341.6A EP3741788A1 (fr) 2019-05-24 2019-05-24 Procédé de production de mélanges de poly-oxyalkylène-polyol
PCT/EP2020/063904 WO2020239525A1 (fr) 2019-05-24 2020-05-19 Procédé de production de mélanges de polyoxyalkylène polyols

Publications (1)

Publication Number Publication Date
EP3976688A1 true EP3976688A1 (fr) 2022-04-06

Family

ID=66647197

Family Applications (2)

Application Number Title Priority Date Filing Date
EP19176341.6A Ceased EP3741788A1 (fr) 2019-05-24 2019-05-24 Procédé de production de mélanges de poly-oxyalkylène-polyol
EP20725571.2A Pending EP3976688A1 (fr) 2019-05-24 2020-05-19 Procédé de production de mélanges de polyoxyalkylène polyols

Family Applications Before (1)

Application Number Title Priority Date Filing Date
EP19176341.6A Ceased EP3741788A1 (fr) 2019-05-24 2019-05-24 Procédé de production de mélanges de poly-oxyalkylène-polyol

Country Status (4)

Country Link
US (1) US20220220304A1 (fr)
EP (2) EP3741788A1 (fr)
CN (1) CN113840859A (fr)
WO (1) WO2020239525A1 (fr)

