DE2105056C3 - Reactor and its use for the treatment of viscous starting materials - Google Patents

Description

16. Reactor according to one of claims 1 to

15, characterized in that the guide surfaces (64) have an aircraft wing-like profile.

17. Reactor according to one of claims 1 to

16, characterized in that the means of supplying the mass at the outer edge of the production room and the conveying means for removing the Mass are arranged in the middle of the production room.

18. Use of a reactor according to one of claims 1 to 17 as a heat exchanger for viscous masses with or without chemical reaction for cooling and / or heating.

19. Use of a reactor according to one of claims 1 to 17 as a mixer for .nehrere highly viscous masses or for mixing solids into highly viscous masses.

The invention relates to a reactor for treating viscous Ausgar.gsmassjn with heating and steam generation, the reactor being in the form of a vertically standing container with an annular Jacket cross-section and with a substantially frustoconical tapering downwards Bottom has circumferential, radially extending agitator arms and agitator blades axially protruding from these a drivable agitator with a vertical shaft in and continuously fed into the reactor Immerse the discharged mass, the liquid level of which is constant at least at the mass inflow of the reactor is automatically regulated to a predetermined level, with the agitator arms and those attached to them Agitator blades over most of their agitation area in that of the frustoconical reactor bottom Formed production space are housed, with the beginning near below the liquid level The agitator blades protrude close to the frustoconical reactor floor and are radial over their axial length Form gaps between them, through the ring-shaped and provided with passage openings, partitions connected to the bottom of the reactor the concentric Rcaktorwelle run and serve as braking elements for the mass flowing radially through the passage openings, and further wherein the reactor bottom near its upper edge to a circumferential, outer bottom ring of the production room is designed with at least one or more floor openings and the agitator arms carry scrapers that engage in the bottom ring.

A reactor of this type is the subject of patent 1,813,956. The invention relates to another Training of this reactor and its use.

The reactor according to the main patent is particularly suitable for the treatment of polymeric products, such as polyamides, e.g. B. Polycaprolactam, and polyesters formed that polymerize when heated or condense in the reactor with the development of vapor drawn off under vacuum ίο. the In the main patent, the design of the agitator blades is primarily for highly viscous or highly viscous masses determined whose viscosity increases due to the water or vapor deposition in the reactor, in particular Masses in the range of viscosities between 300 and 5000 poise (when using the mass). for Masses in this viscosity range were identified as stirring flights in the main patent! uninterrupted surfaces used, which are quite close to the side walls and the bottom of the ring channels of the production room connected.

It has now been shown, however, that especially in the range of viscosities above 50 (X) poise and z. B. up to 20 0 (X) poise (when using the mass), as occurs above all with polycondensation products, the stirring effect, especially the evaporation, is not satisfactory. if undecorated propeller blades be used: because it then exists at higher viscosities of the mass, especially against End of the treatment process, the risk that the agitator blades the mass more or less than in itself Push the closed ring in front of you without the agitation required for the treatment To generate the impeller in sufficient measure, which according to the main patent as an essential result the invention: should occur.

In order to achieve a satisfactory double turbulence and circulation of the mass even at high viscosities, in particular over 10 (XX) poise, the agitator blades and / or the agitator arms of the reactor must be provided with openings for the passage of the material to increase its agitation and mixing as is the subject of additional patent 1939 412 to main patent 1813 956. This proposal points the right way to the desired goal, but does not yet show what it is ^; the dimensioning of the cross-sectional size of the openings of the agitator blades is important in order to generate an optimal circulation movement for the evaporation of the mass at different viscosities.

Experiments have led to the finding for a reactor of the type mentioned that one the desired optimal Umwälzbevvendung obtained by the fact that the agitator blades with one or more through openings of such a size that the relative to the circumferential wings along the ring channels formed by the partition walls running flow of the mass in an area leading the agitator blades in the direction of rotation, which ends in front of a propeller, is divided and only partially over the Rührarmc and / around other part passes under them.

According to the main patent, however, could

Mass flow under the agitator arms

not due to the lack of openings in the wings

take place and the entire relative current had to take place

go over this to the agitator arm while a

Part of the mass no such relative motion at all executed, but pushed away over the bottom of the ring channel assigned to the agitator blade would. The latter appeared in the aforementioned proposal of the first supplementary application Fixed; however, according to this proposal, especially at lower viscosities and relatively large openings in the impellers are undesirable Possibility that no significant mass flow went over the agitator arms and the overturning movement was too low.

