DE102007023757A1 - Plant and method for the continuous industrial production of organosilanes - Google Patents

Abstract

The present invention relates to a plant for the continuous industrial implementation of a reaction, wherein an alpha, beta-unsaturated aliphatic, optionally substituted compound A with an HSi compound B optionally in the presence of a catalyst C and / or other auxiliaries and the system at least the starting material combination (3) for the components A (1) and B (2), at least one multi-element reactor (5), which in turn includes at least two reactor units, and based on a product work-up (8). Furthermore, the invention relates to the use of a plant for the continuous industrial implementation of a hydrosilylation, wherein an alpha, beta-unsaturated aliphatic, optionally substituted compound A with an HSi compound B is optionally reacted in the presence of a catalyst C.

Description

The The present invention relates to a new plant for continuous industrial production of organosilanes by reaction of an α, β-unsaturated aliphatic, optionally substituted compound having a HSi compound as well as a related matter Method.

Organosilanes, such as vinylchloro- and vinylalkoxysilanes ( EP 0 456 901 A1 . EP 0 806 427 A2 ), Chloroalkylchlorosilanes ( DE-AS 28 15 316 . EP 0 519 181 A1 . DE 195 34 853 A1 . EP 0 823 434 A1 . EP 1 020 473 A2 ), Alkylalkoxysilanes ( EP 0 714 901 A1 . DE 101 52 284 A1 ), Fluoroalkylalkoxysilanes ( EP 0 838 467 A1 . DE 103 01 997 A1 ), Aminoalkylalkoxysilanes ( DE-OS 27 53 124 . EP 0 709 391 A2 . EP 0 849 271 A2 . EP 1 209 162 A2 . EP 1 295 889 A2 ), Glycidyloxyalkylalkoxysilanes ( EP 1 070 721 A2 . EP 0 934 947 A2 ), Methacryloxyalkylalkoxysilanes ( EP 0 707 009 A1 . EP 0 708 081 A2 ), Polyetheralkylalkoxysilanes ( EP 0 387 689 A2 ), etc., are of high technical and industrial interest. Processes and plants for their production have long been known. These products are comparatively small tonnage products and are predominantly produced in batch processes. As a rule, multiple-use systems are used in order to achieve the highest possible utilization of the batch systems. However, when changing the product consuming cleaning and rinsing of such batch systems are necessary. In addition, long residence times of the reaction mixture in a large-volume, expensive and labor-intensive batch system are often required in order to achieve sufficient yield. Furthermore, said reactions are often considerably exothermic with heat of reaction in the range of 100 to 180 kJ / mol. Therefore, in the implementation of undesirable side reactions can have a significant impact on selectivity and yield. If these reactions are hydrosilylations, the possible elimination of hydrogen places considerable demands on the safety technology. Furthermore, an educt is frequently introduced together with the catalyst and the other educt is added in a semi-batch procedure. In addition, even small variations in the process control of batch or semi-batch plants can lead to a considerable diversification of the yields and product qualities via different approaches. If you want to transfer results from the laboratory / pilot plant scale to the batch scale (scale up), you often experience difficulties.

Microstructured reactors as such, for example for a continuous production of polyether alcohols ( DE 10 2004 013 551 A1 ) or the synthesis of, inter alia, ammonia, methanol, MTBE ( WO 03/078052 ), are known. Also, microreactors for catalytic reactions are known ( WO 01/54807 ). However, so far the microreactor technology for the industrial production of organosilanes has been omitted or at least not realized. The tendency of alkoxy- and chlorosilanes to hydrolysis - even with small amounts of moisture - and corresponding caking in a Organosilanherstellungsanlage probably to be seen as a sustainable problem.

Therefore the task was up for the industrial production of said organosilanes another possibility provide. In particular, there was the concern, another possibility for the to provide continuous production of such organosilanes, while trying to minimize the above-mentioned disadvantages.

The Asked object is inventively according to the information in the claims solved.

So was in surprising Ways to find a hydrosilylation or the reaction an HSi-containing component with another gaseous or liquid α, β-unsaturated Connection in a simple and economical way in an industrial scale continuously in a plant operating on a multi-element reactor based, perform beneficial can.

Unlike a batch approach, it is possible in the present invention to premix the educts immediately before the multi-element reactor, the pre-mixing can also be done cold, then heat in the multi-element reactor and there targeted and continuously implement. It is also possible to add a catalyst to the educt mixture. Subsequently, the product can be worked up continuously, z. As in an evaporation, rectification and / or using a Kurzweg- or thin-film evaporator - to name just a few options. The heat of reaction liberated during the reaction can advantageously be removed in the multielement reactor via the large surface area of the interior walls of the reactor in relation to the reactor volume and, if provided, to a heat transfer medium. Furthermore, in the present application of multielement reactors, a significant increase in the space-time yield of fast, heat-dissipating reactions is possible. This is made possible in particular by a faster mixing of the educts, a higher average concentration level of the reactants than in the batch process, ie no limitation by educt depletion, and / or an increase in temperature, which can usually cause an additional acceleration of the reactors. In addition, the present invention enables the preservation of process reliability in a comparatively simple and economical manner. So could at present the invention drastic process intensification, in particular a shortening of the process time under reaction conditions by more than 99%, based on the space-time yield, compared to the standard batch process can be achieved. At the same time, increased yields of up to 20% were achieved through higher conversions and selectivities. Preferably, the present reactions were carried out in a stainless steel multi-element reactor. Thus, for the implementation of said implementations can be dispensed with the use of special materials in an advantageous manner. In addition, can be determined by the continuous procedure in reactions to be carried out under pressure a longer service life of the metal reactors, since the material fatigue compared to a batch mode significantly slower. Next, in addition to hydrosilylations, for example, reactions such as those of vinyl chloride and trichlorosilane to vinyltrichlorosilane can be advantageously carried out at a higher temperature. In addition, the reproducibility compared to comparable studies in batch processes could be significantly improved. In addition, there is a significantly reduced scale-up risk in the transfer of the results from the laboratory or pilot plant scale in the present method. In particular, in the present continuous process using a plant according to the invention, wherein a multi-element reactor advantageously includes a prereactor, a surprisingly long plant life even without stoppages caused by caking or deposits are made possible. Moreover, it has surprisingly been found that in the present process it is particularly advantageous to rinse, ie precondition, the multielement reactor before starting the actual reaction with the reaction mixture, especially if it contains a homogeneous catalyst. By this measure, an unexpectedly rapid adjustment of constant process conditions can be effected at a high level.

The present invention thus relates to a plant for the continuous industrial implementation of a reaction in which an α, β-unsaturated aliphatic, optionally substituted compound A is reacted with an HSi compound B, optionally in the presence of a catalyst C and / or optionally in the presence of further auxiliaries and the plant at least on the reactant merge ( 3 ) for the components A ( 1 ) and B ( 2 ), at least one multi-element reactor ( 5 ), which in turn contains at least two reactor units, and at a subsequent product processing ( 8th ).

The 1 to 6 are flow diagrams of plants or system parts as preferred embodiments of the present invention can be seen.

