EP1558375A1

EP1558375A1 - Taylor reactor for substance transformation

Info

Publication number: EP1558375A1
Application number: EP03775153A
Authority: EP
Inventors: Edeltraud Hagemeister; Werner-Alfons Jung; Heinz-Peter Rink; Hans-Ulrich Moritz; Iris Conrad; Tsung-Chieh Cheng; Thomas Vens
Original assignee: BASF Coatings GmbH
Current assignee: BASF Coatings GmbH
Priority date: 2002-10-30
Filing date: 2003-09-16
Publication date: 2005-08-03
Also published as: JP2006504513A; DE10250420A1; US20060062702A1; JP4718185B2; WO2004039491A1; AU2003283244A1

Abstract

The invention relates to a Taylor reactor. In the first embodiment, the housing of said reactor (401) and/or the rotor (404) thereof are constructed in such a way that the cross section area of a reaction volume initially increases between an input and output, and afterwards, stops to increase in the direction of the output at least on one part of the rotor length. In the second embodiment, which can be used widely than the first embodiment, the end of the rotor on the front face thereof is constructed in such a way that the reaction volume exits to the output, at lest significantly without dead volume.

Description

Taylor reactor for material conversions

The present invention relates to a Taylor reactor for physical and / or chemical material conversions, in the course of which an increase in the viscosity of the reaction medium occurs. In addition, the present invention relates to a new process for converting substances using the Taylor reactor and to the use of the substances produced by the new process.

Taylor reactors, which are used to convert substances under the conditions of the Taylor vortex flow, have long been known. In their original embodiment, they consist of two coaxial, concentrically arranged cylinders, the outer of which is fixed and the inner rotates. The volume that is formed between the inner peripheral surface of the outer cylinder and the outer peripheral surface of the inner cylinder serves as the reaction space. With increasing angular velocity of the inner cylinder, a number of different forms of flow occur, which are characterized by a dimensionless characteristic number, the so-called Taylor number Ta. In addition to the angular velocity of the inner cylinder forming the rotor, the Taylor number is also dependent on the kinematic viscosity of the fluid in the reaction volume and on the geometric parameters, the outer radius of the inner cylinder R, and the inner radius of the outer cylinder, according to the following formula:

with d = r _a - n.

At low angular velocity, the laminar Couette flow, a simple shear flow, forms. Will the

Rotation speed of the inner cylinder increased further, kick above a critical value, alternately rotating (contrarotating) vortices with axes along the circumferential direction. These so-called Taylor vortices are rotationally symmetrical, have the geometric shape of a To (Taylor vortex rings) and have a diameter that is approximately as large as the gap width. Two adjacent vertebrae form a pair of vertebrae or a vertebral cell.

This behavior is based on the fact that when the inner cylinder rotates with the outer cylinder at rest, the fluid particles near the inner cylinder are subjected to a stronger centrifugal force than those which are further away from the inner cylinder. This difference in the acting centrifugal forces pushes the fluid particles from the inner to the outer cylinder. The centrifugal force counteracts the viscosity force, since the friction has to be overcome when the fluid particles move. If the speed of rotation increases, then the centrifugal force also increases. The Taylor vortices arise when the centrifugal force becomes greater than the stabilizing viscosity force.

If the Taylor reactor is equipped with an inlet and outlet and operated continuously, a Taylor vortex flow with a low axial flow results. Each pair of vertebrae moves through the gap, with only a small mass exchange between adjacent pairs of vertebrae. The mixing within such vortex pairs is very high, whereas the axial mixing beyond the pair boundaries is only very small. A pair of vortices can therefore be regarded as a well-mixed stirred kettle. The flow system thus behaves like an ideal flow tube in that the vortex pairs move through the gap with a constant dwell time like ideal stirred tanks. However, if the viscosity v of the fluid changes with the progressive conversion in the axial direction of flow as strongly as is the case with the polymerization in bulk, the Taylor vortices disappear or do not occur at all. The Couette flow, a concentric, laminar layer flow, can then be observed in the annular gap. This leads to an undesirable change in the mixing and flow conditions in the Taylor reactor. He has in this operating state flow characteristics of the laminar flow tube _^ are comparable, which is a considerable disadvantage. For example, mass polymerization leads to an undesirably wide molar mass distribution and chemical non-uniformity of the polymers. In addition, due to the poor conduct of the reaction, considerable amounts of residual monomers can result, which then have to be discharged from the Taylor reactor. However, coagulation and deposition of polymers can also occur, which in some circumstances can even lead to the reactor or the product outlet becoming blocked. Overall, the desired products, such as polymers with a comparatively narrow molar mass distribution, can no longer be obtained, but only those which do not meet the requirements in their property profile.

