DE2448418C2 - Method and device for the treatment of exhaust gases emitted during the production of mats or panels made of mineral fibers - Google Patents

Description

The invention relates to a method according to the preamble of claim 1 and a Vorrich- lung for performing the method according to the generic term of claim. 7

In the production of mineral fibers by drawing a melt, drawing gases are used for fiber formation uses the one that emerges from the melting pan after appropriate heating at high speed Unravel the fiber beam by pulling it out. These fiber beams mixed with the drawing gases are followed by Leaving the fiber production apparatus generally added binders, with the addition of Binders by means of spray nozzles to form a fiber mat, the fiber jets are on a Receiving organ, sth? a conveyor belt, collected, wherein the exhaust gases present in the fiber jets or accompanying them are present in the receiving organ pass through openings or perforations. To form the fiber mats, however, it is necessary that the Fiber jets impinge on the receiving organ at a speed that is significantly less than the speed of the fiber jets as they exit the fiber production device. To achieve this, one ensures that correspondingly large amounts of gases from the environment of the fiber production device by the stream exiting the fiberising apparatus at high speed Fibers and drawing gases can be induced. These induced gases cause a corresponding deceleration of the fiber beams. Since the amount of drawing gases required for fiber formation is large, so is the amount of air induced from the environment by the fiber rays on the way to the receiving organ considerably. In practice, the induced amount of gases is equal to ten or twenty times and more of the drawing gases.

Due to the ZieJigase, which is induced from the area

5C adorned gases and that from the supplied binder Thermally released gases result from the Fiber formation is a relatively high proportion of exhaust gases that undergo a cleaning process before being released into the environment must be subjected to.

For example, pure or modified binders are used Phenolic or amino resins used, which are thermosetting, soluble in water or emulsifiable and adhere well to fibers. When adding the binder to the fiber jets are due to thermal Decomposition releases volatile toxic elements. However, there are also the finest drops of binding agent in the exhaust gases that are not captured by the fibers and by the exhaust gas flow through the fiber matlc be taken, which is collected on the receiving organ. This leads in particular under consideration the strict exhaust gas regulations mean that the cleaning of the exhaust gases during fiber production is considerable Is important, especially since the

Fiber formation by pulling involves very large amounts of exhaust gas.

To this extent, however, the above-described method is also therefore disadvantageous because considerable amounts of exhaust gas are generated during fiber formation, which in a downstream Must be subjected to an appropriate cleaning stage.

If you go to it, by using a closed Fiber formation chamber the possibility of inducing gases from the environment by the fiber jets to limit (see. Embodiment according to Fig. 2), so this leads within the fiber formation chamber for the formation of correspondingly strong vortices, which prevent the fibers from forming a mat can be deposited in a suitable manner on the receiving organ. As a result of being inside the fiber formation chamber When eddies occur, the fibers are torn up from the receiving organ and through the fiber formation chamber swirled so that the walls of the fiber formation chamber, but also the nozzles for the addition of binder as well as the fiber-making apparatus become fouled. In extreme cases, the vortices lead even to the fact that the fibers can no longer lay down on the receiving organ.

It is the object of the invention. to create a method which makes it possible to reduce the amount of the Fiber jets induced gases, which are passed through the receiving organ to form the fiber mat, to significantly reduce or even suppress, however, the favorable conditions for the production to maintain the fiber mat.

This object is procedurally in accordance with the invention by the in the characterizing part of Patent claim 1 contained features solved.

According to the invention, the amount of air induced in the conventional method by a Circulation of the exhaust gases is replaced, which is before being supplied to the fiber beams on the exact conditions with With regard to fiber formation, such as speed, temperature and the like, can be adjusted. Here it is necessary that uie exhaust gases are washed before being fed to the fiber jets. The one caused by the ablution Cooling the recirculated exhaust gases prevents pre-hardening that would otherwise occur as a result of overheating of the binder, which in turn has a beneficial effect on fiber formation, in particular the adjustment of the fiber thickness. But cooling is also essential for the mat formation and also to avoid heat-related damage to the system itself.

As a result of the circulation of the exhaust gases, it is possible in a simple manner to convert the exhaust gases into a for to feed the fiber formation and the formation of the fiber mat suitable speed. Because only part of the Exhaust gases must be released to the outside. the amount required for cleaning the exhaust gases is reduced Corresponding effort. The washing process cannot be kept as intensive as with an immediate one Release of the exhaust gases to the outside environment, because the washed exhaust gases are returned to the circuit will. Due to the binding agent constituents still present in the exhaust gases even after washing the circulation to be used for the appropriate impregnation of the fibers is reduced as a result of the circulation Amount of binder.

A suitable device for carrying out the method is provided in the characterizing part of the Patent claim 7 measures contained therein.

Appropriate further developments of the method and the device are defined in the subclaims features included.

In connection with the method according to the invention it should be noted that the washing of Exhaust gases during fiber formation is already known per se (US-PS 35 28 220), before the exhaust gases are discharged to the outside will. Furthermore, there is a cleaning treatment by burning exhaust gases after exhaust gas scrubbing known (DE-OS 15 94 689).

After all, it is known in a field other than fiber formation to reintroduce exhaust gases into the process traced back. DE-OS 21 63 183 is the reference can be seen, in the case of a spray of paint in a spray system through a haze formation Wash water and purified air to ensure appropriate shut-off of the spray area and as a result the recirculation of the cleaned air also to reduce the energy costs incurred for heating.

Exemplary embodiments are described below with reference to the drawing. Therein ze ^{; <} - *.

F i g. 1 a device for forming a fiber mat According to the state of the art,

F i g. 2 a device for forming a fiber mat according to the prior art,

F i g. 3 an embodiment according to the invention,

F i g. 4 a further embodiment according to the invention,

F i g. 5 a further embodiment of the washing chamber,

F i g. 6 shows the course of the degree of effectiveness 20 of the treatment for insolubilization as a function of the temperatures and the time of treatment,

7 shows an apparatus for carrying out the method to treat the water by heating it under pressure,

Fi g. 8 a device for continuous operation for the treatment of waters,

F i g. 9 an apparatus for the thermal treatment of the solid waste products provided by the invention will,

10 shows an apparatus for a further treatment method of solid waste products,

F i g. 11 a device used for the production of Fiberglass is used and is designed according to the invention,

F i g. Figure 12 shows an embodiment of the invention suitable for another fiber optic manufacturing process is,

F i g. 13 a further embodiment of the invention, which is suitable for a method of manufacturing mineral fibers by blowing, and

14 shows a further embodiment of the invention, die ffw <; in processes for the production of mineral fibers, in particular from slag, is suitable.