So is 1 a preferred continuous system in which the educt components A and B in the unit ( 3 ), the unit ( 5 ), which may contain an immobilized catalyst, fed, reacted there and the reaction product in the unit ( 8th ) is worked up.

2 shows a further preferred embodiment of a present continuous plant, wherein a catalyst C of the component B is supplied. But you can also use the catalyst ( 3 ) or - like 3 it can be seen - the catalyst C a mixture of the components A and B shortly before entering the multi-element reactor unit ( 5 ).

Further you can optionally the respective streams mentioned further auxiliaries enforce.

A unit of a reactor unit is understood as meaning an element of the multielement reactor ( 5 ), each element representing a region or reaction space for said reaction, cf. for example ( 5.1 ) (Reactor unit in the form of a pre-reactor) in 4 such as ( 5.5 ) [Reactor unit of an integrated block reactor ( 5.3 )] in 5 such as ( 5.10 ) [Reactor unit of a microtube bundle heat exchanger reactor ( 5.9 )]. Ie. Reactor units of a multi-element reactor ( 5 ) within the meaning of the present invention are in particular stainless steel or quartz glass capillaries, stainless steel pipes or well-dimensioned stainless steel reactors, for example pre-reactors ( 5.1 ), Pipes ( 5.10 ) in microtube bundle heat exchangers [e.g. B. ( 5.9 )] as well as converted areas ( 5.5 ) in the form of integrated block reactors [e.g. B. ( 5.3 )]. In this case, the inner walls of the reactor elements may be coated, for example with a ceramic layer, a layer of metal oxides, such as Al ₂ O ₃ , TiO ₂ , SiO ₂ , ZrO ₂ , zeolites, silicates, to name just a few, but also organic polymers, in particular fluoropolymers, such as Teflon, are possible.

Thus, a plant according to the invention comprises one or more multi-element reactors ( 5 ), which in turn are based on at least 2 to 1,000,000 reactor units, including all natural numbers in between, preferably from 3 to 10,000, in particular from 4 to 1,000, reactor units.

In this case, the reactor or reaction space of at least one reactor unit preferably has a semicircular, semi-oval, round, oval, triangular, square, rectangular or trapezoidal cross-section perpendicular to the flow direction. Preferably has such Cross section a cross sectional area of 75 microns ² to 75 cm ² . Particularly preferred are cross-sectional areas of 0.7 to 120 mm ² and all numerically intervening numerical values. For round cross-sectional areas, a diameter of ≥ 30 μm to <15 mm, in particular 150 μm to 10 mm, is preferred. Square cross-sectional areas preferably have edge lengths of ≥ 30 μm to ≦ 15 mm, preferably 0.1 to 12 mm. In a multielement reactor ( 5 ) of a plant according to the invention reactor units are present with differently shaped cross-sectional areas.

Furthermore, the structure length in a reactor unit, ie from entry of the reaction or product stream into the reactor unit, cf. z. B. ( 5.1 and 5.1.1 ) or ( 5.5 and 5.5.1 ), until the exit, cf. ( 5.1.2 ) respectively. ( 5.5.2 ), preferably 5 cm to 500 m, including all numerically intervening numerical values, more preferably ≥ 15 cm to 100 m, most preferably 20 cm to 50 m, in particular 25 cm to 30 m.

In a plant according to the invention it is preferred to reactor units, their respective reaction volume (also referred to as reactor volume, i.e. the product of cross-sectional area and Structure length) 0.01 ml to 100 l, inclusive of all numerically intervening numerical values. Especially is preferred the reactor volume of a reactor unit of a plant according to the invention 0.05 ml to 10 l, most preferably 1 ml to 5 l, very particularly preferably 3 ml to 2 l, in particular 5 ml to 500 ml.

Furthermore, installations according to the invention can be installed on one or more multi-element reactors ( 5 ), which are preferably connected in parallel. You can said multi-element reactors ( 5 ) but also in succession, so that the product derived from the preceding multi-element reactor can be fed to the inlet of the subsequent multi-element reactor.

Present multi-element reactors ( 5 ) can advantageously with a Eduktkomponentenstrom ( 4 ) respectively. ( 5.2 ), which is suitably divided into the respective partial flows, cf. z. B. ( 5.4 ) in 5 such as ( 5.11 ) in 6 to be fed. After the reaction, the product streams can be combined, cf. z. B. ( 5.7 ) in 5 , ( 5.12 ) in 6 such as ( 7 ), and then advantageously in a workup unit ( 8th ) work up. In this case, such a processing unit ( 8th ) initially have a condensation stage or evaporation stage, optionally followed by one or more distillation stages.

Furthermore, a multi-element reactor ( 5 ) a system according to the invention on at least one, preferably at least two parallel-connected stainless steel capillaries or on at least two quartz glass capillaries connected in parallel or at least one shell-and-tube heat exchanger reactor ( 5.9 ) or at least one integrated block reactor ( 5.3 ).

In this case, it is possible to use stainless steel capillaries or reactors which advantageously consist of a high-strength, high-temperature resistant and stainless stainless steel, for example but not exclusively such capillaries, block reactors or tube bundle heat exchangers of steel of the type 1.4571 or 1.4462, cf. In particular, the steel facing the reaction chamber surface of a stainless steel capillary or a multi-element reactor with a polymer layer, for example a fluorine-containing layer, including Teflon, or a ceramic layer, preferably an optionally porous SiO ₂ -, TiO ₂ - or Al ₂ O ₃ layer, in particular for receiving a catalyst, be equipped.

suitable Stainless steel or quartz glass capillaries are usually commercially available available.

Also, a multi-element reactor ( 5 ) include a shell and tube heat exchanger reactor, which can optionally be carried out in countercurrent temperature. Thus, there is a so-called, preferably microstructured tube bundle heat exchanger reactor used according to the invention, ie micro tube bundle heat exchanger reactor, cf. for example ( 5.9 ) in 6 , suitably from a tube bundle ( 5.10 ), with the respective tubes ( 5.10 ) preferably have the above-mentioned dimensions, are the same, especially in terms of length and diameter, and made of a stainless steel. The inlet levels of the respective tubes ( 5.10 ) are oriented in one plane and have a common educt feed ( 4 ) 5.11 ) and a joint product transfer or merger ( 5.12 ) 7 ). In addition, the tube bundle ( 5.10 ) are bathed by a medium (D) for temperature control ( 5.13 ). Preferably, the tube bundle is flushed against the flow direction with temperature control medium (D, 6.1 . 6.2 ). In this case, such a system in a reactor jacket ( 5.14 ) are introduced, this being advantageous via an educt feed ( 4 ), a product withdrawal ( 7 ), a temperature control ( 6.1 ) and a Temperiermittelabführung ( 6.2 ). It is preferable to switch a microtube bundle heat exchanger reactor ( 5.9 ), see. 6 , at least one pre-reactor ( 5.1 ), see. also 4 , in front.

Furthermore, as a multi-element reactor ( 5 ) advantageously use an integrated block reactor, as he used, for example, as a temperature-adjustable block reactor Tor, constructed of defined structured metal plates (hereinafter also referred to as level), can be seen from http://www.heatric.com/pche-construction.html emerges.