From DE 198 28 742 A1 a Taylor reactor is known in which to solve these problems

a) an outer reactor wall and a. therein a concentrically arranged rotor, a reactor base and a reactor cover, which together define the annular gap-shaped reaction volume,

b) at least one device for metering in educts and c) a device for the product flow

are provided, the annular gap-shaped reaction volume widening in the flow direction, in particular conically widening / as a result, the known Taylor reactor is able to essentially solve the problem of maintaining the Taylor flow with a strong increase in the kinematic viscosity v in the reaction medium.

In this known Taylor reactor, the reaction volume in the form of an annular gap is defined by the concentrically arranged rotor, the reactor base and the reactor cover. This means that the product outlet must be arranged on the side of the Taylor reactor or in the reactor cover and cannot be designed without edges. With this configuration, a trouble-free product outlet can only be implemented with difficulty.

Because of the disadvantageous interaction of flow and geometric configuration, the known Taylor reactor is not yet capable of all safety and process engineering _. Solving problems that occur in bulk polymerization and, on the other hand, it is not yet possible to increase the conversion of the monomers to such an extent that extensive freedom from monomers and a narrow molecular weight distribution and non-uniformity in the molecular weight of the polymers is achieved.

The problem of inadequate mixing of the starting materials can to a certain extent be caused by the connection of a

Mixing unit can be solved before the feed of the starting materials, as described in German patent application DE 199 60 389 A1, meanwhile the bulk polymerization problems described above still occur.

A Taylor reactor is known from US Pat. No. 4,174,097, in which the rotor is rotatably mounted in the inlet region of the starting materials. The rotor is not supported at its other end, but essentially ends in front of the outlet area, which has the same diameter as the outer reactor wall at its widest point. The outlet area narrows in a funnel shape to form an outlet pipe. The well-known Taylor reactor is used to mix liquids of different viscosities and electrical conductivity. It can also be used to react polysocyanates with polyols. The extent to which it can be used in bulk for the polymerization of olefinically unsaturated monomers is not apparent from the American patent.

In the known Taylor reactor, the drive shaft is passed through the reactor floor and the connection to the rotor in the inlet area of the starting materials. However, the ring-shaped reaction volume does not widen in the direction of flow. While in the U.S. patent at column 10, lines 29-33, it is stated that the concentric portions may have configurations other than cylindrical, for example essentially spherical or conical, which configurations are particularly advantageous for bulk polymerization, but will not taught.

It succeeded with the broadening in the flow direction

Taylor reactors having reaction volume, the monomeric

To increase sales and reduce the formation of gel particles, polydispersities> 3 were shown in the production of polyacrylate resins. Sales> 99% could only be realized if a certain content of acrylate monomers was included.

It is therefore an object of the present invention to increase the polydispersities while increasing them _. to reduce sales.

This object is achieved by the Taylor reactors reproduced in the independent claims 1, 10 and 13. If the term "Taylor reactor" is used in the following, it is intended to express that viewed in the direction of the axis of rotation of the rotor - in other words: in the direction of flow of the reaction medium - Taylor vortices arise at least over a portion of the reaction volume during operation of the reactor ,

Surprisingly, it has been shown that with a Taylor reactor in which the reactor housing and / or the rotor are designed in such a way that the cross section of the reaction volume at least initially increases from the inlet to the outlet, the increase in the direction of the outlet - ie in the direction of flow of the reaction medium - at least decreases over part of the length of the rotor, however, the polydispersities can be significantly reduced. A possible explanation for this effect is the reduction or even avoidance of short-circuit currents at the edges that limit the reaction volume, which can occur if the Taylor vortices do not extend to the edges. "Short-circuit current" is thus to be understood as a current inside the reactor in the direction of flow of the reaction media, partially bypassing the mixing process and thus reducing the residence time in the reactor, which leads to lower degrees of polymerization. Tests have shown that the Taylor reactor according to the invention is surprisingly suitable for all substance conversions in which. the kinematic viscosity v of the reaction medium changed significantly in the direction of flow.

Above all, it is surprising that the Taylor reactor according to the invention and the process according to the invention allow radical, anionic and cationic (co) polymerization, graft copolymerization and block copolymerization (collectively called “polymerization”) of olefinically unsaturated monomers in bulk with conversions> 70 mol%. It is even more surprising that conversions> 98 mol% can be achieved without problems, without it occurring in the Taylor reactor according to the invention for the formation of disruptive gas bubbles and / or the deposit and of (co) polymers, graft copolymers and block copolymers

(collectively called "polymers") comes.

Furthermore, it is surprising that the Taylor reactor according to the invention and the method according to the invention permit particularly reliable reaction control of the polymerization in bulk, which is why the polymers can be prepared very safely, reliably and reproducibly. Due to the very low monomer content of the polymers, they can be used for a wide variety of purposes without further purification, without the occurrence of safety-related, process-related toxicological and ecological problems and unpleasant odors.