Family Cites Families (91)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3277138A (en) 1966-10-04 Method for the chlorination of aromatic isocyanates
BE536296A (fr) 1954-03-22
BE538608A (fr) 1954-06-10
DE1030558B (de) 1956-07-21 1958-05-22 Bayer Ag Verfahren zur Herstellung von Urethangruppen enthaltenden Schaumstoffen
DE1022789B (de) 1956-09-29 1958-01-16 Bayer Ag Verfahren zur Herstellung von Schaumstoffen aus Polyoxy- und/oder Polycarboxylverbindungen und Polyisocyanaten
DE1027394B (de) 1956-10-22 1958-04-03 Bayer Ag Verfahren zur Herstellung von Schaumstoffen
BE562425A (fr) 1956-11-16
DE1072385C2 (de) 1958-06-20 1960-07-07 Bayer Ag Verfahren zur Herstellung von harzartigen, gegebenenfalls noch löslichen, beim Erwärmen Isocyanatgruppen freisetzenden Polyadditionsprodukten
BE581667A (fr) 1958-08-15
GB889050A (en) 1959-06-12 1962-02-07 Ici Ltd Process for the manufacture of polyurethanes
US3152162A (en) 1959-07-29 1964-10-06 Bayer Ag Polyisocyanate-carbodiimide adducts and process for the production thereof
NL254612A (fr) 1959-08-12
US3019731A (en) 1960-02-19 1962-02-06 Advanced Oil Tools Inc Jet perforator for well casings
US3190927A (en) 1960-04-13 1965-06-22 Wyandotte Chemicals Corp Process for oxyalkylating solid polyols
NL133051C (fr) 1960-12-05
GB994890A (en) 1961-12-18 1965-06-10 Ici Ltd New organic polyisocyanates and their manufacture
US3455883A (en) 1963-01-09 1969-07-15 Gen Mills Inc Polyisocyanates and derivatives
GB1063525A (en) 1963-02-14 1967-03-30 Gen Tire & Rubber Co Organic cyclic oxide polymers, their preparation and tires prepared therefrom
US3330782A (en) 1963-11-12 1967-07-11 Union Carbide Corp Beta-(n, n-dimethylamino)alkyl ethers as catalysts for isocyanate reactions
US3454606A (en) 1963-11-14 1969-07-08 Union Carbide Corp Isocyanatophenylsulfonyl isocyanates
US3124605A (en) 1963-12-05 1964-03-10 Biuret polyisocyanates
DE1202785B (de) 1964-07-21 1965-10-14 Scholven Chemie Ag Verfahren zur Herstellung von 1-Isocyanato-3-(isocyanatomethyl)-3, 5, 5-trimethylcyclohexan
DE1222067B (de) 1964-11-07 1966-08-04 Bayer Ag Verfahren zur Herstellung von einheitlichen organischen Polyisocyanaten
DE1231688B (de) 1965-04-17 1967-01-05 Bayer Ag Verfahren zur Herstellung von Isocyanatocarbonsaeureestern polyfunktioneller Hydroxyverbindungen
DE1230778B (de) 1965-05-24 1966-12-22 Bayer Ag Verfahren zur Herstellung von acylierten Harnstoffpolyisocyanaten
US3394164A (en) 1965-10-24 1968-07-23 Upjohn Co Stabilized methylenebis-(phenyl isocyanate) compositions
US3492301A (en) 1965-11-01 1970-01-27 Armstrong Cork Co 2,4,6-trisubstituted sulfonylhydrazido-s-triazines
US3567763A (en) 1966-01-06 1971-03-02 Rohm & Haas Ester polyisocyanates
US3629308A (en) 1966-07-25 1971-12-21 Union Carbide Corp Siloxane-oxyalkylene block copolymers
DE1618380C3 (de) 1967-03-08 1975-09-11 Bayer Ag, 5090 Leverkusen Verfahren zur Herstellung eines bei Raumtemperatur flüssigen Diphenylmethan-diisocyanatpräparates
DE1720633A1 (de) 1967-03-15 1971-07-01 Bayer Ag Verfahren zur Herstellung von Polyurethanen
DE1694162A1 (de) 1967-06-27 1971-06-09 Bayer Ag Verfahren zur Herstellung von Urethangruppen aufweisenden Schaumstoffen
DE1720747C3 (de) 1967-11-09 1980-06-26 Bayer Ag Verfahren zur Herstellung von Iso cyanatgruppen aufweisenden Telomerisaten
US3513491A (en) 1968-03-13 1970-05-26 Donald W Gordon Athlete's landing pit with foam-block cushion units
GB1204100A (en) 1968-05-15 1970-09-03 Bayer Ag Process for the production of foam plastics which contain urethane groups
US3823145A (en) 1968-07-26 1974-07-09 Basf Wyandotte Corp Removal of impurities from polyols
DE1804361A1 (de) 1968-10-22 1970-05-14 Bayer Ag Aminoaether als Aktivatoren zur Herstellung von Polyurethanen
DE1929034B2 (de) 1969-06-07 1972-04-20 Farbenfabriken Bayer Ag, 5090 Lever Kusen Verfahren zur herstellung von flammfesten urethangruppen aufweisenden schaumstoffen
AT304874B (de) 1969-06-20 1973-01-25 Bayer Ag Verfahren zur Herstellung von flammwidrigen, gegebenenfalls zellförmigen, Urethangruppen aufweisenden Kunststoffen
DE2002064C2 (de) 1970-01-17 1983-09-01 Bayer Ag, 5090 Leverkusen Verfahren zur Herstellung von flammwidrigen elastischen oder halbelastischen Schaumstoffen
US3829505A (en) 1970-02-24 1974-08-13 Gen Tire & Rubber Co Polyethers and method for making the same
DE2009179C3 (de) 1970-02-27 1974-07-11 Bayer Ag, 5090 Leverkusen Verfahren zur Herstellung von Allophanatpoly isocy anaten
US3941849A (en) 1972-07-07 1976-03-02 The General Tire & Rubber Company Polyethers and method for making the same
US3941769A (en) * 1972-08-22 1976-03-02 Bayer Aktiengesellschaft Process for the preparation of saccharose-hydroxy alkyl ethers
DE2504400A1 (de) 1975-02-01 1976-08-05 Bayer Ag Lagerstabile, carbodiimidgruppen enthaltende polyisocyanate
DE2523633C2 (de) 1975-05-28 1982-12-16 Bayer Ag, 5090 Leverkusen Verfahren zur Herstellung von Polyurethanschaumstoffen und Katalysatoren zur Durchführung des Verfahrens
DE2537685C2 (de) 1975-08-23 1989-04-06 Bayer Ag, 5090 Leverkusen Verfahren zur teilweisen Carbodiimidisierung der Isocyanatgruppen von organischen Polyisocyanaten
DE2552350A1 (de) 1975-11-21 1977-05-26 Bayer Ag Lagerstabile, carbodiimidgruppen enthaltende polyisocyanate
