Device and method for producing powdered polymers

Abstract

An apparatus for production of pulverulent polymers having a reactor for droplet polymerization with an apparatus for dropletization of a monomer solution for the preparation of the polymer. The apparatus for dropletization has holes through which the monomer solution is introduced, an addition point for a gas above the apparatus for dropletization, at least one gas withdrawal point at the periphery of the reactor and a fluidized bed, wherein at least one of the following is fulfilled: an apparatus for increasing turbulence in the gas flow is disposed in the region of the apparatus for dropletization of the monomer solution, an apparatus for increasing turbulence in the gas flow is disposed in the region of the addition point for the gas, the addition point for gas is configured such that elevated turbulence is generated.
A process for producing pulverulent polymers, in which an increase in flow turbulence in the gas flow in the region of the apparatus for dropletization also is disclosed.

Claims

1. An apparatus for production of pulverulent polymers, comprising a reactor (1) for droplet polymerization with an apparatus for dropletization (5) of a monomer solution for the preparation of the polymer, said apparatus for dropletization (5) having holes through which the monomer solution is introduced, an addition point (13) for a gas above the apparatus for dropletization (5), at least one gas withdrawal point (19) at the periphery of the reactor (1) and a fluidized bed (11), wherein at least one of the following features is fulfilled: an apparatus for increasing turbulence (31) in the gas flow is disposed in the region of the apparatus for dropletization (5) of the monomer solution, an apparatus for increasing turbulence in the gas flow is disposed in the region of the addition point (13) for the gas, the addition point (13) for gas is configured such that elevated turbulence is generated.

2. The apparatus according to claim 1, wherein the apparatus for increasing turbulence (31) comprises baffles.

3. The apparatus according to claim 2, wherein the baffles comprise a perforated plate having holes having a diameter of 5 to 200 cm.

4. The apparatus according to claim 1, wherein the apparatus for increasing turbulence (31) comprises gas nozzles (35), gas/liquid nozzles or liquid nozzles.

5. The apparatus according to claim 4, wherein the gas/liquid nozzles or liquid nozzles used for increasing turbulence are part of the apparatus for dropletization (5) of the monomer solution.

6. The apparatus according to claim 4, wherein the gas nozzles (35) used for increasing the turbulence are oriented in direction to the addition point (13) for gas so that a gas jet exiting the gas nozzles (35) is oriented in opposite direction to the gas flow from the addition point (13) for gas.

7. The apparatus according to claim 4, wherein the number of gas nozzles (35), gas/liquid nozzles or liquid nozzles used for increasing turbulence is 0.02 to 2 per square meter of cross-sectional reactor area.

8. The apparatus according to claim 1, wherein the apparatus for increasing turbulence (31) is disposed in a region between 2 m above and 2 m below the apparatus for dropletization (5) and/or up to 2 m below the addition point (13) for gas.

9. The apparatus according to claim 1, comprising baffles, gas nozzles (35), gas/liquid nozzles or liquid nozzles for increasing turbulence (31) disposed at different levels in the reactor (1).

10. The apparatus according to claim 1, wherein the addition point (13) for gas comprises at least one perforated plate having holes having a diameter of 5 to 200 cm.

11. A process for producing pulverulent polymers in an apparatus according to claim 1, comprising: (a) dropletizing a monomer solution in the apparatus for dropletization (5), wherein the monomer droplets produced fall through the reactor (1) and the monomer reacts at least partly to give the polymer, so as to form particles, (b) supplying gas via the addition point (13) for gas above the apparatus for dropletization (5), so as to produce a gas flow from the top downward in the reactor (1), (c) collecting the particles produced in step (a) in the fluidized bed (11), wherein the reaction to give the pulverulent polymer in the individual particles is concluded and there is optionally postcrosslinking in the fluidized bed (11), (d) withdrawing the particles from the fluidized bed (11), wherein there is an increase in flow turbulence in the gas flow in the region of the apparatus for dropletization (5).

12. The process according to claim 11, wherein turbulence is increased using gas nozzles (35) and the ratio of the momentum flow rate of the gas supplied through all gas nozzles (35) to the momentum flow rate of the gas supplied via the addition point (13) for gas is in the range from 0.1 to 50.