The Taylor reactor according to the invention preferably comprises a reaction volume in the form of an annular gap, which preferably has a circular circumference. The ring- gap-shaped reaction volume is defined by or is formed by an outer reactor wall and a rotor arranged concentrically therein, which is arranged rotatably about the axis of rotation.

The outer reactor wall and the rotor have a circular circumference over the entire length of the reaction volume, as seen in cross section. The term "circular" is to be understood as strictly circular, oval, elliptical or polygonal with rounded corners. A strictly circular circumference is advantageous for reasons of simplicity of manufacture, simple construction and significantly easier maintenance of constant conditions over the entire length of the annular gap-shaped reaction volume.

The inner wall of the outer reactor wall and / or the surface of the rotor can be smooth or rough, i.e. the surfaces in question can have a low or high surface roughness. Additionally or alternatively, the inner wall of the outer reactor wall and / or the surface of the rotor can have a relief-like radial and / or axial, preferably radial, surface profile, as described, for example, in US Pat. No. 4,174,907 A or British Pat. GB 1,358,157 becomes. Is a. radial surface profile available, it is advantageously approximately or exactly dimensioned like the Taylor swirl rings.

However, it is advantageous if the inner wall of the outer reactor wall and the surface of the rotor are smooth and without any profile in order to avoid blind spots in which gas bubbles or starting materials, process materials and products can settle. The Taylor reactor according to the invention is - viewed in the longitudinal direction - mounted vertically, horizontally or in a position between these two directions. Vertical storage is an advantage. If the Taylor reactor according to the invention is not mounted horizontally, the reaction medium can flow from bottom to top against the force of gravity or from top to bottom with the force of gravity. According to the invention, it is advantageous if the reaction ^{medium 1 is moved} against gravity.

The viscosity development of the reaction medium can be influenced by influencing the flow rate of the reaction medium through the reactor by varying the inflow rate to the inlet. The reactor can therefore be used for various reaction mixtures.

According to the invention, the increase in the cross section of the reaction volume in the flow direction takes place continuously or discontinuously, in particular continuously, according to suitable mathematical functions. Examples of suitable mathematical functions are straight lines, at least two straight lines that meet at an obtuse angle, parables, hyperbolas, e-functions or combinations of these functions that merge continuously or discontinuously, in particular continuously. The mathematical functions are preferably straight lines, that is to say that the preferably annular-shaped cross section of the reaction volume widens more and more constantly in the flow direction in a first section than in a second section in which the cross section increases less, preferably is constant. The extent of the increase depends on the expected increase in the viscosity of the reaction medium in the flow direction and can vary from Experts can be estimated using Taylor formula I and / or determined using simple preliminary tests.

When the cross-section of the annular gap-shaped reaction volume is enlarged, the outer reactor wall can be cylindrical and the rotor can be conical, the rotor having the largest diameter on the inlet side. Alternatively, the outer reaction wall may be tapered and the rotor cylindrical, i.e. that its cross-section is constant over the entire rotor length. It is advantageous according to the invention if the outer reactor wall is conical in a first region on the inlet side and cylindrical in a second region and the rotor is cylindrical.

Is the outlet arranged axially, i.e. If it opens into the reaction volume in the direction of the axis of rotation of the rotor, the feed of the educts and / or the process substances causes the flow in the reaction volume in the direction of the outlet and through the outlet.

In a further constructive design of a Taylor reactor, the flow around the axis of rotation is also used as a driving force for removing the reaction products, in which the outlet opens into the volume of rotation at a radial distance from the axis of rotation.

The junction can be at any angle between the axis of rotation and the outlet line defined by the outlet. However, it is preferred if the outlet line and the axis of rotation form an angle between 0 ° and 90 °, i.e. the outlet opens into the volume of rotation transversely to the axis of rotation.

In particular, if the outlet is approximately perpendicular to the axis of rotation in the confluence area, the proportion of the flow is around the Maximum axis of rotation on the driving force for removing the reaction products. It is then advantageous to design the end adjacent to the outlet in the manner of a pump rotor in order to generate as strong a current as possible about the axis of rotation in this area.

This is possible without negative effects on the reaction process in the reactor, since due to the high viscosity and the already achieved material conversion of approx. 99% Taylor swirls or reaction processes are no longer necessary.

In the narrowest area of the ring-shaped reaction volume there is at least one inlet for the starting materials, in particular for the olefinically unsaturated monomers, and for suitable process materials, such as catalysts and initiators, above the reactor base. The inlet can be arranged on the side or go through the reactor floor. There are preferably at least two inlets which are arranged on the side and / or pass through the reactor floor. If necessary, further inlets can be provided in the direction of flow through which further starting materials, catalysts or initiators can be metered in, so that the substance conversions, in particular the polymerization, can be carried out in several stages.