The Production of said structured metal plates or planes which then a block reactor can be created, for example, by etching, turning, Cutting, milling, Embossing, rolling, Spark erosion, laser processing, plasma technology or another Technique of the known processing methods done. So be with the utmost precision well-defined and targeted structures, for example Grooves or joints, on one side of a metal plate, in particular a metal plate made of stainless steel, incorporated. The find respective grooves or joints start on a front side of the Metal plate, are continuous and usually end on the opposite face of the Metal plate.

So shows 5 a level of an integrated block reactor ( 5.3 ) with several reactor units or elements ( 5.5 ). In this case, such a level usually consists of a base plate made of metal with metal walls ( 5.6 ), which contain the reaction spaces ( 5.5 ) together with a cover plate made of metal and a unit for tempering ( 6.5 . 6.6 ), preferably a further level or structured metal plate. Furthermore, the unit contains ( 5.3 ) an area ( 5.4 ) for the task and distribution of the educt mixture ( 5.2 ) in the reactor elements ( 5.5 ) and an area ( 5.7 ) for combining the product streams from the reaction areas ( 5.5 ) and removal of the product stream ( 7 ). In addition, as part of an integrated block reactor ( 5.3 ) several such previously described levels be connected one above the other. The bonding can be done for example by (diffusion) welding or soldering; for such and other working techniques applicable here cf. also www. immmainz.de/seiten/de/u_050527115034_2679.php?PHPSESSID=75a6285eb0433122b9cec aca3092dadb. Furthermore, such integrated block reactors ( 5.3 ) advantageous from a temperature control unit ( 6.5 . 6.6 ) surrounding the heating or cooling of the block reactor ( 5.3 ), ie a targeted temperature control enabled. For this purpose, a medium (D), z. B. Marlotherm or Mediatherm, by means of a heat exchanger ( 6.7 ) and via line ( 6.8 ) of a pump ( 6.9 ) and line ( 6.1 ) of the temperature control unit ( 6.5 ) and via ( 6.6 ) and ( 6.2 ) and the heat exchanger unit ( 6.7 ). This can be done in an integrated block reactor ( 5.3 ) optimally controlled by the shortest route, thereby avoiding temperature peaks that adversely affect a targeted reaction, avoid. One can use the integrated block reactor ( 5.3 ) and the relevant temperature control unit ( 6.5 . 6.6 ) but also designed so that between two reactor element levels each have a temperature control is arranged, the more directional leadership of the temperature control medium between the areas ( 6.1 . 6.5 ) and ( 6.6 . 6.2 ).

In plants according to the invention, preference is given in particular to a multielement reactor ( 5 ) containing at least one pre-reactor ( 5.1 ) and at least one further reactor unit, for example a stainless steel capillary, or a prereactor ( 5.1 ) and at least one integrated block reactor ( 5.3 ), see. 4 , or at least one pre-reactor ( 5.1 ) and a shell and tube heat exchanger reactor ( 5.9 ), see. 6 , includes. Furthermore, the prereactor ( 5.1 ) suitably heatable, ie coolable and / or heatable, from (D, 6.3 . 6.4 ).

As a rule, traces of water already lead to the hydrolysis of the alkoxy or chlorosilane educts and thus to deposits or caking. The particular advantage of such an embodiment of a pre-reactor ( 5.1 ) in the context of the multi-element reactor ( 5 ), in particular for the implementation of silanes, is that you can advantageously minimize unplanned downtime or downtime in addition to carrying out the continuous implementation by a targeted separation and discharge of hydrolyzates or particles. So you can the prereactor ( 5.1 ) additionally upstream or downstream of a filter for particle separation. But you can also integrate the filter in the prereactor.

In general, a plant according to the invention for the continuous industrial implementation of reactions based on a reactant combination ( 3 ) for the components A and B, at least one said multi-element reactor ( 5 ) and on a product reconditioning ( 8th ), see. 1 ,

The educt components A and B may each be continuously from a storage unit by means of pumps and optionally by means of differential weighing system in the range ( 3 ) are brought together purposefully. In general, the components A and B are dosed at ambient temperature, preferably at 10 to 40 ° C and in the range ( 3 ) mixed. But you can also preheat at least one of the components, both components or feedstocks or the corresponding mixture. Thus, the said storage unit can be conditioned and the storage containers can be designed to be temperature-controlled. Furthermore, it is possible to combine the educt components under pressure. Via line ( 4 ), the starting material mixture can be mixed with the multielement reactor ( 5 ) continuously.

The multi-element reactor ( 5 ) preferably by means of a tempering medium D ( 6.1 . 6.2 ) brought to the desired operating temperature or maintained, so that undesirable temperature peaks and temperature fluctuations, which are known from batch plants, advantageously avoided in the present inventive system or can be sufficiently low.

The product or crude product stream ( 7 ) is continuously the product processing ( 8th ), for example a rectification unit, wherein, for example, overhead ( 10 ) a low-boiling product F, for example an excessively used and optimally recyclable silane, and via the sump ( 9 ) a heavy boiling product E can decrease continuously. One can leave the unit ( 8th ) but also take sidestreams as a product.

If it is necessary to carry out the reaction of components A and B in the presence of a catalyst C, it is advantageously possible to use a homogeneous catalyst by metering into the educt stream. But you can also use a suspension catalyst, which can also be added to the reactant stream. In this case, the maximum particle diameter of the suspension catalyst should be less than 1/3, preferably 1/10 to 1/100, of the extent of the smallest free cross section of the cross-sectional area of a reactor unit ( 5 ) and the average particle cross-sectional area, preferably 10 ² to 10 ^-6 mm ² , particularly preferably 10 to 10 ^-4 mm ² , very particularly preferably 1 to 10 ^-3 mm ² , so that there is no blockage, but still simple can be separated from the product stream in a downstream arrangement.

So is 2 it can be seen that it is advantageous to add a said catalyst C to component B before it reacts with component A in the range ( 3 ) is merged.

It is possible to use a homogeneous catalyst C or a suspension catalyst C but also a mixture of A and B which is present in line ( 4 ), preferably just before entering the multi-element reactor, via a line ( 2.2 ), cf. 3 ,

In The same way as with a homogeneous catalyst can be the reactant components A and B also other, mainly liquid excipients, for example - but not exclusively - activators, initiators, Stabilizers, inhibitors, solvents or diluent etc., add.

But you can also use a multi-element reactor ( 5 ) equipped with an immobilized catalyst C, cf. 1 , In this case, the catalyst C, for example - but not exclusively - be present on the surface of the reaction space of the respective reactor elements. For carrying out a corresponding coating of the surface, reference is made to all known methods of surface technology.

In general, a plant according to the invention for the continuous industrial implementation of the reaction of a said compound A with a compound B is optionally based in the presence of a catalyst and further auxiliaries on at least one reactant combination ( 3 ), at least one multi-element reactor ( 5 ), which in turn contains at least two reactor units, and on a product workup ( 8th ). Suitably, the reactants or feedstocks are provided in a storage unit for carrying out the reaction and fed or metered as required. In addition, a system according to the invention is equipped with the measuring, metering, shut-off, transport, conveying, monitoring and control units as well as exhaust and waste disposal devices which are conventional in the art. In addition, such a system according to the invention can be advantageously accommodated in a portable and stackable container and handled flexibly. So you can bring a system according to the invention quickly and flexibly, for example, to the respective educt or energy sources. With a system according to the invention, but also with all the advantages, it is possible to continuously provide product at the point at which the product is further processed or used further, for example directly at the customer's.

