MXPA00009957A - Method for producing long-chain polyetherpolyols without reprocessing - Google Patents

Abstract

The invention relates to a method for producing long-chain polyetherpolyols without reprocessing. Oligomeric alkoxylated initiation compounds with molecular weights of between 200 and 1000 are obtained first from low-molecular initiators by catalysis with perfluoroalkyl sulfonates of metals of Group III A of the periodic table (in accordance with the IUPAC Convention of 1970), through reaction with alkylene oxides at reaction temperatures of 80 to 200oC and with concentrations of the catalyst of 5 to 200 ppm. Said initiation compounds are then reacted with alkylene oxides to produce higher-molecular long-chain polyether polyols without being reprocessed and without the catalyst being separated, using highly active DMC catalysts, the concentration of catalysts being 30 ppm or less in relation to the quantity of polyether polyol to be produced.

Description

PROCESS FOR PRODUCTIONS POLYOLS OF LONG CHAIN POLYETER WITHOUT REPROCESSING The present invention relates to a process for the production without reprocessing of long chain polyether polyols.

The polyether polyols are obtained by the polyaddition of alkylene oxides, such as, for example, ethylene oxide, propylene oxide, butylene oxide, to compounds containing active hydrogen atoms, such as alcohols, amines, amides. acids, phenols, which are used in t er alia for the production of plastics based on polyurethane, surfactants and lubricants. The polyaddition of epoxides on initiator compounds is conventionally carried out industrially by alkaline metal catalysis. The alkaline metal catalysts used predominantly are the alkali metal hydroxides. The disadvantages of the production of polyether polyols with catalysis by metal hydroxides Ref. 123796 alkaline, are mainly the elaborate reprocessing of the product due to the neutralization of the alkaline polymer (for example, US 5 715 402, US 4 450 490, US 4 507 475 and US 4 157 598) and the re-arrangements of epoxides by base catalysis, for example propylene oxide, which proceeds as a secondary reaction, to produce propenyl or aulic alcohols, which are increased to monofunctional polyethers having a terminal double bond, which are known as monools. A known method for reducing the monool content in polyether polyols is the use of double metal cyanide (DMC) complex compounds as catalysts for the polyaddition of epoxides to initiator compounds (see for example US 5 documents). 404 109, US 5 829 505, US 5 941 849 and US 5 158 922). The polyether polyols obtained in this way can be processed to produce high grade polyurethanes (eg, elastomers, foams, coatings). EP 700 949, EP 761 708, WO 97/40086 and DE-A 197 45 120.9, 197 57 574.9 and 198 102 269. 0; describe improved DMC-type catalysts that allow a further reduction in the fraction of monofunctional polyethers having terminal double bonds in the production of polyether polyols. The improved DMC catalysts are highly active, and allow the production of polyether polyols at low rates of catalyst use (25 ppm or less), such that it is no longer necessary to separate the catalyst from the polyol (with a example on page 5, lines 24-29 of EP 700 949).

A disadvantage in the use of DMC type catalysts for the production of polyether polyols, is that these catalysts usually require an induction period. Unlike alkali metal catalysts, DMC type catalysts do not initiate epoxide polymerization immediately, once the epoxide and initiator compound have been added to the catalyst. The DMC type catalyst must first be activated with a small amount of epoxide. The induction periods typically have a duration of a few minutes to several hours.

