EP2049243A1

EP2049243A1 - System and process for continuous industrial preparation of organosilanes

Info

Publication number: EP2049243A1
Application number: EP07787231A
Authority: EP
Inventors: Jürgen Erwin LANG; Georg Markowz; Harald Metz; Norbert Schladerbeck; Dietmar Wewers
Original assignee: Evonik Degussa GmbH
Current assignee: Evonik Operations GmbH
Priority date: 2006-08-10
Filing date: 2007-07-09
Publication date: 2009-04-22
Also published as: CN101362775A; WO2008017555A1; DE102007023757A1; CN101362775B

Abstract

The present invention relates to a system for continuous industrial performance of a reaction wherein an a,ß-unsaturated aliphatic, optionally substituted compound A is reacted with an HSi compound B, optionally in the presence of a catalyst C and/or of further assistants, and the system is based at least on the combination of reactants (3) for components A (1) and B (2), at least one multielement reactor (5) which, in turn, comprises at least two reactor units, and on a product workup (8). The invention further relates to the use of a system for continuous industrial performance of a hydrosilylation, wherein an a,ß-unsaturated aliphatic, optionally substituted compound A is reacted with an HSi compound B, optionally in the presence of a catalyst C.

Description

Plant and process for continuous industrial production of orqanosilanes

The present invention relates to a novel plant for the continuous industrial production of organosilanes by reacting an α, ß-unsaturated aliphatic, optionally substituted compound with a HSi compound and a related method.

Organosilanes, such as vinylchloro or 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), and many more, are of great industrial 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, a starting material is often used in a semi-batch mode submitted together with the catalyst and the other reactant added. 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 u. a. 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 object was to provide a further possibility for the industrial production of said organosilanes. In particular, there was a concern to provide a further possibility for the continuous production of such organosilanes, while endeavoring to minimize the disadvantages mentioned above.

The stated object is achieved according to the information in the claims.

Thus, it has surprisingly been found that a hydrosilylation or the reaction of an HSi-containing component with another gaseous or liquid α, ß-unsaturated compound in a simple and economical manner in an industrial scale continuously in a plant, which on a Multi-element reactor based, can perform advantageous.

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. Thus, in the present invention, a 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 carried out by the continuous driving under pressure Reactions a longer service life of metal reactors are found because 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 process 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, wherein an α, ß-unsaturated aliphatic, optionally substituted compound A 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 is based at least on the starting material combination (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 based on a subsequent product work-up (8).

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

Thus, FIG. 1 shows a preferred continuous system in which the reactant components A and B are combined in unit (3), fed to unit (5), which may contain an immobilized catalyst, reacted therein and the reaction product in the unit (8) is worked up.

FIG. 2 shows a further preferred embodiment of a continuous plant according to the invention, in which a catalyst C is fed to component B. However, the catalyst can also be fed to the unit (3) or, as can be seen in FIG. 3, the catalyst C metered into a mixture of the components A and B shortly before entry into the multi-reactor unit (5).

Furthermore, it is possible to add further auxiliaries optionally to the respective streams mentioned above.

In this case, a reactor unit is understood as meaning an element of the multielement reactor (5), each element representing an area or reaction space for the said reaction, cf. for example, (5.1) (reactor unit in the form of a pre-reactor) in Figure 4 and (5.5) [reactor unit of an integrated block reactor (5.3)] in Figure 5 and (5.10) [reactor unit of a Mikrorohrbündelwärmetauscherreaktors (5.9)]. Ie. Reactor units of a multielement reactor (5) in the context of the present invention are in particular stainless steel or quartz glass capillaries, stainless steel tubes or well-dimensioned stainless steel reactors, for example pre-reactors (5.1), tubes (5.10) in microtube bundle heat exchanger reactors [e.g. B. (5.9)] and converted areas (5.5) in the form of integrated block reactors [z. 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 only 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. Such a cross section preferably has a cross-sectional area of 75 μm 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 this case, reactor units with differently shaped cross-sectional areas can be present in a multielement reactor (5) of a system according to the invention.

Further, the structure length in a reactor unit, i. H. 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) or (5.5.2), preferably 5 cm to 500 m, including all numerically intervening numerical values, particularly preferably> 15 cm to 100 m, very particularly preferably 20 cm to 50 m, in particular 25 cm to 30 m.