13. The process according to claim 11, wherein turbulence is increased using gas/liquid nozzles or liquid nozzles and the ratio of the momentum flow rate which is generated through all nozzles to the momentum flow rate which is generated in the apparatus for dropletization (5) is in the range between 0.1 and 100.

14. The process according to claim 11, wherein turbulence is increased using gas nozzles (35) and the exit velocity of the gas from the gas nozzles (35) is in the range from 5 to 1000 m/s.

15. The process according to claim 14, wherein a gas jet exiting the gas nozzles (35) is oriented in opposite direction to the gas flow in the reactor (1) produced in step (b).

16. The process according to claim 11, wherein the addition point (13) for gas comprises at least one perforated plate having holes having a diameter of 5 to 200 cm, such that the gas exits from the addition point (13) for gas with elevated turbulence.

17. The process according to claim 11, wherein the pulverulent polymer is a poly(meth)acrylate.

Description

(1) Illustrative embodiments of the invention are shown in the figures and are explained in more detail in the following description.

(2) The figures show:

(3) FIG. 1 a longitudinal section through a reactor for droplet polymerization with an apparatus for increasing turbulence beneath the apparatus for dropletization,

(4) FIG. 2 a longitudinal section through a reactor for droplet polymerization with an apparatus for increasing turbulence above the apparatus for dropletization,

(5) FIG. 3 an arrangement of radial dropletizer channels of different length and apparatuses for increasing turbulence that are arranged between the channels,

(6) FIG. 4 an arrangement of dropletizer channels arranged in a star shape and apparatuses for increasing turbulence that are arranged between the channels,

(7) FIG. 5 an arrangement of dropletizer channels in rectangular pitch and apparatuses for increasing turbulence that are arranged between the channels,

(8) FIG. 6 an arrangement of dropletizer channels in triangular pitch and apparatuses for increasing turbulence that are arranged between the channels,

(9) FIG. 7 an upper section of a reactor for droplet polymerization, in which the addition point for gas is configured such that elevated turbulence is generated,

(10) FIG. 8 an upper section of a reactor for droplet polymerization having gas nozzles oriented upward as apparatus for increasing turbulence,

(11) FIG. 9 a plot of the standard deviation of the particle temperature as a function of the particle dwell time with and without use of an apparatus for increasing turbulence, where the dotted curve represents the case with and the solid curve the case without increasing turbulence,

(12) FIG. 10 a plot of the overall temperature as a function of the particle dwell time with and without use of an apparatus for increasing turbulence, where the dotted curve represents the case with and the solid curve the case without increasing turbulence.

(13) FIG. 1 shows a longitudinal section through a reactor for droplet polymerization, as used with preference for production of poly(meth)acrylate particles.

(14) A reactor 1 for droplet polymerization comprises a reactor head 3 in which an apparatus for dropletization 5 is accommodated, a middle region 7 in which the polymerization reaction is performed, and a lower region 9 comprising a fluidized bed 11 in which the reaction is concluded.

(15) The polymerization reaction for producing the poly(meth)acrylate is carried out by supplying the apparatus for dropletization 5 with a monomer solution via a monomer feed 12. When the apparatus for dropletization 5 has two or more channels, it is preferable to supply each channel with the monomer solution via a dedicated monomer feed 12. The monomer solution exits through holes, which are not shown in FIG. 1, in the apparatus for dropletization 5 and disintegrates into individual droplets which fall downward within the reactor. A gas, for example nitrogen or air, is introduced into the reactor 1 via a first addition point for a gas 13 above the apparatus for dropletization 5. This gas flow assists the breakup into individual droplets of the monomer solution exiting from the holes in the apparatus for dropletization 5. In addition, the gas flow promotes lack of contact between the individual droplets and coalescence thereof to form larger droplets.