The starting materials can be fed to the feed using customary and known methods and devices, such as metering pumps. The devices can be equipped with the aid of customary and known mechanical, hydraulic, optical and electronic measuring and control devices. In addition, one of the mixing devices, as described, for example, in German patent application DE 199 60 389 A1, column 4, line 55, to column 5, line 34, can be connected upstream of the feed. In the Taylor reactor according to the invention, an outlet area is provided which tapers in the flow direction towards a product outlet.

The front end of the rotor facing the outlet is designed such that the reaction volume opens into the production process at least substantially free of dead volume.

The outlet area and the product outlet are defined by the outer reactor wall.

The tapering of the outlet area can be described by the mathematical functions listed above, with straight lines being preferred. Accordingly, the outlet area preferably tapers conically. The front end of the rotor is then preferably conical in order to achieve — as is preferred — that the cross section of the outlet region is essentially constant in the direction of the axis. This has the effect that dead volumes are avoided, but at the same time there is no disadvantageous back pressure.

The reactor wall in the inlet area, in the area of the annular gap-shaped reaction volume and in the outlet area as well as the inlet or the inlets and the product outlet can be equipped with a heating or cooling jacket, so that they can be heated or cooled in cocurrent or in countercurrent. Furthermore, the Taylor reactor according to the invention is customary and known mechanical, hydraulic, optical and electronic measuring and control devices, such as temperature sensors, pressure meters, flow meters, optical or electronic sensors and devices for measuring substance concentrations, viscosities and other physico-chemical variables, which forward their measured values to a data processing system that controls the entire process.

The Taylor reactor according to the invention is preferably designed to be pressure-tight, so that the reaction medium can preferably be under a pressure of 1 to 100 bar. The Taylor reactor according to the invention can consist of a wide variety of materials, as long as these are not attacked by the starting materials and the reaction products and can withstand higher pressures. Metals, preferably steel, in particular stainless steel, are preferably used.

The Taylor reactor according to the invention can be used for a wide variety of purposes. It is preferably used for material conversions in which the kinematic viscosity v in the reaction medium increases in the direction of flow.

Examples of substance conversions that can be carried out in the Taylor reactor according to the invention with particular advantages are the build-up or breakdown of oligomeric and high-molecular substances, such as. B. the polymerization of monomers in bulk, solution, emulsion or suspension or by precipitation polymerization.

Other examples of such transformations are

polymer-analogous reactions, such as the esterification, amidation or urethanization of polymers which contain side groups which are suitable for such reactions, the preparation of olefinically unsaturated materials which are curable with electron beams or ultraviolet light, the production of polyurethane resins and modified polyurethane resins such as acrylated polyurethanes, the production of (polyJureas or modified (poly) ureas, - the molecular weight build-up of compounds which are associated with

Isocyanate groups are terminated, or reactions which lead to the formation of mesosphases, as described, for example, by Antonietti and Göltner in the article "Superstructure of Functional Colloids: A Chemistry in the Nanometer Range" in Angewandte Chemie, Volume 109, 1997,

Pages 944 to 964, or by Ober and Wengner in the article "Polyelectrolyte-Surfactant Complexes in the Solid State: Facile Building Blocks for Self-Organizing Materials" in Advanced Materials, Volume 9, Issue 1, 1997, Pages 17 to 31 become.

The process according to the invention is used with very particular advantage for the polymerization of olefinically unsaturated monomers in bulk, because the particular advantages of the Taylor reactor according to the invention are particularly open.

The Taylor reactor according to the invention is particularly preferably used for the production of chemically uniformly composed polymers and copolymers. In the copolymerization, the more rapidly polymerizing comonomer or the more rapidly polymerizing comonomers can be metered in via feeds arranged one behind the other in the axial direction, so that the comonomer ratio can be kept constant over the entire length of the reactor. The Taylor reactor is also used with particular advantage for the graft copolymerization.

Here, the so-called backbone polymer can be prepared separately and metered into the Taylor reactor according to the invention via a separate feed or in a mixture with at least one monomer.

The backbone polymer can, however, also be produced in a first section of the Taylor reactor according to the invention, after which at least one monomer which forms the graft branches is metered in via at least one further feed which is offset in the axial direction. The monomer or the comonomers can then be grafted onto the backbone polymer in at least one further section of the Taylor reactor according to the invention. If several comonomers are used, they can be metered in individually via one feed or as a mixture through one feed or several feeds. If at least two comonomers are metered in individually and in succession through at least two feeds, it is even possible to produce graft branches, which are block copolymers in their own right, in a particularly simple and elegant manner.

Of course, this concept described above can also be used to produce block copolymers as such.

