MXPA00012550A

MXPA00012550A - TAYLOR REACTOR FOR MATERIALS CONVERSION IN THE COURSE OF WHICH A CHANGE IN VISCOSITY&ngr;OF THE REACTION MEDIUM OCCURS

Info

Publication number: MXPA00012550A
Application number: MXPA/A/2000/012550A
Authority: MX
Inventors: Heinzpeter Rink; Hansulrich Moritz; Sabine Kossak; Jessica Langenbuch; Werner Alfons Jung
Original assignee: Basf Coatings Ag
Priority date: 1998-06-27
Filing date: 2000-12-15
Publication date: 2002-07-25

Abstract

The invention relates to a Taylor reactor for materials conversion, comprising an outer reactor wall (1) and a rotor (2) concentrically or eccentrically arranged therein, a reactor bottom (3), a reactor lid (4) defining together the annular gap-shaped reactor volume (5), at least one device (6) for dosing educts, in addition to a device (7) for product evacuation, wherein a change in viscosity&ngr;of the reaction medium occurs during materials conversion and the rector wall (1) and/or rotor (2) are geometrically embodied in such a way that conditions for Taylor vortex flow are fulfilled in the reactor volume substantially in the entire reactor facility.

Description

TAYLOR REACTOR FOR CONVERSIONS THAT INCLUDE A CHANGE IN VISCOSITY V OF THE MEANS OF REACTION The present invention relates to a novel Taylor reactor for physical and / or chemical conversions, in the course of which there is a change in the viscosity v of the reaction medium. The present invention also concerns a novel process for conversion that is accompanied by a change in viscosity of the reaction medium under the conditions of Taylor vortex flow. The invention also deals with substances produced using the novel process in the new Taylor reactor, and its use. The Taylor reactors, which serve to convert substances under the conditions of the Taylor vortex flow, are known. These consist essentially of two coaxial concentric cylinders, of which the exterior is fixed, while the interior rotates. The reaction space is the volume formed by the gap between the cylinders. The increase in the angular velocity? - of the inner cylinder is accompanied by a series of different flow patterns that are characterized by dimensionless parameters, known as the Taylor Ta number. As well as the angular velocity of the agitator, the Taylor number also depends on the kinematic viscosity v of the fluid in the gap and on the ^ ^^^^^^ g ^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^ ^^^^^^^ g ^^^^^^^^^^^^^^^^^^^^^^ - ^^^^^^^^^^^^^^ r ^^ * ^ ^^^^^^^^^^^^^^^ geometric parameters. The outer radius of the inner cylinder rlf the internal radii of the outer cylinder r0 and the width of the gap d, the difference between the two radii, according to the following formula: Ta =? - r- d v_1 (d / r?) 1/2 (I) where d = r0 - r-. At low angular viscosity, the Laminar Couette flow is developed, a simple shear stress flow. If the rotation speed of the inner cylinder increases more, then alternately counterrotating vortices are produced above the critical level (which rotate in the opposite direction), with axes along the peripheral direction. These vortexes, called Taylor vortices, are rotationally symmetric, have the geometric shape of a bull (vortex Taylor ring), and have a diameter that is approximately the same size as the hole width. The adjacent vortices form a pair of vortices or a vortex cell. The basis of this behavior is the fact that, in the course of the rotation of the inner cylinder with the outer cylinder at rest, the liquid particles that are close to the inner cylinder are subjected to a higher centrifugal force than those at a greater distance from the cylinder. inner cylinder. This difference in active centrifugal forces displaces the liquid particles from the inner cylinder to the outer cylinder. The centrifugal force acts in the opposite direction to the force of the viscosity, due to the movement of the liquid particles, it is necessary to overcome the friction. If there is an increase in the rotating speed, there is also an increase in centrifugal force. Taylor vortices are formed when the centrifugal force exceeds the stabilizing force of the viscosity. If the Taylor reactor has an inlet and an outlet, and operates continuously, the result is a Taylor vortex flow with a low axial flow. Each pair of vortices passes through the gap, with only a lower level of mass transfer between pairs of adjacent vortices. The mixture within said pairs of vortices is very high, since the axial mixture beyond the limits of the torque is very low. A pair of vortices can therefore be considered a stirred bucket, where the mixing is carried out completely. Consequently, the flow system behaves like an ideal flow tube, in which pairs of vortices pass through the gap with time of -t * a constant stay, like ideal hectic buckets. Taylor reactors, known to date, can be used for polymerization of emulsions. In this context, reference is made by way of example to DE-B-1 241 and EP-A-0 498 583, or to K. Kataoka's article in Chemical Engineering Science 50 (1995) 9, 1409 to 1416. These are also suitable for electrochemical processes, in which case the cylinders function as electrodes. In this context reference is made to the articles by S. Cohén D.M. Maron in Chemical Engineering Journal 27 (1983) 2, 87 to 97, and Couret and Legrand in Electrochimia Acta 26 (1981) 7, 865 to 872, and 28 (1983) 5, 611 to 617. It is also known to use Taylor reactors as photochemical reactors, where the light source is located in the inner cylinder (see in this respect the articles by Szechowski in Chemical Engineering Science 50 (1995) 20, 3163 to 3173, by Haim and Pismen in Chemical Engineering Science 49 (1994) 8, 1119 to 1129, and by Karpel Vel Leitner in Water Science and Technology 35 (1997) 4, 215-222). Its use as bioreactors (see in this respect the article by Huang and Liu in Water Science and Technology 28 (1994) 7, 153 to 158) or as flocculation reactors for purification of wastewater (cf. in this respect the article by Grohmann in BMFT-FB-T 85-070, 1985) has also been described. With all these known conversions in Taylor reactors, there is absolutely, or not significantly, change in the viscosity v of the liquid. As a result, given a strictly cylindrical geometry of the inner and outer cylinders of the Taylor reactor, the conditions for the Taylor vortex flow are maintained throughout the annular gap time, ie, of the total volume of the reactor. However, if the known Taylor reactors are to be used for conversions where there is a substantial change in viscosity v of liquid in the axial flow direction as conversion progress, the Taylor vortices disappear or are not even formed. In this case, the Couette flow, a concentric, laminar flow, is observed in the annular gap, and an undesired change occurs in the mixing and flow conditions within the Taylor reactor. In this operating state, flow characteristics are shown which are comparable to those of the tube laminarly traversed by the flow, which is a considerable disadvantage. For example, in the case of addition polymerization in the volume or in the solution, there is a mass distribution undesirably broad molecular and chemical polydispersity of the polymers. In addition, the poor reaction routine can result in considerable amounts of residual monomers, which then have to be removed from the Taylor reactor. However, there may also be situations of coagulation and electrodeposition of polymers, which in some cases may even lead to blockage of the reactor or output of the product. Undesirable technical effects of this nature, or of a similar kind, also accompany the thermal degradation of materials of high molecular mass, such as polymers, etc. Above all, it is no longer possible to obtain the desired products, such as very exact molecular weight distribution polymers, but only those whose properties profile does not meet the requirements. It is an object of the present invention to propose a new Taylor reactor, from which the disadvantages of the prior art are lacking and which best enable conduction to a simple, elegant, trouble-free and high-throughput conversion of substances even when this conversion is accompanied by a substantial change in the viscosity of the reaction medium. Another object of the present invention is to find a new process for material conversion under the conditions of the Taylor vortex flow, in the course of which there is a substantial change in the viscosity v of the liquid in the annular gap, ie the medium of reaction. Consequently, we have discovered the new Taylor reactor for conducting material conversions with a) an external wall of the reactor (1), inside which there is a concentrically or eccentrically placed rotor (2), a reactor floor (3), and a reactor cover (4), which together define the volume of the annular reactor (5), b) at least one element (6) for measured addition of reagents, and c) an element (7) for the elimination of the product, where d ) during the conversion there is a change in the viscosity v of the reaction medium and e) the wall of the reactor (1) and / or the rotor (2) are or are geometrically designed, in such a way that the conditions for the vortical flow of Taylor are essentially carried out over the entire length of the reactor in the volume of the reactor (5).