(16) In order firstly to make the cylindrical middle region 7 of the reactor very short and additionally to avoid droplets hitting the wall of the reactor 1, the reactor head 3 is preferably conical, as shown here, in which case the apparatus for dropletization 5 is within the conical reactor head 3 above the cylindrical region. However, it is also possible as an alternative to provide the reactor with a cylindrical configuration in the reactor head 3 as well, with a diameter the same as that of the middle region 7. However, a conical configuration of the reactor head 3 is preferred. The position of the apparatus for dropletization 5 is selected such that there is still a sufficiently large distance between the outermost holes through which the monomer solution is supplied and the wall of the reactor to prevent the droplets from hitting the wall. For this purpose, the distance should at least be in the range from 50 to 1500 mm, preferably in the range from 100 to 1250 mm and especially in the range from 200 to 750 mm. It will be appreciated that a greater distance from the wall of the reactor is also possible. This has the disadvantage, however, that a greater distance is associated with poorer exploitation of the reactor cross section.

(17) In order still to obtain better exploitation of the gas supplied via the addition point 13, an apparatus for increasing turbulence 31 is used in accordance with the invention in the region of the apparatus for dropletization 5 of the monomer solution. The apparatus for increasing turbulence increases the turbulence of the gas, such that better mixing of gas and droplets generated by the apparatus for dropletization 5 is achieved. In this way, it is possible for the droplets to more homogeneously release water to the gas. In addition, a more homogeneous temperature distribution over the dwell time of the droplets in the reactor is obtained. The turbulence generated by the apparatus for increasing turbulence 31 is shown here by arrows 33.

(18) The apparatuses used for increasing turbulence 31 may, for example, be baffles or nozzles, especially gas nozzles, gas/liquid nozzles or liquid nozzles. In the embodiment shown here, the apparatus utilized for increasing turbulence 31 comprises gas nozzles 35. In the embodiment shown in FIG. 1, these are disposed beneath, preferably a maximum of 2 m beneath, the apparatus for dropletization 5. The gas jet 37 exiting from the gas nozzles 35 accelerates the gas fed in via the addition point for gas 13. At the same time, the gas exiting from the gas nozzles 35 is slowed down, as a result of which the gas jet 37 is deflected and deformed, such that additional turbulence is induced. It should be ensured here that the difference in velocity

(19) between the gas added through the addition point for gas 13 and the gas added through the gas nozzles 35 is not too great, in order that the turbulence generated is not dissipated by the friction that occurs.

(20) The lower region 9 is capped off with a fluidized bed 11 and the polymer particles formed from the monomer droplets during the fall, fall into said fluidized bed. The postreaction to afford the desired product is performed in the fluidized bed. According to the invention the outermost holes through which the monomer solution is dropletized are positioned such that a droplet falling vertically downward falls into the fluidized bed 11. This can be achieved, for example, by virtue of the hydraulic diameter of the fluidized bed being at least as large as the hydraulic diameter of the area which is enclosed by a line connecting the outermost holes in the apparatus for dropletization 5, the cross-sectional area of the fluidized bed and the area formed by the line connecting the outermost holes having the same shape and the centers of the two areas being at the same position in a vertical projection of one onto the other. The outermost position of the outer holes relative to the position of the fluidized bed 11 is shown in FIG. 1 using a dotted line 15.

(21) In order, in addition, to prevent droplets from hitting the wall of the reactor in the middle region 7 as well, the hydraulic diameter at the level of the midpoint between the apparatus for dropletization and the gas withdrawal point is at least 10% greater than the hydraulic diameter of the fluidized bed.

(22) The reactor 1 may have any desired cross-sectional shape. However, the cross section of the reactor 1 is preferably circular. In this case, the hydraulic diameter is the same as the diameter of the reactor 1.

(23) Above the fluidized bed 11, the diameter of the reactor 1 increases in the embodiment shown here, such that the reactor 1 widens conically from the bottom upward in the lower region 9. This has the advantage that polymer particles that are formed in the reactor 1 and hit the wall can slide downward along the wall into the fluidized bed 11. To avoid caking, it is additionally possible to provide tappers, not shown here, with which the wall of the reactor is set in vibration, as a result of which adhering polymer particles are detached and slide into the fluidized bed 11.

(24) For gas feeding for the operation of the fluidized bed 11, a gas distributor 17 beneath the fluidized bed 11 blows the gas into the fluidized bed 11.

