WO2012116870A1 - Facility for reacting alkylene oxides - Google Patents

Abstract

The present invention relates to a facility for reacting alkylene oxides, comprising at least one reactor vessel, at least one starting material feed line, at least one circulation line having a pump and an injector mixing nozzle, wherein the gas feed of the injector mixing nozzle is connected to the gas chamber of the reactor vessel via a gas line which is connected to at least one starting material feed line. A further aspect of the present invention is a method for producing alkylene oxide derivatives.

Description

 Plant for the conversion of alkylene oxides

The present invention relates to a system for

Reaction of alkylene oxides. In addition, the present invention describes methods for the production of

Alkylene oxide derivatives.

Derivatives of alkylene oxides, in particular of ethylene oxide or propylene oxide, are widely known in the art, these compounds being used, for example, as nonionic surfactants or as monomers having dispersing properties. Among the nonionic surfactants include fatty alcohols which have been reacted with ethylene or propylene oxide. Monomers with dispersing

Properties are in particular (meth) acrylates with

Glycol units.

Accordingly, many methods are known to those previously

to obtain the stated alkylene oxide derivatives. These are inter alia in the publications JP 2008143814 and

JP 2008127302.

The known processes and equipment for carrying them out lead to acceptable yields and qualities of the desired products. Due to the economic importance of the alkylene oxide derivatives to be produced, the long-term need is the economy of

Process continues to improve. In doing so, other peculiarities of the processes for the preparation of these products should not be adversely affected. Accordingly, among other things, the purity and the yield of the alkylene oxide derivatives by a process improvement in

not be affected economically. Furthermore, a plant for carrying out the said processes should be provided, by means of which the process can be carried out in a particularly simple, safe and cost-effective manner.

Furthermore, reactors for the reaction of gases with liquid educts from the document EP 0070797 are known, wherein the reaction mixture is circulated and the gas via an In ektor mixing nozzle in the

Reaction mixture is introduced. The In ektor mixing nozzle is designed so that the gas is sucked in the reactor vessel above the reaction mixture and with the same in

Contact is brought. A gas line between the reactor chamber and injector mixing nozzle is not indicated, and this complex construction is not necessary for the stated reaction. The reaction of alkylene oxides with this plant is not described. Furthermore, a

Introduction of a liquid starting material in the gas supply of the injector mixing nozzle not set forth.

In view of the prior art, it was therefore an object of the present invention to provide a process for the preparation of alkylene oxide derivatives, which is particularly economical.

Moreover, it was an object of the present invention to provide processes for the preparation of alkylene oxide derivatives, which can be carried out easily and safely. In this case, the product should preferably be obtained in high yields and, overall, with low energy consumption. Another object of the invention was a

To provide a method in which an alkylene oxide derivative can be selectively obtained. Furthermore, that should

Process a constant product quality

provide .

Furthermore, a plant for the reaction of alkylene oxides should be provided with the previously

set out procedures simple and inexpensive

can be performed. Here, the system should have a simple structure. Furthermore, a long continuous operation of the system should be made possible without the operation of the system must be interrupted. Furthermore, the system should be able to be easily cleaned.

These are solved as well as other tasks which are not explicitly mentioned, but which are readily derivable or deducible from the contexts discussed hereinbelow, by a plant for the reaction of alkylene oxides with all features of patent claim 1

Variations of the systems according to the invention are provided in the dependent claims appended to claim 1. Regarding a method for

Preparation of alkylene oxide derivatives, claim 6 provides a solution to the underlying problems.

The present invention accordingly relates to a plant for the reaction of alkylene oxides, comprising at least one reactor vessel, at least one

EduktZuleitung, at least one circulation line with a pump and a In ektor mixing nozzle, which thereby

is characterized in that the gas supply of the injector mixing nozzle with the gas space of the reactor vessel via a Gas line is connected to at least one

EduktZuleitung is connected.

This makes it possible to provide an installation and a process for the preparation of alkylene oxide derivatives in an unpredictable manner, with which the said products can be obtained particularly economically.