According to the invention, on the other hand, the cross section of the openings of the agitator blades should depend on the toughness the mass to be treated can be chosen so that the above-mentioned division of the flow adjusts, namely by backing up the mass in front of the agitator blades.

Preferably, the cross-section of the openings of the agitator blades is chosen so small that through the Back pressure of the mass in front of the agitator blades and in front of the leading edge of the agitator arms an initially in the direction of rotation, then to the coding of the ring channel and back to the leading edge Eddy or circulating flow of the mass is formed and behind this edge one over the agitator arm passing, boundary-layer-like partial flow branches off, which is also near the leading edge with Whirling begins.

Both the aforementioned division of the relative flow into partial flows above and below the agitator arm on its own as well as in connection with the latter circulating currents is very advantageous, because in front of, above and behind the agitator arm there is a significantly larger movement and surface area the mass and both mainly for evaporation under vacuum and / or heat exchange with the heated bottom of the reactor is extremely desirable. It is not, however necessary that the said circulation and / or the division of the flow at or in front of the leading one Edge of the agitator arm is generated; it is also possible to have a stirring arm that is wide in the direction of rotation with one or more passage openings immediately or a little in front of the associated impeller to be provided and to begin the upper partial flow at this passage above the agitator arm and let it flow away over it.

The main advantage of the invention is that even masses of great toughness in excess of 5000 poise and treated satisfactorily up to the order of magnitude of 20,000 poise, especially at a relatively lower level Time can be evaporated, resulting in a favorable uniform residence time spectrum. Regardless of these particular advantages in the case of viscous masses, particularly high viscosity, the Reactor with similar advantages, e.g. to shorten the treatment time of the mass or to improve it of the residence time spectrum can also be used for masses of low viscosity below 5000 poise. Furthermore, it has been shown that the reactor according to the invention is not only suitable for the evaporation of Synthetic resin compounds, such as condensation products or polymerization products, are suitable, but also inexpensive as a heat exchanger for other viscous masses with or without chemical reaction, e.g. B. for syrups, Sugar masses, basic foodstuffs, tar products, asphalt for cooling and / or heating can be used. In the case of cooling, the double jacket of the reactor is used instead of a heating means suitably charged with a flowing coolant. The reactor is also suitable for pre-drying of cellulosic masses, e.g. B. in the context of papermaking, with the dehydration then then z. B. is only necessary to a small extent on the paper machine.

Another advantageous field of application of the reactor is its use as a mixer for several highly viscous masses introduced into it with one another or for mixing in dyes, pigments, Stabilizers.

In most applications, the mass is preferably centrally in the operation of the reactor lower bottom part, e.g. introduced by means of a pump via a screw, radially outwards through the passage openings of the dividing walls of the production room and in the upper edge of this The space is discharged by subsidies.

ao The operation of the reactor can, however, also be carried out so that the mass on the outside The edge of the production room is supplied, radially inwards through the openings in the partition walls guided and in the middle by funding, z. B. a screw is discharged.

In the attempts to adapt the reactor according to the invention to the viscosity of the mass being treated, it has been found to be advantageous if the cross section of the openings of the agitator blades

According to the viscosity of the mass at viscosities of more than 5000 poise more than half of the Surface area of each impeller. The agitator blades can expediently cut out from the floor of the ring channel, whose passage transverse

each section is greater than half the active surface of the impeller. Is the viscosity of the If the treated mass is less than 5000 poise, each impeller should preferably have only one opening have for the passage of the lower partial flow, the cross section of which is smaller than half of the active The surface of the impeller is and expediently 20 to 40 ° o of this surface.

It is possible to make the cross-sectional size of the openings of the agitator blades variable.

chen so that, depending on the requirements of the buyer, several different types of reactor are not kept in stock need to be replaced, rather only individual parts of the reactor need to be replaced.

In this sense, agitator parts that the Determine the cross-section of the openings of the agitator blades to change these opening cross-sections be exchangeable for agitator parts, which determine the larger cross-sections, the greater the toughness of the mass to be treated. It can e.g. B. the openings in the agitator blades - and also the openings in the dividing walls of the agitator channels - by changing the agitator blades as required can be set differently. Instead, the entire agitator element located in the production room can be used be exchangeable for an agitator element in which the openings of the agitator blades are so have larger cross-section, the greater the toughness of the mass to be treated and in which the Shape of the agitator blades of the conicity, d. H. the cone angle of the reactor bottom according to the viscosities should be chosen differently and this angle also depends on the

while time can be made dependent on the masses; its top up out and along this

there is therefore generally the last-mentioned upper rope extending backwards, with the separating

Possibility to exchange the entire stirrer or guide surfaces in alignment with the walls of the ring channels

