WO2025051643A1 - Process for producing double metal cyanide catalysts - Google Patents

Abstract

The invention relates to an improved process for producing double metal cyanide (DMC) catalysts for producing polyoxyalkylene polyols, preferably polyether polyols and/or polyether carbonate polyols. The invention also relates to DMC catalysts which are obtainable by means of this process, and to the use of the catalysts according to the invention for producing polyoxyalkylene polyols.

Description

Process for the preparation of double metal cyanide catalysts

The present invention relates to an improved process for the preparation of double metal cyanide (DMC) catalysts for the production of polyoxyalkylene polyols, preferably polyether polyols and/or polyether carbonate polyols. It also relates to DMC catalysts obtainable by this process and to the use of the catalysts according to the invention for the production of polyoxyalkylene polyols.

DMC catalysts are in principle known from the prior art (see, for example, US-A 3,404,109, US-A 3,829,505, US-A 3,941,849 and US-A 5,158,922). DMC catalysts, which are described, for example, in US-A 5 470 813, EP-A 700 949, EP-A 743 093, EP-A 761 708, WO 97/40086, WO 98/16310, WO 00/47649, and WO 2021/165283 A1, have a very high activity in the homopolymerization of epoxides and enable the production of polyether polyols at very low catalyst concentrations (25 ppm or less), so that separation of the catalyst from the finished product is generally no longer necessary. A typical example are the highly active DMC catalysts described in EP-A 700 949, which contain, in addition to a double metal cyanide compound (e.g. zinc hexacyanocobaltate(III)) and an organic complex ligand (e.g. tert-butanol), a polyether with a number-average molecular weight greater than 500 g/mol.

WO 01/39883 A1 discloses a process for the preparation of double metal cyanide (DMC) catalysts for the production of polyether polyols by polyaddition of alkylene oxides to starter compounds containing active hydrogen atoms. The DMC catalyst dispersion is prepared using a mixing nozzle, preferably a jet disperser. The DMC catalysts thus prepared exhibit increased activity, reduced particle size, and narrower particle size distribution in polyether polyol production.

WO 01/80994 A1 also discloses a process for preparing double metal cyanide (DMC) catalysts, in which aqueous solutions of a metal salt and a metal cyanide salt are first reacted in the presence of an organic complex ligand and optionally one or more further complex-forming components to form a DMC catalyst dispersion. This dispersion is then filtered, the filter cake is subsequently washed with one or more aqueous or non-aqueous solutions of the organic complex ligand and optionally one or more further complex-forming components by filter cake washing, and the washed filter cake is finally dried after optional pressing or mechanical dehumidification. The disclosed process shortens the time required for catalyst preparation, with the resulting catalysts having comparable activities in the production of polyether polyols compared to reference catalysts.

EP 700 949 A2 describes a DMC catalyst containing DMC compound, an organic complex ligand and 5 - 80 wt. % of a polyether with a number-average molecular weight > 500 g/mol, wherein the preparation of the DMC catalyst dispersion takes place at room temperature. The catalysts used generally have activity in the production of polyether polyols.

WO 2021/148272 A1 discloses a process for producing a double metal cyanide catalyst (DMC), wherein the resulting DMC catalysts exhibit increased catalytic activity in the production of polyoxyalkylene polyols, for example, in catalyst testing according to the "8K Diol Stressed Test." This involves reacting an aqueous solution of a cyanide-free metal salt, an aqueous solution of a metal cyanide salt, an organic complex ligand, and polypropylene glycol as a complexing component to form a dispersion. The reaction is carried out using a mixing nozzle, and the process temperature of the dispersion during the reaction is between 26°C and 49°C.

US 2019/0185399 A1 discloses a highly active double metal cyanide catalyst, a process for its preparation and applications thereof for the production of polyether polyols, wherein a mixture of a fatty alcohol such as tert-butanol and an alicyclic carbonate such as cyclic ethylene carbonate is used as an organic complex ligand in the preparation of the double metal cyanide catalyst.

The object of the present application was to provide an improved process for the production of double metal cyanide (DMC) catalysts with further increased catalytic activity in the production of polyoxyalkylene polyols, preferably polyether polyols and/or polyether carbonate polyols. This improved activity leads to reduced product viscosity, for example, in catalyst testing in the semibatch polyol production process according to the "8K Diol Stressed Test," which is described, for example, in WO 98/16310 A1, but also in the continuous polyol production process. The aim was therefore to provide more catalytically active DMC catalysts that lead to polyoxyalkylene polyols, preferably polyether polyols and/or polyether carbonate polyols, with a reduced viscosity, which facilitates the further processability of the polyoxyalkylene polyols in the subsequent polyurethaneization reaction. The increased catalyst activity also enables a reduction in the amount of catalyst used, which improves the economics of the process.

At the same time, the production process of the DMC catalyst dispersion should be carried out with a comparably simple apparatus design, low energy consumption during shearing, good temperature control, and also good scalability compared to known technical processes in order to enable easy implementation in existing DMC catalyst production processes, for example in loop reactors.

Surprisingly, it has now been found that a process for preparing a double metal cyanide catalyst (DMC) comprising i) reacting an aqueous solution of a cyanide-free metal salt, an aqueous solution of a metal cyanide salt, an organic complex ligand and optionally a complex-forming component, characterized in that the organic complex ligand contains a dialkyl carbonate, wherein the organic complex ligand contains, in addition to the dialkyl carbonate, preferably dimethyl carbonate, a further compound (1), wherein the compound (1) is one or more compound(s) and is selected from the group consisting of dimethoxyethane, tert-butanol, 2-methyl-3-buten-2-ol, 2-methyl-3-butyn-2-ol, ethylene glycol mono-tert-butyl ether and 3-methyl-3-oxetane methanol and wherein the mass fraction of the dialkyl carbonate is from 1% to 25%, based on the sum of the masses of the compound (1) and the dialkyl carbonate, which solves the above-mentioned problem.

The invention is explained below, whereby the embodiments according to the invention can be combined with one another as desired, unless the technical context indicates otherwise.

Organic complex ligand

In the process according to the invention, the organic complex ligand contains a dialkyl carbonate.

According to the general technical definition, the dialkyl carbonate according to the invention is understood to be a reaction product obtainable from the condensation reaction of carbonic acid (formally CCU'HiO or H2CO3) with alcohols R'-OH and/or ^R2 -OH, where the radicals ^R1 and ^R2 each contain no aromatic units. Preferably, the radicals ^R1 and ^R2 contain only aliphatic hydrocarbon units such as methyl, ethyl, or n-propyl.