One further, particularly noteworthy advantage of a system according to the invention for the continuous industrial implementation of a reaction α, β-unsaturated Compounds A with an HSi compound B is that now over a possibility features, also small special products with sales volumes between 5 kg and 50 000 t p. a., Preferably 10 kg to 10 000 t p. a., in simple and economical to produce continuously and flexibly. It can unnecessary Downtimes, the yield, the selectivity affecting temperature peaks and fluctuations and too long residence times and thus undesirable side reactions advantageous be avoided. In particular one can such a plant also under economic, ecological and customer-friendly aspects optimal for the production of existing Use silanes.

Thus, the present invention also provides a process for the continuous industrial production of an organosilane of the general formula (I) Y-Si (R ') _m (X) _3-m (I), wherein Y is an organo-functional group selected from vinyl, C ₂ - to C ₁₈ -alkyl, C ₃ - to C ₁₅ -fluoroalkyl, C ₃ - to C ₄ -chloroalkyl, aminoalkyl, glycidyloxyalkyl, methacryloxyalkyl, polyetheralkyl and R 'is a C ₁ to C ₄ alkyl group, m is 0 or 1 and X is a hydrolyzable group,
wherein one carries out the reaction of the educt components A and B in at least one multi-element reactor, which in turn is based on at least two reactor units.

The reaction is preferably carried out in at least one multielement reactor ( 5 ), whose reactor units - especially but not exclusively - made of stainless steel or quartz glass or its reaction spaces are limited by stainless steel or quartz glass, wherein the surfaces of the reactor units may be coated or coated, for example with Teflon.

Further is in process of the invention prefers that reactor units are used, their respective Semicircular cross-section, semi-oval-shaped, round, oval, triangular, square, rectangular or trapezoidal.

Advantageously, reactor units are used whose respective cross-sectional area is 75 μm ² to 75 cm ² .

Further it is preferable to use such reactor units having a structure length of 1 cm to 200 m, more preferably 10 cm to 120 m, especially preferably 15 cm to 80 m, in particular 18 cm to 30 m, including all potential Numerical values included by the aforementioned ranges be, have.

So one sets in the method according to the invention suitably reactor units, their respective reaction volume 0.01 ml to 100 l including of all numerically intervening numerical values, preferably 0.1 ml to 50 l, more preferably 1 ml to 20 l, most preferably 2 ml to 10 l, especially 5 ml to 5 l.

In the process according to the invention, the said reaction can also be advantageously carried out in a plant with a multielement reactor ( 5 ) carried out on at least one stainless steel capillary or at least one quartz glass capillary or at least one integrated block reactor ( 5.3 ) or at least one tube bundle heat exchanger reactor ( 5.9 ).

In particular, a multielement reactor ( 5 ) containing at least one pre-reactor ( 5.1 ) includes. The process according to the invention is particularly preferably carried out in reactor units made of stainless steel.

Further it is preferred that in the process according to the invention with the reactant / product mixture in contact surface the reactor units of the multi-element reactor with a catalyst is occupied, especially if one is in the presence of an immobilized Catalyst or heterogeneous catalyst works.

Provided one in the context of the method according to the invention the reaction of components A and B in the presence of a homogeneous Catalyst C is carried out, was surprisingly found that it is particularly advantageous to the multi-element reactor by one or more rinses with a mixture of homogeneous catalyst C and component B or from Homogeneous catalyst C and components A and B or a short-term operation the plant, for example 10 to 120 minutes and optionally with a higher catalyst concentration, precondition.

The for the Preconditioning of the multi-element reactor used substances can caught and later the educt stream are at least proportionally dosed or directly the Product processing supplied and be worked up.

By the preconditioning of the multi-element reactor described above, especially if it is made of stainless steel, you can in surprising and advantageously a faster operating state faster achieve at maximum yield.

At the inventive method you can perform the said reaction in the gas and / or liquid phase. there the reaction or product mixture can be present in one, two or three phases. Preferably leads in the method according to the invention the implementation of single phase, in particular in the liquid phase, by.

So one operates the method according to the invention advantageous using a multi-element reactor at a temperature from 0 to 800 ° C at a pressure of 0.1 to 500 bar abs. Preferably leads you while the reaction of the components A and B, in particular a hydrosilylation, in the multi-element reactor at a temperature of 50 to 200 ° C, preferably at 60 to 180 ° C, and at a pressure of 0.5 to 300 bar abs., Preferably at 1 up to 200 bar abs., Particularly preferably at 2 to 50 bar abs., By.

In general, the differential pressure in a system according to the invention, ie between Eduktzusammenführung ( 3 ) and product processing ( 8th ), 1 to 10 bar abs. Advantageously, you can equip a system according to the invention with a pressure-holding valve, especially when using trimetho xysilane (TMOS). Preference is given to the pressure-holding valve from 1 to 100 bar abs., Preferably to 70 bar abs., Particularly preferably to 40 bar abs., In particular to a value between 10 to 35 bar abs., A.

The reaction can be inventively analog to the space velocity at a linear velocity (LV) of 1 to 1 · 10 ⁴ h ^-1 i. N. Perform. The flow rate of the stream in the reactor units is preferably in the range of 0.0001 to 1 m / s i. N., more preferably 0.0005 to 0.7 m / s, very particularly preferably 0.001 to 0.5 m / s, in particular 0.05 to 0.3 m / s, and all possible numerical values within the abovementioned ranges. If the ratio of reactor surface area (A) to reactor volume (V) is predominant in the reaction according to the invention, an A / V ratio of 20 to 5,000 m ² / m ^{3 is} preferred, including all numerically possible individual values which are mentioned in the cited US Pat Range lie - for the advantageous implementation of the method according to the invention. The A / V ratio is a measure of the heat transfer and possible heterogeneous (wall) in fl uences.

So you lead the reaction in the process according to the invention advantageous for a mean residence time (τ) of 10 seconds to 60 minutes, preferably 1 to 30 minutes, more preferably 2 to 20 minutes, especially 3 to 10 minutes, through. Again, it will be on again all possible Numerical values disclosed by the named area are indicated separately.

As component A, the following α, β-unsaturated compounds can be used in the process of the invention, for example, but not exclusively: acetylene, vinyl chloride (VC), allyl chloride (H ₂ C = CH-CH ₂ Cl), 3-chloro-2-methylpropene -1, allylamine (H ₂ C = CH-CH ₂ NH ₂ ), 3-glycidyloxypropene-1, 3-methylacryloxypropene-1 (allyl methacrylate), butene-1, isobutene [H ₂ C = C (CH ₂ ) ₂ ], Vinylcyclohexene-3, octene-1, isooctene, hexadecene-1, H ₃ C [O- (CH ₂ ) ₂ ] _n O-CH ₂ CH = CH ₂ where n = 1 to 20, in particular the numbers 2, 3, 4 , 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18 and 19, H [O- (CH ₂ ) ₂ ] _n O-CH ₂ CH = CH ₂ with n = 1 to 20, in particular 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18 and 19, F ₃ C (CF ₂ ) _y -CH = CH ₂ with y = 0 to 9, in particular 2, 3, 4, 5, 6, 7 and 8, for example - but not exclusively - 8,8,8,7,7,6,6,5 , 5,4,4,3,3-Tridecafluorocten -1.

