DE2105056B2 - REACTOR AND ITS USE FOR THE TREATMENT OF VISCOSE BASE MATERIALS - Google Patents

Description

The invention relates to a reactor for treating viscous starting materials 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 stirring trough and stirring blades axially protruding therefrom 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 ! The production space formed is housed, with the ones beginning close to 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, go through partition walls connected to the reactor bottom and concentric to the reactor shaft and serve as braking elements for the mass flowing out 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 the patent application P 18 13 956.5 ^ 44. The invention relates to a further embodiment of this reactor and its use.

S The reactor according to the main patent application 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. 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 separation in the reactor, in particular

their masses in the range of viscosities between 300 and 5000 poise (when using the mass). For In the main patent, masses in this viscosity range were used as impellers as uninterrupted surfaces used, which are quite close to the side

ao walls and the floor of the ring channels of the production room connected.

It has now been shown, however, that especially in the range of viscosities above 5000 poise and e.g. up to 20,000 poise (using the mass) as before

as occur especially with polycondensation products, the stirring effect, in particular the evaporation, is not satisfactory if the impeller is not perforated be used; because there is then 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 Slide the closed ring in front of you without the agitation required for the treatment to generate sufficient amounts of the propeller,

which should occur according to the main patent application as an essential result of the invention.

To ensure a satisfactory whirling and circulation of the mass even with high viscosities, in particular over 10,000 poise can be achieved using the stirring blades and / or the stirring trough of the reactor mil Passage openings for the passage of the goods to increase their turbulence and mixing to be provided as it is the subject of additional patent 1939 412 to the main patent application

P 18 13 956.5-44 is. This proposal points the right way to the desired goal, but shows not yet what is important when dimensioning the cross-section size of the openings of the agitator blades, In order to achieve an optimal circulation movement for the evaporation of the mass at different high viscosities to create.

Experiments have led to the finding for a reactor of the type mentioned that one the desired optimal overturning movement thereby

receives that the agitator blades with one or more through openings of this size verseher are that the relative to the revolving vanes along the annular channels formed by the partition walls running flow of the mass in an area leading in the direction of rotation of the agitator blades which ends in front of a propeller each, is divided and only partially over the agitator arms other part passes under them.

After the main patent application, however, konnti

There is no mass flow under the agitator arms due to the lack of openings in the blades take place and had to go over the entire relative flow to the agitator arm, while eii

Part of the mass did not carry out any such relative movement at all, instead of a heating means, the double jacket of the reaction, but rather charged over the bottom of the ring channel appropriately assigned to the gate with a flowing coolant agitator blade. The reactor is also suitable for pre-production. The latter phenomenon was observed when drying cellulose masses, e.g. B. in the context of the aforementioned proposal of the first additions- 5 paper production, with the dehydration followed by remedied; however, after this preliminary work, for example on a paper machine, there was only a small amount, especially with lower viscosities and a small amount of material.
Another advantageous area of application of the desired possibility that no reactor worth mentioning is its use as a mixer for more mass flow passed over the mixing pan and the highly viscous masses introduced into it were too small. or to mix in dyes, pigments

According to the invention, however, the cross-section should th, stabilization means.

the openings of the agitator blades according to the

ability of the mass to be treated is so selected, the reactor drove the mass preferably centrally in the

the, that said division of the flow 15 lower bottom part, z. B. by means of a pump

adjusts, namely introduced by back pressure of the mass in front of a screw, radially outward di'rch

the impellers. the passage openings of the partition walls of the

The cross-section of the openings is preferably guided through the production space and in the upper edge of this

the impeller is chosen so small that it is discharged through the room by means of conveyors

Back pressure of the mass in front of the agitator blades and in front of ao. The operation of the reactor can, however, also be like this

the leading edge of the agitator arms to be carried out that the mass on the outside

next in their direction of rotation, then fed to the bottom of the edge of the production room, radially

Ring channel and back to the front edge running inside through the passage openings of the Ttv \ -, n-

Vortex or circulating flow of the mass formed walls and in its center by conveying

is and behind this edge a on the Rühr- as tel, z. B. a snail is discharged,

poorly passing, boundary-layer-like partial flow In the attempts to use the inventive Rcnk-

branches off to match the same mall near the front edge with the viscosity of the treated mass.