In the following text, the novel Taylor reactor for conducting conversions is abbreviated as "Taylor reactor of the invention". Therefore, the new process for converting materials under the conditions of the Taylor vortex flow is termed as the "process of the invention". In view of the prior art, it was surprising and unpredictable for those skilled in the art that by virtue of the geometrical design of the reactor wall (1) and / or the rotor (2), with axial flow of the reaction medium through the Taylor reactor, it is possible to retain the Taylor vortex flow conditions throughout the length of the reactor, even when there is a substantial change in the viscosity of the reaction medium in the course of its passage through the annular space. The change in viscosity of the reaction medium, according to the invention, includes an increase or a reduction. Both changes can reach several powers of ten in any individual case. An increase of this magnitude in the viscosity v occurs, for example, in the course of addition polymerization in the mass or in the solution. On the contrary, a reduction of said viscosity magnitude v results in the course of depolymerization. However, even under these particularly demanding technical conditions, the Taylor vortex flow is maintained in the Taylor reactor of the invention. In the Taylor reactor of the invention, the outer reactor wall (1) is fixed, while the rotor (2) tour. In another variant, the external reactor wall (1) and the rotor (2) rotate in the same direction, the angular velocity of the rotor (2) being greater than the angular velocity of the external reactor wall (1). In another variant, the external reactor wall (1) and the rotor (2) rotate in opposite directions. Accordingly, the variant comprising the fixed external reactor wall (1) constitutes a special case of the second and third variants, which is, however, preferred due to the simple construction and the considerably greater facility of the technical supervision. The external reactor wall (1) and the rotor (2) have an essentially circular circumference over the entire length of the reactor, as seen in the cross section. In the context of the present invention, the term "essentially circular" means strictly circular, oval, elliptical or triangular, rectangular, square, pentagonal, hexagonal or polygonal with rounded angles. For reasons of ease of production, simplicity of construction and significantly easier maintenance of constant conditions over the entire length of the reactor, a strictly circular circumference is better. According to the invention, the internal wall of the external wall of the reactor (1) and / or the surface of the rotor (2) are either smooth or rough, that is to say, the surfaces in question have a greater or lesser surface roughness. In addition or alternatively, the inner wall of the external reactor wall (1) and / or the surface of the rotor (2) have or have a radial and / or axial surface profile, preferably radial, of the enhancement type. If it is a radial surface profile, it is better than approximately or precisely the same dimensions of the Taylor vortex rings. According to the invention, it is preferred that the inner wall of the external reactor wall (1) and the surface of the rotor (2) be smooth, in order to avoid closed corners in which gas bubbles or reagents and products they could settle. View in the longitudinal direction, the reactor Taylor of the invention is installed vertically, horizontally or in a position between these two directions. According to the invention, vertical mounting is preferable. If the Taylor reactor of the invention is not installed horizontally, it can be traversed by the reaction medium flowing against gravity, from the bottom to the top, or with gravity, from top to bottom. According to the invention, it is preferable if the reaction medium moves in the opposite direction to gravity. The rotor (2) of the Taylor reactor of the invention is installed centrally or eccentrically. That is, its longitudinal axis coincides (centrally) or not (eccentrically) with the longitudinal axis of the external reactor wall (1). In the latter case, the longitudinal axis of the reactor (2) may be parallel to the longitudinal axis of the external reactor wall (1), or it may be inclined at an acute angle relative to it. According to the invention, it is better if the rotor (2) is installed centrally. As additional essential components, the Taylor reactor of the invention comprises a reactor floor (3) and a reactor cover (4), which together with the outer reactor wall (1) and the rotor (2) define the annular volume of the reactor (5), and provide airtight seal to the pressure and to the gas thereof with respect to the outside. The reactor floors (3) and suitable reactor covers (4) are customary and known; as an example, reference is made to DE-B-1 071 241 and EP-A-0 498 583.