In one embodiment of the process according to the invention, the dialkyl carbonate has a structure according to formula (I):

R'-OC(=O)-OR ² (I)

, where R ¹ and R ² are independently methyl, ethyl, iso-propyl, n-propyl, iso-butyl, n-butyl, tert-butyl, iso-pentyl, n-pentyl, tert-pentyl, preferably methyl, ethyl and n-propyl, particularly preferably methyl.

In a preferred embodiment of the process according to the invention, the dialkyl carbonate is one or more compounds and is selected from the group consisting of dimethyl carbonate, diethyl carbonate, di-n-propyl carbonate, di-n-butyl carbonate, preferably dimethyl carbonate, diethyl carbonate, di-n-propyl carbonate, particularly preferably dimethyl carbonate.

In a particularly preferred embodiment of the process according to the invention, the dialkyl carbonate is dimethyl carbonate with R'=R ² =methyl.

According to the invention, the organic complex ligand contains, in addition to the dialkyl carbonate, preferably dimethyl carbonate, another compound (1).

The compounds (1) added as organic complex ligands in the preparation of the DMC catalysts are described, for example, in US 5 158 922 (see in particular column 6, lines 9 to 65), US 3 404 109, US 3 829 505, US 3 941 849, EP-A 700 949, EP-A 761 708, JP 4 145 123, US 5 470 813, EP-A 743 093, WO 99/46042, and WO-A 97/40086. For example, water-soluble organic compounds containing heteroatoms, such as oxygen, nitrogen, phosphorus, or sulfur, which can form complexes with the double metal cyanide compound, are used as organic complexing ligands. Preferred organic complexing ligands are alcohols, aldehydes, ketones, ethers, esters, amides, ureas, nitriles, sulfides, and mixtures thereof.

Particularly preferred compounds (1) are aliphatic ethers (such as dimethoxyethane), water-soluble aliphatic alcohols (such as ethanol, isopropanol, n-butanol, iso-butanol, sec-butanol, tert-butanol, 2-methyl-3-buten-2-ol and 2-methyl-3-butyn-2-ol) and compounds containing both aliphatic or cycloaliphatic ether groups and aliphatic hydroxyl groups (such as ethylene glycol mono-tert-butyl ether, diethylene glycol mono-tert-butyl ether, tripropylene glycol monomethyl ether and 3-methyl-3-oxetane methanol).

In one embodiment of the process according to the invention, the compound (1) is tert-butanol.

In one embodiment of the process according to the invention, the mass fraction of the dialkyl carbonate, preferably of the dimethyl carbonate, is from 2% to 25%, preferably from 7% to 25%, based on the sum of the masses of the compound (1) and the dialkyl carbonate, preferably of the dimethyl carbonate.

Double metal cyanide compound

In one embodiment of the process according to the invention, double metal cyanide compounds of formula (II) are contained in the DMC catalyst:

M _x [M' _x ,(CN) _y ] _z (II), where

M is selected from one or more metal cations of the group consisting of Zn(II), Fe(II), Ni(II), Mn(II), Co(II), Sr(II), Sn(II), Pb(II) and Cu(II), preferably Zn(II), Fe(II), Co(II) and Ni(II), and

M' is selected from one or more metal cations of the group consisting of Fe(II), Fe(III), Co(II), Co(III), Cr(II), Cr(III), Mn(II), Mn(III), Ir(III), Ni(II), Rh(III), Ru(II), V(IV) and V(V), preferably Co(III), Fe(III), Cr(III) and Ir(III), and x, x', y and z are integers and are chosen such that the electron neutrality of the double metal cyanide compound is given, wherein preferably x = 3, x' = 1, y = 6 and z = 2.

In a preferred embodiment of the process according to the invention, the double metal cyanide compound is one or more compounds selected from the group consisting of zinc hexacyanocobaltate(III), zinc hexacyanoiridate(III), zinc hexacyanoferrate(III), and cobalt(II) hexacyanocobaltate(III). Zinc hexacyanocobaltate(III) is particularly preferably used. Cxanide-free metal sac

Cyanide-free metal salts suitable for the preparation of the double metal cyanide compounds preferably have the general formula (III),

M(X) _n (III) where

M is selected from the metal cations Zn ²⁺ , Fe ²⁺ , Ni ²⁺ , Mn ²⁺ , Co ²⁺ , Sr ²⁺ , Sn ²⁺ , Pb ²⁺ and Cu ²⁺ , preferably M is Zn ²⁺ , Fe ²⁺ , Co ²⁺ or Ni ²⁺ ,

X is one or more (i.e. different) anions, preferably an anion selected from the group of halides (i.e. fluoride, chloride, bromide, iodide), hydroxide, sulfate, carbonate, cyanate, thiocyanate, isocyanate, isothiocyanate, carboxylate, oxalate and nitrate; n is 1 if X is sulfate, carbonate or oxalate and n is 2 if X is halide, hydroxide, cyanate, thiocyanate, isocyanate, isothiocyanate or nitrate, or suitable cyanide-free metal salts have the general formula (IV),

M _r (X) ₃ (IV) where

M is selected from the metal cations Fe ³⁺ , Al ³⁺ and Cr ³⁺ ,

X is one or more (i.e. different) anions, preferably an anion selected from the group of halides (i.e. fluoride, chloride, bromide, iodide), hydroxide, sulfate, carbonate, cyanate, thiocyanate, isocyanate, isothiocyanate, carboxylate, oxalate and nitrate; r is 2 if X is sulfate, carbonate or oxalate and r is 1 if X is halide, hydroxide, cyanate, thiocyanate, isocyanate, isothiocyanate, carboxylate or nitrate, or suitable cyanide-free metal salts have the general formula (V),

M(X) _S (V) where

M is selected from the metal cations Mo ⁴⁺ , V ⁴⁺ and W ⁴⁺ X is one or more (i.e. different) anions, preferably an anion selected from the group of halides (i.e. fluoride, chloride, bromide, iodide), hydroxide, sulfate, carbonate, cyanate, thiocyanate, isocyanate, isothiocyanate, carboxylate, oxalate and nitrate; s is 2 if X = sulfate, carbonate or oxalate and s is 4 if X = halide, hydroxide, cyanate, thiocyanate, isocyanate, isothiocyanate, carboxylate or nitrate, or suitable cyanide-free metal salts have the general formula (VI),

M(X) _t (VI) where

M is selected from the metal cations Mo ⁶⁺ and W ⁶⁺

X is one or more (i.e. different) anions, preferably an anion selected from the group of halides (i.e. fluoride, chloride, bromide, iodide), hydroxide, sulfate, carbonate, cyanate, thiocyanate, isocyanate, isothiocyanate, carboxylate, oxalate and nitrate; t is 3 if X is sulfate, carbonate or oxalate and t is 6 if X is halide, hydroxide, cyanate, thiocyanate, isocyanate, isothiocyanate, carboxylate or nitrate,

In a preferred embodiment of the process according to the invention, the cyanide-free metal salt of the aqueous solution of a cyanide-free metal salt is one or more compound(s) and is selected from the group consisting of zinc chloride, zinc bromide, zinc iodide, zinc acetate, zinc acetylacetonate, zinc benzoate, zinc nitrate, iron(II) sulfate, iron(II) bromide, iron(II) chloride, cobalt(II) chloride, cobalt(II) thiocyanate, nickel(II) chloride and nickel(II) nitrate, particularly preferably zinc chloride.