Whirling begins sen, it has been found to be beneficial when

Both the aforementioned division of the relative- the cross-section of the openings of the agitator blades according to flow in partial streams over and under the agitator 30 stipulation of the viscosity of the mass at viscosities alone and in connection with the last- of more than 5000 poise more than half of the circulating currents mentioned is very advantageous, the surface area of each agitator blade is. In doing so, because in front of, above and behind the agitator arm, the agitator blades can expediently have sections from the bottom that are significantly larger in movement and surface area of the annular channel, the passage of which is caused by the mass, and both of these, in particular, each cut greater than half of the active for evaporation under vacuum and / or heat surface of the impeller. If the viscosity of the mass treated in exchange with the heated bottom of the reactor is less than 5000 poise, then it should be extremely desirable.However, each agitator blade is not preferably required to have only one opening in order to have the above-mentioned circulation and / or for the passage of the lower partial flow , the division of the flow at or in front of the front cross-section of which less than half of the active rushing edge of the agitator arm is generated; it is the surface of the impeller and expediently 20 is also possible, an agitating ^{surface which is wide in the direction of rotation is up to 40 0} zo of this surface,
poor with one or more passage openings There is the possibility of changing the cross-sectional size directly or a little in front of the associated agitator or the openings of the agitator blades and the upper partial flow to these, so that depending on the requirements of the buyer not this passage point Above the agitator arm, several different types of reactor are stored in stock and allowed to flow off via this. need to be held, rather only individual ones

The main advantage of the invention is that parts of the reactor need to be replaced.

also masses of great tenacity over 5000 poise and chen.

up to the order of 20,000 poise

treated, in particular in the relatively large cross-section of the openings of the agitator blades

Ringer time can be evaporated, with men, to change these opening cross-sections

an inexpensive, even dwell time spectrum that can be exchanged for agitator parts that run like this

Regardless of these particular advantages, the larger the viscous cross-sections determine the larger the viscous Masses, especially those of high viscosity, mean that the mass to be treated is able to do so

Reactor with similar advantages, e.g. B. for abbreviation z. B. the openings in the stirring blades and also

the treatment time of the mass or for opening the openings in the dividing walls of the stirring channels Improvement of the Verrosflzeilspekteums also on masses - by changing the agitator blades as required low viscosity! applicable below 5000 poise. can be set differently. Instead, you can Furthermore, it has been shown that the 60 according to the invention the entire Rübr reactor located in the production room not only for the evaporation of plant link against an agitator bed austaaschbai Synthetic resin compounds, such as condensation products or in which the openings of the agitator blades are so Polymerization products, but also have a larger cross-section, the greater the toughness stig as a heat exchanger for other viscous masses of the mass to be treated and in which the with or without chemical reaction, e.g. for syrups, 65 shape of the agitator blades of the conicity, i.e. the cone-sugar masses, Basic foodstuffs, tea prop angle of the reactor bottom according to the viscosiducts, Asphalt for cooling and / or heating should be chosen differently and this can be used. In the case of cooling, the angle is also determined by the individually desired

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to

the extent to which the mass can be made dependent; its top up out and along this

it is therefore generally the last-mentioned top side 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 is provided,

should remain the same. In the drawing are embodiments of

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

keep. A reactor according to the invention can therefore be used. 1 shows 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. 1 of the main patent, disregarded

are preferably only the cone angles of the reactors of the agitator blades, which according to a first

door bottoms and the cross-sections of the agitator vane openings- 15 Embodiment of the present invention

genes increasingly chosen from level to level. are educated,

While after the main patent application 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. 1 an excerpt from the

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

tapered agitator arms are shown, the inventions of these parts, which in the execution according to F i g. 1 not

proper aim of dividing the flow of occurrences,

Mass are preferably favored by the fact that F i g. 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 Massc-Tciistroin with at least the fertilizer are indicated by dash-dotted lines.