An inventive method for the preparation of

Alkylene oxide derivatives can be easily and safely carried out. Here, the products in high yields and, in total, with low energy consumption

receive. Thus, the proportion of by-products can be reduced, the use of alkylene oxide reduced and the reaction time can be reduced. In this context, it should be noted that the process according to the invention leads to particularly small amounts of undesirable and critical by-products, for example to di (meth) acrylates.

In addition, the alkylene oxide derivatives can be very

can be selectively obtained, the method a

provides comparatively constant product quality.

Furthermore, a plant for the reaction of alkylene oxides is provided with which the methods set out above can be carried out simply and inexpensively.

Here, the system has a comparatively simple structure. Furthermore, a long continuous operation of the system is possible without the operation of the system

must be interrupted. Furthermore, the system can be cleaned easily. The plant for the reaction of alkylene oxides comprises

at least one reactor vessel, at least one EduktZuleitung and at least one recirculation line with a pump. These components of the system according to the invention are known from the prior art, in which connection, inter alia, in the introductory part of the

referenced documents. Furthermore, particularly suitable reactors and pumps are among others in Dubbel - Paperback for the

Mechanical engineering. 22nd edition. Springer, Berlin 2007. ISBN 978-34040-49714-1 and VDI-Wärmeatlas VDI-Wärmeatlas VDI

Society (ed.) 10th, edit. u. ext. Ed., 2006, ISBN: 978-3-540-25504-8. Advantageously, the reactor vessel as a pressure reactor

be carried out, with preferred reactor vessels

are designed to be tempered and, for example

Half pipe coils may have for cooling. Preferred pumps for circulating the reaction mixture include centrifugal pumps, which preferably include an open barrel, and side channel machines.

The plants according to the invention have a recirculation line, the reaction mixture being conducted in the same. Accordingly, the system of the present invention may be described as

Loop reactor, also called loop reactor or loop reactor can be viewed. In the recirculation line, at least one heat exchanger may preferably be provided. Suitable heat exchangers are, inter alia, in Dubbel - Taschenbuch für die Maschinenbau. 22nd edition. Springer,

Berlin 2007. ISBN 978-3-540-49714-1 and VDI-Wärmeatlas VDI-Wärmeatlas VDI Gesellschaft (Hrsg.) 10., edit. u. ext. Ed., 2006, ISBN: 978-3-540-25504-8. Among other things, surprising benefits can be achieved

be obtained that the heat exchanger as

Shell and tube heat exchanger is executed.

In addition to the injector mixing nozzle, the reactor may preferably have a stirrer which may be provided, for example, in the reactor vessel.

Essential to the invention is the use of an injector mixing nozzle. The type and geometry more preferred

Injector mixing nozzles are designed so that a relatively high suction ratio can be achieved. The

Suction ratio (SVH) is defined as SVH = VI [m ³ / h] / V ² [m ³ / h];

 Vl = volume flow of suction gas from the reactor;

V2 = volume flow of propellant

For a given volume flow of the driving medium, which is generated for example by the pump in the liquid circuit, show injector mixing nozzles with high

Suction a strong volume flow of the gas, which is withdrawn from the gas space of the reactor.

Surprising advantages in particular injector mixing nozzles, with which preferably a suction ratio in

Range of 0.5 to 20, in particular 1 to 10 and particularly preferably in the range of 2 to 7 can be achieved.