Agitator member only in a certain range of for the circulating currents formed at the dividing point

Viscosities in which 'the cone angle 5 of the upper partial flow provided,

should remain the same. In the drawing are fillings from

The reactor according to the invention is also suitable for reactors according to the invention and processes

For example, shown for multi-stage continuous evaporation of mass of their application, namely

sen, which shows an increasingly increased viscosity

echo. It can therefore be a reactor according to the invention io Fig. 1 the general structure of the improved

for all stages of treatment of the mass, e.g. B. Aus reactor in a vertical section through its axis,

damping, in principle the same according to the invention, partly schematically, in its structure essentially

appropriate design can be used. In this case, according to Fig. I of the main patent,

are preferably only the Kegehvinkcl of the Renk- hen from the agitator blades, which according to a first

door bottoms and the cross-sections of the agitator vane openings.

gen \ on increasingly chosen step by step. forms are.

While after the main sponsorship registration a F i g. 2 on a larger scale and with the same representation

times. only according to the strength requirements as shown in FIG

struicrtc and therefore relatively narrow, radial stirrer according to FIG. 1 with additional details

tapered agitator arms are shown, the invent 20 of these parts, which in the embodiment according to FIG

proper aim of dividing the flow of occurrences,

Mass are preferably favored because «Fig. 3 is a side view of the stirrer of the

the agitator arms as guide surfaces for the reactor according to FIG. 1, with parts of the reactor walls

outgoing mass partial flow with at least the fertilizer indicated by dash-dotted lines,

Upper side of the aircraft carrier surface-like profile from FIG. 4 shows a plan view of the stirrer

are formed, they are then in the direction of rotation Fig. 3,

relatively wide. F i g. 5 schematically in an angled

For similar reasons, the cut along the line AD in FIG. 3, which in the upstream flow is expediently at least the catching direction, through an agitator blade in the top of the trailing end of the agitator arm 30 connection with a guide surface and a Dar against the bottom of the associated ring channel towards the position of the flow loop above and below tapers, preferably so that the profile curvature half of the propeller,

The top and bottom of the agitator arm in FIG. 6 in a section corresponding to FIG. 1 Impeller passes over. This results in a different embodiment of the present invention Dead spaces of the flow in front of and behind the 35 present invention, with regard to the impeller Avoided impellers, which are very undesirable. and the guide surfaces is modified.

The speed of the agitator blades or the whole F i g. 7 shows the stirrer according to the embodiment

The agitator also depends on the viscosity of the F i g. 6 in side view,

acting mass and the type of hand- F i g. 8 shows a plan view of the stirrer according to FIG

process. The speed can be used for mixing. 4 "Fig. 7 and

Heating and cooling operations in the range of 1000 poise Fig. 9 is a developed sectional view along line to 5000 poise about ten revolutions per minute A'-B 'of FIG. 6 (by the impeller), which in Umbetragen. During evaporation processes, e.g. B. polyester, running in the direction of catch, in connection with a guide and a viscosity of up to 3000 poise has a surface and a representation of the flow and speed of not more than \ ier revolutions per 45 below and above the impeller.
Minute proved to be expedient because andcrcniaiN the Da F i g. i and 6 the general structure of the power expenditure becomes undesirably large without improving the reactor, apart from the formation of the Ruhr efficiency. For such evaporation blades and associated parts, ir. The masses should therefore show viscosities over 3000 with the main patent, a speed of four revolutions is expedient in the drawing poises, especially in FIGS. 1 and 3 and 4 . for the revs per minute or less, parts of the den that correspond to the main patent are used. This ensures that the reactor is treated gently with the same reference symbols for the product. Embodiments of the invention used.

Since the tangentialc circumferential speed of the According to all the illustrated exemplary embodiments The reactor consists of two main parts, the un-ring channels proportional to the radius is larger than part 1 with the production space 15 and liquid the inner ring channels, should preferably be the keitssumpf. and the top 2 with the steam size the cross-sectional openings of the agitator blades per room. Both parts of the reactor have a Dop impeller from ring channel to ring channel different pel jacket 3 for the circulation of a heating fluid Be selected so that the cross-sectional size 60 or of heating steam, its inflow and out openings of the agitator blades from the radially innermost flow connection are not shown. The reactor parts to the radially outermost ring channel increases. are liquid- and vacuum-tight by means of flanges 4

In the preferred embodiment of the invention, interconnected.

isi the agitator arm at its leading end. The upper part of the reactor has a

as forward-facing, the division of the currents 65 occurs 5, to which a capacitor and a; · Ya-

in two partial flows supporting cutting edge aus- kuumquelk for condensation and rejection ckr

The Rührarmc are also formed in front of the to be treated in the reactor during the evaporation

rarcilcndc front end protruding and connected via ground. For mixed and heating

ίο

Transfer treatment of the mass without vacuum evaporation the condenser can often be omitted and the vacuum pump simply by suction be replaced.