In an analogous manner, the production of core-shell latices can be realized particularly simply and elegantly with the help of the Taylor reactor according to the invention. In the first section of the Tylor reactor according to the invention, the core is first prepared by polymerizing at least one monomer. At least one further comonomer is metered in via at least one further feed and the shell is polymerized onto the core in at least one further section. In this way, several shells can be applied to the core.

Polymer dispersions can also be prepared with the aid of the Tylor reactor according to the invention. For example, at least one monomer in the homogeneous phase, in particular in solution, is polymerized in a first section of the Taylor reactor (co) according to the invention, after which a precipitant is metered in via at least one further device, resulting in the polymer dispersion.

In all applications, the Taylor reactor according to the invention has the particular advantage of a large specific cooling surface, which allows a particularly reliable reaction to be carried out.

The Taylor reactor according to the invention is very particularly preferred for the continuous production of (co) polymers, block copolymers and graft copolymers by free radical, anionic or cationic, in particular free radical, (co) polymerization, block mixed polymerization or

Graft copolymerization (polymerization) of at least one olefinically unsaturated monomer used in bulk by the process according to the invention.

Examples of suitable monomers which are suitable for the process according to the invention are acyclic and cyclic, optionally functionalized monoolefins and diolefins, vinylaromatic compounds, vinyl ethers, vinyl esters, vinyl amides, vinyl halides, allyl ethers and allyl esters, 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 maonoolefins are ethylene, propylene, 1-butene, 1-pentene, 1-hexene, 1-heptene, 1-octene, cyclobutene, cyclopentene, dicyclopentene and cyclohexene.

Examples of suitable diolefins are butadiene, isoprene, cyclopentadiene and cyclohexadiene.

Examples of suitable vinyl aromatic compounds are styrene, alpha-methyl styrene, 2-, 3- and 4-chloro, methyl, ethyl, propyl and butyl and tert-butyl styrene and alpha-methyl styrene.

An example of a suitable vinyl compound or a functionalized olefin is vinylcyclohexanediol.

Examples of suitable vinyl ethers are methyl, ethyl, propyl, butyl and pentyl vinyl ether, allyl monopropoxylate and trimethylolpropane mono, di and triallyl ether.

Examples of suitable vinyl esters are vinyl acetate and propionate and the vinyl esters of versatic acid and other quaternary acids.

Examples of suitable vinylamides are N-methyl-, N, N-dimethyl-, N-ethyl-, N-propyl-, N-butyl-, N-amyl-, N-cyclopentyl- and N-cyclohexylvinylamide as well as N-vinylpyrrolidone and - epsilon-caprolactam.

Examples of suitable vinyl halides are vinyl fluoride and chloride. Examples of suitable vinylidene halides are vinylidene fluoride and vinyl chloride.

Examples of suitable allyl ethers are methyl, ethyl, propyl, butyl, pentyl, phenyl and glycidyl monoallyl ethers.

Examples of suitable allyl esters are allyl acetate and propionate.

Examples of suitable esters of acrylic acid and methacrylic acid are methyl, ethyl, propyl, n-butyl, isobutyl, n-pentyl, n-hexyl, 2-ethyl-hexyl, isodecyl, decyl and cyclohexyl , t-Butylcyclohexyl, norbonyl, isobornyl, 2- and 3-hydroxypropyl, 4-hydroxybutyl,

Trimethylolpropane mono-, pentaerythritol mono- and glycidyl (meth) acrylate. In addition, there 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 into consideration. However, they are not used alone, but always in minor amounts together with the monofunctional monomers.

Examples of suitable amides of acrylic acid methacrylic acid are (meth) acrylic acid amide and (meth) acrylic acid-N-methyl-, -N, N-dimethyl-, -N-ethyl-, -N-propyl-, -N-butyl-, -N -amyl-, -N-cyclopentyl- and -N-cyclohexylamide.

Examples of suitable nitriles are acrylonitrile and methacrylonitrile.

Examples of suitable esters, amides, imides and anhydrides

Maleic acid, fumaric acid and itaconic acid are maleic acid, fumaric acid and itaconic acid dimethyl, diethyl, dipropyl and dibutyl esters, maleic acid, fumaric acid and itaconic acid diamide, Maleic acid, fumaric acid and itaconic acid-N, N ^'dimethyl, N, N, ^N', N ^Λ - tetamethyl-, -N N ^'diethyl, N, ^N', dipropyl, -N , N ^' -dibutyl-, -N, N'-diamyl-, - N, N'-dicyclopentyl- and -N, N ^' -dicyclohexylamide, maleic, fumaric and itaconic amide and maleic, fumaric and itaconic acid N -methyl-, -N-ethyl-, -N-propyl-, -N-butyl-, -N-amyl-, -N-cyclopentyl- and -N-cyclohexylimide as well as maleic, fumaric and itaconic anhydride.