Another disadvantage is that the conventional low molecular weight initiator compounds for the synthesis of the polyether polyol by alkaline metal catalysis, such as, for example, propylene glycol, glycerol or trimethylolpropane, can not be alkoxylated with DMC type catalysts. Thus, DMC type catalysts require the use of alkoxylated initiator compounds, eg, a propylene glycol or a propoxylated glycerol, having molecular weights greater than 200, which have been previously obtained from the starter primers. low molecular weight above, by means of, for example, conventional alkaline metal catalysis (eg, KOH catalysis) and the subsequent reprocessing made by neutralization, filtration and dehydration. Problematically, even very small residual amounts of alkali metal catalyst, in the alkoxylated initiator compounds, can deactivate the DMC catalyst, so that a further phase of additional reprocessing is necessary, which consumes time (for example, the treatment with a ion exchanger or adsorbent), this in order to ensure a complete removal of the alkali metal catalyst of the alkoxylated initiator compound. According to the above, the aim of the present invention is to provide a process for producing polyether polyols, long chain, without reprocessing; wherein the alkoxylated initiator compounds, oligomeric, are first obtained from the low molecular weight initiator compound (for example from propylene glycol or trimethylolpropane), by an alternative catalysis to conventional alkaline metal catalysis, whose alkoxylated initiator compounds, or igomeric compounds, they can then be extended directly, i.e. without further processing or removal of the catalyst, to produce long-chain polyether polyols, by highly active DMC type catalysts at very low catalyst rates (30 ppm or less). German Patent Application No. 197 02 787.3 describes a process for producing polyether polyols by catalysis with acid salts perfluoroalkylsulphonic (perfluoroalkylsulphates) of the metals of group III of the periodic system of the elements (according to the IUPAC convention of the year 1970). Now surprisingly it has been found that, the alkoxylated initiator compounds, oligomers, having molecular weights of between 200 and 1000, which have been obtained by the catalysts of the metal perfluoroalkylsulphonate described in the above-mentioned German patent application, from conventional low molecular weight initiators, such as for example propylene glycol or trimethylolpropane, by reaction with alkylene oxides at reaction temperatures of 80 ° to 200 ° C, and catalyst concentrations of from 5 to 200 ppm, based on with the amount of the alkoxylated, oligomeric initiator compound to be produced, it can be converted directly, i.e., without reprocessing and catalyst removal, by means of highly high-DMC type catalysts at very low catalyst usage rates (30 ppm or less) through the reaction with alkylene oxides, in polyether polyols of long chain, of higher molecular weight. In this way, long-chain polyether polyols can be produced completely without reprocessing. It has also been found that when the alkoxylated initiator compounds are used, obtained by catalysis with the metal per-fluoroalkylsulphates; the induction and alkoxylation times in the DMC catalysis are clearly reduced compared to the use of the corresponding oligomeric initiator compounds, which were produced by alkaline metal catalysis and conventional processing. By shortening the cyclic times in the production of polyether polyols, the reduced induction and alkoxylation times also improve the economic viability of the process. Accordingly, the present invention provides a process for the production of long-chain polyether polyols without reprocessing, in which the alkoxylated, oligomeric initiator compounds having molecular weights of 200 to 1000 are first obtained by catalysis with the per fluoroalkylsulphates of the group III metals of the periodic system of the elements (according to the IUPAC convention of the year 1970), starting from low molecular weight initiators by reaction with alkylene oxides at reaction temperatures of 80 to 200 ° C, and catalyst concentrations of 5 to 200 ppm, whose alkoxylated, oligomeric initiator compounds are subsequently converted without reprocessing or catalyst removal by means of highly active DMC type catalysts at a catalyst concentration of 30 ppm or less, relative to the amount of polyether polyols to be produced, by reaction with alkylene oxides in higher molecular weight long chain polyether polyols. The catalysts used according to the present invention for the production of alkoxylated, oligomeric initiator compounds are the per fluoroalkyl sulphates of group III metals of the periodic system of the elements (according to the IUPAC convention of the year 1970). This includes the metals scandium, yttrium, and rare earth metals lanthanum, cerium, praseodymium, neodymium, prometheus, samarium, europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, and luteum. An additional metal that can be used is "mixed metal" (also known as "didimio"), a mixture of rare earths obtained from the ore. Perfluoroalkylsulphates are considered metal salts of perfluoroalkylsulphonic acids, in which the metal is bound to at least one perfluoroalkylsulfonate group. Other suitable anions may also be present. The preferred compounds are the metal salts of trifluoromethanesulonic acid, which are known as tri fluorometanesulphates or triflates. Preferably the following are used: scandium triflate, yttrium, lanthanum, cerium, praseodymium, neodymium, samarium, europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, and lutetium triflate.

The per-fluoroalkylsulphates can be used individually or as a mixture.