In the device shown schematically in FIG The fibers leaving the fiber production device 11 are used to form a fiber mat pulled out by drawing gases at high temperature and high speed. It imagines here Stream 12 of fiber jets, that is, fibers interspersed with a high proportion of drawing gases. Due to the The high energy of the fiber beams entrains gases from the environment. The stream 12 of fiber beams passes through an impregnation zone, where by means of spray nozzles 13 a suitable binder in the form of a Cloud of fine droplets is dusted onto the fiber beams. A significant proportion of these drops occur on the

Fibers and adheres to them, while the rest with the exhaust gases of stream 12 in the form of drops or of Steam is entrained.

The fiber beams pass through a device 14 which distributes the stream 12 of fiber beams on a receiving member 15 arranged underneath, on which the fiber mat is formed. The receiving member 15 generally consists of an endless, perforated conveyor belt.

A container 16 is arranged below the receiving member 15, in which a ventilator 19 underpressure is generated so that the exhaust gases entrained with the fibers are those formed on the receiving organ Pass through the mat and pull it out of the container 16. These exhaust gases are pull gases from the fiber manufacturing device to induced gases and entrained contaminants such as Binder droplets and the like.

The fiber formation itself takes place within a chamber 22 which is delimited by vertical walls 21 which extend from the receiving member 15 to close to the fiber production device 11. The chamber 22 is, however, in the embodiment according to FIG. 1 open at the top, so that sufficient gases from the environment can be carried away by the stream 12 of fiber beams.

As already mentioned, the material to be processed into fibers is drawn out by drawing gases, which have a high speed, namely up to 100 m / sec and above. That speed is greater than the speed of the fibers and the gases accompanying the fibers when they hit the receiving organ may have to form a fiber mat in a suitable manner. In general, a Speed of about 10 m / sec must not be exceeded. Thus, it is required to be provided by the fiber manufacturing apparatus to decelerate emitted fiber beams until they reach the receiving member 15. This takes place in the embodiment according to FIG. 1 essentially in that the energy of the Fiber beams is transmitted to the induced air. The associated drop due to the induced air but only becomes noticeable accordingly when the fiber beams also travel a sufficient distance to have. Thus, generally the length of that traversed by the stream 12 of fiber beams is The path from the fiber production device 11 to the receiving element 15 is approximately 2 to 3 m, and that over this distance with those gases from the outside environment are considerable and are at least ten or twenty times that of the fiberising apparatus 11 leaving drawing gases. In Fig. 1 is the current of the gases induced from the external environment are denoted by 27. The induced gases pass over here a large size opening 28 in the chamber 22.

In the embodiment according to FIG. 2, identical components are provided with the same reference numerals. This embodiment differs from that according to FIG. 1 in that the chamber is essentially closed and an opening 28 is only present at the top of the fiber-producing device, which in comparison to that according to FIG. 1 has smaller dimensions, so that only a very reduced amount of gases from the external environment can be induced into the chamber. The consequence of this design is that, for example, only a very limited amount of gases can be sucked in from the outside area in zones M and N. However, since the drawing gases there still have a very high speed, this leads to exhaust gases being sucked in from the zones below, such as zone O or P, for example. The gas streams 30, which leave the lower zones of the stream 12, rise as a result along the windc 21 again to the upper zones in the direction of the flow at a higher speed and are captured by the stream 12 and accelerated again. This creates eddies 31 within the chamber 22 between the stream 12 and the walls 21 of the chamber 22. The intensity of these eddies increases with the amount. which cannot be sucked in or carried away from the outside environment. The direction of rotation of the vortices is such that the fibers are torn out of the mat 23 formed on the receiving member 15 and carried upwards so that the fibers settle along the walls 21 of the chamber and on the spray nozzles 13 or the fiber production device 11.

If you reduce the amount of gases coming out of the Au are entrained outside environment, by correspondingly reducing the opening 28 to a value dei is much less than the amount of air that the current ar can induce, the intensity of the vortex 31 becomes so large that the mat to be formed on the receiving member 15 would be destroyed. After all, it can sogai happen that it no longer becomes a sani at all mine of the fibers on the receiving organ 15 comes.

A device which enables the method according to the invention to be carried out is shown in FIG. 3 shown. The chamber 22 is closed at its upper end by a cover 32 which has an opening through which the stream 12 of fiber jets penetrates into the chamber 22. The edges 33 of this opening are tangents to the stream 12 and are profiled in such a way that they facilitate the passage of this stream. For reasons of more convenient utilization, the cover 32 can be arranged at a distance H from the fiber production device 11.

The device of FIG. 3 has a washing chamber 17 which is located behind the container 16 in the direction of flow is arranged. has a generally larger cross section than this and is provided with facilities. in which the exhaust gases 29, d. h "which the fibers between the Manufacturing device 11 and the removal member 15 accompanying gases and the suspended impurities with a washing fluid. especially water. In this wash chamber 17 the exhaust gases are partially freed from the Elemc.i'.en which they contain in suspension and which essentially consist of the fibers and the binder that they carry with them when they enter the impregnation zone and the Cross the fiber mat that is being manufactured. Upon contact with the washing water, the Exhaust gases contain drops of water and therefore tend to aul due to gravity to deposit the bottom of the chamber 17; this phenomenon is also caused by the sudden drop in speed the exhaust gases as a result of the change in de; Cross-section of flow on its path from the container 16 accelerated to the chamber 17. Some of the drops or the contaminating vapors are present absorbed the drop of wash water and dissolved before this. These two processes make up the Washing process of the exhaust gases. The water that was used to see and at least a part of it

has been transferred to the polluting waste gas batch, is discharged through the opening 24.

This device also has a separation system 18 of the cyclone or electrostatic type Separator on, Jas is arranged between the washing chamber 17 and the fan 19 and in which the Exhaust gases are at least partially freed from the water droplets that they have in the course of the washing process and which is important to remove before entering the fan 91. That from the exhaust Washing water obtained in liquid form is discharged from the separation system through the opening 25.

A collector 26 passes through the openings 24 and 25 wash water discharged to the treatment zone.

The stream 12 traverses the impregnation zone 13 and then the device 14 for fiber distribution. The fibers are deposited on the receiving element 15, and the exhaust gases 29 pass through the fiber mat 23 being manufactured, the container 16, the washing chamber 17, the separation system 18 and are pumped back into a connecting pipe 34 by the fan 19. Some of these exhaust gases are discharged from the system via the opening 35. The other part is passed through the tube 34 to the chamber 22, into which it penetrates through an opening 36 which is formed in a zone which is close to the fiber production device 11. The amount of gas entering the chamber via opening 33 is equal to the sum of the amount of gas released by fiber production device 11 and the amount of air 27 induced by it on the pipe with length H in free air. The amount of gas entering the chamber therefore increases with the length W.