The main part of the reactor floor 6, which forms the production space, is frustoconical.

In the illustrated embodiments, the cone angle of the reactor bottom for the treatment of masses with initial viscosities of over 300 poise is an acute angle, for viscosities of up to 20,000 poise and more, a larger cone angle of the reactor bottom is preferable, as in the main patent in FIGS 7 is shown, but is not shown in the embodiment according to FIGS. 6 to ^ for the sake of simplicity. because this version is intended for lower mass viscosities below 5000 poise! is, but depending on the type of use of the reactor z. B. as a mixer or heat exchanger or other physical and chemical purposes also according to the embodiment according to FIG. 6 to 9 an obtuse cone angle can be used for the reactor bottom.

The mass to be treated is fed through an inlet nozzle by means of a pump 8 to be provided with a motor 7 9 fed to a filling pipe 10, the upper end of which opens in the middle of the reactor bottom. The lower end of the tube 10 is closed by means of a vacuum gland 11 and forms the Bearing for a drive shaft 13, which is designated as a whole by 14, driven by a motor 12 Stirrer, which is attached in the production room 15. Between the lower end 16 of the hub 17 of the • Stirrer and the gland 11 can be the drive shaft 13 in the pipe 10 as a screw conveyor 18 for the mass to be continuously fed to the reactor be designed if this has high toughness and the delivery rate of the pump 8 is not sufficient. The conveyed mass passes through a central opening of the base 6 and the hollow hub 17 permanent annular channel 19, furthermore through openings 22 at the lower end of the hub 17, into the stirrer.

The agitator consists essentially of, for example, three agitator arms 20 (see FIGS. 4 and 3) which extend radially outward from the conical hub 17, and agitator blades 21 which are attached to the underside of the agitator arms. The hollow hub 17 has on the upper. End of outlet openings 23 (see FIGS. 4 and 3) for the mass supplied to it. The inflow of the mass is adjusted and automatically controlled by the speed-controlled gear pump 8 and the speed of the drive 7 in accordance with the viscosity of the mass that a liquid level 24 is a short distance from z. B. sets a few millimeters above the top of the agitator arms 20, as indicated by a dashed line in F i g. 1 is indicated as the resting level.

The wings 21 extend from the agitator arms to close to the top of the reactor bottom 6 and taper from the outside inwards in accordance with the cone angle of the reactor bottom. They are arranged at radial distances from one another. Annular partition walls 27, which are fixedly connected to the base 6 and are provided with passage openings 28 near the base, protrude into these distances. These partitions serve to slow down the centrifugal effect exerted on the mass by the stirrer 14 by forcing the mass to flow through the narrow openings 28. The partition walls 27 also form self-contained, concentric annular channels 55, the bottom of which is formed by the reactor bottom 6.

F i g. 1 and 3 to 5 show a first embodiment of the agitator blades 21, in which openings 43 are provided in the form of cutouts of the agitator blades which cover more than half the surface, about 70 to 80 "Ό of the surface of each agitator blade. Openings of this size are preferably intended for higher viscosities of the mass to be treated, in particular viscosity; r η over 5000 poise. A central tongue 61 and an edge part 62 of each agitator blade are formed by the cutouts 43, which form the base 28 or the partition walls 27 or the top the agitator arm 20. In the agitator blades adjacent to the hub 17, a central tongue 61 is omitted of the cone angle of the bottom ό increases ity of the agitator blades increases proportionally to the distance from the central axis of the agitator 14, but in general the mass passing through the agitator blades in each; the ring channels 55 must be the same in the unit of time (except when the scrambled egg starts up or when the mass is first poured in).

On the right side of the FIG. 1 are the agitator blades 21 and the stirring arms 20 are omitted to the Formation of the ring channels 55 to illustrate Fig. 1. 3,4 and 5 / own that each above a partition wall 27 on the upper side 59 each, the agitator arms 20 each have a guide surface 64 is attached. which is roughly the profile of an aircraft carrier surface and extends over the front end 56 of the agitator arm protrudes and also slightly to the rear via the end 57 of the agitator arm which is lagging behind during rotation can protrude. According to FIG. 5, in this embodiment, the agitator blade 21 is seated in the rear Area of the underside of the agitator arm, the front end 56 protruding in front of the agitator arm and the Rear end 57 flush to the rear and curved into the rear of the impeller.