The alkylene oxides are preferably ethylene oxide, propylene oxide, butylene oxide and mixtures thereof. The synthesis of the polyether chains by alkoxylation can, for example, be carried out only with a monomeric epoxide or alternatively also in the form of blocks or randomly different monomeric epoxides. The propylene oxide is used in a particularly preferred way. The low molecular weight initiators used are compounds having molecular weights of 18 to 400 and 1 to 8 hydroxyl groups. The following may be mentioned by way of example: ethylene glycol, diethylene glycol, triethylene glycol, 1,2-propylene glycol, dipropylene glycol, 1,4-butanediol, hexamethyl glycol, bisphenol A, trimethylolpropane, glycerol, pentaerythritol, sorbitol, cane sugar, starch. degraded and water. The low molecular weight initiators can be used individually or as a mixture. The polyaddition catalyzed by the metal perfluoroalkylsulfonates proceeds within the temperature range of 80 to 200 ° C, preferably within the range of 90 to 180 ° C, particularly preferred within 100 to 160 ° C, at a total pressure of 0.001 to 20 bars. The process can be carried out without solvent or in an inert organic solvent, such as, for example, toluene, xylene or THF. The amount of solvent is conventionally 10 to 30 percent by weight. Preferably the reaction is carried out without solvent. The catalyst concentration is in the range from 5 to 200 ppm, preferably from 5 to 100 ppm, particularly preferably from 10 to 50 ppm, in each case in relation to the amount of the alkoxylated initiator compound, oligomeric, to be produced. The reaction times for the polyaddition are within the range from a few minutes to several days. The molecular weights of the alkoxylated, oligomeric initiator compounds produced by the metal fluoroalkyl sulfonates are within the range of 200 and 1000 g / mol, preferably within the range of 200 and 800 g / mol. Polyaddition processes can be performed continuously, in a batch or semi-batches process. The oligomeric, alkoxylated initiator compounds produced in accordance with the present invention can be extended directly, ie, without reprocessing and catalyst removal, additionally by means of DMC type catalysts to produce long-chain, higher molecular weight polyether polyols. high. The highly volatile fractions are preferably first separated from the alkoxylated, oligomeric initiator compound, by distillation under reduced pressure (0.01-100 mbar) and at elevated temperatures (50-150 ° C). The two phases of polyaddition can be carried out separately (temporarily and / or separately, that is, in different reaction vessels) or simultaneously as a so-called "Single reaction vessel". The highly active DMC type catalysts to be used to produce the polyether polyols long chain, without the reprocessing of alkoxylated, oligomeric initiator compounds, are known in principle and are described comprehensively, for example, in EP 700 949, EP 761 708, WO 97/40086 and in DE- A 197 45 120, 197 57 574 and 198 102 269. Typical examples are the highly active DMC catalysts described in EP 700 949, which, apart from a double metal cyanide compound (for example, zinc hexacyanocobaltate) and an organic complex ligand (for example tert-butanol), additionally contain a polyether having an average molecular weight number greater than 500. The alkylene oxides preferably used for the polyaddition are ethylene oxide, propylene oxide, butylene oxide and mixtures thereof. The synthesis of the polyether chains by alkoxylation can, for example, be carried out with only one monomeric epoxide or alternatively also in block form or in a random manner with 2 or 3 different monomeric epoxides. Additional details can be find in the document Ullmanns Encycl Opadi e der i ndus tri el l in Ch emi e, Edition in the English language, 1992, volume A21, pages 670-671. Propylene oxide is used particularly preferably. The initiators used according to the present invention are the alkoxylated, oligomeric initiator compounds having from 1 to 8 hydroxyl groups, which have been previously produced from the aforementioned low molecular weight initiators, by means of catalysis by the per f luoroal quilsul metal strips without the removal of the catalyst, and those having molecular weights of between 200 and 1000 g / mol, preferably between 200 and 800 g / mol. The alkoxylated, oligomeric initiator compounds can be used individually or as a mixture. The polyaddition, catalyzed by the highly active DMC catalysts, of alkylene oxides on the alkoxylated, oligomeric initiator compounds containing active hydrogen atoms, generally proceeds at temperatures of 20 to 200 ° C, preferably within from the range of 40 to 180 ° C, particularly preferable at temperatures of 50 to 150 ° C. The reaction can be carried out at total pressures of 0.001 at 20 bars. The polyaddition can be carried out without solvent or in an inert organic solvent, such as, for example, toluene, xylene or THF. The amount of solvent is conventionally from 10 to 30 weight percent relative to the amount of the polyether polyol to be produced. The preferred reaction is carried out without solvent. The catalyst concentration is 30 ppm or less, preferably 25 ppm or less, particularly preferably 20 ppm or less, in each case in relation to the amount of polyol of long chain polyether to be produced. The lowest catalyst concentration is 0.1 ppm.