In order for the system to be in equilibrium, it is necessary that the amount of water from the system through the outlet port 35 diverted exhaust gases is equal to the amount of gas entering the system through port 33 entry. The amount of exhaust gases to be discharged therefore decreases as the distance W decreases.

F i g. Figure 4 shows a particular embodiment in which the distance W is zero, i.e. in which the fiber-making device 11 or at least the exit openings of the fiber beams lie in the chamber 22. the The amount of exhaust gases to be discharged from the system is substantially the same as that from the manufacturing apparatus 11 fluids dispensed.

The proportion of the exhaust gases that are circulated can therefore in this embodiment values of at least Reach 96 to 97%.

In the case of the FIGS. 3 and 4 shown devices the circulated quantities correspond to those quantities emanating from the device 11 Can induce fiber jets, the flow of gases in the chamber 22 generally in the direction of flow of the stream 12 runs in the absence of disturbing eddies. The recirculated exhaust gases essentially follow the flow lines 37.

Due to the fan 19, the exhaust gases circulated according to the flow lines 37 can be seen give a speed slightly greater than that of the induced atmospheric currents Air is. The unmelted exhaust gases have sufficient energy to avoid a possible backlog of Counteract fibers.

The amount of exhaust gases discharged from the system can only be 3 to 4% of the amounts that are normally used be derived, so that only an extremely small amount of exhaust gas an expensive but effective cleaning treatment must be subjected.

The exhaust gases diverted through the opening 35 are treated by burning; This process is to bring the flue gases to a temperature higher than 600 ⁰ C, above which are converted by combustion in non-contaminating elements of CO2 and H2O, the impurities of the flue gases, in particular the phenolic compounds. This treatment also has the advantage of eliminating odors. The burning takes place in a cleaning device 38 of known type, which consists of a combustion chamber 39, a burner 40, which is supplied with a combustible mixture, and a known flame stabilizer 41. The treatment temperature can be reduced to between 300 and 400 ° C in the presence of a combustion catalyst.

The cleaned exhaust gases are passed through the chimney 42

derived to the atmosphere. At the outlet of the chimney 42, the temperature of the exhaust gases is sufficiently high, and due to the circulation, their throughput is sufficiently low that the condensation of the water vapor, contained in these gases, not until the exhaust gases are completely diluted in the atmosphere he follows. No opaque cloud of smoke thus appears at the exit of the chimney 42.

Due to the exhaust gas circulation, it is not necessary to completely wash the exhaust gases beforehand subject so that the size and investment therefor can be reduced.

Finally, you can not see the amount of exhaust gases to be discharged at the connecting pipe 34, but directly in the Detach chamber 22 through an opening 43 formed in the wall of the chamber in the area in which it is it is necessary to keep the pressure at the desired value, as Fig. 4 shows. The exhaust gases are from the Chamber 22 drawn off by a small auxiliary fan 44 and diverted through pipe 35. The ventilator 19 now only ensures the circulation of the exhaust gases. This embodiment enables a more precise one Definition of the zone with reduced pressure or zero pressure.

The throughput of the binder atomized by the nozzles 13 can be a function of the Adjust the amount of the constituents of the binder that is suspended in the circulated exhaust gases and that deposits on the fiber mat when the exhaust gases pass through it.

The circulation causes the exhaust gases to make repeated and very frequent passes through those in the manufacturing process to carry out the fiber mat located, and although the catching effect of this mat is low, because the speed of the exhaust gases through which it traverses is low, is the number of consecutive passes (about 15 per minute) such that an amount of the constituents of the binder suspended in the exhaust gases which is not negligible, is retained in the mat. This enables the amount of the atomized binder to reduce the more and the efficiency of the binder by about 5% increase, which is an economically not negligible advantage.

In a device such as that shown in FIG. 1 it is necessary to maintain a certain temperature in the chamber 22 and therefore the heat supplied by the material to be drawn and drawing gases derive. Since the material used to impregnate the fibers is thermosetting, it is subject to un-

ter the action of heat of a continuous development which it progresses from the liquid state, by atomizing it into the solid state. When the temperature of the chamber 22 becomes excessive is, the binder can reach a state of development during manufacture of the mat is sufficiently advanced to be able to bind the fibers. worsen. This appearance will referred to as pre-gelation and it is avoided by cooling chamber 22.

In the case of the in Fi g. 1, this cooling takes place by means of induced atmospheric air, the generally has a temperature less than the maximum temperature desired in chamber 22 is. The amount of heat conducted into the chamber by the fiber jets, which corresponds to the fiber production process about 1500 to 15,000 Kcal per kg of material are induced by mixing on the

Air line! then on Di ** Ahtrasp üKprtratrpn Hip rlavnn

give off a small proportion of the washing water when they come into contact with it and the Discharge the rest to the atmosphere.

In the present case, at least part of the heat introduced into the chamber 22 by the fiber jets is absorbed Transfer water by bringing the stream 12 or the exhaust gases into contact with the water. This Water, after it has absorbed the heat conducted into the chamber 22, is removed from and passed through any suitable system external to the device, chilled.

The heat exchange between the stream of fiber jets or the exhaust gases and the cooling water takes place either by direct contact or via a heat-conducting wall separating them. It is known that the amount of heat exchanged per unit of time with this type of transfer corresponds to the temperature difference between the fluid to be cooled and the cooling fluid and the contact area are proportional.

The relatively high gas or exhaust gas velocities, taking into account the dimensions of the system cause the times that are available to carry out the heat exchange are short. For For adequate cooling, the amounts of heat exchanged per unit of time must therefore be large. That's why the exhaust gases are cooled in the containers 16 and washing chambers 17, where the available volumes allow to realize large contact surfaces between the exhaust gases and the cooling water. This large area of contact is achieved in various ways, be it by taking the water in the form of fine droplets dispersed, either by letting it flow out in the form of a film of very small thickness or by it by letting the exhaust gases bubble through the water.