Suitable components B in the process according to the invention are silanes of the general formula (II) HSi (R ') _m X ₃ -m (II), wherein R 'is a C ₁ to C ₄ alkyl group, preferably methyl, m is 0 or 1 and X is a hydrolyzable group, preferably chloride, methoxy, ethoxy.

So If according to the invention it is preferred to use trichlorosilane (TCS), methyldichlorosilane, dimethylchlorosilane, trimethoxysilane (TMOS), Triethoxysilane (TEOS), methyldimethoxysilane or methyldiethoxysilane one.

The Components A and B are preferably employed in the process according to the invention a molar ratio A to B from 1: 5 to 100: 1, more preferably 1: 4 to 5: 1, completely particularly preferably 1: 2 to 2: 1, in particular from 1: 1.5 to 1.5: 1, including all potential Numbers within the aforementioned areas, a.

The inventive method one leads preferentially in the presence of a catalyst C by. One can the method according to the invention but also operate without the addition of a catalyst, in which case usually expected with a significant decrease in yield is.

In particular, the process according to the invention is used for carrying out a hydrosilylation reaction for preparing organosilanes of the formula (I), in particular homogeneous catalysts from the series Pt complex catalyst, for example those of the Karstedt type, such as Pt (0) -divinyltetramethyldisiloxane in xylene, PtCl ₄ , H ₂ [PtCl ₆ ] or H ₂ [PtCl ₆ ] .6H ₂ O, preferably a "Speyer catalyst", cis- (Ph ₃ P) ₂ PtCl ₂ , complex catalysts of Pd, Rh, Ru, Cu, Ag Au, Ir or those of other transition metals or noble metals or corresponding multielement catalysts, whereby the complex catalysts known per se can be used in an organic, preferably polar solvent, for example but not exclusively ethers, such as THF, ketones, such as acetone, alcohols , such as isopropanol, aliphatic or aromatic hydrocarbons, such as toluene, xylene, CHC, CFC, dissolve.

In addition, one can add to the homogeneous catalyst or the solution of Homogenkatalyators an activator, for example in the form of an organic or inorganic acid such as HCl, H ₂ SO ₄ , H ₃ PO ₄ , mono- or dicarboxylic acids, HCOOH, H ₃ C-COOH , Propionic Acid, Oxalic Acid, Succinic Acid, Citric Acid, Benzoic Acid, Phthalic Acid - just to name a few.

Furthermore may be the addition of an organic or inorganic acid to Reaction to take another advantageous function, For example, as a stabilizer or inhibitor of impurities in trace amounts.

Further can also be the surface the present reactor interior walls, especially in the case of metal reactors, under operating conditions act catalytically.

Provided in the method according to the invention uses a homogeneous catalyst or a suspension catalyst, if the olefin component A is added to the catalyst, based on the metal, preferably in a molar ratio of 2,000,000: 1 to 1 000: 1, more preferably from 1 000 000: 1 to 4 000: 1, in particular from 500 000: 1 to 10 000: 1, and all possible numbers within the previously mentioned areas.

However, it is also possible to use an immobilized catalyst or heterogeneous catalyst from the series of transition metals or noble metals or a corresponding multielement catalyst for carrying out the hydrosilylation reaction. So you can, for example - but not exclusively - use precious metal sludge or precious metal on activated carbon. But you can also provide a fixed bed for receiving a heterogeneous catalyst in the field of multi-element reactor. Thus, for example-but not exclusively-heterogeneous catalysts which are supported on a carrier, such as spheres, strands, pellets, cylinders, stirrers, etc., inter alia SiO ₂ , TiO ₂ , Al ₂ O ₃ , ZrO ₂ , in the reaction region of the reactor units contribute.

Examples for integrated Fixed bed block reactors are available at http://www.heatric.com/iqs/sid.0833095090382426307150/mab_reactors.html refer to.

Furthermore, according to the invention, the reaction of a fluoroolefin with an HSi compound can also be carried out in the presence of a free-radical initiator, as it is in particular DE 103 01 997 A1 can be seen.

Further can one dissolve as auxiliaries or diluents, such as alcohols, aliphatic and aromatic hydrocarbons, CKW, CFCs, ethers, esters, ketones - just to name a few - use. Such adjuvants can be removed from the product, for example, in the product workup.

Also can be in the present process inhibitors, for example Polymerization inhibitors or corresponding mixtures, as additional Use excipients.

In the process according to the invention, for example-but not exclusively-the following reactions can be advantageously carried out:
For example, vinyl chloride (VC) can be thermally reacted with trichlorosilane (TCS) with elimination of HCl to give vinyltrichlorosilane (VTCS) and the crude product worked up by distillation. Suitably, VC and TCS are employed in a molar ratio of 1: 1.05 to 1: 2. You can also premix the components. For this you can pre-evaporate TCS. The reaction of the components is generally carried out at 300 to 700 ° C and a pressure of 1 to 100 bar abs., Preferably at 1.5 to 10 bar abs., In particular at 2 to 5 bar abs. You can do without the presence of a catalyst. The thermal conversion of VC and TCS is preferably carried out in a system according to the invention, advantageously using a multi-element reactor which is based on a temperature-controllable prereactor and a downstream heatable, integrated block reactor or prereactor and at least one downstream stainless steel capillary. The prereactor is preferably operated at 200 to 450 ° C and 1 to 10 bar abs. and the downstream of the pre-reactor reactor units preferably at 450 to 650 ° C and 1 to 10 bar abs. The residence time of the reaction mixture in the multi-element reactor is preferably 0.2 to 20 seconds, more preferably 0.5 to 5 seconds. The crude product obtained in the multi-element reactor is suitably condensed in the product work-up and worked up by distillation, preferably in two stages. The task of the crude product is preferably carried out at the top of the column. Thus, it is advantageous to obtain vinyltrichlorosilane which is used in the work-up ( 8th ) can be removed as the bottom product at virtually complete conversion, preferably> 90% and with a purity of about 98%. Furthermore, in the work-up, HCl (g) and excess TCS are generally removed overhead. It is possible to condense TCS and advantageously recycle it as starting material component.