At these low catalyst concentrations, it is not necessary to make the product. To be used in polyurethane applications, it is possible to ignore or not consider the removal of the polyol catalyst, without any negative impact on the quality of the product.

The reaction times for the polyaddition are within the range of a few minutes to several days, preferably a few hours. The molecular weights of the long chain polyether polyols produced using the process according to the present invention are within the range of 1000 to 100000 g / mol, preferably in the range of 1000 to 50000 g / mol , particularly preferred within the range of 2000 to 20,000 g / mol. The polyaddition can be carried out continuously, in a batch or semi-batches process. Highly active DMC catalysts generally require an induction time of a few minutes to several hours. By using the alkoxylated, oligomeric initiator compounds according to the present invention, by catalysis with the metal per-fluoroalkyl sulphates, a clear reduction (approximately 25%) in the induction times in the DMC catalysis is originated or presented, in comparison with the use of the initiator compounds alkoxylates, corresponding oligomers that were produced by alkaline metal catalysis and without conventional reprocessing (neutralization, filtration, dehydration). At the same time, by using the oligomeric initiator compounds produced by catalysis with the metal per-fluoroalkylsulphates, the alkoxylation times in the DMC-type catalysis are also substantially reduced (by approximately 50-60%). This results in a reduction of the complete reaction times (sum of the induction and alkoxylation times) typically by some 50%. In this way, the reduction in cyclic times in the production of polyether polyols improves the economic viability of the process.

Examples Production of highly active DMC type catalyst (synthesis according to EP 700 949).

»Bfc. ' To a solution of 4 g (12 mmol) of potassium hexacyanocobaltate in 70 ml of distilled water, a solution of 12.5 g (91.5 mmol) of zinc chloride in 20 ml of distilled water is added with vigorous stirring (24000 rpm). Immediately afterwards, a mixture of 50 g of tert-butanol and 50 g of distilled water are added to the resulting suspension and subsequently stirred vigorously for 10 minutes (24000 rpm). Then a mixture of 1 g of propylene glycol having an average molecular weight of 2000, 1 g of tert-butanol and 100 g of distilled water is added, and once added it is agitated for 3 minutes (1000 rpm). The solid is isolated by filtration, then stirred for 10 minutes with a mixture of 70 g of tert-butanol, 30 g of distilled water and 1 g of the above polyether (10,000 rpm) and filtered again. The mixture is finally stirred once more for 10 minutes with a mixture of 100 g of tert-butanol and 0.5 g of the above polyether (10000 rpm). After filtration, the catalyst is dried to constant weight at a temperature of 50 ° C and standard pressure.

Production of dry pulverulent catalyst: 6.23 g The elemental analysis and the thermogravimetric analysis: Cobalt = 11.6%, zinc = 24.6%, tert-butanol = 3.0%, polyether = 25.8%.

Example 1 Phase A Production of the oligomeric propoxylated starter compound by means of yttrium triflate catalysis 1839 g of trimethylolpropane (TMP) and 0.12 g of yttrium triflate catalyst (20 ppm, relative to the amount of the propoxylated initiator compound to be produced) are introduced under protective gas (nitrogen) in a 10 liter, glass flask , under pressure, and heated to 130 ° C while stirring. Then 4161 g of oxide of ^ iiÉ ^^ propylene by means of a membrane pump at a temperature of 130 ° C and a total pressure of 1.5 bars. Once the propi-isine oxide has been completely distributed and after the post-reaction time of 5 hours, at a temperature of 130 ° C, the volatile fractions are removed by distillation at a temperature of 105 ° C (1 mbar) and then the temperature is reduced to ambient temperature. The resulting propoxylated initiator compound is a colorless oil having an OH value of 365 mg KOH / g.