As with the Hauptpatenl, the reactor floor is formed near its upper edge to a circumferential outer floor 30, which forms the outermost part 31 of the product tone space and has a substantially horizontally extending floor part 30 α and a vertically extending wall part 30 ft which delimits the production space and with Angle hanging in the flange 4 of the lower part of the reactor? transforms.

In the ring-shaped bottom part 30 ″ there is at least! a discharge opening 32 is attached for the product. The outer ends of the agitator arms 20 carry on dei

Side scraper 33 covering most of the spaces; 31 and take on parts 30 a and 30 h de; Stroke along floor length 30. The one in room 31 revolving parts of the scraper 33 are, as in particular special Fig.3 and 7 show, ausgehuid from the

Ruhr arms are inclined downwards at an acute angle to their circumferential axis and backwards to the circumferential direction a, in order to improve the conveying effect of these scrapers for the material to be discharged.

A discharge pipe connects to the discharge opening 32 34 at. in which a discharge · '-ilineckc 35 circulates, which is also directly to the discharge opening 32 connects. The discharge screw 35 and the discharge pipe 34 go through a connector 29. the liquid-tight jacket of the reactor against the pipe at a nozzle 39 completes, and through a heating jacket 26, which is connected to the connecting part 29 by means of a connecting flange 29 «is connected. The inlet and outlet supports for the heating fluid wedge or steam of the Heating jacket 26 are omitted from the drawing. The screw is driven by a motor 37, the housing of which is connected to the heating jacket, which is closed at the lower and upper ends. The product discharged from the discharge screw passes through the heating jacket 26 and an outlet nozzle 38 and is used by this in the direction of the arrow to a storage space or further treatment, e.g. B. in a downstream reactor of the same design. fed.

Are in a bottom ring 30 several discharge openings 32 attached, so is for each of these discharge openings one discharge screw 35 each with the corresponding associated parts 34, 26, 29, 29 k and 37 to 39 are provided.

As can be seen, the mass in production ¹ , room 15 receives a centrifugal acceleration from the stirrer 14, by means of which it passes through the openings 28 and over the agitator arms 20 into the edge area 31 of the production room during the evaporation M in the middle area of the production room . Here, the steamed product is grasped by the scrapers 33 and continuously fed to the discharge screw 35 or the discharge screw 35. These ensure that on parts 30 α and 30 /? of the bottom ring 30 do not form any deposits of the product, even in the conical part of the bottom 6 and on the partition walls 27 due to the centrifugal flow of the mass and the agitating action of the agitator blades 21 and Rü'iiarme20. as well as on these themselves.

The liquid level 24 is in this process in a known manner automatically to a lower height of a few millimeters over the agitator arms with the help of a z. B. optical and / or electrical discharge device which controls the delivery rate of the pump 8 on its motor 7 in a manner known per se.

As a result of the vapor deposition and the action of the stirring arms 20, bubbles that break open at the liquid level 24 and splashes of the mass can occur above the scrapers 33, which could undesirably settle on the inner wall of the reactor. To prevent this, a splash guard ring 42 is placed on the angled portion of the bottom ring 30 on the outer edge of the reactor bottom, which protrudes above the liquid level and overlaps the bottom. Furthermore, the scrapers 33 have parts 33a protruding towards the splash guard ring 42 via the agitator arms. which act as a scraper on the inside of the protective ring and also prevent the deposition of mass on this and 7. B. have the shape of a round rod.

Apart from the construction and mode of operation of the agitator blades 21 and agitator arms 21, the construction and mode of operation described above is essentially the same as in the main board application. The essence of the l'rligation, however, lies precisely in the improved construction and mode of operation of the agitator blades and the agitator arms, which for the embodiment according to FIGS. 1 and 3 to 5 can best be found in FIG. 5. results.

According to FIG. 5 is the cross-sectional profile of the agitator arm similar to the profile of an airplane wing and forms the surface 59 of the agitator a guide surface for the partial flow 65, which over the Arm goes away. The division into partial flows 65 and 66 of the opposite to the direction of rotation 67 of the Agitator 20 and the agitator blade 21 relative to this incoming total wet sirömiing 68 in the Annular channel 55 is supported by a front cutting edge 63 of the agitator arm. By the way, she comes due to the fact that the impeller exerts a damming effect against the Sirömuiigsrichiung 68, the The smaller the passage cross-section of the openings 43, the larger it is. This creates a jam effect under the agitator arm a reverse circulating flow in the direction of arrow 69 and thereby a build-up of the mass beyond the regulated massixeau 24 present when the ruler is at rest up to a little beyond the surface of the contact surfaces, as indicated by the dashed arrow lines 70. From this circulating flow, which is also partially retrograde, the upper partial flow branches off from, the boundary layer-like, as shown with the crossed lines 71, over the middle part and the rear end 57 of the agitator arm extends away.