(25) Since gas is introduced into the reactor 1 both from the top and from the bottom, it is necessary to withdraw gas from the reactor 1 at a suitable position. For this purpose, at least one gas withdrawal point 19 is disposed at the transition from the middle region 7 having a constant cross section to the lower region 9 which widens conically from the bottom upward. Here, the wall of the cylindrical middle region 7 projects into the lower region 9 which widens conically in the upward direction, the diameter of the conical lower region 9 at this position being greater than the diameter of the middle region 7. In this way, an annular chamber 21 which encircles the wall of the middle region 7 is formed, into which the gas flows and can be drawn off through the at least one gas withdrawal point 19 connected to the annular chamber 21.

(26) The further-reacted polymer particles of the fluidized bed 11 are withdrawn via a product withdrawal point 23 in the region of the fluidized bed.

(27) FIG. 2 shows a reactor for droplet polymerization in an alternative embodiment.

(28) By contrast with the reactor for droplet polymerization 1 shown in FIG. 1, the apparatus for increasing turbulence 31 in the reactor 1 shown in FIG. 2 is disposed above the apparatus for dropletization 5 of the monomer solution. In FIG. 2 as well, gas nozzles 35 for increasing turbulence are shown by way of example. The gas jet 37 that exits from the gas nozzles 35 increases the turbulence in the gas flow, and the increase in turbulence in the case of gas nozzles 35 disposed above the apparatus for dropletization 5 sets in at a higher position than in the variant shown in FIG. 1 with gas nozzles 35 beneath the apparatus for dropletization 5. In the adjustment of the turbulence, it therefore has to be ensured that the monomer droplets that leave the apparatus for dropletization 5 do not hit the apparatus for dropletization 5 and thus lead to formation of deposits. Especially in the case of use of gas nozzles 35, it is possible to adjust the turbulence in a simple manner by altering the velocity of the gas leaving the gas nozzles 35.

(29) In order, more particularly, in the case of an apparatus for increasing turbulence 31 disposed beneath the apparatus for dropletization 5, to prevent formation of a deposit on the apparatus for increasing turbulence 31, the individual baffles or nozzles of the apparatus for increasing turbulence 31 are positioned such that they are arranged between the individual dropletizer units of the apparatus for dropletization 5. This is shown by way of example for the use of gas nozzles 35 as the apparatus for increasing turbulence 31 and dropletizer channels 25 as dropletizer units of the apparatus for dropletization 5 in FIGS. 3 to 6.

(30) FIG. 3 shows an arrangement of radial dropletizer channels of different length.

(31) In a first embodiment, the apparatus for dropletization has radial channels 25. In this case, one portion of the channels 25 projects into the middle of the reactor 1. A further portion of the channels 24 projects less far into the reactor 1, and so, especially in the outer regions of the reactor where the distance between the radial channels 25 projecting into the middle of the reactor 1 is high, further channels 24 through which monomer solution can be introduced into the reactor 1 are provided. This allows more homogeneous distribution of the droplets over the total reactor cross section.

(32) The individual gas nozzles 35 which are used for increasing turbulence are positioned between the channels 24, 25. In this case, for homogeneous turbulence and hence a homogeneous gas flow in the reactor, the gas nozzles 25 are distributed homogeneously over the reactor cross section.

(33) A corresponding star-shaped arrangement of the channels 25 is shown in FIG. 4.

(34) Both in the case of the embodiment shown in FIG. 3 and in the case of that shown in FIG. 4, it is possible to align the channels 24, 25 at an angle β to the horizontal. For this purpose, it is especially advantageous when the channels 24, 25 rise toward the middle of the reactor. This alignment affords a more homogeneous distribution of the droplets in the reactor 1 and prevents premature contact of the droplets with the reactor wall.

(35) Further possible arrangements of the channels are shown in FIGS. 5 and 6. In these, however, an arrangement with an angle β to the horizontal can be achieved only with difficulty, such that the channels 25 in this case preferably run horizontally. FIG. 5 shows an arrangement in rectangular pitch, in which the individual channels 25 are each arranged at an angle of 90° to one another, such that the points of intersection 27 of the channels each form rectangles, preferably squares.

(36) FIG. 6 shows an arrangement in triangular pitch. The channels 25 here are each arranged at an angle of 60° relative to one another, such that the points of intersection 27 of the channels 25 each form equilateral triangles. However, this additionally requires the channels that run parallel in each case always to have an equal separation.