Phase B Production of long-chain polyether polyols, from the propoxylated, oligomeric initiator compound by DMC catalysis. 460 g of the propoxylated initiator compound from phase A, and 0.12 g of the DMC catalyst (20 ppm, relative to the amount of the long-chain polyether polyol to be produced) are introduced to protective gas (or trógeno) in a flask of 10 liters, glass, under pressure, and heated to 105 ° C while stirring. The propylene oxide (approximately 50 g) is then distributed in a single portion until the total pressure has reached 1.5 bars. No additional propylene oxide is distributed until an accelerated pressure drop is observed. This accelerated pressure drop indicates that the catalyst is activated. The remaining propylene oxide (5490 g) is then continuously distributed at a constant total pressure of 1.5 bars. Once the propylene oxide has been completely distributed and after a post-reaction time of 5 hours at a temperature of 105 ° C, the volatile fractions are removed by distillation at a temperature of 105 ° C (1 mbar) and then the temperature is reduced to room temperature. The resulting long chain polyether polyol has an OH value of 28.5 mg KOH / g and a double bond content of 7 mmol / kg. The induction time was determined from the time / conversion curve (propylene oxide consumption [g] versus reaction time [min]) to From the intersection of the tangent at the highest point of the time / conversion curve with the extended baseline of the curve. The propoxylation time corresponds to the period between the activation of the catalyst (end of the induction period) and the end of the propylene oxide distribution. The total time of the reaction is the sum of the induction and propoxylation times.

Induction time: 180 minutes Propoxylation time: 240 minutes Total reaction time: 420 minutes Comparative Example 2 Production of the long-chain polyether polyol by DMC catalysis from the oligomeric propoxylated starter compound, which was obtained by means of KOH catalysis and without conventional reprocessing (removal of the catalyst by neutralization and filtration).

J As in Example 1, phase B, but initial introduction of 437 g of a poly (oxypropylene) triol having an OH value of 580 mg KOH / g (produced from trimethylolpropane and propylene oxide by KOH catalysis and without conventional reprocessing) distribution of a total of 5563 g of propylene oxide.

The resulting long chain polyether polyol has an OH value of 29.3 mg KOH / g and a double bond content of 6 mmol / kg.

Induction time: 240 minutes Propoxylation time: 555 minutes Total reaction time: 795 minutes Example 3 Phase A Production of oligomeric propoxylated starter compound by means of yttrium triflate catalysis, 2627 g of trimethylolpropane (TMP) and 0.12 g of yttrium triflate catalyst (20 ppm, relative to the amount of the propoxylated starter compound to be produced) are introduced under protective gas (nitrogen) in a 10 liter glass flask. , under pressure, and heated to 130 ° C while stirring. Then 3375 g of propylene oxide are distributed by means of a membrane pump at a temperature of 150 ° C and a total pressure of 1.5 bars. Once the propylene oxide has been completely distributed and after the post-reaction time of 5 hours at a temperature of 150 ° C, the volatile fractions are removed by distillation at a temperature of 105 ° C (1 mbar) and then the temperature is reduced to the ambient temperature.

The resulting propoxylated initiator compound is a colorless oil having an OH value of 538 mg KOH / g.

Phase B Production of the long-chain polyether polyol from the oligomeric propoxylated starter by DMC catalysis. 324 g of the propoxylated initiator compound from phase A, and 0.18 g of the DMC catalyst (30 ppm, relative to the amount of the long chain polyether polyol to be produced), are introduced under protective gas (nitrogen) in a 10-liter flask, glass, pressurized, and heated to 105 ° C while stirring. The propylene oxide (approximately 30 g) is then distributed in a single portion until the total pressure has reached 1.5 bars. No additional propylene oxide is distributed until an accelerated pressure drop is observed. This accelerated pressure drop indicates that the catalyst is activated. This remaining propylene oxide (5646 g) is then distributed continuously at a constant total pressure of 1.5 bars. Once the propylene oxide has been completely distributed and after a post-reaction time of 5 hours at a temperature of 105 ° C, the volatile fractions are removed by distillation at a temperature of 105 ° C (1 mbar) and then the temperature is reduced to room temperature. The resulting long chain polyether polyol has an OH value of 29.8 mg KOH / g and a double bond content of 6 mmol / kg.

Induction time: 390 minutes Propoxylation time: 405 minutes Total reaction time: 795 minutes Comparative Example A The production of the long-chain polyether polyol by DMC catalysis, from the oligomeric propoxylated initiator compound, which was obtained by means of KOH catalysis and without conventional reprocessing.

As in Example 3, phase but initial introduction of 316 g of a poly (oxypropylene) triol having an OH value of 550 mg KOH / g (produced from trimethylolpropane and propylene oxide by KOH catalysis and without conventional reprocessing) after an initial distribution of approximately 50 g of propylene oxide increases up to a total pressure of 1.5 bars, no pressure drop occurs during a period of 22 hours, i.e., the catalyst is not activated.