At 73 it is shown in the same type of representation as this upper partial flow detaches itself from the agitator arm and merges in the annular channel 55 with the lower partial flow, which is shown there in a dash-dotted line at 72. united.

This lower partial flow is that part 66 of the total flow 68, which passes through the openings 43.

As soon as steady flow conditions have occurred after the mass has been poured into the reactor and the upper partial flow 65 has formed. is behind the impeller, the sum of Tcilströme 72 and 73, of course, 68. in the time unit is equal to the inflowing relative to the paddle total flow Nonetheless is constantly a part of this total flow in the dash-dotted recirculation flow 69 and 71 (unteihalh the quiescent levels 24 and 70) above the Quiet level obtained, which corresponds to the objectives of the invention and is extremely desirable; because as a result, new parts of the mass repeatedly come before they either flow over the agitator in direction 65 or pass through the agitator blades in direction 72 under the agitator arm, on the surface of the flow, which causes evaporation or other treatment processes, such as mixer or heat exchange, heavily favored. As a result, the dwell time was shorter or the mass throughput pn time unit was selected to be larger and still results in a more favorable degree of efficiency.

This effect is favored in a well-known manner by the fact that, due to the high vacuum of, for example, 0.3 Torr, the so-called bubbles are created on the mass surface, through which the surface is further enlarged. It is advantageous that the agitator blade 21 is curved and steadily j.

has the following profile, through the dead space of the flow in front of and behind the Mixing arm can be avoided.

For the described formation of circulating currents and an appropriate ratio of the one flowing over the agitator blade in the unit of time and on the other hand through the stirring flights! through the openings 43 flowing amounts it comes in According to the invention, the passage cross-section to choose the openings of the agitator blades in accordance with the viscosity of the mass to be treated. If this cross section is chosen too small, the back pressure at 69 in front of the agitator paddle closes large, and it can even happen that behind the impeller at 72 below level 24 at all no more partial flow escapes, it is practical the entire mass goes over the paddle, which is very undesirable because then the area the vortex 70 seen in the direction of rotation is too short and too high and fewer mass particles per Line unit reach the surface.

Conversely, it is desirable that the larger Part or at least half of the flow goes through the openings 43 and remains in the Rir.gkanal.

This goal is achieved in the embodiment according to FIG. 5 at high viscosities e.g. over 5000 poise and up to 20 (100 poise and more achieved by the fact that the openings 43 a larger part, more than half and up to 70 "0 to SO ¹¹ O of the cross-sectional area of the impeller (active surface) , take in.

But if masses with lower viscosity, z. B. are treated under 5! R) 0 poise, according to the invention the impellers and the Rührarmc adapted to these relatively low viscosities of the mass and recommends an embodiment as shown in FIGS. ft to 9 is shown. There this embodiment with regard to the remaining parts and the general structure of FIGS. 1 and 2 to 5, matching parts are in Figures 6 to 9 have the same symbols as in Figure 9. 1 to 5 and have parts of the same Function as in the first embodiment, which are modified in the second embodiment, the same reference numbers are given with the addition nj «.

The Rührarmc are therefore in Fig. 6 to 9 with 20 o, the agitator blades with 21 ", the passage openings mil 43 "and the webs protruding from the hub marked 17".

The Rührarmc 20 α are according to F i g. 7 and 8 are essentially designed in the same way as according to FIGS. 3 and 4; however, as shown in FIG. 9 can be seen, the agitator blades 21 "on the underside of the agitator 20" in such a way that they protrude longer stretched over almost the entire depth of the annular channel 55 far behind the end 57 of each blade and their rear surface is flush with the tapered end 57 adjoins with a curvature which merges in an almost perpendicular direction to the bottom 6 of the annular channel 55.

This modification in the attachment and design of the agitator blades 21 α is advantageous for materials of low viscosity, but could also be used in the Auslührimgsform me FIGS. 3 and 5.

Essential for the treatment of masses of lower viscosity, e.g. B. less than 5000 poise, is in the embodiment of FIG. 6 to 9, however, the difference is that the impeller has only one opening 43 a smaller cross section than the sum of the openings 43 per impeller, preferably with a cross section that is only about a third of the effective depth of the impeller measured perpendicular to the bottom 6 of the annular channel amounts to.