Metallc anidsak

Metal cyanide salts suitable for the preparation of the double metal cyanide compounds preferably have the general formula (VII)

(Y) _a M'(CN) _b (A) _c (VII) where

M' is selected from one or more metal cations of the group consisting of Fe(II), Fe(III),

Co(II), Co(III), Cr(II), Cr(III), Mn(II), Mn(III), Ir(III), Ni(II), Rh(III), Ru(II), V(IV) and V(V), preferably M' is one or more metal cations from the group consisting of Co(II), Co(III), Fe(II), Fe(III), Cr(III), Ir(III) and Ni(II),

Y is selected from one or more metal cations of the group consisting of alkali metal (ie Li ⁺ , Na ⁺ , K ⁺ , Rb ⁺ , Cs ⁺ ) and alkaline earth metal (ie Be ²⁺ , Ca ²⁺ , Mg ²⁺ , Sr ²⁺ , Ba ²⁺ ),

A is selected from one or more anions of the group consisting of halides (i.e. fluoride, chloride, bromide, iodide), hydroxide, sulfate, carbonate, cyanate, thiocyanate, isocyanate, isothiocyanate, carboxylate, oxalate or nitrate and a, b and c are integers, the values for a, b and c being chosen such that the electroneutrality of the metal cyanide salt is given; a is preferably 1, 2, 3 or 4; b is preferably 4, 5 or 6; c preferably has the value 0.

In a preferred embodiment of the process according to the invention, the metal cyanide salt of the aqueous solution of a metal cyanide salt is one or more compound(s) and is selected from the group consisting of potassium hexacyanocobaltate(III), potassium hexacyanoferrate(II), potassium hexacyanoferrate(III), calcium hexacyanocobaltate(III) and lithium hexacyanocobaltate(III), particularly preferably potassium hexacyanocobaltate(III).

Complexing component

In one embodiment of the process according to the invention, the reaction in step i) takes place in the presence of a complex-forming component.

The complexing component can be selected from the compound classes of polyethers, polyesters, polycarbonates, polyalkylene glycol sorbitan esters, polyalkylene glycol glycidyl ethers, polyacrylamide, poly-(acrylamide-co-acrylic acid), polyacrylic acid, poly(acrylic acid-co-maleic acid), polyacrylonitrile, polyalkyl acrylates, polyalkyl methacrylates, polyvinyl methyl ether, polyvinyl ethyl ether, polyvinyl acetate, polyvinyl alcohol, poly-N-vinylpyrrolidone, poly(N-vinylpyrrolidone-co-acrylic acid), polyvinyl methyl ketone, poly(4-vinylphenol), poly(acrylic acid-co-styrene), oxazoline polymers, polyalkyleneimines, maleic acid and maleic anhydride copolymers, hydroxyethyl cellulose and polyacetals, or glycidyl ethers, glycosides, carboxylic acid esters of polyhydric alcohols, esters or amides, cyclodextrins or phosphorus compounds.

In one embodiment of the process according to the invention, the complexing component is a polyether.

In a preferred embodiment, the polyether has a number-average molecular weight of > 500 g/mol, wherein the number-average molecular weight is calculated from the determined OH number.

The OH numbers are determined according to DIN 53240.

Suitable polyethers include those produced by ring-opening polymerization of cyclic ethers, which cyclic ethers may also include, for example, oxetane polymers and also Tetrahydrofuran polymers are suitable. Any catalysis is possible. The polyether has suitable end groups, such as hydroxyl, amine, ester, or ether end groups.

In a particularly preferred embodiment, the polyether has an average hydroxyl functionality of 2 to 8 and a number-average molecular weight in the range from 500 g/mol to 10,000 g/mol, preferably from 700 g/mol to 5,000 g/mol, wherein the number-average molecular weight is calculated from the determined OH number.

In a particularly preferred embodiment, the polyethers are polyether polyols, which are obtained by reacting alkylene oxides and H-functional starter compounds in the presence of acidic, basic, and/or organometallic catalysts. These organometallic catalysts include, for example, double metal cyanide (DMC) catalysts.

Suitable polyether polyols are poly(oxypropylene) polyols, poly(oxypropyleneoxyethylene) polyols, polytetramethylene ether glycols and block copolymers containing poly(oxy)ethylene, poly(oxy)propylene and/or poly(oxy)butylene blocks such as, for example, poly(oxy)ethylene-poly(oxy)propylene block copolymers with terminal poly(oxy)ethylene blocks.

In a preferred embodiment, the polyether polyol is a poly(oxypropylene) polyol having a number-average molecular weight of > 500 g/mol, wherein the number-average molecular weight is calculated from the determined OH number.

In a particularly preferred embodiment, the polyether polyol is a poly(oxypropylene) polyol, preferably a poly(oxypropylene) diol and/or a poly(oxypropylene) triol having a number-average molecular weight of 700 g/mol to 4000 g/mol, wherein the number-average molecular weight is calculated from the determined OH number.

In an alternative embodiment, the polyethers have an average hydroxyl functionality of 2 to 8 and a number-average molecular weight in the range from 150 g/mol to less than 500 g/mol, preferably from 200 g/mol to 400 g/mol, wherein the number-average molecular weight is calculated from the determined OH number.

In a preferred alternative embodiment, the alternative polyethers are polyether polyols, wherein these alternative polyether polyols have an average hydroxyl functionality of 2 to 8 and a number-average molecular weight in the range from 150 g/mol to less than 500 g/mol, preferably an average hydroxyl functionality of 2 to 8 and a number-average molecular weight in the range from 200 g/mol to 400 g/mol, wherein the number-average molecular weight is calculated from the determined OH number. These alternative polyether polyols are also obtained by reacting alkylene oxides and H-functional starter compounds in the presence of acidic, basic and/or organometallic catalysts. These organometallic catalysts are, for example, double metal cyanide (DMC) catalysts.