In a plant according to the invention, preference is given to reactor units whose respective reaction volume (also referred to as the reactor volume, ie the product of Cross-sectional area and structure length) 0.01 ml to 100 l, including all numerically intervening numerical values. The reactor volume of a reactor unit of a system according to the invention is particularly preferably 0.05 ml to 10 l, very particularly preferably 1 ml to 5 l, very particularly preferably 3 ml to 2 l, in particular 5 ml to 500 ml.

Furthermore, systems according to the invention can be based on one or more multi-element reactors (5), which are preferably connected in parallel. However, said multi-element reactors (5) can also be switched one behind the other so that the product which originates from the preceding multi-element reactor can be fed to the inlet of the subsequent multi-element reactor.

Present multielement reactors (5) can advantageously be combined with a reactant component stream (4) or (5.2), which is suitably divided into the respective sub-streams, cf. z. B. (5.4) in Figure 5 and (5.11) in Figure 6, are fed. After the reaction, the product streams can be combined, cf. z. B. (5.7) in Figure 5, (5.12) in Figure 6 and (7), and then work up advantageously in a workup unit (8). In this case, such a processing unit (8) initially have a condensation stage or evaporation stage, which optionally followed by one or more distillation stages.

Furthermore, a multielement reactor (5) of a system according to the invention can be based on at least two stainless steel capillaries connected in parallel or on at least two quartz glass capillaries connected in parallel or at least one tube bundle heat exchanger reactor (5.9) or at least one integrated block reactor (5.3).

In this case, one can use stainless steel capillaries or reactors, which advantageously consist of a high-strength, high-temperature-resistant and stainless steel, For example, but not exclusively, such capillaries, block reactors or tube bundle heat exchangers of steel type 1.4571 or 1.4462, see. 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 generally available commercially.

Also, a multi-element reactor (5) may include a shell and tube heat exchanger reactor, which may optionally also be temperature-controlled in countercurrent. Thus, there is a so-called, preferably micro-structured tube bundle heat exchanger reactor used according to the invention, ie micro tube bundle heat exchanger reactor, cf. For example, (5.9) in Figure 6, suitably from a tube bundle (5.10), wherein the respective tubes (5.10) preferably have the above dimensions are the same, especially in terms of length and diameter, and made of a stainless steel. The inlet planes of the respective tubes (5.10) are oriented in one plane and have a common educt feed (4), (5.11) and a common product removal or combination (5.12), (7). In addition, the tube bundle (5.10) can be lapped by a medium (D) for tempering (5.13). Preferably, the tube bundle is flushed against the flow direction with tempering medium (D, 6.1, 6.2). In this case, such a system can be introduced into a reactor jacket (5.14), the latter advantageously having an educt feed (4), a product removal (7), a temperature-control agent supply (6.1) and a temperature-control agent removal (6.2). Preference is given to switching a microtube bundle heat exchanger reactor (5.9), cf. FIG. 6, at least one pre-reactor (5.1), cf. also Figure 4, above. Furthermore, it is possible to use as a multielement reactor (5) advantageously an integrated block reactor, as used, for example, as a temperature-controllable block reactor constructed from defined metal plates (also referred to as plane below) from http://www.heatric.com/pche-construction.html is apparent.

The production of said structured metal plates or planes, from which a block reactor can then be produced, can take place, for example, by etching, turning, cutting, milling, embossing, rolling, spark erosion, laser processing, plasma technology or another technique of the processing methods known per se. Thus, with the utmost precision well-defined and selectively arranged structures, such as grooves or joints, on one side of a metal plate, in particular a metal plate made of stainless steel, incorporated. In this case, the respective grooves or joints start on a front side of the metal plate, are continuous and usually end on the opposite end face of the metal plate.