Top side of the aircraft carrier surface-similar 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. Fig. 5 schematically in an angled

For similar reasons, in favor of the section along the line AB 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 stirring trough 30 connection with a guide surface and a position against the bottom of the associated annular channel, the flow course is above and below the tapered position, preferably so that the profile curvature the half of the propeller,

Top and bottom of the agitator arm in FIG. 6 in one of the F i g. 1 corresponding cut subsequent ends Impeller passes over. This creates a different embodiment of the vorlieden Dead spaces of the flow in front of and behind the 35 lowing invention in terms of the impeller Avoided impellers, which are very undesirable. and the guide surfaces is modified,

The speed of the propeller or the whole. ^Fi £ ·. ⁷ according to the stirrer of 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, 40 F i g. 7 and

Heating and cooling processes in the range of 1000 poise F i g. 9 shows a developed section along the line to 5000 poise about ten revolutions per minute A'-B ' of FIG. During evaporation processes, l. B. polyester, fangrichiung runs, in connection with a guide and a viscosity of up to 3000 poise has an area and a representation of the flow and speed of no more than four revolutions per 45 below and above the impeller.
Minute proved to be useful, since otherwise the Da F i g. 1 and 6 the general structure of the power expenditure becomes undesirably large without improving the reactor, apart from the formation of the stirring efficiency. For such evaporation blades and associated parts, in accordance with the masses should therefore represent viscosities above 3000 with the main patent, a speed of four revolutions is expedient in the drawing poise, especially in FIGS. 1 and 3 and 4, for the slopes 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 tangential rotational speed of the According to all drawn embodiments

Agitator blades on the larger radially outer 55, the reactor consists of two main parts, the un-

Ring channels proportional to the radius is larger than part 1 with the production room 15 and liquid

in the inner ring channels, should preferably be the keitssumpf, and the upper part 2 with the steam

Size of the cross-sectional openings of the agitator blades depending on. Both parts of the reactor have a double

iRShr & ügel differentiated from ring channel to ring channel 3 for the circulation of a heating fluid

borrowed be chosen in such a way that the cross-sectional size S ₀ or of heating steam, its inflow and outflow

The openings of the agitator blades from the radially innermost flow connection are not shown. The reactor door

sma radially outermost annular channel increases. are liquid- and vacuum-tight by means of flanges 4

In the preferred embodiment of the invention, they are interconnected.

dung is the paddle at its leading EODE The upper Reakiortefl has a Dampfausals front-facing, the division of the flows S ₅ irittsstutzen 5, support to which a capacitor and a Vain two substreams cutting edge Removing kuumquelle for condensing and suction of the formed, further are the stirring tank with in front of the protruding front end to be treated in the reactor during evaporation and is connected via ground. For mixed and heating

Transfer treatment of the mass without vacuum openings 28 to flow. The partitions 27 form in the Evaporation can often be dispensed with the condenser remaining closed, concentric ring ca- and the vacuum pump by simple suction channels 55, the bottom of which is replaced by the reactor bottom 6 will. forms is.

The reactor base that forms the production room 5 F i g. 1 and 3 to 5 show a first embodiment 6, the main part of the agitator blade 21 is frustoconical and has openings 43 in FIG educated. Form of cutouts of the agitator blades provided