Suitable alternative polyether polyols are poly(oxypropylene) polyols, poly(oxypropyleneoxyethylene) polyols, polytetramethylene ether glycols and block copolymers containing poly(oxy)ethylene, poly(oxy)propylene and/or poly(oxy)butylene blocks such as Poly(oxy)ethylene-poly(oxy)propylene block copolymers with terminal poly(oxy)ethylene blocks. Tripropylene glycol, triethylene glycol, tetrapropylene glycol, tetraethylene glycol, dipropylene glycol monomethyl ether, tripropylene glycol monomethyl ether, as well as monoalkyl and dialkyl ethers of glycols and poly(alkylene glycol)s are also suitable.

In a particularly preferred alternative embodiment, the alternative polyether polyol is a polypropylene glycol and/or a polyethylene glycol having a number-average molecular weight in the range from 150 g/mol to less than 500 g/mol, wherein the number-average molecular weight is calculated from the determined OH number.

Mixing nozzle

The DMC catalyst dispersion is preferably prepared using a mixing nozzle (e.g. a smooth jet nozzle, Levos nozzle, Bosch nozzle and the like), particularly preferably a jet disperser, as described in patent application WO 01/39883 A1.

mit: Ap: Druckverlust in der Düse The basic design and mode of operation of suitable mixing nozzles are described below. Fig. 1 shows the schematic design of a simple smooth jet nozzle. The reactant stream 1 is first accelerated in nozzle 3 and atomized at high flow velocity into the slow-flowing reactant stream 2. In this process, reactant stream 2 is accelerated and reactant stream 1 is decelerated. Part of the kinetic energy of reactant stream 1 is converted into heat during this process and is therefore no longer available for the mixing process. The two reactant streams are then mixed via the turbulent breakup of the resulting jet into vortices of varying sizes (vortex cascade). Compared to a stirred tank, concentration differences can be reduced much more quickly in this way, as significantly higher and more homogeneous power densities can be achieved. The average power density P is calculated using the following formula:

with: Ap: pressure loss in the nozzle

V : Volume flow

V: Volume of the nozzle bore

The use of such nozzles will be referred to as Method 1 below.

In a smooth jet nozzle, a first reactant stream is first accelerated in a nozzle and then atomized at high flow velocity into a slow-flowing second reactant stream. The two reactant streams are then mixed via the turbulent breakup of the resulting jet into vortices of varying sizes (vortex cascade). Compared to a stirred tank, this method allows Concentration differences can be reduced much more quickly because significantly larger and more homogeneous power densities can be achieved.

jet disperser

A jet disperser as shown in Fig. 2 or Fig. 3 is particularly preferably used for the process according to the invention. The jet disperser can be constructed such that (Fig. 2) two nozzles 5 and 6 are arranged one behind the other. The reactant stream 1 is initially strongly accelerated in the nozzle 5 due to the cross-sectional constriction. The accelerated jet draws in the second component due to the high flow velocity. The distance between the nozzles is preferably selected such that only nucleation but no crystal growth occurs in the mixing chamber 4 due to the short residence time. The nucleation rate of the solid is therefore crucial for the optimal design of the jet disperser. A residence time of 0.0001 s to 0.15 s, preferably 0.001 s to 0.1 s, is advantageously set. Crystal growth only occurs in outlet 3. The diameter of nozzles 6 should preferably be selected to further accelerate the partially mixed reactant streams. Due to the additional shear forces generated in nozzles 6, the state of homogeneous mixing is achieved in a shorter time than with method 1 through faster vortex decay. In contrast to method 1, this makes it possible to achieve a state of ideal mixing of the reactants even in precipitation reactions with very high nucleation rates, allowing the establishment of defined stoichiometric compositions during the precipitation reaction. Nozzle diameters of 5000 pm to 50 pm, preferably 2000 pm to 200 pm, have proven to be favorable for pressure losses in the nozzle of 0.1 bar to 1000 bar or power densities in the range of l*10 ⁷ W/m ³ to l*10 ¹³ W/m ³ . This mixing process will be referred to as Method 2 in the following.

Depending on the desired particle size, n additional nozzles (where n = 1 - 5) can be connected downstream, resulting in a multi-stage jet disperser. Such a multi-stage jet disperser is shown in Fig. 3. Following nozzle 6, the dispersion is passed through nozzle 7 once more. The same applies to the design of the nozzle diameters as for nozzle 6.

The additional advantage of additional dispersers compared to Method 2 is that the high shear forces in the nozzles can mechanically crush already formed particles. This makes it possible to produce particles with diameters ranging from 10 pm to 0.1 pm. Instead of using several nozzles in series, comminution can also be achieved by circulating the dispersion. The use of such nozzles is referred to below as Method 3.

Due to the energy dissipation in the nozzles and the crystallization enthalpy, the dispersion may heat up. Since the temperature has a significant influence on the crystal formation process, a heat exchanger can be installed behind the mixing device for isothermal process control.

Easy scale-up is possible, for example, by using a larger number of holes, connecting multiple mixing elements in parallel, or increasing the free nozzle area. However, the latter cannot be achieved by increasing the nozzle diameter, as this creates the possibility of core flow, which would impair the mixing result. For nozzles with large free nozzle areas, slots with a corresponding area are therefore preferred.

The DMC catalyst dispersion is preferably prepared using a mixing nozzle, particularly preferably a jet disperser. Examples of suitable apparatus are shown in Figures 4 and 5. Figure 4 shows a semi-batch process using a loop reactor, and Figure 5 shows a continuous process for preparing the DMC catalyst dispersion.

In one embodiment of the process according to the invention, the preparation of the double metal cyanide catalyst (DMC) comprises i) in a first step the reaction of an aqueous solution of the cyanide-free metal salt, the aqueous solution of the metal cyanide salt, the organic complex ligand and optionally the complex-forming component, wherein the organic complex ligand contains the dialkyl carbonate according to the invention, to form a dispersion;

(ii) optionally, in a second step, separating the solid from the dispersion obtained from (i);

(iii) optionally in a third step, washing the isolated solid with an aqueous solution of an organic complex ligand by means of a filter cake wash;

(iv) and optionally in a fourth step, drying the resulting solid.

Step i)

Preferably, the aqueous solutions of the cyanide-free metal salt, e.g., zinc chloride, used in stoichiometric excess (at least 50 mol% based on the metal cyanide salt), and the metal cyanide salt, e.g., potassium hexacyanocobaltate, are first reacted in the presence of the organic complex ligand containing the dialkyl carbonate according to the invention, forming a dispersion. This DMC catalyst dispersion is preferably prepared using a mixing nozzle, particularly preferably a jet disperser.