For the preparation of vinyltrichlorosilane or vinylmethyldichlorosilane but can also acetylene with trichlorosilane or methyldichlorosilane at a pressure of ≥ 1 to 4 bar abs., And a temperature of 60 to 180 ° C in the presence of a homogeneous catalyst by the novel process. Suitably acetylene is used in a multiple molar excess. Acetylene is preferably added to trichlorosilane in a molar ratio of 1.5: 1 to 20: 1. The Edukt- and the product mixture are usually two-phase. In the implementation usually ensures a good mixing of the components. Sc can be particularly in capillary reactors cause a particularly advantageous mixing and heat transfer through the so-called Taylor flow. In addition, it can be ensured by the use of a system according to the invention here for an improvement of the mass transfer and the heat transfer. As homogeneous catalysts are advantageously used platinum-containing catalysts which are introduced into the trichlorosilane. In this case, it is advantageous to use a solution of TCS and platinum (IV) chloro acid or hexachloroplatinic acid (H ₂ PtCl ₆ .6H ₂ O) as starting material component. The concentration of the homogeneous catalyst is preferably 1 to 10 ppm by weight, based on the silane component. Also preferred because of their high catalytic activity and high resistance, which means a particularly low consumption of catalyst are homogeneous catalysts as reaction products of platinum (IV) chloro acid with ketones, preferably ketones, which are free of aliphatic multiple bonds, such as cyclohexanone, methyl ethyl ketone acetylacetone and / or acetone phenone, especially cyclohexanone. These reaction products can be prepared, for example, by heating a solution of commercial platinum (IV) chloro acid in the ketone with which this acid is to be reacted for 0.5 to 6 hours at 60 to 120 ° C and in the form of the solution thus obtained Removal of the water formed in the reaction, z. B. with sodium sulfate, are used. To prepare this solution, per part by weight of platinum (IV) chloroacid, preferably 20 to 2,000 parts by volume of ketone are used. However, it is also possible to use other noble metal catalysts dissolved in an inert solvent or a finely dispersed heterogeneous catalyst, for example Pt sludge or Pt on activated carbon. In addition, in addition to the educt components, a substantially inert carrier gas, for example argon or nitrogen, can be used. Furthermore, it is preferred to use a multi-element reactor having a comparatively small structure length, in particular 1 to 100 cm, and a hydraulic diameter of 0.1 to 75 cm ^{2 of} the respective reactor units. The crude product thus obtained is subsequently worked up by distillation, it being possible to recycle the acetylene-containing fraction.

In the process according to the invention, it is likewise possible to react α, β-unsaturated olefins or halogen-substituted olefins advantageously with a hydrogenchlorosilane or a hydrogenalkoxysilane in the presence of a catalyst, as is the case in particular with regard to the starting materials and the particular feedstock and operating parameters EP 0 519 181 B1 . DE 195 34 853 A1 . EP 0 823 434 A1 . EP 1 020 473 A2 . EP 0 714 901 B1 . DE 101 52 284 A1 such as EP 0 838 467 A1 can be seen. Thus, alkylchlorosilanes, haloalkylchlorosilanes, such as chloroalkylchlorosilanes or fluoroalkylchlorosilanes, and also fluoroalkylalkoxysilanes, to name a few, can advantageously be prepared by the process according to the invention.

Consequently is the disclosure of the aforementioned and subsequent intellectual property rights fully attributable to the present application.

It is also possible to prepare aminoalkylalkoxysilanes by hydrosilylation of α, β-unsaturated alkenylamines in the presence of a suitable catalyst by the process according to the invention. For example - but not exclusively - are educt and operating parameters EP 0 709 391 A1 refer to.

Furthermore, advantageously 3-glycidyloxyalkylalkoxysilanes can advantageously be prepared by the process according to the invention by hydrosilylation of allylglycidyl ether in the presence of a catalyst, cf. among others EP 0 934 947 A2 and EP 1 070 721 A2 ,

Likewise, in a surprisingly simple and economical manner, 3-methacryloxyalkylalkoxysilanes can be obtained by the process according to the invention. Thus, the reaction according to the invention of an allyl methacrylate with a hydrogenalkoxysilane in the presence of a homogeneous catalyst and a polymerization inhibition system could also be carried out without the occurrence of the dreaded "popcorn formation." For the implementation, it is possible, for example, but not exclusively, to calculate educt and operating parameters EP 0 707 009 A1 and EP 0 706 081 A2 underlie.

Furthermore, polyether-functional alkoxysilanes can advantageously be obtained by the process according to the invention. For example, starting materials and operating parameters EP 0 387 689 A1 be removed.

In general, the process according to the invention is carried out as follows:
As a rule, the reactant components A and B and optionally C and, if appropriate, further auxiliaries are metered in and mixed. It is endeavored to meter a homogeneous catalyst with an accuracy of ≤ ± 20%, preferably ≤ ± 10%. In special cases, one can dose the homogeneous catalyst in the mixture of the components A and B only shortly before entering the multi-element reactor. Subsequently, it is possible to feed the starting material mixture to the multielement reactor and to react the components under temperature control. However, it is also possible first to rinse or precondition the multielement reactor with a catalyst-containing educt or reactant mixture before the temperature is advanced to carry out the reaction. It is also possible to carry out the preconditioning of the multielement reactor at a slightly elevated temperature. The product streams (crude product) combined in the multielement reactor can subsequently be worked up in a suitable manner in a product work-up of the plant according to the invention.

Thus, one can the process of the invention using a An inventive In an advantageous manner continuously with a product discharge of 10 kg to 50 000 t pa, in particular ≤ 10 000 t pa, operate.

Therefore is also the subject of the present invention the use of a inventive plant for the continuous industrial implementation of a hydrosilylation, where an α, β-unsaturated aliphatic, optionally substituted compound A with an HSi compound B optionally in the presence of a catalyst C and / or further auxiliaries implements.

In particular, but not exclusively, the following special products from the series of organosilanes of the general formula (I) can be prepared particularly advantageously by the process according to the invention:
Vinyl trichlorosilane, 3-chloropropyltrichlorosilane, 3-chloropropylmethyldichlorosilane, propyltrichlorosilane, isobutyltrichlorosilane, octyltrichlorosilane, isooctyltrichlorosilane, Hexedecyltrichlorsilan, hexadecyltrimethoxysilane, hexadecyltriethoxysilane, 3-glycidoxypropyltrimethoxysilane, tridecafluoro-1,1,2,2-tetrahydrooctyltrichlorsilan, tridecafluoro-1,1,2,2- tetrahydrooctyltrimethoxysilane, tridecafluoro-1,1,2,2-tetrahydrooctyltriethoxysilane, 3-methacryloxypropyltrimethoxysilane, 3-aminopropyltrimethoxysilane, 3- (methylpolyethyleneglycol) propyltrimethoxysilane with an average of 10 polyethylene glycol units.

The The present invention is further illustrated by the following examples without to restrict the subject.

Examples

example 1

Preparation of 3- (methylpolyethylene glycol) propyltrimethoxysilane

The propyltrimethoxysilane for the continuous preparation of 3- (methyl polyethylene glycol) (Dynasylan ^® 4140) used system consisted essentially of the reactant reservoir vessels, HPLC pumps, regulating, measuring and dosing units, a T mixer, a prereactor made of stainless steel (diameter 10 mm, length 50 mm), a tube bundle heat exchanger reactor (80 individual tubes, each with a diameter of 2 mm and a length of 300 mm), cf. this too 6 , Temperature control, a pressure-holding valve, a stripping column operated with N ₂ and connecting lines in the system for educt feed, between the above-mentioned system parts as well as product, recycling and flue gas removal. Furthermore, a temperature control over a heating and cooling system was provided for the pre-reactor and the shell-and-tube heat exchanger reactor.