In the illustrated embodiments, that which is more than half of the surface is about 70 Conical angle of the bottom of the reactor for the treatment of up to 80 ° / o of the surface of each impeller Masses with initial viscosities over 300 Poise ίο chen. Openings of this size are preferred for an acute angle, with viscosities up to 20,000 poise higher viscosities of the mass to be treated, especially and more is a larger cone angle of the reactor - special viscosities over 5000 poise, provided, To prefer the bottom, as in the main patent in the By the cutouts 43 is a middle tongue 6 and 7 is shown in the embodiment 61 and an edge portion 62 of each agitator blade is formed, according to FIG. 6 to 9 for the sake of simplicity but not 15 of the floor 28 or the partition walls 27 or is shown because this embodiment is directly adjacent for the small top of the agitator arms 20 Viscosities of the mass below 5000 poise is agitated. When the hub 17 is located adjacent is true, but depending on how the impeller is used, a central tongue 61 is not required. In the rest of the reactor z. B. as a mixer or heat exchanger or gene grows the size of the cutouts 43 in the other physical and chemical purposes also 20 dimensions radially from the outside in, such as the depth of the according to the embodiment according to FIG. 6 to 9 a production room 15 radially from the outside to the inside obtuse cone angle for the reactor bottom according to the cone angle of the bottom 6 can be turned is. takes. This increase in due to the impeller

The mass to be treated is by means of a through openings 43 is desirable because Motor 7 to be provided pump 8 by an input as the peripheral speed of the agitator pnportrittsstutzen 9 fed to a filler pipe 10 whose tional the distance voa the central axis of the stirrer upper end in the middle of the reactor bottom mün- 14 increases, but in general by the det. The lower end of the tube 10 is by means of an impeller passing through mass in each of the Vacuum stuffing box 11 closed and forms the ring channels 55 in the unit of time must be the same Bearing for a 30 driven by a motor 12 (except when the stirrer starts up or when the first Drive shaft 13 of the mass designated as a whole with 14 filling).

Stirrer, which is attached in the production room 15. On the right side of Fig. 1 are the agitator

Between the lower end 16 of the hub 17 of the gel 21 and the stirring arms 20, the stirrer and the stuffing box 11 can be used to illustrate the drive formation of the ring channels 55.
shaft 13 in the pipe 10 as a screw conveyor 18 for the 35 Fig. 1, 3, 4 and 5 show that in each case above the reactor continuously supplied mass of a partition wall 27 at the top 59 of each of the be formed, if this has high toughness stirring arms 20 each a guide surface 64 is attached. and the delivery rate of the pump 8 is insufficient. which has approximately the profile of an aircraft carrier surface. The conveyed material protrudes through a considerable opening in the middle and over the front end 56 of the agitator arm of the base 6 and the hollow hub 17 and also over the annular channel 19 that remains during the rotation, and also through openings 22 rushing end 57 of the agitator arm somewhat backwards at the lower end of the hub 17, into the agitator. can protrude. According to FIG. 5 sits at this

The stirrer consists essentially of, for example, three guides of the stirring blades 21 each in the rear stirring arms 20 (see FIGS. 4 and 3), which extend from the area of the underside of the stirring arm with the pre-conical hub 17 extending radially outward, 45 rushing end 56 protrudes in front of the agitator arm and that and from agitator blades 21, which are attached to the underside of the rear end 57 flush and arched to the rear in the agitator arms. The hollow hub 17 has the rear of the impeller passes over,
at the upper end outlet openings 23 (see Fig. 4 As in the main patent, the reactor bottom is close

and 3) for the irr supplied mass. The inflow of its upper edge to a circumferential outer of the mass is formed by the drefazaMgeregelte toothed 50 bottom ring 30, which forms the outermost part 31 and through the speed of the drive 7 of the production drum and a substantially depending on the viscosity of the mass. floor part 30 a running horizontally and is automatically controlled so that a liquid wall part 306 has a vertical wall part 24 at a small distance of 2 B. less delimits the production area and with bends millimeters above the top of the stirrer arms 20 55 long set in the flange 4 of the lower reactor part, as transitions by a dashed lime in Fig. 1,
indicated as a stationary level ^ In the annular bottom part 30 α is at least