The monomers described above can be polymerized by radical, cationic or anionic polymerization. They are advantageously polymerized by free radicals. The usual and known inorganic radical initiators or initiators such as

Hydrogen peroxide or potassium peroxodisulfate or the usual and known organic radical initiators or initiators such as dialkyl peroxides, e.g. B. di-tert-butyl peroxide, di-tert-amyl peroxide and

dicumyl peroxide; Hydroperoxides, e.g. B. cumene hydroperoxide and tert.

butyl hydroperoxide; Perester, e.g. B. tert-butyl perbenzoate, tert.

, Butyl perpivalate, tert-butyl per-3,5,5-trimethylhexanoate and tert-butyl per-

2-ethylhexanoate; Bisazo compounds such as azobisisobutyronitrile; or C-C starters such as 2,3-dimethyl-2,3-diphenyl-butane or hexane can be used. However, styrene can also be used, which initiates polymerization thermally even without a radical initiator.

In the process according to the invention, at least one of the monomers described above is metered in via a lateral inlet into the inlet region of the Taylor reactor according to the invention. At least one of the radical initiators or initiators described above is preferably metered in together with at least one monomer via a further side feed. The monomer or monomers are at least partially polymerized in the reaction volume under the conditions of the Taylor flow. The resulting liquid polymer is conveyed from the reaction volume in the form of an annular gap into the outlet area and from there into the product outlet and discharged via the pressure-maintaining valve.

In the process according to the invention, the conditions for the Taylor flow are preferably met in part of the annular gap-shaped reaction volume or in the entire annular gap-shaped reaction volume, in particular in the entire annular gap-shaped reaction volume.

The temperature of the reaction medium can vary widely in the process according to the invention and depends in particular on the monomer with the lowest decomposition temperature, on the temperature at which the depolymerization begins, and on the reactivity of the monomer or monomers and the initiators. The polymerization is preferably carried out at temperatures from 100 to 200, preferably 130 to 180 and in particular 150 to 180 ° C.

The polymerization can be carried out under pressure. The pressure is preferably 1 to 100, preferably 1 to 25 and in particular 1 to 15 bar.

The throughput time can vary widely and depends in particular on the reactivity of the monomers and the size, in particular the length, of the Taylor reactor according to the invention. The throughput time is preferably 15 minutes to 2 hours, in particular 20 minutes to 1 hour. It is a very special advantage of the Taylor reactor according to the invention and of the method according to the invention that the conversion of the monomers is> 70 mol%. Surprisingly, conversions> 80, preferably> 90, particularly preferably> 95, very particularly preferably> 98 and in particular> 98.5 mol% can be achieved without problems. Here, as is customary in bulk polymerization, the kinematic viscosity v can increase at least tenfold, in particular at least a hundredfold.

The molecular weight of the polymers prepared using the process according to the invention can vary widely and is essentially limited only by the maximum kinematic viscosity v at which the Taylor reactor according to the invention can maintain the conditions of the Taylor flow. The number average molecular weights of the polymers prepared in the process according to the invention are preferably 800 to 50,000, preferably 1,000 to 25,000 and in particular 1,000 to 10,000 Daltons. The non-uniformity of the molecular weight is preferably <10, in particular <8.

Exemplary embodiments of the invention are shown in the drawing. Show it:

Fig. 1 - schematically - an embodiment of a Taylor reactor according to the invention according to the first alternative of the invention in longitudinal section;

Fig. 2 shows another embodiment of an inventive Taylor reactor according to the first alternative of the invention in one

Fig. 1 corresponding representation; 3 shows an embodiment of a Taylor reactor according to the invention in accordance with the second alternative of the invention in a view corresponding to FIG. 1;

Fig. 4 shows an embodiment of a Taylor reactor according to the invention, in which both alternatives of the invention are implemented, in a view corresponding to Fig. 1 and 2.

Fig. 5 shows an embodiment of a Taylor reactor according to the invention according to the third alternative of the invention in a view corresponding to Fig. 1 and

6 shows a section along section line VI - VI in FIG. 5

The Taylor reactor designated 100 as a whole in FIG. 1 comprises a reactor housing 103, the lower region of which, as shown in FIG. 1, which corresponds to the normal operating position of the Taylor reactor 100, is designed as an application region 108. Two laterally opposite inlets 108.1, through which starting materials and / or process substances can be fed, open into the reaction volume 102, which is formed between the outer peripheral surface 104.3 of a cylindrical rotor 104 and the inner peripheral surface 103.1 of the reactor housing 103.