As another additional component, the Taylor reactor of the invention further comprises at least one customary and known element (6) for dosed addition of reagents. An example of an appropriate element (6) is a nozzle of appropriate cross section. The element (6) can be installed on the reactor floor (3), the reactor cover (4), the external reactor wall (1), or the rotor (2). In addition, the Taylor reactor of the invention may comprise at least one other element (6) placed at the same height as the first, or without converging with it in the direction of flow. Another element (6) more is especially preferred when there must be subsequent dosing of the reactants and catalysts. Normally, the elements (6) are connected by means of appropriate lines to the dosing pumps, reservoir containers, etc. Another essential component of the Taylor reactor of the invention is the element (7) for elimination of the products. Depending on the circumstances, the element (7) is installed on the reactor floor (3), the outer reactor wall (1), or the reactor cover (4). It is also usually connected by means of appropriate lines to the dosing pumps, reservoir containers, etc. According to the invention, it is 12 ^^^ ¡^^^^ -í8 ^ ¿J¡ ^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^ ^^ particularly preferable to place the element (7) at the upper end of the Taylor reactor of the invention, preferably being given the highest point, because with this configuration the formation of a gas phase is avoided. This is particularly necessary when there are risks of formation of explosive mixtures or deposit of solids, such as polymers of the gas phase. The components of the Taylor reactor of the invention, especially the external reactor wall (1), the rotor (2), the reactor floor (3), the reactor cover (4), the element (6) for dosed addition of reagents, and the element (7) for the removal of products, can consist of any of a variety of suitable materials. Examples of suitable materials are plastic, glass or metals, such as stainless steel, nickel or copper. The individual components can each be produced from different materials. The selection of materials is conducted by the use given to the Taylor reactor of the invention, and by the specific conditions of the reaction, and can, therefore, be carried out in a simple manner by the person skilled in the art. Where, for example, the Taylor reactor of the invention is to be used as a photoreactor, the reactor (2) may consist of glass, which is transparent to actinic light. If there is to be visual supervision of the Taylor vortex rings and their axial movement during the conversions, it is better, according to the invention, to fabricate the outer reactor wall (1) of glass or transparent plastic. Said Taylor reactors of the invention are also remarkably well suited for conducting preliminary experiments. Otherwise, it is better, according to the invention, to use stainless steel. The rotor (2) is connected to an infinitely adjustable drive in a customary and known manner, by means of a magnetic coupling, for example. In addition to the essential components described in detail above, the Taylor reactor of the invention may also comprise customary and known elements serving for heating and / or cooling, and for measuring pressure, temperature, concentration, viscosity and other physicochemical variables, and also they can be connected to the usual and well-known mechanical, hydraulic and / or electronic measuring and control devices. All these components of the Taylor reactor of the invention are connected to each other, so that the reaction medium is enclosed in a pressure and gas tight manner, and appropriately thermally conditioned. The thermal conditioning is preferably carried out in one or more temperature zones that are operated concurrently or countercurrently. When the Taylor reactor of the invention is used for the process of the invention, in which the viscosity of the reaction medium increases sharply in the direction of flow, the external reactor wall (1) and / or the rotor (2) are designed geometrically, so that the annular gap opens in the direction of flow. In this case, according to the invention, the annular gap - dista in the longitudinal section through the Taylor reactor of the invention - can be opened continuously or discontinuously according to the suitable mathematical function suitable. The extent of the opening followed by the expected increase in the viscosity of the reaction medium in the direction of flow, and the person skilled in the art can calculate it on the basis of the formula Taylor and / or determine it by means of simple preliminary experiments. Examples of suitable mathematical functions according to which the circumference of the outer reactor wall (1) and / or the rotor (2) increases or increases - seen in the longitudinal section through the Taylor reactor of the invention - are straight lines, at least two straight lines crossing each other at an obtuse angle, hyperbolas, parabolas, functions and, or combinations of these functions with continuous or discontinuous transitions between them. In principle, the amplitude can be achieved by an increase in the circumference of the external reactor wall (1) as seen in the direction of flow, the circumference of the rotor (2) remains constant, in the same way increasing, or decreasing. Second, this can be achieved by maintaining the diameter of the external reactor wall (1) constant, while reducing the circumference of the rotor (2). In view of the fact that the circumference of the rotor (2) is reduced, the area for the transfer of the frictional forces becomes smaller each time, and, therefore, the rotor (2) would have to turn faster each time , preference is given to those variants of the invention, wherein the circumference of the rotor (2) remains constant, or increases in the same way. The Taylor reactors useful in the invention have a conical external reactor wall (1) which, consequently, has the shape of a single trunk or is composed of a plurality of trunks. The trunk or trunks can have a distortion in the form of a pillow or in the form of a