The preparation of the DMC catalyst dispersion in a semi-batch process using a jet disperser in combination with a loop reactor (as shown in Fig. 4) is explained below. Here, either the aqueous solution of a cyanide-free metal salt from tank B2 can be circulated and the aqueous metal cyanide solution from tank B1 added, or vice versa. When both streams are combined in the mixing device M, a dispersion of the DMC compound is formed. The preparation of the dispersion of the DMC compound can be carried out according to Method 1, 2 or 3, preferably method 2 or 3. The advantage of these methods is the possibility of achieving a constant reactant ratio throughout the entire precipitation process.

After precipitation, the dispersion formed is preferably circulated through the jet disperser for a few minutes to several hours.

The nozzle diameters are preferably between 2000 pm and 200 pm with pressure losses in the nozzle between 0.1 bar and 1000 bar.

The organic complex ligand containing the dialkyl carbonate according to the invention can be present in the aqueous solution of the cyanide-free metal salt and/or the metal cyanide salt, or it is added directly to the dispersion obtained after precipitation of the double metal cyanide compound (via container B1 or B2).

In one embodiment of the process according to the invention, a complexing component is subsequently added to the dispersion circulating through the jet disperser via container B1 or B2. The complexing component is preferably used in a mixture of water and the organic complexing ligand containing the dialkyl carbonate according to the invention.

The metering of the complexing component into the circuit and subsequent recirculation preferably takes place under pressure in the nozzle between 0.001 bar and 10 bar. According to the invention, the DMC catalyst dispersion can also be prepared in a continuous process, as shown by way of example in Fig. 5. The aqueous solutions of the cyanide-free metal salt and the metal cyanide salt are reacted according to method 1, 2, or 3 in the mixing device M1, forming a dispersion. The organic complexing ligand containing the dialkyl carbonate according to the invention can be present in the aqueous solution of the cyanide-free metal salt and/or the metal cyanide salt. In this case, the mixing stage M2 is omitted in Fig. 5. It is also possible to add the organic complex ligand containing the dialkyl carbonate of the invention after precipitation of the double metal cyanide compound via the mixing device M2. To increase the residence time of the dispersion, it can be circulated via the mixing device M2. Subsequently, the complex-forming component can be added to the mixing device M3, preferably in a mixture of water and organic complex ligand containing the dialkyl carbonate of the invention, and recirculated to increase the residence time.

Process temperature

In one embodiment of the process according to the invention, a process temperature between 20°C and 90°C, preferably between 30°C and 80°C, particularly preferably between 40°C and 60°C, is used in step i). The process temperature corresponds to the process temperature in container B2 in Fig. 4. Step (ii)

In a preferred embodiment of the process according to the invention, in a second step (ii) the solid is separated from the dispersion obtained from (i).

The solid (i.e. the precursor of the catalyst according to the invention) is isolated from the dispersion by known techniques such as centrifugation or filtration.

Suitable filter devices are described, for example, in “Ullmann's Encyclopedia of Industrial Chemistry”, Vol. B 2, Chapters 9 and 10, VCH, Weinheim, 1988 and H. Gasper, D. Oechsle, E. Pongratz (eds.): “Handbook of industrial solid/liquid filtration”, Wiley-VCH Verlag GmbH, Weinheim, 2000.

The pressure drop required for filtration can be applied by gravity, by centrifugal force (e.g. filter centrifuges), preferably by gas differential pressure (e.g. vacuum filters or pressure filters) or by liquid pressure (e.g. filter presses, drum or disc filters and possibly cross-flow filtration modules).

Both discontinuous and continuous filter devices can be used to separate the catalysts. Examples of discontinuous filter devices include peeler and inverting filter centrifuges, membrane, chamber, frame, or tubular filter presses, automatic press filter machines, auto-press devices, disc pressure, candle, and plate filters, as well as vacuum and pressure Nutsche filters. Examples of continuously operating filter devices include screen belt presses, pressure and vacuum drum filters, pressure and vacuum disc filters, belt filters, and cross-flow filters.

Vacuum or pressure filters or nutsches are particularly suitable for filtering the DMC catalyst dispersion on a laboratory scale, and pressure nutsches, filter presses and automatic press filters on a pilot plant and industrial scale.

Membrane filter presses have proven particularly suitable for pilot and pilot plant scale applications. These presses, with the aid of a suitable filter cloth, preferably a membrane cloth, enable the filtration of the DMC catalyst dispersion due to an applied fluid pressure gradient.

Filtration is generally carried out at temperatures of 10 to 80°C. The applied pressure differences can be 0.001 bar to 200 bar, preferably 0.1 bar to 100 bar, particularly preferably 0.1 bar to 25 bar, whereby the applied pressure difference depends on the device used.

Step (Ui)

The isolated solid obtained in step (ii) can be washed by redispersion or filter cake washing. In a preferred embodiment of the process according to the invention, in a third step (iii), the isolated solid is washed with an aqueous solution of an organic complex ligand by means of a filter cake wash.

Here, the filter cake is washed preferably by mashing or, preferably, by flow-through washing. The washing liquid flows through the cake, displacing the liquid previously contained in the cake, whereby diffusion effects also come into play. Dehumidification of the washed cake can be achieved by gas differential pressure, centrifugal force, or mechanical pressing, or preferably by a combination of gas differential pressure dehumidification followed by mechanical pressing. The pressure for mechanical pressing can be applied either mechanically or by membranes.

Filter cake washing simplifies and accelerates the production process. The preferred ratio of washing liquid to filter cake volume is the amount that completely replaces the amount of liquid present in the original filter cake.

In an alternatively preferred embodiment of the process according to the invention, the isolated solid is subsequently washed in a third process step with an aqueous solution of the organic complex ligand (e.g., by redispersion and subsequent re-isolation by filtration or centrifugation). In this way, for example, water-soluble by-products, such as potassium chloride, can be removed from the catalyst according to the invention. The amount of the organic complex ligand in the aqueous wash solution is preferably between 40 and 80 wt. %, based on the total solution.

Optionally, in the third step, complex-forming component is added to the aqueous washing solution, preferably in the range between 0.5 and 5 wt.%, based on the total solution.

Furthermore, it is advantageous to wash the isolated solid more than once. Preferably, in a first washing step (iii-1), the solid is washed with an aqueous solution of the organic complex ligand (e.g., by redispersion and subsequent reisolation by filtration or centrifugation) in order to remove, for example, water-soluble by-products such as potassium chloride from the catalyst according to the invention. Particularly preferably, the amount of organic complex ligand in the aqueous washing solution is between 40 and 80 wt. %, based on the total solution of the first washing step. In the further washing steps (iii-2), either the first washing step is repeated once or several times, preferably one to three times, or preferably a non-aqueous solution, such as a mixture or solution of organic complex ligand and complex-forming component, preferably in the range between 0.5 and 5 wt. %, based on the total amount of the washing solution of step (iii-2)), is used as the washing solution, and the solid is washed therewith once or several times, preferably one to three times.