The injector mixing nozzle has a gas supply and a supply for a liquid flow. Furthermore, the gas supply of the injector-mixing nozzle is connected to the gas space of the reactor vessel via a gas line which is connected to at least one EduktZuleitung, so that by the liquid stream, a gas via the gas supply of the In ektor mixing nozzle from the reactor vessel is sucked. Of particular advantage may be a throttle valve, which is provided in the gas line, which connects the gas space of the reactor with the In ector mixing nozzle. In this way, in particular, the gas flow in the gas line can be adjusted independently of the circuit of the liquid flow to the injector mixing nozzle. Further, in the gas line to the injector mixing nozzle

at least one EduktZuleitung provided. Of the

Feed point of EduktZuleitung in the gas line to the injector mixing nozzle is preferably designed so that a liquid in the gas line to the injector mixing nozzle can be introduced. Accordingly, a pressure-maintaining valve can be provided in the educt feed line via which an educt can be introduced into the gas line to the injector mixing nozzle. Furthermore, the liquid educt which can be introduced into the reactor can be metered via a pump from a storage container into the gas line to the injector mixing nozzle.

The feed point of the educt feed line into the gas line to the injector mixing nozzle can advantageously be selected such that the reactant liquid introduced into the gas feed line travels a distance of at least 50 mm, more preferably at least 100 mm in the gas flow of the gas feed line before contact with the circulation flow. Preferably, this is

Distance at most 2000 mm, more preferably at most 1000 mm.

Of particular interest is, inter alia, a plant which is designed as a feedbatch plant. A feedbatch system allows the supply of a portion of the educts during the Implementation of the reaction, wherein during the reaction, only an insignificant part of the products obtained is derived from the reactor. In particular, samples of the reaction mixture which serve to analyze the progress of the reaction can be regarded as an insignificant part.

 Preferably, the plant can be designed so that at least one of the reactants is substantially completely charged, whereas another reactant to

preferably at least 60% by weight, preferably at least 80% by weight and particularly preferably at least 95% by weight, can be introduced via the educt feed line provided in the gas feed of the injector mixing nozzle. For example, preferably at least 90% by weight, especially

preferably at least 95% by weight of an alcohol or an acid, for example (meth) acrylic acid, are introduced into the reactor vessel, whereas preferably at least 60% by weight, preferably at least 80% by weight and more preferably at least 95% by weight of the insertable

Alkylene oxides via the provided in the gas line to the gas supply of In ektor mixing nozzle feedstock

can be initiated.

The geometries of the cables, in particular the

EduktZuleitung, the gas line and the circuit current are preferably chosen so that the

 Flow rate in the educt feed, the

Gas line and / or the circulating current in the range of 0.2 m / s to 20 m / s. An inventive system is used in particular for

Preparation of alkylene oxide derivatives. Derivatives of

Alkylene oxide are in particular compounds by

Reaction of alkylene oxides can be obtained. To the Preferred derivatives of alkylene oxide include, in particular, esters and ethers which have one or more alkylene glycol units.

Alkylene oxides are known in the art, these compounds can be obtained in particular by epoxidation of alkenes. Among the preferred alkylene oxides include ethylene oxide, propylene oxide and / or butylene oxide. These compounds may be used singly or as mixtures of two or more. to

Preparation of particularly preferred derivatives of

Alkylene oxides, the composition of the alkylene oxides used can be varied, for example

To obtain block copolymers. In particular, preferred block copolymers can be obtained by polymerization of ethylene oxide and propylene oxide.

Of particular interest are, in particular, processes in which at least one alkylene oxide is fed in liquid phase into the reactant feed line of the reaction mixture, which is provided in the gas feed line of the injector mixing nozzle.

The addition time of the alkylene oxide is preferably in the

Range of 10 minutes to 48 hours, more preferably in the range of 30 minutes to 24 hours.

Furthermore, methods are preferred in which the

Dosing ratio in the range of 5 to 500, in particular in the range of 20 to 200 and particularly preferably in the range of 40 to 80. The dosing ratio (DV) describes the weight ratio of the stream of alkylene oxide addition (dosing) to Kreislaufström (circulation), so that DV = Ml [kg / h] / M2 [kg / h] with Ml = circulating rates; M2 = dosing quantity.

Preferably, the filling and the amount of

added educt be chosen so that the level of the reactor vessel to the end of the reaction below the

Outlet of In ektor mixing nozzle is located.