barrel. However, trunks without distortion are particularly preferred. The Taylor reactors useful in the invention further comprise a conical or cylindrical rotor (2). With regard to the shape of the conical rotor (2), the comments made in the paragraph ainterior apply mutatis mutandis. Similarly, the cylindrical rotor (2) can have a distortion in the form of a pillow or in the form of a barrel. According to the invention, cylindrical rotors without distortion are particularly preferred. When the Taylor reactor of the invention is used for the process of the invention, in which the viscosity of the reaction medium is drastically reduced in the direction of flow, the external reactor wall (1) and / or the rotor ( 2) can be designed geometrically, so that the annular gap narrows in the direction of flow. In this case, according to the invention, the annular gap. viewed the longitudinal section through the Taylor reactor of the invention - it can be done in continuous or discontinuous narrowing in accordance with any suitable suitable mathematical function. The extension of the constriction is guided by the expected decrease in the viscosity of the reaction medium in the direction of flow, and the person skilled in the art can calculate it based on the Taylor formula (1), and / or determine it by means of simple preliminary experiments. Examples of suitable mathematical functions according to which the circumference of the wall of the external reactor (1) and / or the rotor (2) is reduced or reduced seen from the longitudinal section through the Taylor reactor of the invention - are straight lines, at least two straight lines that intersect at an obtuse angle, hyperbolas, parabolas, functions, or combinations of these functions with continuous or discontinuous transitions between them. In principle, the narrowing can be achieved by a reduction in the circumference of the wall of the external reactor (1), as seen in the direction of flow, the circumference of the rotor (2) remains constant, with the increase or in the same way with the reduction. Secondly, it can be achieved by keeping the diameter of the external reactor wall (1) constant while increasing the circumference of the rotor (2) . In view of the fact that if the circumference of the rotor (2) is reduced, the area for the transfer of the frictional forces becomes increasingly smaller, and, therefore, the rotor (2) would have to rotate more and more fast, preference is given to those variants of the invention, wherein the circumference of the rotor (2) remains constant or increases in the same way. In the present also, the Taylor reactors useful of the invention have a conical external reactor wall (1) which, consequently, has the shape of a single trunk or is composed of a plurality of trunks. The trunk or trunks can have a distortion in the form of a pillow or in the form of a barrel. However, trunks without distortion are particularly preferred. The Taylor reactors useful of the invention further comprise a conical or cylindrical rotor (2). With respect to the shape of the conical rotor (2), comments are made in the previous paragraph that apply mutatis mutandis. Similarly, the cylindrical rotor (2) can have a distortion in the form of a pillow or in the form of a barrel. According to the invention, cylindrical reactors without distortion are particularly preferred. The Taylor reactor of the invention is ideally suited to drive the process of the invention. The process of the invention can be operated continuously or discontinuously; however, it is particularly useful, in the case of continuous operation. To conduct the process, the reagent or reagents are or are continuously measured for volume 19 -Ml - ^ ---- üß annular reactor (5) by means of at least one element (6). The resulting products are continuously removed from the Taylor reactor of the invention by means of the element (7), and are processed appropriately. In the process of the invention, the residence time in the reactor is between 0.5 minutes and 5 hours, preferably 2 minutes and 3 hours, with particular preference 10 minutes and 2 hours, and in particular, 15 minutes and 1.5 hours. The appropriate residence time for the conversion in question can be determined by the person skilled in the art on the basis of simple preliminary experiments, or by making a calculation based on the kinetic data. The pressure in the annular reaction body (5) is from 0 to 200 bars, and thus the process of the invention can also be carried out with liquefied or supercritical gases, such as supercritical carbon dioxide. Preferably, the pressure is from 0.5 to 100 bars, in particular from 0.5 to 50 bars. When the process of the invention is conducted at a relatively high pressure, in the Taylor reactor of the invention, and its incoming and outgoing lines, they must have a pressure design, in order to satisfy the safety provisions. The process of the invention is conducted at temperatures between -100 and 500 ° C. For this purpose, the twenty The reactor Taylor of the invention is equipped with known and customary suitable cooling and / or heating elements. Preferably, the reaction temperatures are between -10 and 5 300 ° C, in particular 50 and 250 ° C. The appropriate temperature for the conversion in question can be determined by the person skilled in the art on the basis of simple preliminary experiments or can be calculated on the basis of known thermodynamic data. Preferably, the Taylor Ta number of the reaction medium or liquid is from 1 to 10,000, preferably from 5 to 5,000, and in particular from 10 to 2,500. At the same time, the Reynolds number, which is defined by equation (II), must then be 1 to 10, 000. Re = vd / v (II) where v is the axial velocity, and d = rs - r- (r- = outer radius of the inner cylinder; 20 r0 = inner radius of the outer cylinder, and d = a width of hollow). In the process of the invention, there is a change in the viscosity v of the reaction medium. Eeta viscosity can increase or decrease. The change can reach several powers of ten, without disturbing the driving twenty-one of the process of the invention. All this is necessary