Thus, FIG. 5 shows a plane of an integrated block reactor (5.3) with a plurality of reactor units or elements (5.5). In this case, such a level usually consists of a base plate made of metal with metal walls thereon (5.6), the reaction chambers (5.5) together with a cover plate made of metal and a unit for temperature control (6.5, 6.6), preferably a further level or textured metal plate, limit. Furthermore, the unit (5.3) contains an area (5.4) for feeding and distributing the educt mixture (5.2) into the reactor elements (5.5) and a region (5.7) for combining the product streams from the reaction areas (5.5) and discharging the product stream (7). , In addition, in the context of an integrated block reactor (5.3), several such previously described levels can 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.imm- mainz.de/seiten/de/u_050527115034_2679.php?PHPSESSID=75a6285eb0433122b9c ecaca3092dadb. Furthermore, such integrated block reactors (5.3) are advantageously surrounded by a temperature control unit (6.5, 6.6) which enables the heating or cooling of the block reactor (5.3), ie a targeted temperature control. For this purpose, a medium (D), z. B. Marlotherm or Mediatherm, by means of a heat exchanger (6.7) tempered and fed via line (6.8) a pump (6.9) and line (6.1) of the temperature control unit (6.5) and via (6.6) and (6.2) removed and the heat exchanger unit (6.7 ). In this case, it is possible to optimally control the heat of reaction released in an integrated block reactor (5.3) by the shortest route, thereby avoiding temperature peaks which adversely affect a targeted reaction. However, the integrated block reactor (5.3) and the associated temperature control unit (6.5, 6.6) can also be designed such that a temperature control plane is arranged between two reactor element planes, which guides the temperature control medium even more directionally 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) comprising at least one pre-reactor (5.1) and at least one further reactor unit, for example a stainless steel capillary, or a pre-reactor (5.1) and at least one integrated block reactor (5.3), cf. FIG. 4, or at least one pre-reactor (5.1) and a shell-and-tube heat exchanger reactor (5.9), cf. Figure 6, includes. Furthermore, the prereactor (5.1) is suitably tempered, d. H. cooled and / or heated, off (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 in addition to carrying out the continuous reaction by a targeted Separation and discharge of hydrolyzates or particles unscheduled Stillbzw. Can advantageously minimize downtime. So you can pre-reactor (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 Eduktzusammenführung (3) for the components A and B, at least one said multi-element reactor (5) and on a product work-up (8), cf. FIG. 1

In this case, the educt components A and B can each be combined in a targeted manner from a storage unit by means of pumps and optionally by means of differential weighing system in the area (3). As a rule, components A and B are metered at ambient temperature, preferably at 10 to 40 ^° C., and mixed in region (3). 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), it is possible to continuously feed the educt mixture to the multielement reactor (5).

In this case, the multielement reactor (5) is preferably brought to or maintained at the desired operating temperature by means of a temperature control medium D (6.1, 6.2) so that undesirable temperature peaks and temperature fluctuations known from batch systems are advantageously avoided or adequately achieved in the present system according to the invention can become low.

The product or crude product stream (7) is continuously the product work-up (8), for example, a rectification, fed, for example, about Head (10) a low-boiling product F, for example, an excessively used and optimally recyclable silane, and on the bottom (9) a heavy boiling product E can continuously decrease. It is also possible to remove side streams as a product from the unit (8).

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, advantageously 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 preferably 10 to 10 ^{~ 4} mm ² , very particularly preferably 1 to 10 ³ mm ² , so that there is no blockage advantageous, but still can be easily separated from the product stream in a downstream arrangement.

Thus, FIG. 2 reveals that it is advantageous to meter in a said catalyst C to component B before it is combined with component A in region (3).

It is possible to meter in a homogeneous catalyst C or a suspension catalyst C but also a mixture of A and B which is conducted in line (4), preferably just before entry into the multielement reactor via a line (2.2), cf. FIG. 3.

In the same way as in the case of a homogeneous catalyst, it is also possible to add further, predominantly liquid auxiliaries, for example but not exclusively, activators, initiators, stabilizers, inhibitors, solvents or diluents to the reactant components A and B, etc. But you can also choose a multi-element reactor (5), which is equipped with an immobilized catalyst C, see. FIG. 1. In this case, the catalyst C can be present, for example-but not exclusively-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 work-up (8). 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, control units and exhaust gas 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.

Another particularly noteworthy advantage of a plant according to the invention for the continuous industrial implementation of a reaction of α, ß-unsaturated compounds A with a HSi compound B is that it now has a Possibility to produce even small special products with sales volumes between 5 kg and 50 000 t pa, preferably 10 kg to 10 000 t pa, in a simple and economical way continuously and flexibly. In this case, unnecessary downtime, the yield, the selectivity influencing temperature peaks and fluctuations and too long residence times and thus unwanted side reactions can be advantageously avoided. In particular, such an installation can also be used optimally for the production of existing silanes from an economical, ecological and customer-friendly point of view.

Thus, the subject of the present invention is 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 ₈ -alkyl, C ₃ - to C ₆ -fluoroalkyl, C ₃ - to C ₄ -chloroalkyl, aminoalkyl, glycidyloxyalkyl, methacryloxyalkyl, polyetheralkyl and R 'for a d -C ₄ -alkyl group, m is 0 or 1 and X represents 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.