Also of particular interest are systems which are designed such that the reactor residence time (RWZ) in the

Range of preferably 1 to 60 minutes, especially 2 to 20 minutes and more preferably 5 to 15 minutes. Processes with these reactor residence times are particularly preferred.

The reactor residence time (RWZ) is defined as:

RWZ [h] = V _R [m ³ ] / V _u [m ³ / h]; V _R = reactor volume; V _u

 Umwälzvolumenstrom

According to a particular aspect of the present invention, in particular derivatives of (meth) acrylic acid can be formed. The term comprises (meth) acrylic acid

Methacrylic acid, acrylic acid and mixtures thereof.

Advantageously, the process according to the invention can be used in particular for the preparation of glycol esters of (meth) acrylic acid. These include, for example

Hydroxyalkyl (meth) acrylates such as 2-hydroxyethyl methacrylate, 2-hydroxyethyl acrylate, 2-hydroxypropyl methacrylate, 2-hydroxypropyl acrylate, 3-hydroxypropyl methacrylate, 3-hydroxypropyl acrylate, hydroxybutyl methacrylate and

Hydroxybutyl acrylate. Particularly preferred are in particular methods for

Preparation of polyalkylene glycol mono (meth) acrylates. The term polyalkylene glycol mono (meth) acrylate is used in the context of the present invention in particular

Monoesters of (meth) acrylic acid derived from an ether, especially a polyether.

To the ether compounds, of which the

(Meth) acrylic ester is derived, in particular poly-C ₂ -C 4 -alkylene glycol compounds, which are variously referred to as poly-C ₂ -C 4 -alkylene oxides or poly (oxy-C ₂ -C 4 -alkylene) compounds. These ethers usually have at least 2, often at least 4 and especially at least 5 and usually not more than 500, often not more than 400, z. B. 2 to 100 and especially 3 to 50 repeat units derived from C ₂ -C 4 alkylene glycols. These compounds can be linear or branched. Preferred polyalkylene glycol mono (meth) acrylates can be described by the general formula (I)

wherein R is hydrogen or a methyl group, n indicates the number of repeating units and usually for a number in the range of 2 to 100, in particular in the range of 3 to 50, particularly preferably in the range of 4 to 15 and very particularly preferably in the range of 5 to 10, A is C ₂ -C 4 -alkylene, such as 1, 2-ethanediyl, 1, 3-propanediyl, 1, 2-propanediyl, 1, 2-butanediyl or 1, 4-butanediyl and R ^{1 is} hydrogen.

Of particular interest are in particular

Polyalkylene glycol mono (meth) acrylates, which preferably have a number average molecular weight in the range of 200 to 6000 g / mol, more preferably in the range of 500 to 5000 g / mol, determined by their hydroxyl number. According to a particular aspect of the present invention, it is preferable to prepare a polyethylene mono (meth) acrylate having an average of about 3 to 10, especially

preferably comprises about 4 to 6 units of

Ethylene oxide are derived. The radical R ¹ in these compounds particularly preferably represents hydrogen, A

exclusively 1, 2-ethanediyl and n is an integer in the

Range from 3 to 10, more preferably 4 to 6.

According to another embodiment of the present invention

Invention may be preferred

Polypropylene glycol mono (meth) acrylate, which comprises on average about 3 to 10, more preferably about 4 to 6 units derived from propylene oxide. Particularly preferably, the radical R ¹ in these compounds is hydrogen, A is 1, 2-propanediyl and n is an integer in the range from 3 to 10, particularly preferably 4 to 6.

Accordingly, (meth) acrylic acid and / or hydroxyalkyl (meth) acrylates can be used in particular as starting materials.

This can in particular

Polyalkylenglykolmono (meth) acrylates by the reaction of (meth) acrylic acid and / or hydroxyalkyl (meth) acrylates with at least one alkylene oxide are obtained. to

Preparation of hydroxyalkyl (meth) acrylates with a

Alkylene glycol group in the molecule is generally

 (Meth) acrylic acid used.