to ensure that the annular gap of the Taylor reactor of the invention expands or narrows in correspondence with the change in viscosity in the course of the conversions, so that the vortical Taylor flow is maintained throughout the reactor . The course of the change in speed can be determined by a person skilled in the art, based on simple preliminary experiments. A very particular advantage of the Taylor 10 reactor of the invention and of the process of the invention is to join the spatial succession in the Taylor reactor with the temporal succession of intermittent or semi-continuous processes (measurement). The Taylor reactor of the invention and the process of the invention, therefore, provide the advantage of a continuous, almost "single-stage" process, so that a first reaction can be carried out in the first subsection traversed by the flow of the Taylor reactor and a second, third, etc., reaction in a second or subsequent subsection, as seen in the axial direction of the down-flow of another element (6) for dosing reagents and / or catalysts. Examples of conversions for which the process of the invention can be employed for particular advantage are, in particular, preparation or division 22 ?? taa ^^ ??? , ^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^ . of substances of low or high molecular mass, such as the polymerization of monomers in bulk, solution, emulsion or suspension, or by polymerization of precipitation, on the one hand, and polymerization of the resulting polymers or other materials of high molecular mass, on the one hand, and the other side. In the context of the present inventions, the term "polymerization" encompasses not only addition polymerization, copolymerization and block copolymerization, but also polycondensation and polyaddition. Other examples of such conversions are: analogous reactions of polymers, such as the esterification, amidation or urethanization of polymers containing side groups suitable for said reactions, the preparation of curable olefin-unsaturated materials using electron beams or ultraviolet light, preparation of polyurethane resins and modified polyurethane resins, such such as acrylated polyurethanes, the preparation of (poly) ureas or modified poly (poly) ureas, the accumulation of molecular weight of compounds terminated by isocyanate groups, or reactions leading to the formation of 2. 3 ^ Ü-tili --- ^ ---- mesophases, as described, for example, by Antonietti and Göltner in the article "Überstruktur funktioneller Kolloide: eine Chemie im Nanometerbereich [Superstructure of functional colloids: A chemistry in the margin of the nanometer "] in Angewandte Chemie 109 (1997) 944-964, or by Ober and Wengner, in the article "Polyelectrolytesurfactant complexes in the State Solid: Easy Building Blocks for Materials Self-Optimizing "in Advanced Materials, 9 (1997) 1, 17 to 31. With very particular advantage, the process of the invention is used for the polymerization of unsaturated olefin monomers, since in this case the particular advantages of the Taylor reactor of the Accordingly, the process of the invention is used with particular preference for the preparation of copolymers of chemically uniform composition.In this utility, the comonomer or the comonomers of much higher polymerization is or they are measured by the element (6) placed in succession in the axial direction, so that the proportion of comonomers remains constant over the entire length of the reactor. The process of the invention is also used with particular preference for graft copolymerization of a chain. In this utility, in the first subsection of the Taylor reactor of the invention, the main polymer is prepared, after which, at least one comonomer forming the ramifications of the graft is measured by means of at least one other element (6), deviated in the axial direction. Subsequently, according to the invention, the comonomer or comonomers is or are grafted onto the main polymer in at least one other subsection of the Taylor reactor of the invention. When two or more comonomers are used, they can be dosed individually by means of one element (6) in each case, or as a mixture, by another or more elements (6). When at least two comonomers are dosed individually and in succession by at least two elements (6), it is even possible to prepare graft branches which themselves are block copolymers, in a particularly simple and elegant manner. Of course, this concept, as described above, can also be used to prepare block copolymers per se. Similarly, the preparation of core / shell latices can be carried out in a particularly simple and elegant manner with the aid of the process of the invention. Initially, in the first subsection of the Taylor reactor of the invention, the core is prepared by polymerizing at least one monomer. By means of at least one other element (6), at least one other comonomer is metered and the cover is polymerized in the core in at least one other subsection. In this form, it is possible to apply a plurality of covers to the core. The preparation of polymer dispersions can also be carried out with the aid of the process of the present invention. For example, at least one polymer in a homogeneous phase, especially in solution, is (co) polymerized in a first subsection of the Taylor reactor of the invention, after which, a precipitate is dosed by means of at least one other element (6), resulting in polymer dispersions. For all applications, the Taylor reactor of the invention has a particular advantage of a large specific cooling area that allows a particularly safe reaction regime. Examples of suitable monomers for the process of the invention are monoolefins and acyclic and cyclic diolefins, with dysfunction and function, vinylaromatic compounds, vinyl ethers, vinyl esters, vinyl amides, vinyl halides, allyl ethers and esters of allyl, acrylic acid and methacrylic acid and their esters, amides and nitriles, and maleic acid, fumaric acid and itaconic acid and their esters, amides, imides and anhydrides. Examples of suitable monoolefins are ethylene, propylene, 1-butene, 1-pentene, 1-hexene, 1-heptene, 