The wings 21 extend from the agitator arms to a discharge opening 32 for the product attached close to the top of the reactor bottom 6 and the outer ends of the agitator arms 20 carry scraper 33, which is the largest part, on the young side, corresponding to the cone angle of the “o side of the reactor floor from the outside to the inside. They are in ra- 31 occupy and arranged on the parts 30 a and 30 b of the dialen distances from each other. The circumferential parts of the scrapers 33 that are firmly connected to space 31 protrude from the floor 6 and are like insberingf & migej partition walls 27, which near the floor show special FIGS. This "5 Ruhr arms inclined at an acute angle to the order-partitions serve alas for braking of the Ruh- running axle down and direction to the revolving 26 ¥ * ^U *? * * ^E ^^ '° ψ ^ ^{ί & η} ZeatnfugalWfffonig," back In order to force the conveying effect of this mdem se to improve the mass through the narrow Ott scraper for the material to be discharged.

" I

At the discharge opening 32 there is essentially the same discharge as in the main patent

support tube 34 in which a discharge screw 35 registration. The essence of the invention, however, lies

which is also directly related to the straight line in the improved construction and effectiveness

support opening 32 connects. The discharge screw 35 wise the impeller and the agitator arms, which are for

and the discharge pipe 34 go through an attachment 5 the embodiments according to FIG. 1 and 3 to 5, am

final part 29, the liquid-tight double jacket best from FIG. 5, results.

of the reactor against the pipe at a nozzle 39. According to FIG Agitator flange 29 α is connected. The inlet and outlet are a guide surface for the partial flow 65, which passes over the inlet connection for the heating liquid or steam of the agitator arm. The division into partial flows of the heating jacket 26 are omitted in the drawing. 65 and 66 of the counter to the direction of rotation 67 of the screw is driven by a motor 37. Agitator 20 and the agitator blade 21 relative to thieves, the housing of which is connected to the total mass flow 68 arriving at the lower and upper ends in the closed heating jacket. The ring channel 55 is supported by a front cutting edge. The product 63 of the agitator arm discharged by the discharge screw is supported. It comes through the heating jacket 26 and an outlet through the fact that the agitator from a Stauwirstutzen 38 and is exerted by this effect in the direction of arrow against the flow direction 68, which a storage space or further treatment, z. B. the greater, the smaller the cross-section of the openings 43 in a downstream reactor of the same design. This back-up effect is produced, under the agitator arm, a declining circulation

If there are several discharge opening flows in the direction of arrow 69 in a base ring 30 and thereby one openings 32, then for each of these damming of the mass via the discharge opening when the stirrer is idle a discharge screw 35 with the regulated mass level 24 is out to something corresponding associated parts 34, 26, 29, 29 a 25 beyond the surface of the guide surfaces, as and 37 to 39 provided. is indicated by the dashed arrow lines 70.

As can be seen, the mass in the production area is also partially declining from this surrounding area 15 through the stirrer 14, a centrifugal circulating flow branches off the upper partial flow 65 acceleration through which they during the evaporation from, the boundary layer-like, as with the crossed angefung lines 71 given from the middle area of the production room 30, over the middle part through the openings 28 and over the agitator and rear end 57 of the agitator arm 20 runs away into the edge area 31 of the product.

entry area. Here the evaporated at 73 is shown in the same way as the product is grasped by the scrapers 33 and this upper partial flow continuously detaches from the agitator arm from the discharge screw 35 or the discharge screw 35 and is fed into the annular channel 55 with the lower part 35. These ensure that the flow, which is not shown there in dash-dotted line at 72 parts 30 α and 30 b of the bottom ring 30, unites.

Deposits of the product form, which also in the ke- This lower partial flow is that part 66 of the

frustoconical part of the base 6 and to the overall flow 68, which flows through the openings 43

Partitions 27 by the centrifugal flow of 40 passes through.