(37) Irrespective of the arrangement of the channels 25 that are used as dropletizer units, the baffles or nozzles, for example the gas nozzles 35, are positioned in homogeneous distribution over the reactor cross section between the dropletizer units. In the case of rectangular pitch or triangular pitch, the position of the baffles or nozzles in each case is preferably at the center of the rectangles or triangles formed by the channels 25.

(38) The necessary supply of gas and/or liquid is preferably via conduits 39 which, in the case of an arrangement as shown in FIGS. 3 and 4, run between the channels 24, 25, or, in the case of an arrangement as shown in FIG. 5 or 6, run above the channels 25, in order to prevent droplets generated in the apparatus for dropletization 5 from falling onto the conduits 39 and leading to formation of deposits there.

(39) As an alternative to the embodiments shown here, it is of course also possible to arrange the channels such that the distance between channels arranged in parallel varies, or the distance between the channels arranged in parallel is equal in each case but the distances between the channels that are arranged in parallel and run in different directions are different. In addition, it is also possible to arrange the channels at any other angle relative to one another.

(40) Especially in the case of a circular reactor cross section, however, preference is given to the arrangements shown in FIGS. 3 and 4. In this case, however, the number of channels may vary as a function of the circumference of the reactor. In addition, it is possible to configure the channels with different lengths, as shown in FIG. 3, such that they project into the reactor 1 to different extents. However, a rotationally symmetrical arrangement is always preferred.

(41) The position of dropletizer plates 26 which conclude the channels for supply of the monomer solution at the base thereof, and in which the holes through which the monomer solution is dropletized into the reactor are formed, is shown in FIGS. 3 to 6 by the dotted areas.

(42) According to the invention, the number of channels 24, 25 is selected such that the ratio of the area covered by the channels 24, 25 or the dropletizer head in the reactor relative to the area which is defined by the circumference of a line along the outermost holes is less than 50%. This ensures that sufficient gas can flow past the channels 24, 25 and adequate contact between gas and droplets leaving the channels 24, 25 is achieved.

(43) A further means of generating elevated turbulence in the gas flow is shown in FIG. 7. Here, by contrast with the embodiments in FIGS. 1 to 6, the addition point for gas 13 is configured such that elevated turbulence is generated. For this purpose, the addition point for gas 13 comprises at least one perforated plate 41 through which the gas is guided. The perforated plate has holes having a hydraulic diameter of 5 to 200 cm, preferably of 10 to 100 cm. It is particularly advantageous when two or more perforated plates are arranged one on top of another and at least the last perforated plate in flow direction of the gas, as described above, has holes having a hydraulic diameter of 5 to 200 cm. The perforated plates are preferably arranged such that the holes of the individual perforated plates are not exactly one on top of another. This means that the centers of holes lying one on top of another are not on a vertical axis.

(44) The shape of the holes can be chosen as desired. However, preference is given to circular holes.

(45) In the case of configuration of the addition point for gas 13 such that elevated turbulence is generated, the gas flow already has turbulence 33 above the apparatus for dropletization 5, which leads to a more homogeneous distribution of the droplets generated in the apparatus for dropletization 5 over the reactor cross section. However, the increase in turbulence is to be locally limited and is preferably to be effective only in the region of or beneath the dropletizer units. This ensures the desired improvement in mixing of the drying gas with the monomer solution introduced in droplet form and results in more homogeneous distribution of the droplets over the reactor cross section, without resulting in unwanted effects such as formation of deposits on the reactor wall.

(46) A preferred embodiment of the apparatus for increasing turbulence is shown in FIG. 8.

(47) In difference to the apparatuses for increasing turbulence as shown in FIGS. 1 and 2 with gas nozzles 35 being oriented downward, in FIG. 8 the gas nozzles 35 are oriented vertically upward. Thus, a gas jet 37 exits each gas nozzle 35 which is directed opposite to the flow direction of the drying gas applied via the addition point for gas 13. Due to the gas exiting the gas nozzles 35 in opposite direction to the gas flow of the drying gas turbulence 33 is generated in the region of the apparatus for dropletization 5. As the drying gas is the mean gas stream, the total gas flow is directed downwards and the drying gas flow remains turbulent in direction of flow of the drying gas while streaming past the apparatus for dropletization 5. Due to the orientation of the gas nozzles 35 vertically upward the turbulence is induced further upstream of the apparatus for dropletization 5. As a result the transverse spreading of the turbulence in the drying gas flow down to the apparatus for dropletization 5 is improved and thus can influence the monomer solution exiting the apparatus for dropletization 5 more effectively and more uniformly.