Nevertheless, there results for the partial flow 73 flowing out via the agitator arm 20 a and that through the Partial flow 72 passing through opening 43 ″ of the agitator blade, a quantity ratio per unit of time, that about the one according to FIG. 5 is the same. d. H. the larger partial flow through the openings 43u and the smaller one goes over the paddle 20 a; because the opening 43 "offers despite its small cross-sectional size a mass of lower viscosity only about as much flow resistance as the larger one Cross-section of the cutouts 43 forms a tougher must.

Accordingly, there is a circulating flow in the region of the retrograde eddy indicated in the lower partial flow 66 "at 69", ie the incoming flow 68 is retrograde eddy, similar to that at 69 in FIG. 5; However, this vortex formation begins according to the curved profile shape provided on the underside of each wing 21 ″ with small vortices in the vicinity of the opening 43 ″, which, nestled against this underside, become steadily larger up to the front edge 63 of the agitator arm. They then go into vertebrae 71 and 70 with a similar course as in FIG. 5 over. The vortices 70 continue with a smaller diameter in the flow direction 68 over the front end of the agitator arm 20 α and also generate the boundary layer-like flow 65 here, which merges into the flow 73 at the rear end of the agitator arm and the agitating surfaces.

The inventive division process desired in front of the front edge 63 of the agitator arm and the The circulation required for the treatment of the mass is therefore also carried out for masses of lower viscosity, as is the case with the embodiment according to FIG for masses of high viscosity has been described.

The invention thus provides the possibility, through suitable design and arrangement of the agitator blades the treatment effect on the viscosity of the initial massc adapt. It is sufficient for this. the stirrer 14 as a whole in one embodiment, z. B: according to FIG. 3 and 4, to be detached from its shaft and against one equipped with other agitator blades Stirrer, e.g. B. according to FIG. 7 and 8, to be exchanged. For this purpose, the upper part 2 dc < Reactor on the flanges 4 from the lower part 1 are gelösi.

If the flanges 4 are not screwed for the sake of tightness, but welded, or screwed and welded, the weld would have to be for this purpose broken up and renewed after the replacement. However, a reactor is usually used for eir and the same mass and one and the same type of treatment ordered and built so that according to requirements the replacement of the stirrer at the factory before the reactor parts 1 and 1 are welded together 2 can be made. Instead, the kit can adapt the agitator blades to the viscosity Mass be provided that the agitator blades are attached to the associated agitator arms interchangeably, si.

Λα i n
ι.
η

that a training according to FIG. 5 can be replaced by a training according to FIG. 9 and vice versa. This possibility of a releasable connection of the agitator blades is not shown in the drawing. but familiar to the expert.

F i g. 2 shows only as a diagram (not as a practically advantageous embodiment) how the cross-section of the passage openings 43 'of the agitator blades 21 can be changed in accordance with the viscosity. It does not matter whether the openings in the agitator blades 21 or 21 α are shown as in FIG Openings in the form of cutouts 43 or holes 43 have α . The setting of the passage cross-section of the openings is indicated by the cover plates 44, which are optionally screwed or, better, welded onto the agitator blades 21 via one or more of the openings 43 'by means of screws 45. Instead, a plate 47 can be attached by means of screws 48 or welded on (shown in dash-dotted lines) to each opening or to only one or two openings per wing. To the passage cross section of the partition walls 27, as required, for. B. to be able to change the viscosity of the mass or the speed of the agitator arms, a cover ring 49 at the level of the openings 28 of the partition walls 27 can be provided and welded on or adjustably attached. According to FIG. 2, the cover ring has a cutout SO each in the region of the openings 28, so that it closes or opens the openings 28 completely or partially.

For this purpose 2 sheets of drawings

Claims (15)