Step (iv) In a preferred embodiment of the process according to the invention, the solid obtained is subsequently dried in a fourth step (iv).

The isolated and optionally washed solid is then dried, optionally after pulverization, at temperatures of generally 20 - 100°C and at pressures of generally 0.1 mbar to atmospheric pressure (1013 mbar).

Steps (ii) and (Ui)

In a preferred embodiment of the process according to the invention, steps (ii) and (iii) are carried out in a filter press.

It has proven advantageous to press the washed filter cake after filter cake washing at pressures of 0.5 to 200 bar, preferably at the highest possible pressure. This can be done, for example, directly after filter cake washing in a filter press or by means of other suitable pressing devices that enable the application of mechanical pressure so that the liquid present in the filter cake can escape through a membrane or a suitable filter cloth. The mechanical dehumidification of the filter cake following filter cake washing, preferably carried out before drying, can preferably take place in the filter press, preferably by mechanical pressing by pressure applied to the membranes. Mechanical dehumidification preferably leads to the greatest possible removal of the washing liquid from the filter cake.

Steps (ii), (iii) and (iv)

The DMC catalyst is then dried at temperatures ranging from approximately 20 to 100°C and at pressures ranging from approximately 0.1 mbar to atmospheric pressure (1013 mbar). Contact dryers, convection dryers, and spray dryers are suitable for this purpose. Drying is preferably carried out directly in devices for mechanical liquid separation, if suitable (e.g., Nutsche dryers, centrifugal dryers, "hot filter presses").

In a particularly preferred embodiment of the process according to the invention, steps (ii), (iii) and (iv) are carried out in a heatable filter press.

The preferred method for this process is a heatable filter press. It is constructed like a conventional filter press with a membrane package. The membrane plates used differ from conventional membrane plates in that a heating medium can flow through the space behind the membrane. Liquid-tight (so-called "drip-tight" or "gas-tight") membrane filter plates are preferred.

The heated heating medium flows on the back of the press membranes, completely separated from the filter cake by the press membrane and the filter medium, past the filter cake and heats it in the process. The press medium is under sufficiently high pressure to ensure contact between the To ensure the membranes are bonded to the filter cakes. The filter cakes can be heated on one or both sides. Heating on both sides is advantageous in terms of drying time.

To support the drying process, a vacuum is applied on the filtrate side. This vacuum can be generated, for example, by a liquid ring pump. The extracted vapor stream is cooled upstream of the vacuum pump to condense the volatile components (e.g., tert-butanol and water). The measured and controlled variables are the condensed amount, the pressure in the press's filtrate system, and the filter cake temperature.

In the described process, the membrane pressures are preferably between 0.1 bar and 10 bar. Temperatures of the pressing and heating medium are between 30°C and 80°C, preferably between 40°C and 60°C. The filtrate-side pressure is preferably less than 100 mbar. The flow rate of the heating medium should be selected high enough to ensure good heat transfer between the heating medium and the product. Drying times are generally between a few minutes and several hours, usually one to ten hours. Residual moisture levels below the target value of approximately 5% are reliably achieved with this type of drying.

In further process steps, the product thus isolated and freed from secondary components can be ground and packaged.

Product-by-process claim

Another object of the present invention is the DMC catalyst produced by the process according to the invention.

A further object of the present invention is the use of the DMC catalysts prepared by the process according to the invention in a process for preparing polyoxyalkylene polyols, preferably polyether polyols by polyaddition of alkylene oxides to starter compounds containing active hydrogen atoms and/or polyether carbonate polyols by polyaddition of alkylene oxides to starter compounds containing active hydrogen atoms in the presence of carbon dioxide.

Due to their extraordinarily high activity, the DMC catalysts prepared by the process according to the invention can often be used in very low concentrations (25 ppm and less, based on the amount of polyoxyalkylene polyol, preferably polyether polyol, to be added). If the polyoxyalkylene polyols, preferably polyether polyols, prepared in the presence of the DMC catalysts prepared by the process according to the invention are used to produce polyurethanes, removal of the catalyst from the polyoxyalkylene polyol, preferably polyether polyol, can be dispensed with without adversely affecting the product qualities of the resulting polyurethane. The OH numbers were determined according to DIN 53240. The viscosities were determined using a rotational viscometer (Physica MCR 51, manufacturer: Anton Paar) according to DIN 53018.

The catalyst was prepared using an apparatus according to Fig. 4 from WO 01/39883 A1.

In a loop reactor containing a jet disperser according to Fig. 2 of WO 01/39883 A1 with a bore (diameter 0.7 mm), a solution of 258 g of zinc chloride in 937 g of distilled water and 135 g of tert-butanol was circulated at 50°C (determined in container D2 in Fig. 4 of WO 01/39883 A1). A solution of 26 g of potassium hexacyanocobaltate in 332 g of distilled water was added. The pressure drop in the jet disperser was 2.9 bar. The resulting dispersion was then circulated for 60 min at 50°C with a pressure drop in the jet disperser of 2.9 bar. A mixture of 5.7 g of tert-butanol, 159 g of distilled water and 27.6 g of polypropylene glycol 1000 (PPG-1000) was then added and the dispersion was then circulated for 80 min at 50°C and a pressure drop in the jet disperser of 2.9 bar.

230 g of the resulting dispersion were filtered in a pressure filter with a 20 ^cm² filter area and then washed with a mixture of 82 g of tert-butanol, 42.3 g of distilled water, and 1.7 g of polypropylene glycol 1000. The washed filter cake was mechanically pressed between two strips of filter paper and finally dried for 2 h at 60°C under high vacuum at approximately 0.05 bar (absolute).

Example 2:

The catalyst was prepared using an apparatus according to Fig. 4 from WO 01/39883 A1.

In a loop reactor containing a jet disperser according to Fig. 2 of WO 01/39883 A1 with a bore (diameter 0.7 mm), a solution of 258 g of zinc chloride in 937 g of distilled water, 128.2 g of tert-butanol, and 6.8 g of dimethyl carbonate was circulated at 50°C (determined in container D2 in Fig. 4 of WO 01/39883 A1). A solution of 26 g of potassium hexacyanocobaltate in 332 g of distilled water was added. The pressure drop in the jet disperser was 2.9 bar. The resulting dispersion was then circulated for 60 min at 50°C with a pressure drop in the jet disperser of 2.9 bar. A mixture of 5.4 g of tert-butanol, 0.3 g of dimethyl carbonate, 159 g of distilled water and 27.6 g of polypropylene glycol 1000 (PPG-1000) was then added and the dispersion was then circulated for 80 min at 50°C and a pressure drop in the jet disperser of 2.9 bar. 230 g of the resulting dispersion were filtered through a pressure filter with a 20 ^cm² filter area and then washed with a mixture of 82 g of tert-butanol, 42.3 g of distilled water, and 1.7 g of polypropylene glycol 1000. The washed filter cake was mechanically pressed between two strips of filter paper and finally dried for 2 h at 60°C under high vacuum at approximately 0.05 bar (absolute).