(48) Irrespective of the arrangement of the dropletizer units, the baffles or nozzles of the apparatus for increasing turbulence 31 are always positioned such that no droplets can fall onto the baffles or nozzles. In addition, the baffles or nozzles are arranged in homogeneous distribution over the reactor cross section, in order to obtain a homogeneous gas flow and equal turbulence over the entire reactor cross section, in order that a homogeneous product is formed.

EXAMPLE

(49) The example which follows shows a comparison of the operation of a droplet polymerization reactor with and without generation of turbulence in the gas flow. For the comparison, results which have been determined by computer with the aid of numerical flow simulation have been cited. Two cases are considered in the comparison:

(50) (1) Operation of a reactor for droplet polymerization as shown in FIG. 1 with 16 gas nozzles for increasing the turbulence, with the gas nozzles each distributed homogeneously over the circumference on two theoretical concentric circles having diameters of 3.8 and 5.8 m and in symmetrical arrangement based on the dropletizer channels, and with 8 gas nozzles positioned on each of the concentric circles. For this purpose, 8 dropletizer channels are envisaged, which are arranged in a star shape in accordance with the embodiment shown in FIG. 4. The gas volume flow rate through all nozzles together is 7500 m.sup.3 (STP)/h. The nozzles have an orifice diameter of 45 mm. The diameter in the middle portion of the reactor with constant hydraulic diameter is 10.3 m. The diameter of the reactor at the level of the dropletizer units is 7.2 m. The gas volume flow rate which is applied by the addition point for gas 13 is 175 000 m.sup.3 (STP)/h.

(51) (2) Operation of the droplet polymerization reactor under the same conditions as in the first case, but without turbulence nozzles and the additional gas stream thus fed in.

(52) FIG. 9 shows, for both cases computed, the plot of the standard deviation of the particle temperature as a function of the particle dwell time, the plot for the first case with gas nozzles for increasing turbulence being shown by a dotted line and the plot for the second case without increasing turbulence by a solid line. For this purpose, the particle dwell time in seconds is shown on the abscissa and the standard deviation on the ordinate. The higher the standard deviation, the less homogeneously the particles are heated. In the dwell time range from 0 to 6 s, the standard deviation in the case of operation with turbulence nozzles is up to 5 K less than in the case without turbulence nozzles. The dwell time of 6 s corresponds to the average time that the particles take to reach the fluidized bed at the lower end of the reactor.

(53) FIG. 10 shows the gas temperature of the gas surrounding the particles along their trajectory as a function of the particle dwell time. Here too, the particle dwell time is shown in seconds on the abscissa. The ordinate shows the temperature of the gas surrounding the particles in ° C. Here too, the first case with gas nozzles for increasing turbulence is shown by a dotted line and the second case without an additional increase in turbulence by a solid line. In the case of operation with gas nozzles for increasing turbulence, the gas temperature drops more quickly, which means that the particles are heated more quickly on average. Both the standard deviation of the particle temperature and the gas temperature of the gas surrounding the particles along their trajectory show that the drying of the particles in operation with gas nozzles for increasing the turbulence proceeds more homogeneously and quickly, the effect of which is that the particles reach the fluidized bed at the lower end of the reactor in a drier state and hence have a lower tendency to agglomerate.

LIST OF REFERENCE SIGNS

(54) 1 reactor for droplet polymerization 3 reactor head 5 apparatus for dropletization 7 middle region 9 lower region 11 fluidized bed 12 monomer feed 13 addition point for gas 15 position of the outermost holes in relation to the fluidized bed 17 gas distributor 19 gas withdrawal point 21 annular chamber 23 product withdrawal point 24 channel 25 channel 26 dropletizer plate 27 point of intersection of the channels 29 reactor axis 31 apparatus for increasing turbulence 33 turbulence 35 gas nozzles 37 gas jet 39 conduit 41 perforated plate