Patent claims: 1. Reactor for the treatment of viscous outgassing masses with heating and steam formation, whereby the reactor is in the form of a vertical container with an annular jacket cross-section and essentially frustoconical with itself has a downward tapering bottom and circumferential, radially extending agitator arms and axially protruding agitator blades of a drivable agitator with a vertical shaft in immerse the masses continuously fed into and removed from the reactor, their liquid level constant at least at the mass addition * s soot of the reactor automatically to a specified value Level is regulated, with the agitator arms and the attached agitator blades via the largest part of their agitating surface in that formed by the frustoconical reactor floor *> Production room are housed, with the beginning close below the liquid level Propeller blades protrude close to the frustoconical reactor floor and over their axial length Form radial spaces between them, s5 through the annular and with passage openings provided, with the reactor bottom connected partition walls pass through the concentric run to the reactor shaft and as Bretmorgane for the radially through the passage openings outflowing mass serve, and furthermore, the reactor bottom close to its upper edge a circumferential, outer floor ring of the production room with at least one or more Bottom openings is formed and the agitator arms engaging in the bottom ring scraper wear, according to patent 1,813,956, thereby characterized in that the agitator blades (21, 21a) with one or more continuous Openings (43, 43 a) are provided in such a size that the relative to the circumferential Agitator blades along the annular channels (55) formed between the partition walls (27) running flow of the mass in an area leading the agitator blades in the direction of rotation is divided and only partially (65) over the agitator arms (20), the other part (66) pass under this. 2. Reactor according to claim 1, characterized in that the cross section of the openings (43, 43 a) of the agitator blades (21, 21 a) depending on the viscosity of the treated mass at viscosities of more than 5000 poise more than half of the surface each impeller is. 3. Reactor according to claim 1 or 2, characterized in that agitator parts (21, 46), which determine the cross-section of the openings (43, 43 a) of the agitator blades, are exchangeable for changing these cross-sections against Rürirwcrkteilec, the openings (43, 43 a) the impeller (21, 21a) determine the larger the cross-section, the greater the viscosity of the mass to be treated. 4. Reactor according to claim 2 or 3, characterized in that the entire rotating agitator element (20, 20 a; 21, 21 a) located in the production room can be exchanged for an agitator element in which the openings (43, 43 a) of the agitator blades ( 21, 21a) have the larger the cross-section, the greater the viscosity of the mass to be treated. 5. Reactor according to one of claims 1 to 4, characterized in that the cross-section of the openings (43, 43 a) of the agitator blades (21, 21a) is chosen so small that the mass in front of the agitator blades and in front of the leading one is backed up Front edge (56) of the agitator arms (20, 20u) forms a vortex or circulating flow (67) of the mass that initially runs in the direction of rotation, then to the bottom (58) of the annular channel (55) and back to the front edge, and overflows behind this edge Boundary-layer-like partial flow passing away from the agitator arm branches off, which likewise begins with eddies near the leading edge. 6. Reactor according to one of claims 1 to 5, characterized in that the agitator arms (20, 20 a) as guide surfaces (58) for the partial mass flow passing over them with at least an Profile similar to the harmonic of the aircraft wing are trained. 7. Reactor according to claim 6, characterized in that the trailing end (57) of the Mixing arms (20, 20 a) at least on their top against the bottom (58) of the associated Ring channel (55) tapers out. 8. Reactor according to claim 6 or 7, characterized in that the trailing end (57) the agitator arms (20, 20 a) in one to the curvature of the profile of the top and the course of the Underside of the agitator arms adjoining agitator blades (21, 21 α) merges. 9. Reactor according to one of claims 1 to 8, characterized in that the agitator blade (21 α) each has only one opening (43 a) for the passage of the lower partial flow (66) whose Cross section is smaller than half of the active surface of the impeller (21 α). 10. Reactor according to one of claims 1 to 8, characterized in that the agitator blades (21, 21 a) have cutouts (60) from the bottom (6) of the annular channel (55), the passage cross-section of which is greater than half of the active surface of the agitator blade. 11. Reactor according to claim 10, characterized in that the between two cutouts (60) of an impeller (21) formed tongue (61) greater distance from the bottom (58) of the Annular channel (55) has than the adjacent to close to the bottom and to the side walls (27) of the annular channel adjoining tongues (62). 12. Reactor according to one of claims 1 to 11, characterized in that the cross-sectional size of the openings (43, 43 a) of the ruin blades (21, 21a) for each agitator blade from Ringkanu! (55) is selected to be different from the ring channel. 13. Reactor according to claim 12, characterized in that that when the mass flows radially from the inside to the outside, the cross-sectional size of Openings (43, 43 a) of the agitator blades per agitator blade from the radially innermost to the radially outermost Ring channel is increasingly chosen. 14. Reactor according to one of claims I to 13, characterized in that the agitator arm (21, 2Ia) at its leading end (56) as forward-facing, supporting the division of the flows into two or more partial flows (65, 66) Cutting edge is formed. 15. Reactor according to one of claims 1 to 14, characterized in that the agitator arms (21, 21 a) have guide surfaces (64) projecting in front of the leading front end and extending upwards beyond its upper side and along this rearwardly extending walls (27) of the annular channels (55) ) are provided for the upper partial flow (65) and the vortex (70) formed before the division.