DE2558523A1 (de) 1975-12-24 1977-07-07 Bayer Ag Verfahren zur herstellung neuer polysiloxan-polyoxyalkylen-copolymerer
DE2618280A1 (de) 1976-04-27 1977-11-17 Bayer Ag Neue katalysatoren fuer die herstellung von polyurethanschaumstoffen
DE2624527A1 (de) 1976-06-01 1977-12-22 Bayer Ag Verfahren zur herstellung von polyurethanen
DE2624528C2 (de) 1976-06-01 1984-03-01 Bayer Ag, 5090 Leverkusen Verfahren zur Herstellung von Polyurethanschaumstoffen
DE2636787A1 (de) 1976-08-16 1978-02-23 Bayer Ag Verfahren zur herstellung von polyurethanen
DE2732292A1 (de) 1977-07-16 1979-02-01 Bayer Ag Verfahren zur herstellung von polyurethankunststoffen
US4332936A (en) 1978-10-16 1982-06-01 Mobay Chemical Corporation Method of making polyether polyols from solid hydroxyl containing initiators
DD147469A3 (de) 1979-08-24 1981-04-08 Siegbert Loeschau Verfahren zur herstellung eines homogenen,fluessigen vorpolymerisats
DE3229216A1 (de) 1982-08-05 1984-02-09 Basf Ag, 6700 Ludwigshafen Verfahren zur reinigung von rohen polyether-polyolen
US4521548A (en) 1983-04-12 1985-06-04 The Dow Chemical Company Preparation of polyether polyols
DD216248A1 (de) 1983-06-27 1984-12-05 Schwarzheide Synthesewerk Veb Verfahren zur herstellung von polyetheralkoholen
DD219204A1 (de) 1983-11-03 1985-02-27 Schwarzheide Synthesewerk Veb Verfahren zur herstellung von polyetheralkoholen
US5158922A (en) 1992-02-04 1992-10-27 Arco Chemical Technology, L.P. Process for preparing metal cyanide complex catalyst
DE4209358C2 (de) 1992-03-23 2003-06-26 Basf Schwarzheide Gmbh Verfahren zur Herstellung von Polyetheralkoholen
JP3263450B2 (ja) 1992-11-27 2002-03-04 三井化学株式会社 粗ポリオキシプロピレンポリオールの精製方法
US5712216A (en) 1995-05-15 1998-01-27 Arco Chemical Technology, L.P. Highly active double metal cyanide complex catalysts
US5470813A (en) 1993-11-23 1995-11-28 Arco Chemical Technology, L.P. Double metal cyanide complex catalysts
CA2143389C (fr) 1994-03-17 1999-05-18 Tohoru Nagashima Elastomere de polyurethane microcellulaire et methode de preparation
US5811566A (en) 1994-07-18 1998-09-22 Asahi Glass Company Ltd. Process for purifying a polyether
US5482908A (en) 1994-09-08 1996-01-09 Arco Chemical Technology, L.P. Highly active double metal cyanide catalysts
WO1996020972A2 (fr) 1995-01-05 1996-07-11 Bayer Corporation Procede d'elimination d'un materiau a ph basique contenu dans un polyol de polyether
US5545601A (en) 1995-08-22 1996-08-13 Arco Chemical Technology, L.P. Polyether-containing double metal cyanide catalysts
US5627120A (en) 1996-04-19 1997-05-06 Arco Chemical Technology, L.P. Highly active double metal cyanide catalysts
DE19627907A1 (de) 1996-07-11 1998-01-15 Basf Ag Verfahren zur Herstellung von kompakten oder zelligen Polyurethan-Elastomeren und hierfür geeignete Isocyanatprepolymere
DE19628145A1 (de) 1996-07-12 1998-01-15 Basf Ag Verfahren zur Herstellung von zelligen Polyurethan-Elastomeren
US5714428A (en) 1996-10-16 1998-02-03 Arco Chemical Technology, L.P. Double metal cyanide catalysts containing functionalized polymers
US5786405A (en) 1996-11-01 1998-07-28 Bayer Corporation Amine-initiated polyether polyols and a process for their production
DE19905611A1 (de) 1999-02-11 2000-08-17 Bayer Ag Doppelmetallcyanid-Katalysatoren für die Herstellung von Polyetherpolyolen
US6376625B1 (en) 1999-08-25 2002-04-23 The Dow Chemical Company Process for purifying polyethers
RO118433B1 (ro) 2000-03-03 2003-05-30 Sc Oltchim Sa Procedeu de obtinere a polieterilor polioli, pe baza de zaharoza, pentru spume poliuretanice rigide
DE10024313A1 (de) 2000-05-17 2001-11-22 Basf Ag Verfahren zur Abtrennung von Alkalimetallionen aus Alkoxylaten
US6491846B1 (en) * 2001-06-21 2002-12-10 Bayer Antwerpen, N.V. Process for the in-situ production of polyol blends, the in-situ produced polyol blends, and their use in the production of viscoelastic foam
DE10237910A1 (de) 2002-08-14 2004-02-26 Basf Ag Verfahren zur Herstellung von hochfunktionellen Polyetherolen
DE10237914A1 (de) 2002-08-14 2004-02-26 Basf Ag Verfahren zur Herstellung von Polyetherolen auf Basis von Oligo- und/oder Polysacchariden
US6696383B1 (en) 2002-09-20 2004-02-24 Bayer Polymers Llc Double-metal cyanide catalysts which can be used to prepare polyols and the processes related thereto
US6869543B2 (en) 2003-02-21 2005-03-22 Bayer Polymers Llc Amine-initiated polyether polyols and a process for their production
DE10336938A1 (de) * 2003-08-07 2005-03-10 Basf Ag Offenzellige Polyurethan-Hartschaumstoffe
US6962967B2 (en) 2004-03-31 2005-11-08 Basf Corporation Method of purifying polyether polyols of non-volatile impurities
US9284401B2 (en) 2006-11-13 2016-03-15 Bayer Materialscience Llc Process for the preparation of polyether-ester polyols
DE102007038436A1 (de) 2007-08-16 2009-02-19 Bayer Materialscience Ag Verfahren zur Herstellung von Polyolen
DE102008011683A1 (de) 2008-02-28 2009-09-03 Bayer Materialscience Ag Verfahren zur Herstellung von Polyolen
DE102008051882A1 (de) * 2008-10-16 2010-04-29 Bayer Materialscience Ag Verfahren zur Herstellung von Polyetheresterpolyolen
SG11201809538TA (en) * 2016-05-13 2018-11-29 Covestro Deutschland Ag Method for the preparation of polyoxyalkylene polyols