Preferably, the reaction is carried out in at least one multi-element reactor (5), the 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, the surfaces of the reactor units may be coated or occupied , for example with Teflon. Furthermore, in the case of processes according to the invention, preference is given to using reactor units whose respective cross-section is semicircular, semi-oval, 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 .

Furthermore, preference is given to using those reactor units which have a structure length of 1 cm to 200 m, particularly preferably 10 cm to 120 m, very particularly preferably 15 cm to 80 m, in particular 18 cm to 30 m, including all possible numerical values Be included above areas.

Thus, in the process according to the invention, reactor units are suitably used whose respective reaction volume is 0.01 ml to 100 l including all numerically intermediate numerical values, preferably 0.1 ml to 50 l, particularly preferably 1 ml to 20 l, very particularly preferably 2 ml to 10 1, in particular 5 ml to 5 1.

In the process according to the invention, the said reaction can also advantageously be carried out in a plant with a multi-element reactor (5) which is based 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 multi-element reactor (5) which contains at least one pre-reactor (5.1) is preferred. The process according to the invention is particularly preferably carried out in reactor units made of stainless steel. It is further preferred that in the process according to the invention, the surface of the reactor units of the multielement reactor which is in contact with the starting material / product mixture is coated with a catalyst, in particular when working in the presence of an immobilized catalyst or heterogeneous catalyst.

If, in the context of the process according to the invention, the reaction of components A and B is carried out in the presence of a homogeneous catalyst C, it has surprisingly been found that it is particularly advantageous to pass the multielement reactor through one or more rinses with a mixture of homogeneous catalyst C and component B or Homogeneous catalyst C and components A and B or a short-term operation of the plant, for example, for 10 to 120 minutes and optionally with a higher catalyst concentration, precondition.

The substances used for the preconditioning of the multielement reactor can be collected and later metered into the educt stream at least proportionally or fed directly to the product work-up and worked up.

By the above-described preconditioning of the multi-element reactor, especially if it consists of stainless steel, one can achieve a constant operating state with maximum yield in a surprising and advantageous manner more quickly.

In the process according to the invention, it is possible to carry out the said reaction in the gas and / or liquid phase. The reaction or product mixture can be present in one, two or three phases. In the process according to the invention, the reaction is preferably carried out in a single-phase, in particular in the liquid phase. Thus, the process of the invention is advantageously carried out using a multielement reactor at a temperature of 0 to 800 ⁰ C at a pressure of 0.1 to 500 bar abs. Preference is given to the reaction of components A and B, in particular a hydrosilylation, in the multi-element reactor at a temperature of 50 to 200 ⁰ C, preferably at 60 to 180 ⁰ C, and at a pressure of 0.5 to 300 bar abs., preferably at 1 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, d. H. between Eduktzusammenführung (3) and product work-up (8), 1 to 10 bar abs. Advantageously, one can equip a system according to the invention with a pressure-holding valve, in particular when using trimethoxysilane (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 according to the invention analogously to the space velocity at a linear velocity (LV) of 1 to 1 ^■ 10 ⁴ h ^'1 i. N. perform. In this case, the flow velocity of the material stream is situated in the reactor units preferably in the range of 0.0001 to 1 m / s iN, more preferably 0.0005 to 0.7 m / s, most preferably 0.001 to 0.5 m / s, in particular 0.05 to 0.3 m / s, and all possible numerical values within the above If the ratio of reactor surface area (A) to reactor volume (V) is predominant in the reaction according to the invention, then an AV ratio of 20 to 5,000 m ² / m ^{3 is} preferred, including all numerically possible individual values The AV ratio is a measure of the heat transfer and of possible heterogeneous (wall) influences. Thus, the reaction in the process according to the invention is advantageously carried out at a mean residence time (.tau.) Of 10 seconds to 60 minutes, preferably 1 to 30 minutes, more preferably 2 to 20 minutes, in particular 3 to 10 minutes. Here again, all possible numerical values disclosed by the named area are referred to separately.

As component A, the following α, β-unsaturated compounds can be used in the process according to the invention, for example: 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 ], vinyl cyclohexene-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, 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 ) _V- 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-tridecafluoro-octene-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.