In the case of the in FIG. 3 device shown give z. B. Atomizer 45 cooling water in the form of webs or curtains from fine drops. the curtains running essentially perpendicular to the direction of flow of the exhaust gases 29. The exhaust gases, which have passed through the fiber mat being produced, reach the container 16 at a temperature of about 80 to 100 ^{° C. and are cooled down to a temperature of about 30 °} C. when they come into contact with the water curtains. The temperature of the water at the entrance of the atomizer 45 is about 15 to 20 ° C according to the possibilities of the cooling devices. Upon contact with the flue gases to the cooling water ewärmt to a temperature of about 30 to 40 ⁰ C in accordance with the flow rate of the atomizers 45th

The circulated portion of the cooled exhaust gases occurs after passing through the separation system 18 and the Fan 19 in the chamber 22, where it is released by mixing with the from the fiber production device II The gases cool these and the fibers in the same way as the atmospheric air in the case of the in Fig. 1 performs the device shown.

In Fig. 4 another embodiment is shown, in which the cooling water flows over partitions 46 in the form of a film of very small thickness. The exhaust gas flow 29 flows along these partitions, brushes the film of water and cools down when touched.

In Fig. 5 shows a further exemplary embodiment. In this device, the exhaust gas flow 29 opens out through the opening 47 below the free surface the amount of water contained in the container 48, which is arranged in. Sfömiingsrirhtiing behind the container 16 is, whereby in this amount and in the extension of the opening 47 it causes an intensive inflation, which generates gas bubbles, the liquid walls of which form a large water-exhaust contact surface.

Another method is to remove from the chamber 22 the material to be processed into fibers and to dissipate heat added to the draw gases by directly cooling stream 12 by sprinkled water on him. The supply of water to the stream thus takes place in a zone where the contact surfaces cannot be very large as the space available is limited. but where the Temperature difference between the fluid to be cooled and the cooling fluid is large.

Different types of implementation are envisaged. For example, in the case of FIG. 3 embodiment shown set up atomizers 49 between the fiberising apparatus 11 and the spray nozzles 13 for the binder are arranged, a jet finer Drops of water against the stream to be cooled.

The drops reach the stream 12 in a zone where the latter has a high temperature, which ^{can reach up to 600 °} C., and are evaporated immediately.

Considerable amounts of heat of around 650 to 700 Kcal per kilogram of evaporated water required for evaporation of the drops are necessary are taken from the stream 12, which is therefore a very rapid one Cooling is subjected to its temperature at the level of the spray nozzles 13 to a size of about 100 up to 120 ° C. The generated steam is together with the exhaust gases across the fiber mat 23 to the Container 16 and the washing chambers 17, where it comes into contact with the water curtains that flow from the atomizers 45, condensed and its stored heat to that of the atomizers 45 transferred cooling water.

The arrangement of the atomizers 49 for the supply of cooling water against the flow 12 between the fiber production device 11 and the spray nozzles 13 is useful because the temperature difference between the flow to be cooled and the water and thus the heat transfer is greatest in this zone, and finally the atomization of the binder to a stream of fiber beams with a sufficiently low temperature (100 to 120 ⁰ C) takes place, so that the decomposition of the binder by loss of volatile elements is very limited or zero

This results in an increase in the binder efficiency of about 5% and a consequent one

Reduction of pollution in exhaust gases.

Another embodiment is shown in FIG. 4, in which the device 50 for spraying cooling water is arranged against the flow 12 between the spray nozzles 13 and the receiving member 15. As with the In the embodiment of FIG. 3, the cooling water passes through the mat 23 in the form of steam. This water condenses by transferring its heat to films of water that extend over the partition walls 46 of the washing chamber 17 stream.

This water is through openings 24 and 25, the bottom of the containers 16 and 17 and the separation system 18 are arranged, derived from the device to a device 51 in which the water of solid, suspended particles, especially fibers, is freed.

The device 51 can be a known vibrating or rotating machine filter, a decanter or a centrifuge also of known type.

The water freed from the solid, suspended particles is collected in a container 52 and then guided by gravity or by means of a pump 53 / u to a cooling station 54. At the exit of this Station, the chilled water can be diverted from the system or reused.

The station 54 may consist of a cooling tower 106 of known type, in which the water on contact with Air is cooled. However, if the washing water is directly cooled in the tower 106, there is a danger air pollution from the most volatile elements of pollutants in the wash water r.

This risk is small because of the amount of impurities that are released in this way from the tower 106 into the Atmosphere released is less than 5% of the amount released by the chimney 35 with a non-circulation working device like the one in FIG. 1 shown is delivered.

This risk is eliminated by the fact that the washing water is cooled in a heat exchanger 105, the The cooling fluid is unpolluted water that is in the cooling tower under the action of the pump 107 runs around. So that no water is released from the device in liquid form in order to avoid the environment by polluting impurities that the water contains, the water runs in a closed one Circle the device around.

In the case of the FIGS. 3, 4 and 5 shown devices the closed circuit, which is followed by the cooling and washing water, is the following:

The water leaving the cooling station 54 is supplied by the pump 55 to the atomizers 49 and / or the device 50, which are located in the chamber 22, and to the steam condensation and exhaust gas scrubbing devices, which lie in the chamber 17 and which the atomizer

45 of FIG. 3 or the partitions with the water film

46 of FIG. 4 or the container 48 of FIG. 5 include.

The wash water and condensed steam, laden with impurities, fibers and binder components, flow through the openings 24 and 25 at the bottom of the washing chamber 17 and the separation system 18 are, in a collector 26, which leads them to the filter device 51, from the washing water separates the solid, suspended waste products 56, fibers and insoluble binder ingredients.

These waste products are collected in a conveyor 57. The filtered wash water that only impurities and contains dissolved binder components, is carried out by gravity or by means of the pump 53 to the treatment station 54.

When the washing water circulates in the closed circuit, it is necessary to determine the concentration of the dissolved or suspended in the filtered water. cn to keep constituents below a certain size; this is about 3 to 4%, calculated in the mass unit of dry materials per mass unit of water. Above

ίο this size is part of the wash water dissolved or suspended material (mainly microfibers or microparticles of the binder, which are not captured by the filter device 51 and soluble binder components) on various Divide the device. The binder becomes polymerized and forms viscous or rigid Layers, which progressively the washing water outlet openings 45, 49 and 50 and which in the receiving organ 55 closed openings for the passage of the exhaust gases 29. This results in a reduction the amount of discharged exhaust gases and the cooling of these exhaust gases, which comes to a standstill after a short time the device leads.

In order to keep the concentration of the water in the materials carried under the desired value, is it is necessary to remove considerable amounts of material from the wash water. A significant proportion of around 20 to 30% of the binder sprayed onto the fibers by the spray nozzles 13 is already found through the described process in the wash water again. In large factories this results in 3,000 to 5,000 kg of binder per day (calculated in dry materials) in the closed circulation circuit of the washing water to introduce, and in order to keep the concentration at an equilibrium value, it is necessary to that To remove water binding agent quantities which are equal to the imported ones.