Depending on the nature of the alkylene oxide derivative of (meth) acrylic acid to be prepared, the molar ratio of alkylene oxide to (meth) acrylic acid and / or hydroxyalkyl (meth) acrylate can be within a wide range. In a preparation of products having an alkylene glycol group in the molecule, surprising advantages can be achieved in that the molar ratio of alkylene oxide to (meth) acrylic acid in the range of 0.95: 1 to 1.5: 1, particularly preferably in

Range from 1: 1 to 1.1: 1. These values are based on the total amount of added starting materials, since the

Alkylene oxide is preferably introduced via the EduktZuleitung in the reaction mixture, which is provided in the gas supply of the In ektor mixing nozzle.

Surprising advantages in the preparation of derivatives having two or more alkylene glycol groups in the molecule can be achieved when the molar ratio of

Alkylene oxide to (meth) acrylic acid and / or

Hydroxyalkyl (meth) acrylate according to the desired product, wherein the molar ratio of alkylene oxide to (meth) acrylic acid and / or hydroxyalkyl (meth) acrylate

preferably in the range of 1: 1 to 1000: 1, especially

preferably 2: 1 to 100: 1, most preferably 3: 1 to 10: 1 may be.

The preparation of ethylenically unsaturated alkylene oxide derivatives, which are preferably derived from (meth) acrylic acid, can be carried out in the presence of polymerization inhibitors take place, these can be used in many cases already for the preparation of the unsaturated compounds. The preferred polymerization inhibitors include, in particular, phenol compounds, such as, for example

Hydroquinones, hydroquinone ethers, such as

 Hydroquinone monomethyl ether, tert-butylhydroquinone, 2,6-di-tert-butylhydroquinone, 2,5-di-tert-butylhydroquinone, 2,4-dimethyl-6-tert-butylphenol or di-tert-butylcatechol; p-phenylenediamines, such as N, N'-diphenyl-p-phenylenediamine, N, N'-di-2-naphthyl-p-phenylenediamine, N, N'-di-p-tolyl-p-phenylenediamine, N- 1,3-dimethylbutyl-iV '-phenyl-p-phenylenediamine and N-1,4-dimethylpentyl-iV' -phenyl-p-phenylenediamine; Amines, such as thiodiphenylamine and phenothiazine;

Kupferdialkyldithiocarbamate, such as

 Copper dimethyldithiocarbamates, copper diethyldithiocarbamates and copper dibutyldithiocarbamates;

 Nitroso compounds such as nitrosodiphenylamine, isoamyl nitrite, N-nitrosocyclohexylhydroxylamine, N-nitroso-N-phenyl-N-hydroxylamine and their salts; and N-oxyl compounds, such as, for example, 2,2,4,4-tetramethylazetidine-1-oxyl, 2,2-dimethyl-4,4-dipropylazetidine-1-oxyl, 2,2,5,5-tetramethylpyrrolidine-1; oxyl, 2, 2, 5, 5-tetramethyl-3-oxopyrrolidin-1-oxyl, 2,2,6,6-tetramethylpiperidine-1-oxyl, 4-hydroxy-2,2,6,6-tetramethylpiperidine-1-one oxyl, 6-aza-7,7-dimethyl spiro [4,5] decane-6-oxyl, 2,2,6,6-tetramethyl-4-acetoxypiperidine-1-oxyl and 2, 2, 6, 6 Tetramethyl-4-benzoyloxypiperidine-1-oxyl; Methylene blue, nigrosine base BA, 1,4-benzoquinone, hindered phenols,

For example, 2, 4-dimethyl-6-tert-butylphenol and / or tocopherol compounds, preferably tocopherol. The polymerization inhibitors may be used singly or in the form of mixtures and are generally available commercially. For further details, reference is made to the usual technical literature, in particular to the Rompp-Lexikon Chemie; Publisher: J. Falbe, M. Regitz; Stuttgart, New York; 10th edition (1996); Reference "Antioxidants" and cited references cited here.