The part 103.2 of the reactor housing 103 adjoining the inlet region 108 is designed to widen conically up to the point 103.3, so that the cross section of the reaction volume 102 increases in the part 103.2. At the point 103.3 there is a cylindrical part 103.4 of the reactor housing 103, which extends beyond the upper end face 104.2 of the rotor 104. On The cylindrical part 103.4 is followed by a funnel-shaped outlet area 109 which opens into an outlet 110 which serves to discharge the reaction products. The outlet 110 is a

Pressure-maintaining valve 111 is connected downstream, with which the reaction media in the reaction volume can be kept under a predeterminable pressure.

The rotor 104 is mounted rotatably about an axis A on the inlet-side end wall 105 shown in FIG. 1 below. A drive shaft 107, which is passed through the end wall 105 and is connected to a rotary drive (not shown in the drawing), for example an electric motor, is used to introduce a torque causing the rotation into the rotor 104. The sealing of the reaction volume 102 in the area of the passage of the drive shaft 107 through the end wall 105 is provided by a mechanical seal 106 which is arranged between the end 104. 1 of the rotor 104 shown in the drawing below and the end wall 105.

For the purpose of premixing the starting materials and / or process substances supplied to the reaction volume, one or more inlets can be equipped with mixing devices 112.

As can be seen from FIG. 1, the design of the reactor housing 103 and the rotor 104 has the effect that the cross section of the reaction volume in the reactor housing part 103.2, seen from the inlet to the outlet, initially increases, but the increase from the point 103.3, however, in the exemplary embodiment illustrated to the Value 0 - decreases to the outlet in the cylindrical housing part 103.4.

The exemplary embodiment shown in FIG. 2 is largely identical in its technical configuration with that according to FIG. 1 match. In order to avoid repetitions, only the differences will be explained below. Components corresponding to the exemplary embodiment from FIG. 1 are provided with reference numerals increased by 100.

In the exemplary embodiment shown in FIG. 2, the reactor housing 203 is designed to widen conically up to the outlet region 209. In order to bring about the decrease in the cross section of the reaction volume of the outlet in accordance with the invention, the rotor 204, which is cylindrical in the lower region according to FIG. 2, has a point 204.3 from which it merges into a region 204.4 which widens conically towards the outlet region 209. The taper corresponds to that of the reactor housing 203, so that the cross section of the reaction volume remains constant from the point 204 to the upper end of the rotor.

In the case of the Taylor reactor shown as a whole in FIG. 3, designated 301, which is an exemplary embodiment according to the second alternative of the invention, only the differences from the Taylor reactor according to FIG. 1 are discussed. Reference is once again made to the description of FIG. 1, the corresponding components in FIG. 3 being provided with reference numbers increased by 200.

The reactor housing 303 of the Taylor reactor 301 is designed to widen conically from the inlet region 308 to the outlet region 309. The rotor 304 has a cylindrical shape which merges into a cone 313 at the point 304.3. The cone angle d is selected such that the cone surface 314 runs parallel to the wall 303.4 of the reactor housing 303 delimiting the outlet region 309. In this way it is achieved that the reaction volume. opens into the outlet 310 at least substantially free of dead volume. This will take effect avoided that 304 parts of the reaction medium are deposited above the rotor, which would lead to an undesired further polymerization by extending the residence time in the reactor.

Fig. 4 shows a particularly preferred embodiment of a Taylor reactor according to the invention, in which both alternatives of the invention are realized. The Taylor reactor, now designated 401, comprises a reactor housing 403 which corresponds to that shown in FIG. 1. The rotor 404 - like that in FIG. 3 - is provided with a cone 413 at its upper end.

In this particularly preferred embodiment, short-circuit currents in the reaction volume 402 and the formation of dead spaces in the outlet area 409 are avoided.

Claims

Expectations:

1. Taylor reactor (101, 201, 301, 401), with a reactor housing (103, 203, 303, 403), with a volume arranged in the reactor housing (103, 203, 303, 403) and rotatable about an axis Rotor (104, 204, 304, 404), with one between the inner peripheral surface of the reactor housing (103, 203, 303, 403) and the outer peripheral surface (104.3, 204.3, 304.3, 404.3) of the rotor (104, 204, 304, 404 ) formed reaction volume (102, 202, 302,

402), with at least one inlet (108.1, 208.1, 308.1, 408.1) for the educts and / or process substances, and with at least one outlet (110, 210, 310, 410) for the reaction products, which is in the direction of the axis (A) from the inlet (108.1, 208.1, 308.1,

408.1) is arranged at a distance, characterized in that the reactor housing (103, 203, 303, 403) and / or the rotor (104, 204, 304, 404) are equipped such that the cross section of the reaction volume (102, 202, 302 , 402) from the inlet (108.1, 208.1, 308.1, 408.1) to the outlet (110, 210, 310,

410) initially increases, the cross-sectional increase does not increase at least over part of the length of the rotor (104, 204, 304, 404).