Thus, according to the invention, preference is given to trichlorosilane (TCS), methyldichlorosilane, Dimethylchlorosilane, trimethoxysilane (TMOS), triethoxysilane (TEOS), methyldimethoxysilane or methyldiethoxysilane.

In the process according to the invention, components A and B are preferably employed in a molar ratio A to B of 1: 5 to 100: 1, more preferably 1: 4 to 5: 1, very preferably 1: 2 to 2: 1, in particular of 1: 1, 5 to 1, 5: 1, including all possible numbers within the aforementioned ranges.

The process according to the invention is preferably carried out in the presence of a catalyst C. However, it is also possible to operate the process according to the invention without the addition of a catalyst, in which case a clear decrease in the yield is generally to be expected.

In particular, the process according to the invention is used for carrying out a hydrosilylation reaction for the preparation of organosilanes of the formula (I), in particular homogeneous catalysts of 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] and 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 or noble metals or corresponding multielement catalysts.

In this case, the known complex catalysts 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 , to solve.

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.

In addition, the addition of an organic or inorganic acid to the reaction mixture can take on another advantageous function, for example as a stabilizer or inhibitor of impurities in the trace range.

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

If a homogeneous catalyst or a suspension catalyst is used in the process according to the invention, 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 1,000,000: 1 up to 4 000: 1, in particular from 500 000: 1 to 10 000: 1, and all possible figures within the abovementioned 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. So you can, for example - but not exclusively - also heterogeneous catalysts that bring on a carrier such as beads, strands, pellets, cylinders, stirrers, etc., inter alia _SiO2, _TiO2, Al2O3, _ZrO2, in the reaction zone of the reactor units.

Examples of integrated fixed bed catalyst block reactors are available at http://www.heatric.com/iqs/sid.0833095090382426307150/mab_reactors. html to take.

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

Furthermore, solvents or diluents, such as alcohols, aliphatic and aromatic hydrocarbons, CHC, CFC, ethers, esters, ketones - to name a few - can be used as auxiliaries. Such adjuvants can be removed from the product, for example, in the product work-up.

Likewise, inhibitors, for example polymerization inhibitors or corresponding mixtures, can be used as additional auxiliaries in the present process.

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 ⁰ 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 multielement reactor which is operated on a temperature-controllable prereactor and a downstream heatable, integrated block reactor or prereactor and based at least one downstream stainless steel capillary. The prereactor is preferably operated at 200 to 450 ⁰ C and 1 to 10 bar abs. and the pre-reactor downstream reactor units preferably at 450 to 650 ⁰ 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, vinyltrichlorosilane is advantageously obtained which can be removed in work-up (8) as 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 passed 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 be acetylene with trichlorosilane or methyldichlorosilane at a pressure of> 1 to 4 bar abs., And a temperature of 60 to 180 ⁰ 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. Thus, particularly in capillary reactors, it is possible to effect a particularly advantageous mixing and heat transfer by 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 PtCIe ^■ 6H ₂ O) as a starting 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 ⁰ 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 described with regard to the starting materials and the particular feedstock and operating parameters, in particular 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 and EP 0 838 467 A1 can be found. Thus, alkylchlorosilanes, haloalkylchlorosilanes, such as chloroalkylchlorosilanes or fluoroalkylchlorosilanes, and fluoroalkylalkoxysilanes, to name but a few, can be prepared by the process according to the invention in an advantageous manner.

Thus, the disclosure of the aforementioned and subsequent intellectual property rights is to be fully attributed 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, educt and operating parameters EP 0 709 391 A1 can be found.

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. u. a. 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 system for inhibiting polymerization could also be carried out without the occurrence of the dreaded "popcorn formation." For the implementation, it is possible to use, for example but not exclusively, educt and operating parameters from EP 0 707 009 A1 and EP 0 706 081 A2.

Furthermore, polyether-functional alkoxysilanes can advantageously be obtained by the process according to the invention. Starting materials and operating parameters can be found, for example, in EP 0 387 689 A1. 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, the process of the invention using an inventive system in an advantageous manner continuously with a product output of 10 kg to 50 000 t p. a., In particular <10 000 t p. a., operate.

Therefore, the present invention also relates to the use of a plant according to the invention for the continuous industrial implementation of hydrosilylation, wherein an α, ß-unsaturated aliphatic, optionally substituted compound A with an HSi compound B optionally in the presence of a catalyst C and / or other auxiliaries implements.