Surprising benefits can be achieved in particular

Reaction mixtures are obtained which contain preferably 1 to 5000 ppm, more preferably 5 to 1000 ppm and most preferably 10 to 100 ppm of polymerization inhibitor. The reaction temperature in the production of

 Alkylene oxide derivatives of (meth) acrylic acid is preferably in the range of 50 ° C to 100 ° C, more preferably in

Range from 60 to 80 ° C. The absolute pressure in the

Reactor vessel of this reaction may preferably be in the range of 0 to 6 bar, in particular in the range of 1 to 5 bar, more preferably in the range of 2 to 3 bar.

For the implementation of catalysts are preferably used. Preferred catalysts are inter alia in

EP-A-1 231 204 filed on 31.01.2002 at the European Patent Office, EP 02002363.6, the disclosure of which is hereby incorporated by reference, in particular the catalysts and methods described therein

Preparation of hydroxyalkyl (meth) acrylates in the

present application for the purposes of the disclosure. According to another disclosed embodiment, alcohols can be used as starting materials for the preparation of alkylene oxide derivatives. Among the preferred alcohols include methanol, ethanol and propanol, although also ether derivatives of these alcohols can be used, such as methyl triglycol (MTG).

The reaction temperature in the production of

Alkylene oxide ethers are preferably in the range from 50 to 200.degree. C., more preferably in the range from 120.degree. C. to 150.degree. The absolute pressure in the reactor vessel of this reaction may preferably be in the range from 0 to 6 bar, more preferably in the range from 2 to 3 bar.

Preferably, the reaction of alcohols with

Alkylene oxides carried out under catalysis. Preferred catalysts include, but are not limited to, strong bases such as alcoholates, oxides and hydroxides of

Alkali metals. These include, for example, NaOH, KOH, NaOCH ₃ , and NaOC ₂ H ₅ .

Depending on the nature of the ether derivatives to be prepared

Alkylene oxides, the molar ratio of alkylene oxide to alcohol can be in a wide range. At a

Production of products having an alkylene glycol group in the molecule can be achieved surprising advantages that the molar ratio of alkylene oxide to

Alcohol in the range of 1: 1 to 1000: 1, more preferably in the range of 5: 1 to 100: 1. These values relate to the total amount of educts added since the alkylene oxide is preferably introduced into the reaction mixture via the educt feed line, which is provided in the gas feed line of the injector mixing nozzle. A preferred embodiment of a plant for

Implementation of the method set out above is set forth in FIG.

1 shows a plant for the reaction of alkylene oxides 1, which comprises a reactor vessel 2, a feed line 3, a circulation line 4 with a pump 5 and an injector mixing nozzle 6, wherein the gas supply of the injector mixing nozzle 6 with the gas space of the reactor vessel via a Gas line 7 is connected. It is essential to the invention that the gas line 7 is connected to at least one educt feed line 3.

The reactor vessel 2 is preferably designed as a pressure reactor and can have a temperature control, for example a jacket cooling 8. Furthermore you can

surprising advantages can be achieved with a stirrer 9, which is provided in the reactor vessel.

The reaction mixture is circulated via a recirculation line 4, so that the same from the

Reactor vessel 2 is pumped via a pump 5 to the injector mixing nozzle 6. For the dissipation of heat, the

Circulation line 4 to be equipped with a heat exchanger 10. By introducing liquid into the

corresponding supply line of the injector-mixing nozzle 6, a negative pressure in the gas supply of the injector-mixing nozzle 6 are generated, so that gas from the gas space of the

Reactor vessel 2 is withdrawn via the gas line 7. For controlling the gas flow or the negative pressure in the gas line 7, a throttle valve 11 may be provided in the same. In the gas line 6 performs a EduktZuleitung 3, preferably for introducing a liquid in the

Gas line 7 is suitable. Preferably, therefore, the EduktZuleitung 3 may be equipped with a pressure-holding valve 12. Furthermore, for the dosage of the educt, which is preferably present in the liquid phase in the