The catalyst was prepared using an apparatus according to Fig. 4 from WO 01/39883 A1.

In a loop reactor containing a jet disperser according to Fig. 2 of WO 01/39883 A1 with a bore (diameter 0.7 mm), a solution of 258 g of zinc chloride in 937 g of distilled water, 121.5 g of tert-butanol, and 13.5 g of dimethyl carbonate was circulated at 50°C (determined in container D2 in Fig. 4 of WO 01/39883 A1). A solution of 26 g of potassium hexacyanocobaltate in 332 g of distilled water was metered in. The pressure drop in the jet disperser was 2.9 bar. The resulting dispersion was then circulated for 60 min at 50°C with a pressure drop in the jet disperser of 2.9 bar. A mixture of 5.1 g of tert-butanol, 0.6 g of dimethyl carbonate, 159 g of distilled water and 27.6 g of polypropylene glycol 1000 (PPG-1000) was then added and the dispersion was then circulated for 80 min at 50°C and a pressure drop in the jet disperser of 2.9 bar.

230 g of the resulting dispersion were filtered in a pressure filter with a 20 ^cm² filter area and then washed with a mixture of 82 g of tert-butanol, 42.3 g of distilled water, and 1.7 g of polypropylene glycol 1000. The washed filter cake was mechanically pressed between two strips of filter paper and finally dried for 2 h at 60°C under high vacuum at approximately 0.05 bar (absolute).

Example 4:

The catalyst was prepared using an apparatus according to Fig. 4 from WO 01/39883 A1.

In a loop reactor containing a jet disperser according to Fig. 2 of WO 01/39883 A1 with a bore (diameter 0.7 mm), a solution of 258 g of zinc chloride in 937 g of distilled water, 108 g of tert-butanol, and 27 g of dimethyl carbonate was circulated at 50°C (determined in container D2 in Fig. 4 of WO 01/39883 A1). A solution of 26 g of potassium hexacyanocobaltate in 332 g of distilled water was metered in. The pressure drop in the jet disperser was 2.9 bar. The resulting dispersion was then circulated for 60 min at 50°C with a pressure drop in the jet disperser of 2.9 bar. A mixture of 4.6 g of tert-butanol, 1.1 g of dimethyl carbonate, 159 g of distilled water and 27.6 g of polypropylene glycol 1000 (PPG-1000) was then added and the dispersion was then circulated for 80 min at 50°C and a pressure drop in the jet disperser of 2.9 bar. 230 g of the resulting dispersion were filtered through a pressure filter with a 20 ^cm² filter area and then washed with a mixture of 82 g of tert-butanol, 42.3 g of distilled water, and 1.7 g of polypropylene glycol 1000. The washed filter cake was mechanically pressed between two strips of filter paper and finally dried for 2 h at 60°C under high vacuum at approximately 0.05 bar (absolute).

Example 5

The catalyst was prepared using an apparatus according to Fig. 4 from WO 01/39883 A1.

In a loop reactor containing a jet disperser according to Fig. 2 of WO 01/39883 A1 with a bore (diameter 0.7 mm), a solution of 258 g of zinc chloride in 937 g of distilled water, 94.5 g of tert-butanol, and 40.5 g of dimethyl carbonate was circulated at 50°C (determined in container D2 in Fig. 4 of WO 01/39883 A1). A solution of 26 g of potassium hexacyanocobaltate in 332 g of distilled water was metered in. The pressure drop in the jet disperser was 2.9 bar. The resulting dispersion was then circulated for 60 min at 50°C with a pressure drop in the jet disperser of 2.9 bar. A mixture of 4.0 g tert-butanol, 1.7 g dimethyl carbonate, 159 g distilled water and 27.6 g polypropylene glycol 1000 (PPG-1000) was then added and the dispersion was then circulated for 80 min at 50°C and a pressure drop in the jet disperser of 2.9 bar.

230 g of the resulting dispersion were filtered in a pressure filter with a 20 ^cm² filter area and then washed with a mixture of 82 g of tert-butanol, 42.3 g of distilled water, and 1.7 g of polypropylene glycol 1000. The washed filter cake was mechanically pressed between two strips of filter paper and finally dried for 2 h at 60°C under high vacuum at approximately 0.05 bar (absolute).

Example 6 (Comparison)

The catalyst was prepared using an apparatus according to Fig. 4 from WO 01/39883 A1.

In a loop reactor containing a jet disperser according to Fig. 2 of WO 01/39883 A1 with a bore (diameter 0.7 mm), a solution of 258 g of zinc chloride in 937 g of distilled water, 114.3 g of tert-butanol, and 20.7 g of cyclic ethylene carbonate was circulated at 50°C (determined in container D2 in Fig. 4 of WO 01/39883 A1). A solution of 26 g of potassium hexacyanocobaltate in 332 g of distilled water was added. The pressure drop in the jet disperser was 2.9 bar. The resulting dispersion was then circulated for 60 min at 50°C with a pressure drop in the jet disperser of 2.9 bar. A mixture of 4.8 g of tert-butanol, 0.9 g of cyclic ethylene carbonate, 159 g of distilled water and 27.6 g of polypropylene glycol 1000 (PPG-1000) was then added and the dispersion was then circulated for 80 min at 50°C and a pressure drop in the jet disperser of 2.9 bar. 230 g of the resulting dispersion were filtered through a pressure filter with a 20 ^cm² filter area and then washed with a mixture of 82 g of tert-butanol, 42.3 g of distilled water, and 1.7 g of polypropylene glycol 1000. The washed filter cake was mechanically pressed between two strips of filter paper and finally dried for 2 h at 60°C under high vacuum at approximately 0.05 bar (absolute).

Catalyst testing (“8K Diol Stressed Test”):

The DMC catalysts were tested in the so-called "8K Diol Stressed Test." Starting from a bifunctional polypropylene glycol starter with an OH number of 147 mg KOH/g ("Arcol Polyol 725" from Covestro), a polypropylene glycol with a calculated OH number of 14 mg KOH/g, i.e., a molecular weight of 8,000 g/mol ("8K Diol"), was produced with a short propylene oxide dosing time (30 minutes). The decisive assessment criterion for catalyst quality/activity in this test is the viscosity of the resulting polyol; a DMC catalyst of higher quality/activity leads to a lower 8K Diol viscosity.