Also Published As

Publication number Publication date
EP3741788A1 (fr) 2020-11-25
CN113840859A (zh) 2021-12-24
WO2020239525A1 (fr) 2020-12-03
US20220220304A1 (en) 2022-07-14

Similar Documents

Publication Publication Date Title
EP2177555B1 (fr) Procédé de fabrication de polyéther-ester-polyols
EP1345988B1 (fr) Elastomeres de polyurethanne presentant une stabilite a l'hydrolyse amelioree
EP2770010B1 (fr) Procédé destiné à la fabrication de polyols de polyéther
EP2800769B1 (fr) Procédé de production de mousses dures à base de polyuréthane et à base de polyisocyanurate
EP2828309B1 (fr) Procédé de production de mousses dures de polyuréthane et mousses dures de polyuréthane
EP2804886B1 (fr) Procédé destiné à la fabrication de mousses rigides de polyuréthane
EP2820057B1 (fr) Polyéther-ester-polyols et leur utilisation pour la fabrication de mousses rigides de polyuréthane
EP2655475A1 (fr) Procédé de production de polyéther-ester polyols
EP2770009B1 (fr) Procédé destiné à la fabrication de polyols de polyéther
DE19933819A1 (de) Kompakte und/oder zellige Polyurethanelastomere mit nanoskaligen Füllstoffen
EP4077474B1 (fr) Procédé de fabrication de polyols polyester polyoxyalkylène
EP3762442B1 (fr) Mousses de polyuréthane à base de polyéther carbonates polyoles
EP2483327B1 (fr) Procédé de production de polyols contenant des groupes amino
WO2020239525A1 (fr) Procédé de production de mélanges de polyoxyalkylène polyols
WO2023057328A1 (fr) Procédé de préparation de polyester polyoxyalkylène polyols
DE10063496A1 (de) Polyurethanelastomere mit verbesserter Hydrolysestabilität
WO2023144056A1 (fr) Production de mousses de polyuréthane souples aliphatiques dans un procédé de prépolymère à base de polyisocyanates oligomères aliphatiques et de composés à fonction monohydroxy

Legal Events

Date Code Title Description
STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: UNKNOWN

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE INTERNATIONAL PUBLICATION HAS BEEN MADE

PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: REQUEST FOR EXAMINATION WAS MADE

17P Request for examination filed

Effective date: 20220103

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: EXAMINATION IS IN PROGRESS

17Q First examination report despatched

Effective date: 20230417

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: COVESTRO DEUTSCHLAND AG