Examples 1 and 5 show that the propoxylated, oligomeric initiator compounds are obtained by catalysis with the metal per-fluoroalkyl sulphates described in DE-A 197 02 787 at very low proportions of catalyst (20 ppm), from initiators. below jtjst - J == a ». conventional molecular weight (for example, propylene glycol trimethylolpropane) by reaction with propylene oxide, whose propoxy, oligomeric initiator compounds can be converted directly, ie without reprocessing and catalyst removal, by means of highly active DMC-type catalysts at very low proportions of catalyst (< 50 ppm) by reaction with propylene oxide, in long chain polyether polyols. Thus, using the process according to the present invention, it is possible to produce long chain polyether polyols completely without reprocessing. A comparison of Example 1 with Comparative Example 2 shows that when using the propoxylated, oligomeric initiator compounds obtained by catalysis with metal per-fluoroalkylsulfonates, the induction and propoxylation times in DMC catalysis are clearly shortened in comparison with the use of corresponding initiator compounds, which were produced by KOH catalysis and without conventional reprocessing (neutralization, filtration, dehydration). In the process according to the present invention, this shortens the total reaction times of the DMC catalysis by some 50%.

It is noted that in relation to this date, the best method known to the applicant, to carry out the aforementioned invention is that it is clear from the present description of the invention.

Having described the invention as an antecedent, the content of the following is claimed as property:

Claims (6)

1. A process for the production of long-chain polyether polyols without reprocessing, characterized in that the alkoxylated initiator compounds, which have molecular weights of 200 to 1000, are first obtained by catalysis with per-fluoroalkylsulphates of group III metals A of the periodic system of the elements (according to the IUPAC convention of the year 1970), from low molecular weight initiators by reaction with alkylene oxides at reaction temperatures of 80 to 200 ° C and catalyst concentrations of 5%. at 200 ppm, whose alkoxylated, oligomeric initiator compounds are then converted without reprocessing and removal, by means of highly active DMC type catalysts at a catalyst concentration of 30 ppm or less, relative to the amount of polyether polyol to be produced, by the reaction of alkylene oxides, in long-chain polyether polyols of molecular weight m Higher

2. A process for producing polyether polyols of long chain without reprocessing, according to claim 1, characterized in that of the per fluoroalkyl sulfonates of the metals of group III A of the periodic system of the elements (in accordance with the IUPAC convention of the year 1970 ), which are used are the corresponding trifluoromethanesulfonates (triflates).

3. A process for the production of polyether polyols of long chain without reprocessing, according to claim 1, characterized in that the per fluoroalkyl sulphonate of the metals of group III A of the periodic system of the elements (according to the IUPAC convention of the year 1970), is selected from the compounds triflate of scandium, yttrium, lanthanum, cerium, praseodymium, neodymium, samarium, europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, and lutetium or mixtures thereof.

4. A process for producing long-chain polyether polyols without reprocessing, according to claim 1, characterized in that the low molecular weight initiators that are used are ethylene glycol, diethylene glycol, ethylene glycol, 1,2-propylene glycol, dipropylene glycol, 1,4-butane diol, hexamethylene glycol, bisphenol A, trimethylolpropane, glycerol, pentaerythritol. , sorbitol, sugar cane, degraded starch, water and mixtures thereof.

5. A process for producing long-chain polyether polyols without reprocessing, according to the rei indication 1, characterized in that the production of alkoxylated, oligomeric initiator compounds, by the reaction of low molecular weight initiators with alkylene oxides, by means of the catalysis with the per fluoroalkyl sulphonates of group III A metals from the periodic system of the elements (according to the IUPAC convention of 1970), is carried out at reaction temperatures of 90 to 180 ° C and catalyst concentrations of 5%. at 100 ppm, relative to the amount of the alkoxylated, oligomeric starter compound to be produced.

6. A process for producing long-chain polyether polyols without reprocessing, according to claim 1, characterized in that the production of alkoxylated initiator compounds, oligomeric, by the reaction of low molecular weight initiators with alkylene oxides by means of catalysis with the per fluoroalkylsulphates of the metals of group III A of the periodic system of the elements (according to the IUPAC convention of the year 1970), it is carried out at reaction temperatures of 100 to 160 ° C and in catalyst concentrations of 10 to 50 ppm, relative to the amount of the alkoxylated, oligomeric initiator compound to be produced.