EduktZuleitung 3 a pump 13 may be provided. The

EduktZuleitung 3 connects preferably one

Eduktvorratsbehälter 14 with the gas line 7. Between the junction of EduktZuleitung 3 with the gas line 7 and In ektor mixing nozzle 6 is a

Mixing section 15. Figure 2 shows a preferred embodiment of an injector mixing nozzle 6 in detail. This preferred injector-mixing nozzle 6 is connected to the circulation line 4, so that a

Circulating flow can be formed. By supplying a liquid under pressure in this supply line 4 and the

Derivation thereof via the nozzle outlet 61 is in

 Nozzle body 62 generates a negative pressure, which can be used to suck in a gas stream via the gas supply line 7. Into the gas supply line 7 performs a educt feed line 3, which is equipped with a pressure-holding valve 12. The entry point of EduktZuleitung 3 with the

 Pressure holding valve 12 is preferably selected so that a mixing section 15 between feed point 63 and

Nozzle entry 64 is obtained. Hereinafter, the present invention is based on

Examples and comparative examples are explained, without this being a restriction. example 1

In a plant according to FIG. 1, methacrylic acid was reacted with ethylene oxide. For this purpose, 5300 kg (61.6 kmol) of methacrylic acid were added to the reactor vessel and treated with 12 kg (52.4 mol) of chromium acetate and 2.5 kg (20.1 mol) of HQME and heated to a temperature of 70 ° C. Subsequently, the mixture was passed through a pump in the injector mixing nozzle, wherein a circulating volume flow of about 70 m ³ / h was set. Subsequently, 2720 kg (61.7 kmol) of ethylene oxide via the EduktZuleitung in the

Gas supply of In ektor mixing nozzle given. The

Dosing was chosen so that a reaction temperature of 70 ° C was not exceeded and was about 900 kg / h (20.4 kmol / h).

After the addition of the intended amount, the

Reaction mixture for a further 5 hours at a temperature of 70 ° C recirculated.

The total reaction time of the reaction was 8 hours. The resulting reaction mixture was analyzed with the proportion of 2-hydroxyethyl methacrylate being about 95.4% as determined by GC-FID (gas chromatography combined with a flame ionization detector). The largest proportion of by-product was formed by diethylene glycol methacrylate at a level of about 3.60%. A special

critical by-product is ethylene glycol dimethacrylate with a proportion of about 0.11%. Comparative Example 1

Example 1 was substantially repeated, with 2740 kg (62.2 kmol) of ethylene oxide added directly to the reactor vessel.

The dosage was chosen so that a

 Reaction temperature of 70 ° C was not exceeded and was about 800 kg / h (20.4 kmol / h). The total reaction time of the reaction was 8.5 hours.

The resulting reaction mixture was analyzed with the proportion of 2-hydroxyethyl methacrylate being about 95.1% as determined by GC-FID (gas chromatography combined with a flame ionization detector). The largest proportion of by-product was formed by diethylene glycol methacrylate at a level of about 3.83%. A special

critical by-product is ethylene glycol dimethacrylate with a proportion of about 0.14%.

The experiments presented show that through the

The system according to the invention reduces the consumption of alkylene oxide, minimizes the formation of critical by-products, in particular of dimethacrylates and the

Reaction time can be reduced.

Example 2

In a system according to FIG. 1

Hydroxypropyl methacrylate reacted with propylene oxide. For this purpose, 577 kg (4 kmol) of hydroxypropyl methacrylate were added to the reactor vessel and treated with 13.4 kg boron trifluoride acetic acid complex and 750 g (6.04 mol) HQME and heated to a temperature of 50 ° C. Subsequently, the mixture was passed through a pump in the In ektor mixing nozzle, wherein a circulating volume flow of about 10 m ³ / h was set. Subsequently, 976 kg (16.8 kmol) of propylene oxide were added via the educt feed line into the gas feed of the injector mixing nozzle. The metered amount was chosen so that a reaction overpressure of 3.5 bar was not exceeded and was about 120 kg / h (2.07 kmol / h). After the addition of the intended amount, the

 Reaction mixture for a further 2 hours at a temperature of 50 ° C recirculated.