Several extraction methods are possible:

One of these methods is to treat at least part of the wash water in a centrifuge, which can separate solid, suspended, much smaller particles from the water than the filtration device 51 can. The water treated by the centrifuge 58 can return to the container 52, ie this F i g. 3 shows, or, what is more advantageous, are fed back into the atomizers 49.

Another method is to treat the water by adding a flocculant and then excrete the flocculated material.

Both of these processes have the disadvantage that the water essentially contains the insoluble constituents be withdrawn that it contains. The dissolved binder that makes up most of the material to be removed is not or only slightly influenced.

One method of extraction is to use the filtered or centrifuged wash water, in order to dilute the binder when it is sprayed against the fibers from the spray nozzles 13. The decrease filtered water can be at any point in the circle downstream of the cooling station 54 in the direction of flow or more advantageously downstream of the centrifuge 58 by means of the valve 59, as shown in FIG. 3 shows.

Another method is to add the wash water as the cooling fluid of stream 12 in chamber 22 use. The washing water is then supplied by the atomizers 49 of the Γ i g. 3 or 50 of FIG. 4 against the Stream 12 directed

Both of these methods have the advantage that they

Allow reuse of part of the binder contained in the wash water, thereby reducing the sprayed The amount of binder that can be regulated as a function of the amount of binder is the mat 23 of withholds the water sprayed by the atomizers 49; this enables an improvement in the impregnation efficiency, however, these methods do not allow sufficient washing water to be obtained Extract amounts of dissolved binder to make the concentration of the water below the desired one Worth keeping. This is done according to two procedures that it does allow the extraction of significant amounts of dissolved binder from the closed loop recirculated water to complete.

One of these methods is to burn off a small portion of e'Ma 1 to 5% of the washing water throughput in the circulation circuit in a suitable device 60. This is in Fi g. 4, is of known type and comprises: a burner 61 which is supplied with a combustible air-fuel mixture: an injector sprayer 62 into which the water to be treated passes through line 63 u.id in the form of droplets under pressure is sprayed into the flame of the burner 61 under the action of the atomizing air 64; a reaction chamber 65 in which the washing water is treated under the action of the heat given off by the burner 61. This consists first of all in evaporating the washing water and then bringing the generated steam, as well as the binder components carried along by the water, to a temperature of around 800 ^° C., which enables these polluting binder components to be converted into non-polluting elements such as CO2 and H2O.

The non-polluting steam escapes through the chimney 66 from the system at a high temperature and thus avoids the formation of an opaque cloud of steam.

The point of use for the water to be treated is generally between the pump 53 and the Cooling station 54. as in FIG. 4 shows.

This method has the advantage that it contains all Binder components in the treated wash water are extracted and converted into non-contaminating Elements are converted. It has the disadvantage that it requires a considerable amount of energy and therefore is very costly. The Influence of Treatment Costs on the Price of Fiber Products Made can be reduced if some of the heat amount of high temperature steam is in one Recovering heat exchanger that produces superheated steam for various uses.

Another method is to take a minor Part of about 1 to 5% of the throughput of the wash water, which entrains the dissolved binder, during the circulation subject to a heat treatment in the circuit in order to make the binder insoluble and it then by any suitable separation method such as filtration. Flocculation. Centrifuge the To separate water.

It was found that. if that's for cooling and washing of the exhaust gases, the water used, which is therefore the binding agent or dissolved binding agent components after the filtration contains, has been kept at a certain temperature for a certain time, a proportion of the dissolved binder that increases with temperature and time is converted into insoluble particles and therefore finds itself suspended in the water and therefore easily separated from it can be.

The proportion of dissolved material made insoluble by the treatment characterizes the degree of effectiveness the treatment.

The treatment temperature has a considerable influence on the efficiency. For example, it was found that for a water which contains 1% constituents of dissolved binder, the treatment efficiency was as follows:

40% if the water is at 40 ^° C. for 8 days

was held.

40% if the water was ^{kept at 70 0} C for 3 days,

40% if the water is on for 3 minutes

160 ° C was kept,
60%. if the water was ^{kept at 180 0} C for 3 minutes,
95%. when the water is on for 3 minutes

240 ⁰ C was held.

F j g. 6 shows the course of the efficiency of the treatment depending on the temperature and the treatment time.

In large factories for the production of bonded fiberboard, in which the quantities of water to be treated can reach 50 mV hours, it is necessary to determine the shortest treatment times and thus to use them at high temperatures above 100 ° C. in order to avoid the arrangement of treatment plants of considerable dimensions work. This leads to the treatment being carried out in an enclosed space under pressure at a temperature which is approx. 5 ¹ C below the boiling point of the water at the pressure of the enclosed space, so that the water remains in the liquid phase for the duration of the treatment . This solution has the further advantage that it requires only a small amount of energy.

the. Apart from the losses, only the increase corresponds to the heat that the water increases its temperature is supplied.

With the same extracted amount of dissolved binder, this process is four times less expensive than the procedure described above by burning off.

One of the common drawbacks of heating water in an enclosed space is the contains dissolved binder or binder components even at a low concentration, consists in that an insoluble binder deposit forms on the walls of the enclosed space, which very quickly reaches a thickness sufficient to accommodate the outlet openings to clog the enclosed space or the enclosed space itself.

It has been found that when the heat, the / ur Treatment is necessary. is released within the bulk of the / u treating water and the wall of the enclosed space at a temperature below that for the duration of the treatment the bulk of the treated water is maintained, no deposit is formed on the wall and it is insoluble made binder in the water remains suspcndicrl. This causes the water, be it by mixing with hot fluids such as preferably superheated water vapor or combustion gas of a submerged Burner, be it through bodies that concentrate energy in the bulk of the water like a electric arc, to be heated.

A wide range of operating conditions are possible, e.g. B. 6 to 40 bar for the absolute pressures, 160 to 240 ⁰ C for the temperatures. 3 to 10 minutes for the duration of the treatment.

The following conditions arise because of a tradeoff between energy costs and the maintenance costs of the system:

Temperature:
Pressure:
Duration:
Efficiency:

200 ⁰ C

16 bar absolute
5 minutes
70 to 80%

This treatment process can be carried out in a device with discontinuous operation or in a device with continuous operation.