Mass and by the stirring action of the impeller 21 as soon as after filling the mass into the reactor

and agitator arms 20, just as stationary flow conditions have occurred on these themselves

be avoided. and the upper partial flow 65 is formed

The liquid level 24 becomes the sum of the partial flows 72 in this front behind the agitator blade

gear in a manner known per se automatically on little 45 and 73 in the unit of time, of course, the same

greater height of a few millimeters above the agitator - the total flow relative to the agitator arm

poor with the help of a z. B. optical and / or elec- tion 68. Regardless of this, a part is constantly being generated

tric discharge device is set, which in itself this total flow in the dash-dotted line shown

As is known, the delivery rate of pump 8 is set at circulating flow 69 and 71 (below the

their engine 7 controls. 5 «yard levels 24 and 70) above the resting level

Due to the vapor deposition and the effect of stirring, which corresponds to the aims of the invention, poor 20 arise at the liquid level 24 and is extremely desirable; because as a result, bubbles and can repeatedly come above the scraper 33 new parts of the mass, splashes of the mass occur, which can either settle in the direction 65 over the stirrer on the inner wall of the reactor or flow away in the direction 72 under resting. To prevent this, step on the outer arm through the agitator blades, to the edge of the reactor bottom on the bend of the surface of the flow, which the Ausdampfunj bottom ring 30 put a splash guard ring 42 on, or other treatment processes, such as mixing which protrudes above the liquid level and den or heat exchange, strongly favored as a result, the bottom ring reached over. Furthermore, the scrapers 33 60 ffie have a shorter dwell time or the mass throughput pn over the mixer against the splash guard ring 42 can be selected to be larger and results in protruding TeOe 33 a, which is nevertheless more favorable on the inside.
Attack protective ring as a scraper and also to this effect will prevent the deposition of mass in a known manner and z. B. still favored by the fact that the high Va have the shape of a round rod. 65 kuum from z. B. 0.3 Torr at the mass surface di

Apart from the construction and the effect mentioned bubbles arise through which the obei

wise the agitator 21 and agitator arms 21 is the area is increased even further. Is advantageous

Construction and mode of operation described above that the agitator blade 21 is a curved, steadily a

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has a profile adjoining the agitator arms, due to the essential for the treatment of masses low-

the dead space of the flow in front of and behind the rer viscosity, e.g. below 5000 poise, is at the

Agitator arm venniedea. Embodiment according to Fig. 6 to 9, however, the un-

For the described formation of circulating flow difference that the agitator blade has only one opening 43 openings and an appropriate ratio of the 5 smaller cross-sections than the sum of the openings in the time unit on the one hand over the agitator blades 43 per agitator blade, preferably with an opening and on the other hand, or by means of the agitator blade through cross-section, which is only about a third of the effective quantities flowing through the openings 43 in the sense of the invention, measured perpendicular to the bottom of the annular channel, is the transverse passage depth of the agitator blade
Section of the openings of the agitator blades in accordance with io backpressure at 69 before the impeller to flow 72 turn ratio per unit time is large, and it may even happen that behind the approximately to that of FIG. 5 is the same, ie where impeller exceeded ¹ at 72 below the level 24 15 in the case of the larger partial flow through the openings 43 a no partial flow at all emerges, but rather practically and the smaller one goes through the agitator arm 20 α; because table the entire mass over the agitator arm away - the opening 43 a offers despite its small cross-section, which is very undesirable because then the sectional size of a mass of lower viscosity only reaches the vortex 70 seen in the direction of rotation too short about as much flow resistance as the ground becomes too high and fewer mass particles per 20 ßere cross section of the cutouts 43 reach the O ¹ surface in a tougher time unit. Mass forms.

On the contrary, it is desirable, conversely, that the greater than this, the circulating flow is in the range

ßer part or at least half of the flow of the lower partial flow 66 α at 69 α

goes through the openings 43 and in the annular canal indicated retrograde eddies, i. H. the arriving

stays. As the changing flow 68 retrograde eddies, similar

This goal is preferably achieved in the case of the, in particular that at 69 in FIG. however, this begins

eddy formation intended for evaporation processes in accordance with the

5 at high viscosities e.g. see each wing 21a provided curved profile

over 5000 poise and up to 20 000 poise and more filform with small eddies near the opening

achieved in that the openings 43 a size 30 43 a, which, attached to this underside, up to

ren part, more than half and up to 70% up to the front edge 63 of the agitator arm become steadily larger.