The total reaction time of the reaction was 10 hours. The neutralization of the reaction mixture takes place

then at 70 ° C with the addition of 45.5 kg

 Sodium carbonate decahydrate. After the neutralization time of 4 hours, the reaction mixture was cooled and filtered. It will be about 1500 kg

Polypropylene glycol monomethacrylate obtained, which is a

OH number of 133 mg KOH / g possesses what one

 Propoxylierungsgrad of 5.3 corresponds.

Example 3

In a plant according to FIG. 1, methyltriglycol was reacted with ethylene oxide. To this end, 1300 kg (7.92 kmol) of methyltriglycol were added to the reactor vessel and treated with 40 kg (0.74 kmol) NaOCH ₃ and heated to a temperature of 125 ° C. Subsequently, the mixture was passed via a pump in the injector mixing nozzle, wherein a

Circulating volume flow of about 70 m ³ / h was set.

This was followed by 7630 kg (173.21 kmol) of ethylene oxide the educt feed into the gas supply of the injector mixing nozzle given. The metered amount was chosen so that a reaction overpressure of 0.61 bar was not exceeded and was about 950 kg / h (21.57 kmol / h).

After the addition of the intended amount, the

Reaction mixture further circulated for 2 hours at a temperature of 125 ° C. The total reaction time of the reaction was 10 hours. About 6300 kg of methoxypolyethylene glycol compound are obtained, which has an OH number of 55 mg KOH / g, which corresponds to a molecular weight of 1018 g / mol.

Claims

claims 1. plant for the reaction of alkylene oxides 1, comprising at least one reactor vessel 2, at least one  EduktZuleitung 3, at least one circulation line 4 with a pump 5 and an In ektor mixing nozzle 6, characterized in that the gas supply of the injector Mixing nozzle 6 is connected to the gas space of the reactor vessel 2 via a gas line 7, which is connected to at least one EduktZuleitung 3. 2. Installation according to claim 1, characterized in that in the recirculation line 4 at least one heat exchanger 10 is provided. 3. Plant according to claim 1 or 2, characterized  characterized in that a pressure-holding valve 12 is provided in the EduktZuleitung 3. 4. Plant according to at least one of the preceding  Claims, characterized in that in  Reactor vessel 2 is provided with a stirrer. 5. Installation according to at least one of the preceding  Claims, characterized in that the injector Mixing nozzle achieved a suction ratio in the range of 0.5 to 20. 6. A process for the preparation of alkylene oxide derivatives, characterized in that for carrying out the Process a plant according to at least one of Claims 1 to 5 is used. 7. The method according to claim 6, characterized in that at least one alkylene oxide is fed in the liquid phase in the EduktZuleitung the reaction mixture, which is provided in the gas line to In ektor-mixing nozzle. 8. The method according to any one of claims 6 or 7, characterized in that the method is carried out with a metering ratio in the range of 5 to 500. 9. The method according to any one of claims 6 to 8, characterized in that the pressure at which the reaction takes place in the range of 1 to 5 bar. 10. The method according to any one of claims 6 to 9, characterized in that ethylene oxide and / or propylene oxide is used as starting material. 11. The method according to any one of claims 6 to 10, characterized in that (meth) acrylic acid and / or at least one hydroxyalkyl (meth) acrylate is used as starting material. 12. The method according to claim 11, characterized in that the molar ratio of alkylene oxide to  (Meth) acrylic acid in the range of 1.1: 1 to 1: 1. 13. The method according to claim 11, characterized in that the molar ratio of alkylene oxide to (Meth) acrylic acid and / or hydroxyalkyl (meth) acrylate in the range of 2: 1 to 100: 1. 14. The method according to any one of claims 6 to 10, characterized in that an alcohol is used as starting material. 15. The method according to claim 14, characterized in that the molar ratio of alkylene oxide to alcohol in the range of 5: 1 to 100: 1.