In particular - but not exclusively - one can according to the invention Process the following special products from the series of organosilanes of general formula (I) produce particularly advantageous:

Vinyl trichlorosilane, 3-chloropropyltrichlorosilane, 3-chloropropylmethyldichlorosilane, Propyltri- chlorosilane, isobutyltrichlorosilane, octyltrichlorosilane, isooctyltrichlorosilane, Hexedecyltri- chlorosilane, hexadecyltrimethoxysilane, hexadecyltriethoxysilane, 3-Glycidyloxypropyltri- trimethoxysilane, 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 present invention will be further illustrated by the following examples without limiting the subject matter.

Examples

example 1

Preparation of 3- (methylpolyethylene glycol) propyltrimethoxysilane

The for the continuous preparation of 3- (methyl polyethylene glycol) propyltrimethoxy- silane (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. also FIG. 6, temperature control, a pressure-maintaining valve, a stripping column operated with N ₂ and connecting lines in the system for reactant feed, between the abovementioned plant sections and product, recycling and waste 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. The polyetherolefin (ZALP 500, Goldschmidt) and an acetonic, HOAc-containing solution of H ₂ PtCl ₆ (53 g of H ₂ PtCl ₆ .6H ₂ O in 1 l of acetone) were initially stirred at room temperature in a molar ratio of olefin: Pt = 48,000: 1 and olefin: acetic acid = 1: 0.01 dosed or mixed and mixed in the 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, set to 110 ⁰ C and operated continuously over 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 continuously into the stripping column and at a jacket temperature of 150 ^0, p = (= 150 ⁰ C Volume flow = 150 l / h, T) stripped 20 mbar, with N ₂ continuously 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 plant used for the continuous production of hexadecyltrimethoxysilane 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), a stainless steel capillary ( Diameter 1 mm, length 50 m), a heat bath with temperature control for the temperature control of the pre-reactor and the capillary, a pressure-maintaining valve, a wiped Thin-film evaporator and connecting lines in the system for reactant feed between the abovementioned plant components as well as product, recycling and flue-gas removal.

First, at room temperature, the olefin hexadecene-1 (purity 93%, Degussa AG) and an acetone solution of H ₂ PtCl ₆ - OH 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 flow rate of total Vz kg / h, the temperature was raised in the bath and set in the reactor system to 140 ⁰ 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 Stainless steel (diameter 5 mm, length 40 mm), two parallel connected 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 N ₂ operated stripping and a downstream short-path evaporator and connecting lines in the system for the educt feed, product, recycling and flue 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 - OH 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 per mole of TMOS of 2,6-di-tert-butyl-4-methylphenol (Ionol CP, Shell) were added, 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 throughput of a total of Vz kg / h, the temperature was raised in the bath, adjusted in the reactor system to 75 ⁰ C 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 (O) -divinyltetramethyldisiloxane in 100 g of XyIoI, 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 Vz kg / h, the temperature was raised in the bath, set in the reactor system to 110 ⁰ 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 . The resulting top product, essentially TCS, could be used as recycling. Almost 0.5 kg of hydrosilylation product was withdrawn from the bottom of the stripping column per hour. For example, fluoroalkyltrichlorosilane obtained can be reacted with an alcohol be reacted to obtain so advantageous fluoroalkylalkoxysilane.

Claims

claims:

1. plant for the continuous industrial implementation of a reaction, wherein an α, ß-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 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 based on a product work-up (8).

2. 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.

3. 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 .

4. Plant according to one of claims 1 to 3, characterized by

Reactor units whose respective reaction volume is 0.01 ml to 100 l.

5. Plant according to one of claims 1 to 4, characterized by at least one reactor unit having a structure length 1 cm to 200 m.

6. Installation according to one of claims 1 to 5, characterized by at least one multi-element reactor (5) based 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 shell-and-tube heat exchanger reactor (5.9).

7. Plant according to one of claims 1 to 6, characterized by a multi-element reactor (5), the (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).

8. Process for the continuous industrial production of an organosilane of the general formula (I)

Y-Si (R ') _m (X) ₃ _-m (I),

where Y is an organo-functionality from the series vinyl, C ₂ - to cis-alkyl,

C ₃ - to C ₆ fluoroalkyl, C ₃ - to C ₄ chloroalkyl, aminoalkyl, glycidyloxyalkyl, methacryloxyalkyl, Polyetheralkyl and R 'is a C to C ₄ alkyl group, and m is 0 or 1, X is a hydrolyzable group represents,

wherein the reaction of the educt components A and B in at least one

Multielementreaktor performs, which in turn is based on at least two reactor units.