First, at room temperature, the polyetherolefin (ZALP 500, Goldschmidt) and an acetonic, HOAc-containing solution of H ₂ PtCl ₆ (53 g H ₂ PtCl ₆ .6H ₂ O in 11% acetone) in a molar ratio of olefin: Pt = 48 000: 1 and olefin: acetic acid = 1: 0.01 dosed or mixed and mixed in a T-mixer with trimethoxysilane (TMOS, Degussa AG) in a molar ratio of olefin: TMOS = 1: 0.85 and fed to the reactor system. The pressure was 25 ± 10 bar. When starting up the system, the system should be kept as free of H ₂ O as possible. Furthermore, the system was rinsed for 2 hours prior to raising the temperature in the reactor with educt mixture. At a throughput of a total of 1/2 kg / h, the temperature was advanced in the reactors, adjusted to 110 ° C and operated continuously for 18 days. After reactor samples were taken at intervals for GC-WLD measurements. The conversion based on the olefin was on average 96% and the selectivity, based on the α-product, was 75%. The crude product thus obtained was driven continuously into the stripping column and stripped continuously at a jacket temperature of 150 ° C., p = 20 mbar, with N ₂ (volume flow = 150 l / h, T = 150 ° C.). The overhead was condensed and consisted of 85% recyclable TMOS (12% tetramethoxysilane, 3% methanol). Were removed from the sump continuously rounded 0.5 kg / h hydrosilylation (Dynasylan ^® 4140).

Example 2

Preparation of hexadecyltrimethoxysilane

The for the continuous production of hexadecyltrimethoxysilane used Plant consisted mainly of educt reservoirs, HPLC pumps, Control, measuring and Dosing units, a T-mixer, a pre-reactor made of stainless steel (Diameter 5 mm, length 40 mm), a stainless steel capillary (diameter 1 mm, length 50 m), one heat bath with temperature control for the temperature control of the pre-reactor and the capillary, a pressure holding valve, a wiped thin film evaporator and connecting lines in the plant for educt feed between the abovementioned plant components and product, recycling and Evacuation.

First, at room temperature, the olefin hexadecene-1 (purity 93%, Degussa AG) and an acetone solution of H ₂ PtCl ₆ · 6H ₂ O (Speyerkatalysator) in a molar ratio of olefin: Pt = 12 500: 1 metered, mixed and im T-mixer mixed with trimethoxysilane (TMOS, Degussa AG) in a molar ratio of olefin: TMOS = 1: 0.15 and fed to the reactor system. The pressure was 25 ± 10 bar.

When starting up the system, a H ₂ O- as well as O ₂ -free state of the system should be sought. Furthermore, the system was rinsed with educt mixture for 1 hour prior to raising the temperature in the reactor system. At a continuous throughput of a total of ½ kg / h, the temperature was raised in the temperature control and adjusted in the reactor system to 140 ° C and operated continuously for 16 days. After reactor samples were taken at intervals for GC-WLD measurements. The conversion (including rearranged educt) based on the olefin was on average 36% and the selectivity based on TMOS was 99%. The crude product thus obtained was continuously driven into the vacuum-operated thin-film evaporator. The overhead product was condensed, analyzed, post-condensed and recycled. In the bottom continuously around 0.5 kg / h of a mixture of hexadecene and Dynasylan ^® were discharged and 9116 continuously fed to a further separation unit.

Example 3

Preparation of 3-methacryloxypropyltrimethoxysilane

The plant used for the continuous production of 3-methacryloxypropyltrimethoxysilane consisted essentially of the educt reservoirs, HPLC pumps, control, measuring and metering units, a T-mixer, a pre-reactor made of stainless steel (diameter 5 mm, length 40 mm), two parallel switched stainless steel capillaries (each 1 mm in diameter and a length of 25 m), a heat bath with temperature control for the prereactor and the two capillaries, a pressure-holding valve, a stripping column operated with N ₂ and a downstream short-path evaporator and connecting lines in the system for the educt feed, Product, recycling and waste gas removal.

First, at room temperature, the olefin 3-methacryloxypropene-1 (allyl methacrylate, Degussa AG / Röhm) and an acetone solution of H ₂ PtCl ₆ · 6H ₂ O (Speyerkatalysator) in a molar ratio of olefin: Pt = 16 300: 1 metered mixed and in the T-mixer with trimethoxysilane (TMOS, Degussa AG), to which 3.8 g of 2,6-di-tert-butyl-4-methylphenol (Ionol CP, Shell) were added per mole of TMOS, in a molar ratio of olefin TMOS = 1: 1 mixed and fed continuously to the reactor system. The pressure was 25 ± 10 bar. When starting up the system, a H ₂ O and O ₂ -free state of the system should be ensured. Furthermore, the system was rinsed with educt mixture for 1 hour prior to raising the temperature in the reactor system. At a continuous flow rate of ½ kg / h in total, the temperature was raised in the temperature control bath, adjusted to 75 ° C. in the reactor system and operated continuously for 11 days. After the reactor system, samples were taken at intervals on the crude product stream and analyzed by GC-WLP measurements. The conversion based on the olefin was 99% on average and the selectivity based on the α product was 75%. The product stream thus obtained was continuously stripped. The top product was fed to a thermal afterburning and the bottoms product (3-methacryloxypropyltrimethoxysilane) fed continuously with 0.4 kg / h of purification by means of thin-film or short-path evaporator.

Example 4

Preparation of tridecafluoro-1,1,2,2-tetrahydrooctyltrichlorosilane

The equipment used for the production of tridecafluoro-1,1,2,2-tetrahydrooctyltrichlorosilane (Dynasylan ^® 8061) consisting essentially of the reactant reservoir vessels, metering or diaphragm pumps, regulating, measuring and dosing units, a T-mixer, a Edelstahlkapillaren (1 mm diameter, 50 m length), a heat bath with temperature control for prereactor (diameter 5 mm, length 40 mm) and capillary, a pressure relief valve, a continuously operated with N ₂ stripping and in the plant for the feedstock and product -, recycling and flue gas discharge required lines.

First, at room temperature, the olefin 3,3,4,4,5,5,6,6,7,7,8,8,8-tridecafluoroctene-1 (ET 600, Clariant) and Karstedt catalyst [0.01 mol Pt (0) -divinyltetramethyldisiloxane in 100 g of xylene, CPC072, Degussa AG] in a molar ratio of olefin: Pt = 4 500: 1, mixed and mixed in a T-mixer with trichlorosilane (TCS, Degussa AG) in a molar ratio of olefin: TCS = 1: 1.3 mixed and fed continuously to the reactor system. The pressure was 25 ± 10 bar. When starting up the system, a H ₂ O and O ₂ -free state of the system should be ensured. Furthermore, the system was rinsed with the starting material mixture A + C for 2 hours prior to raising the temperature in the reactor system. At a continuous throughput in the sum of about ½ kg / h, the temperature was raised in the bath, set in the reactor system to 110 ° C and operated continuously for 10 days. After the reactor system, samples were taken at intervals from the crude product stream and analyzed by GC-WLP measurements. The conversion, based on TCS, was 99.5% and also the selectivity, based on the target product, was 98.5%. The thus obtained stream of reaction product was fed continuously to a stripping column operated with N ₂ . Resulting top product, in essence TCS, could be recycled. Almost 0.5 kg of hydrosilylation product was withdrawn from the bottom of the stripping column per hour. For example, obtained fluoroalkyltrichlorosilane can be reacted with an alcohol to advantageously obtain fluoroalkylalkoxysilane.