General implementation:

A 1-liter stainless steel reactor was charged with 75 g of a bifunctional polypropylene glycol starter (OH number = 147 mg KOH/g) and 30.7 mg of DMC catalyst. After five nitrogen/vacuum exchanges between 0.1 and 3.0 bar (absolute), the reactor contents were heated to 130°C with stirring (800 rpm). The mixture was then stripped with nitrogen for 30 minutes at 130°C and 100 mbar (absolute). Subsequently, 7.5 g of propylene oxide were added at 130°C and 100 mbar (absolute) to activate the catalyst. Catalyst activation was evident in an accelerated pressure drop in the reactor. After catalyst activation, the remaining propylene oxide (685.7 g) was added over 30 minutes at 130°C with stirring (800 rpm). After a post-reaction time of 30 minutes at 130°C, volatile components were distilled off under vacuum (< 10 mbar) at 90°C for 30 minutes. The product was then cooled to room temperature and removed from the reactor.

The OH number and viscosity (25°C) of the resulting product were measured. In the event of a deviation between the measured and calculated OH number (14 mg KOH/g), a "corrected viscosity" was determined from the measured viscosity using the following formula: Corrected viscosity (25°C) = Measured viscosity (25°C) + 659 * (OH number - 14)

The results of the catalyst tests in the “8K Diol Stressed Test” are summarized in Table 1.

Table 1:

The results show that double metal cyanide catalysts prepared using dimethyl carbonate as the organic complexing ligand in the "8K Diol Stressed Test," a semi-batch polyol production process, lead to lower viscosity values of the polyols compared to a double metal cyanide catalyst without the use of dimethyl carbonate as the organic complexing ligand. Furthermore, the use of a mixture of cyclic ethylene carbonate and t-BuOH as organic complexing ligands in the preparation of the DMC catalyst in the "8K Diol Stressed Test," according to the teaching of US 2019/0185399 A1, leads to a higher viscosity than inventive DMC catalysts based on dimethyl carbonate and t-BuOH as the complexing ligand with a comparable mass fraction of alkyl carbonate.

Claims

1. A process for the preparation of a double metal cyanide catalyst (DMC) comprising i) reacting an aqueous solution of a cyanide-free metal salt, an aqueous solution of a metal cyanide salt, an organic complex ligand and optionally a complex-forming component, characterized in that the organic complex ligand contains a dialkyl carbonate, wherein the organic complex ligand contains, in addition to the dialkyl carbonate, preferably dimethyl carbonate, a further compound (1), wherein the compound (1) is one or more compound(s) and is selected from the group consisting of dimethoxyethane, tert-butanol, 2-methyl-3-buten-2-ol, 2-methyl-3-butyn-2-ol, ethylene glycol mono-tert-butyl ether and 3-methyl-3-oxetane methanol and wherein the mass fraction of the dialkyl carbonate is from 1% to 25%, based on the sum of the masses of the compound (1) and the dialkyl carbonate. 2. The process according to claim 1, wherein the dialkyl carbonate has a structure according to formula (I): R'-OC(=O)-OR ² (I) , where R ¹ and R ² are independently methyl, ethyl, iso-propyl, n-propyl, iso-butyl, n-butyl, tert-butyl, iso-pentyl, n-pentyl, tert-pentyl, preferably methyl, ethyl and n-propyl, particularly preferably methyl. 3. The process according to claim 1 or 2, wherein the dialkyl carbonate is one or more compounds and is selected from the group consisting of dimethyl carbonate, diethyl carbonate, di-n-propyl carbonate, di-n-butyl carbonate, preferably dimethyl carbonate, diethyl carbonate, di-n-propyl carbonate, particularly preferably dimethyl carbonate. 4. A process according to any one of claims 1 to 3, wherein the dialkyl carbonate is dimethyl carbonate. 5. A process according to any one of claims 1 to 4, wherein the compound (1) is tert-butanol. 6. Process according to one of claims 1 to 5, wherein the mass fraction of the dialkyl carbonate, preferably of the dimethyl carbonate, is from 2% to 25%, preferably from 7% to 25%, based on the sum of the masses of the compound (1) and the dialkyl carbonate, preferably the dimethyl carbonate, is. 7. Process according to one of claims 1 to 6, wherein double metal cyanide compounds of formula (II) are contained in the DMC catalyst M _x [M' _x ,(CN) _y ] _z (II), and M is selected from one or more metal cations of the group consisting of Zn(II), Fe(II), Ni(II), Mn(II), Co(II), Sr(II), Sn(II), Pb(II) and Cu(II), preferably Zn(II), Fe(II), Co(II) and Ni(II), and M' is selected from one or more metal cations of the group consisting of Fe(II), Fe(III), Co(II), Co(III), Cr(II), Cr(III), Mn(II), Mn(III), Ir(III), Ni(II), Rh(III), Ru(II), V(IV) and V(V), preferably Co(III), Fe(III), Cr(III) and Ir(III), and x, x', y and z are integers and are chosen such that the electron neutrality of the double metal cyanide compound is given, wherein preferably x = 3, x' = 1, y = 6 and z = 2. 8. The method according to any one of claims 1 to 7, wherein the double metal cyanide compound is one or more compound(s) and is selected from the group consisting of zinc hexacyano->cobaltate(III), zinc hexacyanoiridate(III), zinc hexacyanoferrate(III) and cobalt(II) hexacyanocobaltate(III), preferably zinc hexacyanocobaltate(III). 9. The method according to any one of claims 1 to 8, wherein the metal cyanide salt is one or more compound(s) selected from the group consisting of potassium hexacyanocobaltate(III), potassium hexacyanoferrate(II), potassium hexacyanoferrate(III), calcium hexacyanocobaltate(III) and lithium hexacyanocobaltate(III), preferably potassium hexacyanocobaltate(III). 10. The process according to any one of claims 1 to 9, wherein the reaction in step i) is carried out in the presence of a complexing component. 11. The process according to claim 10, wherein the complexing component is a polyether, preferably a polyether polyol. 12. The process according to any one of claims 1 to 11, wherein the reaction in step i) is carried out using a mixing nozzle, preferably a jet disperser. 13. Double metal cyanide catalyst (DMC) obtainable according to one of claims 1 to 12. 14. Use of a double metal cyanide catalyst (DMC) according to claim 13 for Production of polyoxyalkylene polyols, preferably polyether polyols and/or polyether carbonate polyols.