1-octene, cyclobutene, cyclopentene and cyclohexene. Examples of suitable diolefins are butadiene, isoprene, cyclopentadiene and cyclohexadiene. Examples of suitable vinylaromatic compounds are styrene, alpha-methylstyrene, 2-, 3- and 4-chloro-, -methyl-, -ethyl-, -propyl- and -butyl- and -tertyl-butylstyrene and -alpha-methylstyrene. An example of a suitable vinyl compound or a functionalized olefin is vinylcyclohexanediol. Examples of suitable vinyl ethers are methyl, ethyl, propyl, butyl and pentylvinyl ether, allyl monopropoxylate, and also trimethylolpropane monoallyl, diallyl and triallyl ether. Examples of suitable vinyl esters are vinyl acetate and vinyl propionate, and also vinyl esters of Versatic acid and other quaternary acids. Examples of suitable vinyl amides are N-methyl-, N, N-dimethyl-, N-ethyl-, N-propyl-, N-butyl-, N-amyl-, N-cilcopentyl- and N-cyclohexylvinylamide, and also N-vinylpyrrolidone and epsilon-caprolactam. Examples of suitable vinyl halides are vinyl fluoride and vinyl chloride. Examples of suitable vinylidene halides are vinylidene fluoride and vinylidene chloride. Examples of suitable allyl ethers are methyl, ethyl, propyl, butyl, pentyl, phenyl and glycidylmonalyl ether. Examples of suitable allyl esters are allyl acetate and allyl propionate. Examples of suitable esters of acrylic and methacrylic acid are methyl (meth) acrylate, ethyl, propyl, n-butyl, isobutyl, n-pentyl, n-hexyl, 2-ethylhexyl, isodecyl, decyl, cyclohexyl, t-butylcyclohexyl, norbornyl, isobornyl, 2- and 3-hydroxypropyl, 4-hydroxybutyl, trimethylolpropane mono -, pentaerythritol mono- and glycidyl. Also suitable are the di-, tri- and tetra (meth) acrylates of ethylene glycol, di-, tri- and tetraethylene glycol, propylene glycol, dipropylene glycol, butylene glycol, dibutylene glycol, glycerol, trimethylolpropane and pentaerythritol. However, they are not used alone, but always in small amounts, along with monofunctional monomers. Examples of suitable amides of acrylic acid and methacrylic acid are (meth) acrylamide, and also N-methyl-, N, N-dimethyl-, N-ethyl-, N-propyl-, N-butyl-, N-amyl-, N-cyclopentyl- and N-cyclohexyl (meth) -acrylamide. Examples of suitable nitriles are acrylonitrile and methacrylonitrile. Examples of suitable esters, amides, imides and anhydrouss of maleic acid, fumaric acid and itaconic acid are dimethyl, diethyl, dipropyl and dibutyl maleate, fumarate and itaconate, maleamide, fumaramide and itaconamide, and NN '-dimethyl-, N, N, N ', N'-tetramethyl-, N, N'-diethyl-, N, N'-dipropyl-, N, N'-dibutyl-, N, N' -diamyl-, N, N '- dicyclopentyl and N, N '-dicyclohexyl-maleamide, -fumaramide and -itaconamide, maleimide, fumarimide and itaconamide, and N-methyl-, N-ethyl-, N-propyl-, N-butyl-, N-amyl-, N -cyclopentyl-, and N-cyclohexyl-maleimide, -fumarimide and itaconimide, and also anhydrous maleic, fumaric and itaconic. The monomers described above can be polymerized with free radicals, cations or anions. Advantageously, they are polymerized with free radicals. For this purpose, known customary free radical inorganic initiators, such as hydrogen peroxide or potassium peroxodisulfate, or known and customary free radical organic initiators, such as dialkyl peroxides, for example peroxide, can be used. di-butyl, di-teramyl peroxide, and dicumyl peroxide; hydroperoxides, for example, eumenos hydroperoxide and tertbutyl hydroperoxide; by esters, for example, terbutyl perbenzoate, terbutyl perpivalate, terbutyl per-3,5,5,5-trimethylhexanoate and terbutyl per-2-ethylhexanoate; bisazo compounds, such as azobisisobut ironitrile; or C-C initiators, such as 2,3-dimethyl-2, 3-diphenylbutane or -hexane. Also suitable, however, is styrene, which initiates thermal polymerization, even without free radical initiators. The polymers prepared according to the invention have particular advantages and are therefore remarkably suitable for all applications, as commonly contemplated for substances of high molecular mass of this kind, such as, for example, the production of moldings. In particular, however, they are suitable as components for paints, adhesives and other coating materials, and also films. In this case, they can be used in particular as binders, since paints, adhesives and other coating materials, and also films, comprise or consist of the binders prepared according to the invention have particularly remarkable performance properties. The particular advantages of the process of the invention are apparent in particular in paints comprising the binders prepared according to the invention. Depending on their composition, these paints are physically dried or cured thermally, with actinic light, especially with ultraviolet light, or by means of electron bases. These are present as powder coating materials, powder suspension coating materials, coating materials dissolved in organic media, or aqueous coating materials. These may comprise color pigments and / or effect. They are used as architectural coatings for interior and exterior sectors, such as coating materials for furniture, windows, coils and other industrial applications, such as automotive finishes for original equipment (OEM), or as automotive refinishes. In the context of their use in the automotive sector, they are suitable as electrodeposition coating materials, fillers, base coatings and transparent coatings. In all these applications, the coating materials comprising the binders prepared according to the invention are superior to conventional coating materials. The present invention is illustrated by the drawing (Figure 1) and the example. Figure 1. Longitudinal section through the Taylor reactor of the invention, with a conical external reactor wall (1) for visual supervision of the Taylor vortex flow. Example 1 The chain extension of the partially hydrolyzed polyvinyl acetate (polyvinyl alcohol) with glutaraldehyde using a Taylor reactor of the invention and the process thereof. The chain extension of acetate Partially hydrolyzed polyvinyl (content of the hydroxyl group: 88 percent of moles, acetate group content: 12% of moles) was carried out using the Taylor reactor of the invention according to