F i g. Figure 7 shows a discontinuous operation apparatus for performing this treatment process. The water to be treated is by means of the motor-operated valve 67 in the enclosed Room 68 introduced The amount of water introduced or the charge represents 70 to 80% of the capacity this enclosed space. The heating fluid, preferably superheated steam, arrives then into the enclosed space through the nozzle 69, the outlet of which is immersed The amount of steam is regulated by the motor-driven valve 70 controlled by the regulator 71.

The treatment cycle is as follows:

The enclosed space 68 contains a charge of water to be treated at atmospheric pressure. At the desired treatment pressure, z. B. 16 bar absolute. The valve 70 opens, and the steam flows out through the nozzle 69. mixes with the water to be treated and transfers to it, by condensing, its entire stored, detectable Warmth. The temperature and pressure in the enclosed space 68 increase until they are about 200 ° C and Ib bar absolutely reach. The introduction of steam will then interrupted. The nozzle 69 was designed so that this temperature and pressure rise rapidly with takes less than a minute. The water is heated to 200 ° C. and 16 bar for 2 to 4 minutes absolutely held. Thereafter, a pump 72 is put into operation to over the double wall 74 a to direct a new batch of water to be treated into a container 73. During his passage in the double Wall causes the water to be treated, which has a temperature of about 40 ° C at the inlet, cooling the treated water contained in the enclosed space 68. The dimension the double wall 74 was determined so that the water to be treated in the container 73 with a Temperature of about 80 ° C arrives.

An additional coolant circulates in the second double wall 75 and stops the cooling of the treated water contained in the enclosed space 68. This cooling is considered complete considered when the temperature of the treated water falls below 100 ° C and preferably to 40 to 50 ° C. At this point, a motor-driven valve 76 is gradually opened to reduce the pressure in the to dismantle enclosed space 68.

The treated water flows to a filtering station 51 or to a flocculation, decanting or centrifuging device. which separates the binder made insoluble by the treatment from the treated water.

The filtered water flows into the container 52 and the extracted waste products 56 are dumped into a conveyor 57
When the enclosed space 68 is empty, the valve 76 is closed and the valve 67 is opened so that the preheated water to be treated, contained in the container 73, can flow into the enclosed space 68 by gravity. A vent valve 67a completes the system. A new cycle

ίο can begin.

Fig.8 shows an apparatus with continuous Operation for the implementation of the treatment process.

A pump 77 sends the water to be treated at treatment pressure to a mixer 78, in one Opening nozzle 79 through which the heating fluid, Water vapor, arrives. This steam mixes with the water to be treated and transfers it all its heat on this by condensing it.

The steam flow rate is determined by the motor-driven one Ventii 80 regulates, which is controlled by the controller 81, to at the output of the mixer 78 the Maintain desired treatment temperature. At the output of the mixer 78, in which there is about 10 Seconds remain, the water to be treated passes through a reactor 82 where the binder is insoluble is made and its dimensions are determined such that the residence time of the to be treated Water of treatment time, d. H. 2 to 4 minutes, is equivalent to.

On leaving the reactor the water is cooled in a heat exchanger 83 to a temperature below 100 ⁰ C and preferably to 40 to 50 ° C. A portion of this cooling is provided by the water to be treated, the preheated in this way in the cooling coil 84 of about 40 ⁰ C to about 80 ° C.

At the outlet of the heat exchanger 83, the treated and cooled water is passed through a pressure reducing valve relaxed to atmospheric pressure, which, controlled by a regulator 87, the treatment pressure in the Chamber maintains.

The expanded water flows to a filter device 51 or a flocculation decanter or a centrifugation device which is insoluble in the water to be treated by the treatment made binder separates. The filtered water flows to the container 52, and the waste products 56, the residues from the treatment are dumped into a conveyor 57.

The device of FIG. 8 with continuous operation c-allows more adaptable and less expensive treatment than that in FIG. 7 shown.

Another method is to subject a portion of the wash water containing contaminant elements to bacteriological treatment in a ventilated pool. In such a pool, the bacterial organisms present enzymatically lead to decomposition, in particular of the phenol products which are present in the water. Treatment by a process that corresponds to a complete oxidation reaction leads to the conversion of phenol products in particular into non-polluting elements such as CO2 and H2O. So that this reaction is complete. it is necessary to provide the bacterial organisms and the oxidation reaction with the necessary oxygen by ventilating the pool.
The devices for the production of fiberboard

emit a large amount of waste products of various types, all of which are binders or contaminants Contain binder components.

First of all, these are the manufacturing waste products, that are discarded by quality control. These waste products contain impurity elements in a very dispersed form, but are bulky. After all, it is the waste products coming from the filtration of the cooling and washing water, the fibers and contain a very high concentration of binder and binder components. All these Waste products have traditionally been stored in abandoned quarries.

Efforts are being made, however, to ban this practice since it has a polluting effect

The invention provides a method for converting the waste products into non-polluting elements. It consists in subjecting the waste products to a thermal treatment after prior preparation, which converts _{the contaminating materials into non-contaminating elements such as CO 2} and H _{2 O by burning them off}

F i g. 9 shows an apparatus which enables this method to be carried out

The waste products 56 that come from stations for thermal treatment and filtration of the water, are forwarded by the conveyor 57 and conveyed into a mixer 88, where they are mixed with the waste 87 bonded fiber products coming off the production lines.

At the outlet of the mixer 88, the mixture is tipped into an incinerator 90 by means of a conveyor 89. The heat released by the burner 91 brings the waste products to a temperature higher than 1000 ^° C. At this temperature, the binder and the binder components are converted into non-polluting elements such as H ₂ O and CO ₂ and together with the combustion gases from the burner 91 through the Chimney 93 discharged into the atmosphere. The material that forms the fibers softens by the heat and collects at the bottom of the furnace 90 and is discharged from the latter via the outlet 92 in the form of a viscous thread and is cooled in the container 94 filled with water. The cooled material is in the form of granules that can be converted back into fibers.

Fig. 10 shows another device that does the treatment which enables waste products.

The mixture of waste products 56 and 87 exiting mixer 88 is deposited by conveyor 89 on a belt 94 which passes through furnace 95. Due to the heat emitted by radiation or electrical resistance burners%, this brings the waste products to a temperature of around 600 to 700 ^° C. At this temperature, the binder or the binder components contained in the waste products are converted into non-polluting elements such as CO; and H ₂ O, which are discharged through the chimney 97.

The fibers, which make up the bulk of the waste products by volume, are under the action the heat softens, rearranges and cakes together into plates 98 of volume bound, which is much less than the initial volume of the waste products. These plates can then be reintroduced into the fiber production cycle.