9. The method according to claim 8, characterized in that one carries out the reaction in at least one multi-element reactor whose reactor units are made of stainless steel or whose reaction spaces are limited by stainless steel.

10. The 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 .

11. The method according to any one of claims 8 to 10, characterized in that one uses reactor units whose respective reaction volume is 0.01 ml to 100 l.

12. The method according to any one of claims 8 to 11, characterized in that one uses reactor units having a structure length of 5 cm to 200 m.

13. The method according to any one of claims 8 to 12, characterized in that one carries out the reaction in a multi-element reactor (5) 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

Shell-and-tube heat exchanger reactor (5.9) based.

14. The method according to any one of claims 8 to 13, characterized in that the reaction is carried out in a multi-element reactor (5) which contains at least one pre-reactor (5.1).

15. The method according to any one of claims 8 to 14, characterized in that preconditioning the reactor units of the multi-element reactor before carrying out the reaction.

16. The method according to any one of claims 8 to 15, characterized in that the standing in contact with the reactant / product mixture surface of the reactor units of the multi-element reactor is coated with a catalyst.

17. The method according to any one of claims 8 to 16, characterized in that a multielement reactor at a temperature of 0 to 800 ⁰ C and at a pressure of 0.1 to 500 bar abs. operates.

18. The method according to any one of claims 8 to 17, characterized in that one carries out the reaction at a linear velocity (LV) of 1 to 1x10 ⁴ h ^"1 i. N.

19. The method according to any one of claims 8 to 18, characterized in that the reaction at a flow rate of 0.0001 to 1 m / s i.N. performs.

20. The method according to any 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 mVm ³ .

21. The method according to any one of claims 8 to 20, characterized in that one carries out the reaction at an average residence time of 10 seconds to 60 minutes.

22. The method according to any one of claims 8 to 21, characterized in that one carries out the reaction in the gas or liquid phase.

23. The method according to any one of claims 8 to 22, characterized in that the method with a product output of 5 kg to 50 000 t p. a. operates.

24. The method according to any one of claims 8 to 23, characterized in that one obtains the organosilane of the general formula (I) by a hydrosilylation tion reaction.

25. The method according to any one of claims 8 to 24, characterized in that one comprises an unsaturated aliphatic component A from the series acetylene, vinyl chloride, allyl chloride, 3-chloro-2-methylpropene-1, allylamine, 3-glycidyloxypropene-1, 3-methacryloxypropene-1, propene-1, butene-1, isobutene, vinylcyclohexene-3, octene-1, isooctene, hexadecene-1, H ₃ C [O- (CH ₂ ) 2] nO-CH ₂ CH = CH ₂ with n = 1 to 20, H [O- (CH ₂ ) 2] nO-CH ₂ CH = CH ₂ with n = 1 to 20, F ₃ C (CF ₂ VCH = CH ₂ with y = 0 to 9, with a silane (component B) of 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,

implements.

26. The method according to any one of claims 8 to 25, characterized in that one carries out the reaction in the presence of a catalyst C.

27. The method according to any one of claims 8 to 26, characterized in that the reactant components A and B and optionally C is metered and mixed, then a defined volume flow of the educt mixture the

Multielementreaktor feeds and converts.

28. The method according to any one of claims 8 to 27, characterized in that one uses the components A and B in a molar ratio of 1 to 5 to 100 to 1.

29. The method according to any one of claims 8 to 28, characterized in that one uses the homogeneous catalyst in a molar ratio to the component A of 1 to 2,000,000 to 1 to 1,000.

30. The method according to any one of claims 8 to 29, characterized in that one doses the homogeneous catalyst with an accuracy of <± 20%.

31. The method according to any one of claims 8 to 30, characterized in that one doses the homogeneous catalyst in the mixture of the components A and B shortly before entering the multi-element reactor.

32. The method according to any one of claims 8 to 31, characterized in that one brings together the product streams of the multi-element reactor and worked up subsequently.

33. Use of a system according to any one of claims 1 to 7 for the continuous industrial implementation of a hydrosilylation, wherein an α, ß-unsaturated aliphatic, optionally substituted compound A with an HSi compound B optionally in the presence of a catalyst C and / or other auxiliaries according to any one of claims 8 to 32.