Figure 1. The Taylor reactor had a wall of reactor outside 25 cm high (1) made of glass, of 32 ua-Hi-aM --- ií ------- ^^ i-k strictly circular circumference, whose circumference and, respectively, diameter, increased linearly along the axis of the reactor, as seen in the direction of flow. Thus, the minimum diameter of the outer reactor wall (1) on the reactor floor (3) was 52 mm, and the maximum diameter of the reactor cover (4) was 102 mm. The Taylor reactor of the invention further comprised a linear, centrally mounted, strictly cylindrical rotor (2) made of stainless steel, with a radius of 21 mm. As a result, there was an increase in gap width d of 5 mm at the lower end of the Taylor reactor to 30 mm at the upper end. By means of a straight arrow (2.1), which passed through the seal through the reactor cover (4), the rotor (2) was connected to an infinitely adjustable agitator motor. The reactor cover (4) and the reactor base (3) were made of stainless steel; the seal between them and the corresponding end of the reactor wall (1) was comprised of known polymer joints. The element (6) for dosed addition of the reagents, and the element (7) for the discharge of the product were the glass thrusters with threads, to which a feed hose and a discharge hose were attached by means of coupling rings. 33 --- ÉÍI-M ---- The Taylor reactor was continuously fed by means of the element (6) with a mixture of 4 parts of polyvinyl alcohol, 96.16 parts of water and 0.16 parts of glutaraldehyde with a volume flow of 33.3 ml / min. Just before entry into the Taylor reactor, 42% concentrated nitric acid was dosed into the mixture by means of a separate pump, with a volume flow of 0.16 ml / min. the average stay time in the Taylor reactor was 30 minutes at a temperature of 22 ° C. The agitator speed was 250 rpm. The viscosity of the starting material was 10 mm2 / s. In the element (7), the extended chain polyvinyl alcohol solution had a viscosity of 47 mm2 / s. 15 The conversion of the material, that is, the reaction, was conducted in a total time of 5 hours, corresponding to 10 average stay times. Throughout the Taylor reactor, the Taylor vortices and thus the desired mixing and flow conditions are maintained during this period, despite the increase in viscosity. Therefore, it was possible to conduct the reaction without disruption during the entire period of time. Example 2 The preparation of a solution polymer in a reactor 3. 4 -El-Mt-lM ----- - * - * ---- tk ----------? - ^^ Taylor of the invention. A mixture of 15.8 parts of styrene, 16.5 parts of MMA, 11.6 parts of terbutylcyclohexyl acrylate, 24.7 parts of hydroxypropyl methacrylate, 22.3 parts of Shellsol A, 7.4 parts of xylene, 0.3 parts of diterbutilperoxide, 0.05 parts of terbutylperoxyethylhexanoate and 1.2 Dicumyl peroxide parts were measured using two pumps in a 200 ml conical stainless steel Taylor reactor with heatable jacket. The initial material was measured on the reactor floor, while the resulting polymer was continuously removed at the reactor outlet, at the top in the reactor wall. The reaction was conducted at a temperature of 160 ° C and with an agitator speed of 300 min. "The average residence time of the reaction mixture in the reactor was 30 minutes.The melt of the resulting polymer had a content of the solids of 68.4% (1 hour, 130 ° C) and a viscosity of 3.0 dPas (50% concentration in butyl acetate) The measurement of the polymer by gel chromatography gives an Mn of 3215 and an Mw of 8081. The transition temperature of the polymer glass was 69 ° C, determined by means of DSC at the mid point of DSC. Example 3 The preparation of a coating material using the solution polymer of Example 2. 3.1 A solution of curing agent was prepared by mixing the following components: 98% butyl acetate 40.5 parts xylene 4.0 parts butyl glycol acetate 6.0 parts catalyst solution (from according to section 3.3) 1.5 parts DesmodurR Z43701 'L5.0 parts DesmodurR 33902) 33.0 solid parts (% by weight) 42.2 parts 3.2 An adjustment additive was prepared by mixing the following components: xylene 20.0 parts solvent naphtha3 'L5.0 parts mineral concentrate 135/180 10.0 parts butyl glycol acetate 5.0 parts acetate butyl 98% 50.0 parts 3.3 A catalyst solution was prepared by mixing 1.0 parts of ibutyltin dilaurate and 99 parts of 98% butyl acetate. 3.4 A leveling agent solution was prepared by mixing 5.0 parts of a commercial leveling agent, with poly-modified methylpolysiloxane base (Baysilone® 0L444) and 95 parts of xylene. 3.5 A reserve coating material was prepared by mixing the following components: butyl acetate 4.0 5 parts xylene 4.15 parts Tinuvin® 292s) 0.95 parts 10 Sanduvon® VSU6) 1.20 parts catalyst solution (according to section 3.3) 3.7 parts 15 agent solution leveler (according to section 3.4) 2.0 parts triisodecyl phosphite 0.05 parts 20 solution polymer (ex. 2) 70.85 parts MacrynalR SM5137 '13.1 parts 180 parts of reserve 25 coating material according to section 3.5 were mixed with 37 & amp; & amp; j & amp; a? ^ w ^^ ^^^. 90 parts of hardening agent solution according to section 3.1, and 16.2 parts of adjusting additive according to section 3.2, and the mixture was applied. The processing properties of the coating material were excellent. Life in the crucible was 4 hours. The attenuation of the pendulum from a week-old coating film dried at room temperature was 136 seconds. The resulting transparent layer was applied on a conventional base coat of the Glasurit Reihe 55 brand. The coatings obtained by drying at 60 ° C for 30 minutes had a gloss for DIN 67530 of 87 °, measured at an angle of 20 °. The coatings had a good appearance of top coat. 1 Commercial polyisocyanate of Bayer AG, based on isophorone diisocyanate, with a solids content of 70 percent. 2 Commercial polyisocyanate of Bayer AG, based on hexamethylene diisocyanate. 3 Commercial aromatic hydrocarbon mixture from Shell GmbH. 4 Commercial leveling agent of Bayer AG. 5 Commercial light stabilizer from Ciba Geigy, based on sterically constricted amine (HALS). 6 Commercial light stabilizer from Sandoz 7 Acrylate resin with hydroxyl content from Bayer AG.