In the case of the FIGS. 3 and 4 shown devices one gives the lid 32, which has the opening 33, through which the stream 12 penetrates into the chamber 22, and the other walls 21 of which have a shape which makes it possible Sound-absorbing panels 99 inside the chamber 22 and look-absorbing panels 100 outside the Chamber 22 to be arranged. The reduction in the sound levelE achieved by the arrangement of these panels is, in the zone that surrounds the fiber production device 11, here is 20 to 30 decibels, -'as the ίο Significantly improved working conditions for workers. 1 devices have the considerable volumes to be discharged through the chimney 35, and the effort to reduce the batch losses therein to limit, led to a chimney with a large cross-section directly at the outlet of the ventilator 19 install and thus radiate almost the entire sound power that is emitted by it.

In the case of the FIGS. 3 and 4 allows the small volume of the discharged Exhaust gases to remove the outlet parts of the exhaust gases from the fan 19. You arrange it on the connecting pipe 34 at one separated from the fan 19 by at least one bend and a length of tube Place that is sufficient that at least part of the sound line emitted by the fan 19 is absorbed by the tube 34. The reduction in the sound level in the surrounding chimney 35 Zone can reach 10 decibels or more.

F i g. 11 shows an apparatus comprising: A fiber manufacturing apparatus 101 in which the molten material 102 is poured into one at a high speed rotating body is introduced, which has a certain number of openings on its circumference through which the material exits under the action of centrifugal force The resulting threads then become the action of an annular concentric jet of hot drawing gases at great speed which is generally downward and draws them into fine fibers.

A fiber distributor 14 that moves the stream 12 back and forth.

A cooling device comprising atomizers 50 to directing the cooling jet onto stream 12. This device is between the distribution device 14 and the spray nozzles 13 arranged.

A receiving member 15 for forming the mat, which consists of a perforated tape.

A cuboid chamber 22, the bottom of the perforated Aufna'hmeorgan 15, laterally from the vertical Walls 21 and above is bounded by a horizontal cover 32, which is at a distance of 00 mm from the fiber production device 101 and has a circular opening 33 which the stream 12 crosses. The edges of this opening are profiled to facilitate the entry of the jet 12, and are tangents to these. The vertical walls 21 delimit the perforated receiving member 15 the mat-making zone.

A container 16 which is located under the perforated receiving member 15 is arranged in the mat production zone and by a fan 19 with negative pressure is applied.

A washing chamber 17 which is arranged downstream of the container 16 and atomizer 45 arranged to form curtains of water droplets on the path of the exhaust gases 29.

A separation system downstream of the chamber 17 in the direction of flow 18 in the form of a cyclone.

A fan 19 that circulates all the gases that make up the fibers accompany the receiving organ 15, forces this to traverse and they in the connecting pipe 34 promotes.

A connecting pipe 34, the rear end of which in the direction of flow through the opening 36 into the fiber distribution device 14 opens. Circulated amounts of exhaust gas of around 90 to 95% pass through the receiving organ 15 and are guided from the connecting pipe 34 into the chamber 22 via the opening 36

A line 35, which lies on the pipe 34, conducts 5 to 10% of the exhaust gases that have passed through the receiving member 15 to the burning device 39. After passing through the combustion device, where they are brought to a temperature higher than 600 ° C, are the exhaust gases released into the atmosphere.

Absorbent panels 99 and insulating panels 100 attached to walls 21 and 32 in the zone near the Fiber production device 101 are arranged.

A pit 103, which receives the washing and cooling water, those with fibers, binders and binder components, dissolved and in suspension, are loaded and come from ports 24 and 25 that arrive the chamber 17 and the cyclone 18 are arranged.

A pump 104 which directs the water contained in the pit to a filter device 51

A vibrating filter device 51 which separates the insoluble waste products from the wash water.

A container 52 placed under the filter 51 in which the filtered water is collected.

A heat exchanger 105, in which the water contained in the container 52 under the action of the pump 53 rotates, cools down and the heat stored on contact with the exhaust gases 29 on its passage through chambers 22 and 70 and container 16.

A cooling tower 106, holding the cooling water of the heat exchanger 105 rotates under the action of the pump 107.

A pump 55 that recirculates the water in the tank 52 and delivers it to the atomizers 50, the Device for condensation and washing of the exhaust gases 29. of the station 108 for the preparation of the impregnation and pumped back to the water treatment station 109.

A water treatment station 109, in. Which is absolutely kg bringing the water to be treated by the pump 77 to a pressure of 16 and then passes through a heat exchanger 83 where it is heated to about .3O ⁰ C. At the outlet of this heat exchanger, the water to be treated passes into a mixer 78, where it is brought into contact with a stream of preferably superheated steam and thus brought to a temperature of 200 ° C., at which it is held in the reactor 82 for 2 to 4 minutes , which is arranged at the output of the mixer 78. At the outlet of the reactor 82, the treated water is cooled to a temperature of 40 to 50 ° C, then expanded to atmospheric pressure by the pressure reducing valve 86 and passed to a centrifuge UO, which separates the binder made insoluble by the treatment from the treated water . The treated water is returned to tank 52.

A fresh water supply line 111 which opens into the container 52 and enables the quality of the water to be kept constant in the system. M.

Sponsors 57 and 112. The waste products of fiI-trierslation 51 and the water treatment station 109 as well as the production lines to the station 113 for Treatment of waste products results.

A station 113 for the treatment of waste products, which consists of a furnace equipped with a gas jet pipe or electrical resistors and in which the waste products are brought to a temperature of about 600 to 700 ° C to produce the binder and to burn off the binder components and to bake the fibers together to form sheets of small dimensions, which can then be reintroduced into the fiber production cycle.

F i g. Figure 12 shows another device comprising:

A fiber manufacturing device in which the molten Material, in particular glass, flows from a crucible 114 in the form of threads 115 solidify before they come into contact with drive rollers 116 which heat the solid strands into one High velocity gas jet 117 usually in a direction practically perpendicular to this ray. This causes the end of the strands to heat up and becomes soft, see that the ray pulls them fibers and they to the Mattenherstellungsoi * an in the form of a Stroms 12 can promote.

A cooling device having atomizers 50 to spray cooling water onto stream 12.

Spray nozzles 13, in order to spray the binding agent onto the stream 12, which are in the direction of flow of the stream 12 are arranged behind the cooling device.

A receiving member 15, which consists of a perforated tape.