Claims (33)

Plant for the continuous industrial implementation of a reaction, wherein an α, β-unsaturated aliphatic, optionally substituted compound A with an HSi compound B is optionally reacted in the presence of a catalyst C and / or further auxiliaries and the plant at least on the Eduktzusammenführung ( 3 ) for the components A ( 1 ) and B ( 2 ), at least one multi-element reactor ( 5 ), which in turn contains at least two reactor units, and on a product workup ( 8th ). Plant according to claim 1, characterized by one or more multi-element reactors ( 5 ) which include at least 2 to 1,000,000 reactor units. Plant according to claim 1 or 2, characterized by reactor units, wherein the reaction space of at least one reactor unit has a round, oval, square, rectangular or trapezoidal cross-section with a cross-sectional area of 75 microns ² to 75 cm ² . Installation according to one of claims 1 to 3, characterized by reactor units whose respective reaction volume is 0.01 ml to 100 l. Installation according to one of claims 1 to 4, characterized by at least one reactor unit having a structure length of 1 cm up to 200 m. Installation according to one of claims 1 to 5, characterized by at least one multi-element reactor ( 5 ) on at least two parallel connected stainless steel capillaries or on at least two quartz glass capillaries connected in parallel or at least one integrated block reactor ( 5.3 ) or at least one tube bundle heat exchanger reactor ( 5.9 ). Installation according to one of claims 1 to 6, characterized by a multi-element reactor ( 5 ), (i) at least one pre-reactor ( 5.1 ) and at least one further reactor unit or (ii) at least one pre-reactor ( 5.1 ) and at least one integrated block reactor ( 5.3 ) or (iii) at least one pre-reactor ( 5.1 ) and at least one shell and tube heat exchanger reactor ( 5.9 ) includes. Process for the continuous industrial production of an organosilane of the general formula (I) Y-Si (R ') _m (X) _3-m (I), in which Y is an organofunctionality from the group consisting of vinyl, C ₂ - to C ₁₈ -alkyl, C ₃ - to C ₁₆ -fluoroalkyl, C ₃ - to C ₄ -chloroalkyl, aminoalkyl, glycidyloxyalkyl, methacryloxyalkyl, polyetheralkyl and R 'is a C ₁ to C ₄ alkyl group, m is 0 or 1 and X represents a hydrolyzable group, wherein the reaction of the educt components A and B is carried out in at least one multi-element reactor, which in turn is based on at least two reactor units. Method according to claim 8, characterized in that that the reaction is carried out in at least one multi-element reactor whose Reactor units made of stainless steel or its reaction spaces through Stainless steel are limited. A method according to claim 8 or 9, characterized in that one uses reactor units whose respective cross-sectional area is 75 microns ² to 75 cm ² . Method according to one of claims 8 to 10, characterized in that reactor units are used whose respective reaction volume is 0.01 ml to 100 l. Method according to one of claims 8 to 11, characterized that reactor units are used which have a structure length of 5 cm up to 200 m. Method according to one of claims 8 to 12, characterized in that the reaction in a multi-element reactor ( 5 ) carried out on at least one stainless steel capillary or at least one quartz glass capillary or at least one integrated block reactor ( 5.3 ) or at least one tube bundle heat exchanger reactor ( 5.9 ). Method according to one of claims 8 to 13, characterized in that the reaction in a multi-element reactor ( 5 ) carrying at least one pre-reactor ( 5.1 ) includes. Method according to one of claims 8 to 14, characterized that the reactor units of the multi-element reactor before carrying out the Implementation preconditioned. Process according to one of Claims 8 to 15, characterized in that the surface of the reactor units of the multi-element reactor which is in contact with the educt / product mixture is occupied with a catalyst. Method according to one of claims 8 to 16, characterized that is a multielement reactor at a temperature of 0 to 800 ° C and at a pressure of 0.1 to 500 bar abs. operates. Method according to one of claims 8 to 17, characterized in that the reaction at a linear velocity (LV) of 1 to 1 × 10 ⁴ h ^-1 i. N. performs. Method according to one of claims 8 to 18, characterized that is the reaction at a flow rate of 0.0001 up to 1 m / s i.N. performs. Method according to one of claims 8 to 19, characterized in that one carries out the reaction at a ratio of reactor surface to reactor volume (A / V) of 20 to 50 000 m ² / m ³ . Method according to one of claims 8 to 20, characterized that the reaction at a mean residence time of 10 seconds until 60 minutes. Method according to one of claims 8 to 21, characterized in that one carries out the reaction in the gas or liquid phase. Method according to one of claims 8 to 22, characterized that the process with a product output of 5 kg to 50 000 t p. a. operates. Method according to one of claims 8 to 23, characterized that the organosilane of the general formula (I) by a hydrosilylation reaction receives. Process according to one of Claims 8 to 24, characterized in that an unsaturated aliphatic component A from the series acetylene, vinyl chloride, allyl chloride, 3-chloro-2-methylpropene-1, allylamine, 3-glycidyloxypropene-1, 3-methacryloxy-propene 1, propene-1, butene-1, isobutene, vinylcyclohexene-3, octene-1, iso-octene, hexadecene-1, H ₃ C [O- (CH _{2) 2] n} O-CH ₂ CH = CH ₂ with n = 1 to 20, H [O- (CH ₂ ) ₂ ] _n O-CH ₂ CH = CH ₂ with n = 1 to 20, F ₃ C (CF ₂ ) _y -CH = CH ₂ with y = 0 to 9, with a silane (component B) of the general formula (II) HSi (R ') _m X _3-m (II), wherein R 'is a C ₁ to C ₄ alkyl group, m is 0 or 1 and X is a hydrolyzable group. Method according to one of claims 8 to 25, characterized that the reaction is carried out in the presence of a catalyst C. Method according to one of claims 8 to 26, characterized that the reactant components A and B and optionally C are metered in and mixes, then supplying a defined volume flow of the educt mixture to the multi-element reactor and implements. Method according to one of claims 8 to 27, characterized that the components A and B in a molar ratio of 1 to 5 to 100 to 1. Method according to one of claims 8 to 28, characterized that the homogeneous catalyst in a molar ratio to Component A of 1 to 2 000 000 to 1 to 1 000 sets. Method according to one of claims 8 to 29, characterized that one doses the homogeneous catalyst with an accuracy of ≤ ± 20%. Method according to one of claims 8 to 30, characterized that the homogeneous catalyst in the mixture of the components A and B are metered just before entering the multi-element reactor. Method according to one of claims 8 to 31, characterized that one the product streams of the multi-element reactor and then worked up. Use of a plant according to one of claims 1 to 7 for the continuous industrial implementation of a hydrosilylation, where an α, β-unsaturated aliphatic, optionally substituted compound A with an HSi compound B optionally in the presence of a catalyst C and / or further auxiliaries according to one of the claims 8 to 32 implements.