Claims

1. A Taylor reactor for conducting material conversions, with a) an external wall of the reactor (1), inside which there is a concentrically or eccentrically placed rotor (2), a reactor floor (3), and a reactor cover (4) ), which together define the annular volume of the reactor (5), b) at least one element (6) for measured addition of reagents, and c) an element (7) for the elimination of the product, wherein d) during the conversion there is a change in the viscosity v of the reaction medium and e) the reactor wall (1) and / or the rotor (2) are or are geometrically designed, in such a way that the conditions for the Taylor vortex flow are essentially met throughout the length of the reactor in the reactor volume (5). The Taylor reactor according to claim 1, wherein the outer reactor wall (1) and the rotor (2) rotate in the same direction, the angular velocity of the rotor (2) is higher than that of the external reactor wall ( 1), or where the external reactor wall (1) is fixed while the rotor (2) rotates. The Taylor reactor according to claim 1 or 2, wherein the external reactor wall (1) and the rotor (2) have an essentially circular circumference over the entire length of the reactor, as seen in the cross-section. 4. The Taylor reactor according to any of claims 1 to 3, which is installed vertically, where the reaction medium moves against gravity. 5. The Taylor reactor according to any of claims 1 to 4, wherein the rotor (2) is centrally mounted. 6. The Taylor reactor according to any of claims 1 to 5, wherein the element (7) for the removal of the products is placed at the highest point of the lid of the reactor (4). 7. The Taylor reactor according to any of claims 1 to 6, wherein the external reactor wall (1) and / or the rotor (2) are or are geometrically designed, so that the amular gap is expanded in the direction of the flow. 8. The Taylor reactor according to claim 7, wherein the circumference of the external reactor wall (1) increases as seen in the direction of flow, the circumference of the rotor (2) remains constant, increases in the same way or is reduced. 9. The Taylor reactor according to claim 7 or 8, wherein the external reactor wall (1) has the shape of a single trunk or is composed of a plurality of trunks. The Taylor reactor according to any of claims 1 to 6, wherein the external reactor wall (1) and / or the rotor (2) are or are geometrically designed, so that the annular gap narrows in the direction of the flow. The Taylor reactor according to claim 10, wherein the circumference of the wall of the external reactor (1) is reduced as seen in the flow direction, the circumference of the rotor (2) remains constant, increases, and is reduced in equal shape. 1

2. The Taylor reactor according to claim 10 or 11, wherein the external reactor wall (1) has the shape of a single trunk or is composed of a plurality of trunks. 1

3. A process for converting substances, wherein the viscosity v of the reaction medium increases in the course of the reaction, under the conditions of the Taylor vortex flow, which is conducted using a Taylor reactor, according to any of claims 1 to 9. 1

4. The process according to claim 13, wherein a first reaction is carried out in the first subsection crossed by the flow of the Taylor reactor, and a second, third, etc. The reaction is carried out in a second or another subsection - as seen in the axial flow direction - downstream of at least one other element (6) for dosing reagents and / or catalysts. 1

5. The use of the process according to the claim 13 or 14, for preparing addition polymers, copolymers, block copolymers and graft copolymers, polycondensation products and polyaddition products, core / shell latices, polymer dispersions, products of reactions analogous to polymers, such as esterification, amidation or urethanization of polymers containing secondary groups suitable for said reactions, unsaturated olefin materials that can be hardened with electron beams or ultraviolet light, or mesophases. 1

6. A process for converting substances, wherein the viscosity v of the reaction medium falls in the course of the reaction, under the conditions of the Taylor vortex flow, which is conducted using a Taylor reactor according to any of claims 1 to 6 and 10 to 12. 1

7. The process according to claim 16, wherein a first reaction takes place in the first subsection traversed by flow of the Taylor reactor and a second, third, etc. reaction takes place in a second or another subsection - as seen in the direction of axial flow - downstream of at least one other element (6) for dosing reagents and / or catalysts. 1

8. The use of the process according to claim 16 or 17, for the separation of substances of high molecular mass. 1

9. The use of the substances prepared by the process according to claim 13 or 14, as components of moldings, paints, adhesives and other coating and film materials.