80% of the cross-sectional area of the impeller (active You then go into vortices 71 and 70 with something similar

Surface). Course as in FIG. 5 over. The vertebrae 70 settle

But if masses with lower viscosity, z. B. are treated with a smaller diameter in the direction of flow below 5000 poise, then should invention 68 via the front end of the agitator arm 20 α continue to the agitator blades and the agitator arms and also generate the boundary layer-like, relatively low viscosities of the mass adapted flow 65, which are at the rear end of the agitator arm and and an embodiment is recommended that merges the agitating surfaces into the flow 73,
as shown in Figs. 6 to 9 is shown. Since the distribution, desired according to the invention, of this embodiment with regard to the remaining 40 aisles in front of the front edge 63 of the agitator arm and the parts and the general structure are shown in FIG. 1 and for the treatment of the mass desired circulation 2 to 5 corresponds, corresponding parts are in tongue therefore also for masses of lower Visden Fig. 6 to 9 with the same characters as in kosity, as in the embodiment of Fig. 5F i g. 1 to 5 and have parts of the same for high viscosity masses has been described.
Function as in the first embodiment, the 45 The invention thus provides the possibility of being modified in the second embodiment, suitable design and arrangement of the agitator blades the same reference numerals with the addition "α" he the treatment effect on the viscosity of the withstand, gangue adapt. To do this, it is sufficient to

The agitator arms are therefore in Fig. 6 to 9 with rer 14 as a whole in the one embodiment,

20 a, z the impeller 21 a, the Durchtrittsöffnun- 50th B. according to FIG. 3 and 4 to detach from its shaft

genes with 43 a and those that protrude from the hub and are equipped with other propellers against one

Bars designated with 17 'α. killed stirrer, z. B. according to FIG. 7 and 8, to be exchanged.

The agitator arms 20 α are shown in FIG. 7 and 8 in the we- For this purpose, the upper part 2 of the

sentlichen in the same way as according to FIGS. 3 and 4; Reactor detached from the lower part 1 at the flanges 4

however, as can be seen from FIG. 9, the agitators are seated.

wing 21 α on the underside of the stirring trough. If the flanges 4 are not

20 a, that they screwed longer stretched over almost the whole, but welded, or screwed and

Depth of the annular channel 55 far behind the end 57 each welded, so for this purpose the welding

of the wing protrude downwards and their rear upper seam broken open and renewed after the exchange

surface should be flush with the tapered end 57 60. A reactor is usually used for a

adjoins with a vault that extends to the bottom 6 and the same mass and one and the same treatment

of the ring channel 55 ordered and built in an almost vertical direction, so that depending on the requirements

transforms. the replacement of the stirrer at the factory

This change in the attachment and training before the 2, welding together of the reactor parts 1 and

tion of the agitator blades 21a is advantageous for masses 65 2 can be made. Instead, for

low viscosity, but could also adapt the agitator blades to the viscosity of the

Eührungsform according to Fig. 3 and 5 are used, it should be provided that the agitator blades are attached to the

ien. associated agitator arms are interchangeably attached, so

(Ό

that a design according to Fig. 5 can be replaced by a design 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.

2 shows only a schematic (not to be practically advantageous embodiment), as the cross section of through-openings 43 'of the impeller 21 in accordance with the viscosity changed is Here, it is immaterial whether the passage openings of the stirring blades 21 or 21a as shown in Figure 2, that is, a number of circular holes is shown (as was done at 43 'only to simplify the drawing and simplify the illustration), or whether the openings are in the form of cutouts, 43 or holes 43 α . The setting of the passage cross-section of the openings is indicated by means of 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 phantom) to each opening or to only one or two openings per wing. In order to be able to change the passage cross-section of the partition walls 27 as required, for example according to the viscosity of the mass or the speed of the agitator arms, a cover ring 49 can be provided at the level of the openings 28 of the partition walls 27 and welded on or adjustably attached. According to FIG. 2, the cover ring has a cutout 50 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 (19)