A cuboid chamber 22, the bottom of the perforated band, to the side of the vertical walls 21, bounded at the top by the cover 32 and at the rear by the vertical wall 118, which is about 200 mm from the Exit opening of the jet 117 is arranged remotely and has a rectangular opening 33 through which the stream 12 traverses.

The edges of this opening are contoured to facilitate entry of the stream 12 and are tangent on these. The vertical walls 21 delimit the mat-making zone on the perforated belt 15.

E-ien container 16, which under the perforated tape in the mat production zone is arranged.

A washing chamber 17, which is arranged under the container 16 and has openings 47, which under the Surface of a quantity of water 48 mint and through which the exhaust gases 29 flow. Atomizers 45 do that Wash water, which drains an overflow opening 24 to the collector 26.

In the direction of flow behind the chamber 17, a separation system 18 in the form of a cyclone.

A fan 19, which forces all the gases that accompany the fibers onto the receiving member 15, to close it durchn-ieren and promotes them into the connecting pipe 34.

A connecting pipe 34, the rear end of which in the flow direction enters the chamber 22 via two openings which are formed in the two vertical walls 21 on either side of the fiber manufacturing device lie, opens into a zone that is close to this. Circulated emissions, up to 95% of that of the perforated Belt volumes passing through are entered into chamber 22 via these openings directed.

A line 43 which opens into the chamber 22 in a zone at the lower end thereof in the direction of flow Chamber lies, as well as the portion of the unrecirculated exhaust gases, via the fan 44 to the combustor 39 derives.

Absorbent panels 99 and insulating panels 100,

those on walls 21, 32 and 118 in the zone near the Fiber manufacturing device are arranged.

A pit 103 that collects the washing and cooling water, those with fibers. Binders and binder components. dissolved or in suspension, are loaded and come from the openings 24 and 25 at the bottom of the Chamber 17 and the Abscheidsystetn JfJ are arranged.

A pump 104 which directs the water contained in the pit to a filter device 51.

A vibrating filter device 51. the separates the insoluble waste products from the wash water.

A container 52. the one under the filter device 51 is arranged and collects the filtered water.

A heat exchanger 105, in which the water contained in the container 52 under the action of the pump 53 revolves and cools down by the contact with the exhaust gases 29 as it passes through the chambers 22 and 17 emit stored heat.

The device just described also has as shown. a water treatment station and a station for the treatment of waste products, which are the same as those described above with reference to FIG. 11 have been described.

Fig. 13 shows a further device which has:

A fiber manufacturing apparatus into which the molten material is fed from the feeder 118 of a furnace flows through the openings of one or more rows of nozzle nipples which are provided on a drawing nozzle 119 are, whereby a large number of threads of material is generated that flow into a drawing zone in which they traversed between converging gas jets of high velocity. The exit openings 120 of the rays are very close to the filaments of the glass, and the rays spread downward in one direction to the direction of movement the glass thread from a practically parallel direction. The rays become very common formed by high pressure steam.

A cooling device 50 for spraying cooling water onto the stream 12.

Spray nozzles 13 to spray the binder onto stream 12.

A fiber distribution device 14, which consists of two compressed air nozzles, around the fibers in a wanted one Direction to direct.

The device shown in Fig. 13 corresponds to the rest of those of FIG. 11.

F 1 g. Figure 14 shows another device comprising:

A fiber reeling device. in which the material in the liquid state and in thread form 121 on the circumference of a rotor 122. which moves at high speed is directed at high speed by nozzles emerging from orifices 123. The rotating body 122 converts part of the material it receives under the action of centrifugal force, into fibers and directs the other part to a second rotor 124. which is carried out by a corresponding The process of converting some of the material it picks up into fibers. The number of rotors 122 is im generally limited to 2 or 3.

Fluid jets are passed through a ring of openings 125 surrounding rotors 122 and 124 also released at great speed, which act on the fibers produced to make them To direct acceptance body. These jets are formed by high pressure air or steam.

The openings 125 are also generally used to facilitate the spraying of the binder onto the Ensure fibers.

The device of FIG. 14 corresponds otherwise that of FIG. 12.

In addition 12 sheets of drawings

Claims (9)

Patent claims: 1. Process for the treatment of exhaust gases in the manufacture of mats or panels from mineral fibers be delivered, in which the fibers after being drawn at the exit from the fiber production device Binder is supplied and the fibers are finally passed to a receiving member to form the fiber mat or fiber board and a part of the exhaust gases, which are composed of the drawing gases from the fiber production device, of these induced gases as well as of entrained impurities, after traversing the mats or plates and the receiving member are washed with water and a Part of the exhaust gas is released into the atmosphere after a cleaning treatment, thereby characterized in that the washed exhaust gases are at least partially recycled and thereby form the gases for fiber formation or fiber transport to the receiving organ or add. 2. The method according to claim 1, characterized in that that the amount of exhaust gases emitted into the atmosphere is equal to the amount of the Drawing process is necessary gasu 3. The method according to claim 1 or 2, characterized in that the in the fiber production zone recirculated gases between the production and the receiving organ along a Path are guided, which is parallel to that of the drawing fluids. 4. The method according to claim 1, characterized in that that the washing water is used again after partial cleaning and either again as washing water or cooling water atomized onto the fibers and thereby also to reduce the the binding agent required to produce the mat is used 5. The method according to claim 1 or 2, characterized in that the not recirculated, Exhaust gas to be released into the atmosphere prior to direct or catalytic combustion is fed. 6. The method according to claim 5, characterized in that the exhaust gas previously an electrostatic Is subjected to cleaning. 7. Device for carrying out the method according to claim 1 with a fiber production device, a chamber surrounding the fibers between a fiber production device and a the take-up element forming the mat, with exhaust gas contacting devices and a device for separating the water from the exhaust gases, characterized by an opening (27) through which the Stream (12) of fibers and fluids from the fiber making device (11) enters this chamber (22), a device for recirculating the Exhaust gases and devices (45) in the direction of flow behind the receiving element (15) for making contact of the exhaust gases with the washing water, one behind the receiving element (15) in the recycling circuit arranged fan (19). a connecting pipe (34) leading the exhaust gases into the chamber and a Pipe (35) supplying exhaust gas from a cleaning device (38) upstream of the outlet into the atmosphere. 8. Apparatus according to claim 7, characterized in that the inlet opening of the exhaust gases to Cleaning device (38) leading pipe (35) to the connecting pipe (34) between the fan (19) and chamber (22) is located 9. Apparatus according to claim 8, characterized that the inlet opening of the cleaning device (38) leading to the pipe (35) on the Wall of the chamber (22) is arranged