2. Taylor reactor according to claim 1, characterized in that the rotor (104, 204, 304, 404) is arranged concentrically in the reactor housing (103, 203, 303, 403).

3. Taylor reactor according to claim 1 or 2, characterized in that the reaction volume (102, 202, 302, 402) is formed in an annular gap.

4. Taylor reactor according to claim 3, characterized in that the reaction volume (102, 202, 302, 402) is a circular

Scope.

5. Taylor reactor according to one of claims 1 to 4, characterized in that the decrease in the increase in the cross section of the reaction volume (102, 202, 302, 402) takes place continuously.

6. Taylor reactor according to one of claims 1 to 4, characterized in that the decrease in the increase in the cross section of the reaction volume (102, 202, 302, 402) takes place discontinuously.

7. Taylor reactor according to claim 6, characterized in that the reactor housing (103, 203, 303, 403) and / or the rotor (104, 204, 304, 404) in the direction of the axis (A) at least two

Have sections whose inner peripheral surface and / or outer peripheral surface form different angles to the axis (A).

8. Taylor reactor according to one of claims 1 to 7, characterized in that the ratio of the radius of the

Reactor housing (r _a ) to the radius of the rotor (η) at least for part of the length of the reaction volume (102, 202, 302, 402) is <1.4.

9. Taylor reactor according to one of claims 1 to 8, characterized in that the rotor (104, 204, 304, 404) is cylindrical.

10. Taylor reactor, with a reactor housing (103, 203, 303, 403), with a rotor (104, 204, 304) arranged rotatably about an axis (A) in the volume enclosed by the reactor housing (103, 203, 303, 403) , 404), with one between the inner peripheral surface (103.1, 203.1, 303.1, 403.1) of the reactor housing (103, 203, 303, 403) and the outer peripheral surface (104.3, 204.3, 304.3, 404.3) of the rotor (104, 204, 304, 404) formed reaction volume (102, 202, 302, 402), with at least one inlet (108.1. 208.1, 308.1, 408.1) for the starting materials and / or process substances, in particular according to one of claims 1 to 9, characterized in that an outlet area (109, 209, 309, 409) opening into an outlet (110, 210, 310, 410) is provided, which is located in the reactor housing

(103, 203, 303, 403) at one end of the rotor (104, 204, 304, 404) connects to the reaction volume (102, 202, 302, 402) and to an outlet (110; 210, 310, 410) narrowed, and that the front end of the rotor (104, 204, 304, 404) is designed such that the reaction volume (102, 202, 302,

402) opens into the outlet (110, 210, 310, 410) at least essentially without dead volume.

11. Taylor reactor according to claim 10, characterized in that the end face of the rotor (104, 204, 304, 404) is formed such that the cross section in the direction of the axis (A) of the outlet area (109, 209, ^' 309, 409) is at least substantially constant.

12. Taylor reactor according to claim 10 or 11, characterized in that the reactor housing (1093, 203, 303, 403) is designed such that the outlet region (109, 209, 309,

409) funnel-shaped and the front end of the rotor (104, 204,

304, 404) are conical.

13. Taylor reactor, with a reactor housing (503), with one in the one enclosed by the reactor housing (503). Volume rotatable about an axis (A) rotor (504), with a reaction volume (502) formed between the inner peripheral surface (503.1) of the reactor housing (503) and the outer peripheral surface (504.3), with at least one inlet (508.1) for the starting materials and / or process substances and with at least one outlet (510) for the reaction products, in particular according to one of claims 1 to 12, characterized in that the outlet (510) radially spaced from the axis (A) in the Reaction volume (502) opens.

14. Taylor reactor according to claim 13, characterized in that the outlet (510) opens transversely, preferably perpendicular to the axis (A) into the reaction volume (502).

15. Taylor reactor according to claim 13 or 14, characterized in that the region (B) of the rotor (504) adjacent to the outlet (510) comprises means for generating a circular flow about the axis (A).

16. Taylor reactor according to claim 15, characterized in that the region (B) of the rotor (504) adjacent to the outlet (510) is designed in the manner of a centrifugal pump rotor.

17. A method for converting substances in which the kinematic viscosity v of the reaction medium increases in the flow direction of the reactor, characterized in that a Taylor reactor according to one of claims 1 to 16 is used for this.

18. Use of a method according to claim 17 for the production of polymers, copolymers, block polymers, graft copolymers, polycondensation and polyaddition products, core-shell

Latices, polymer dispersions, of products by polymer-analogous reaction, such as esterification, aniation or urethanization of polymers which contain side groups which are suitable for such reactions, of olefinically unsaturated materials curable with electron beams or ultraviolet light, or of mesosphases.

19. Use of the substances produced by the method according to claim 17 as components of molded parts, films, coating materials, in particular paints, adhesives and

Sealants.