Patent claims: 1. Reactor for the treatment of viscous starting materials with heating and steam formation, wherein the reactor is in the form of a vertical container with an annular jacket cross-section and essentially frustoconical has a bottom tapering downwards and circumferential, radially running 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 inflow of the reactor automatically to a predetermined value Level is regulated, with the agitator arms and the attached agitator blades via the largest part of their agitating surface in the * o 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, as 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 braking elements 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 application P 18 13 956.5-44, characterized in that the agitator blades (21, 21 α) with one or more through 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) vt-running flow of the mass in an in Direction of rotation of the agitator blades leading area is divided and only partially (65) over the Agitator arms (20) away, to the other part (66) passes under these. 2. Reactor according to claim 1, characterized in that the cross section of the openings (43, 43 a) the agitator blades (21, 21a) according to the viscosity of the treated mass at viscosities of more than 5000 poise is more than half the surface area of each impeller. 3. Reactor according to claim 1 or 2, characterized in that agitator parts (21, 46), the Determine the cross-section of the openings (43, 43 a) of the agitator blades in order to change them Cross-sections are interchangeable with agitator parts, the openings (43, 43 a) of the agitator blades (21, 21a), the larger the cross-section, the greater the viscosity of the material to be treated Mass is. 4. Reactor according to claim 2 or 3, characterized in that the entire rotating agitator element (20, 20 a; 21, 21a) 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 α) of the agitator blades (21, 21a) so low is chosen that by back pressure of the mass in front of the agitator blades and in front of the leading one Front edge (56) of the agitator arms (20, 20 a) initially in the direction of rotation, then to Bottom (58) of the annular channel (55) and back to the leading edge running vortex or circulating flow (67) of the mass and behind this edge a Boundary layer-like partial flow branches off, which also branches off near the leading edge with eddies begins 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 the top of the aircraft wing-like profile are formed. 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 α) 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) only one opening (43 α) each for the passage of the lower partial flow (66), the cross section of which is smaller than half of the active Surface of the impeller (21 α) is. 10. Reactor according to one of claims 1 to 8, characterized in that the agitator blades (21, 21 α) have cutouts (60) from the bottom (6) of the annular channel (55), the passage cross-section of which each is greater than half of the active surface of the impeller. 11. Reactor according to claim 10, characterized in that that the tongue formed between two cutouts (60) of a stirring wing (21) (61) has a greater distance from the bottom (58) of the annular channel (55) than the neighboring to close to the bottom and adjacent to the side walls (27) of the annular channel tongues (62). 12. Reactor according to one of claims 1 to 11, characterized in that the cross-sectional size of the openings (43, 43 α) of the agitator blades (21, 21a) for each agitator blade of Ringkana (55) is selected to be different from the ring channel. 13. Reactor according to claim 12, characterized in that the flow of the mass radia from the inside to the outside, the cross-sectional size of the openings (43, 43 a) of the agitator blades per agitator blade gel is chosen increasingly from the radially innermost to the radially outermost ring channel. 14. Reactor according to one of claims 1 bi 13, characterized in that the agitator (21, 21a) at its leading end (56) al forward-facing, aiding the division of the streams into two or more Tefl streams (65, 66) Cutting edge is formed. 15. Reactor according to one of claims 1 to 14, characterized in that the Ruhr arms (21, 21a) with in front of the leading front end protruding and extending over its upper side upwards and along this to the rear, with the partition walls (27) of the annular channels (55) aligned guide surfaces (64) for the upper part flow (65) and the front the division formed vortices (70) are provided. 16. Reactor according to one of claims 1 to 15, characterized in that the guide surfaces (64) have an airplane wing-like profile. 17. Reactor according to one of claims I to 16, characterized in that the means of supplying the mass at the outer edge of the production room and the means of conveying the material away 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 several highly viscous masses or for mixing solids into highly viscous masses.