KR810000078B1 - Inhibition and purification method of pollutants spilled out during mineral fiber production - Google Patents

Abstract

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Description

Inhibition and purification method of pollutants spilled out during mineral fiber production

1 is an explanatory diagram of a conventional collecting device to which the present invention can be applied.

FIG. 2 is a view similar to that of FIG. 1 in which the chamber wall extends to the fiber making apparatus. FIG.

3 is a general schematic view of the fiber collecting device according to the present invention.

4 is a general schematic view of a star-shaped embodiment of the present invention.

5 is a star-shaped embodiment of the toxic substance washing room.

6 is a diagram showing the change in efficiency of insoluble treatment with treatment time and temperature.

7 is an explanatory diagram of a washing water treatment apparatus by heating under pressure.

8 is an explanatory diagram of a continuous process apparatus of washing water treatment.

9 is an explanatory view of a heat treatment facility of scrap metal waste of the present invention.

10 is a star-shaped embodiment of the device of FIG.

11 is an overall view of a fiber collecting device for producing fiber glass according to the present invention.

12 is another exemplary embodiment of a fiber glass manufacturing process.

Figure 13 is another embodiment of the present invention applied to the mineral fiber manufacturing process by the ball.

14 shows another embodiment of the invention suitable for the manufacturing process of mineral sulphates and especially solvents.

The present invention relates to a method for removing the toxic or odor pin contaminants contained in the waste or waste liquid discharged from the mineral mu production apparatus or reducing the noise generated at the same time while suppressing harmful elements.

Therefore, the present invention is applied to a factory facility for producing a product by applying a cloth to the fiber by using a thermoplastic binder to the fibrous blanket, mat, pad or mineral fiber paper.

In general, the binders used in the preparation are based on phenolformaldehyde or aminoplasts and pure or modified phenolic or aminoplast resins. The reason is that they show very convenient features for the preparation of their fiber assemblies, in fact they are thermoset and water soluble, and also adhere well to the fibers and are relatively low in cost. The binders are dissolved or dispersed in water, and some additives are added to make a suitable binder for spraying the fibers.

Due to the heat effects given during the production of textile products, phenolformaldehyde, iodine, ammonia and fibrous degradation products release toxic opportunistic elements with an irritating odor that can be felt at very low concentrations.

Other binders are being used for cheap base oils.

Some extracts of natural products are hardened by drying, such as linseed oil, by oxidation and others are thermoplastic, for example bitumen. All of this is in the process of binding the fibers, raising the temperature to some extent and keeping the temperature high enough to remove harmful or unneeded elements by volatile and odorous elements.

The term “binder” as used in the following text refers to one or all of these binding products, and they are either in liquid form or dissolved in water or other liquids, or in emulsion form.

FIELD OF THE INVENTION The present invention relates to one facility for the manufacture of textile material aggregates, the sieving of which is located immediately behind the fiber making apparatus and is called the fiber collecting or fiber forming section. In particular, the following operations are carried out primarily in this facility.

Conveying the fiber from the textile manufacturing apparatus to a mat or a blanket forming apparatus.

-Applying a binder to the fiber, which generally causes the binder to bind to the pollutant.

Application of a binder to a fiber collecting device, which generally uses perforated belt extraction in the collecting device.

Cooling the gas and fibers used to thin or guide the fiber, which is generally done by means of air containing gas.

To induce air by inhalation and to separate the fibers from the gas when the blanket is formed.

-Dispose of fabric blankets or mats so that they do not remain in any element of the facility.

In the fiber collection or forming section, a large amount of gas and water come into contact with binders that contain and attract pollutants. This water and gas are contaminated by pollution processes, as is commonly known in the manufacturing process of solidifying blankets, mats or fabrics with binders. I will explain this.

A) Pollutants released in gaseous form take the following steps. The binder is injected into a stream of fibers and gases from the fiber manufacturing apparatus, and the binder is present in the form of clouds of fine particles. Some of these binders are absorbed by the fibers, some are exposed to the walls of the device, and others are detected as gases or toxic substances in the form of fine particles and vapors. These two fluid contaminant forms coexist, one is present as a contaminant by the fine particles of the binder and the other is present as a contaminant by the vapor of the binder. In applying the binder, the atomizing or dispersing device of the binder is used to treat particles of a very wide diameter. If the fine particles are not absorbed by the fibers, they are pulled through the blanket formed by the gas phase flow and are present in the gas phase flow. Particles of the binder exposed on the fiber during application of the binder are subject to the kinetic effect of the gas phase flow through the formed blanket.

Many heme particles are extracted from the fibers, migrate through the blanket and are found to be contained in the exhaust gas. Finally, the necessity to ensure a uniform distribution of the binder in the blanket is necessary to disperse the binder in the fibers and in the gaseous flow in the vicinity of the fiber making apparatus, and these gaseous streams are still well defined in geometric form. The temperature is still high enough that some binder or at least most of the volatilized elements will evaporate. These polluting vapors mix with the gases and contaminate them.

In the text below, the word “fume” is used to denote a gaseous effluent passing through a fiber blanket and exiting the collection device. That is to say generically the gases used to thin or guide the fibers, the fluids containing these gases, and the polluting elements in the form of particles or vapors contained in these fluids.

It is understood that various devices of the present invention, in other words, operating procedures and elements of the device, can use "fumes" having a wide range of components and pollutants. While suitable for handling all components of such toxic substances, the various devices of the present invention also handle gases with pollutant elements produced in working with fibres, regardless of whether or not the pollution is due to binders in the fibres.

B) The function performed by the water in the fiber collecting device will generate a large amount of contaminant pollutants in any facility where the binder is used. In operations where water is used,

(1) When the binder is used in the liquid phase, the binder is diluted and transported.

(2) Clean and remove toxic substances.

In operations where the maximum amount of pollutants in the toxic substance is contained in the form of particles or vapors, the pollutants are converted to toxic substances and transferred to the wash water when caught by the particles of the scrubbing water. In jobs where fibers are caught or loaded into the jaws of the collecting device, they are absorbed by toxic substances.

(3) Clean other parts of collection facilities (pore belts, toxic material conduits, etc.) to discharge binders or attached fibers.

Binder elements are attached to the wash water during this operation and these binder elements are soluble, insoluble or vapor phase, and the concentration of the pollutant reaches a high value.

The above-mentioned upwards is based on the description of measurements and observations made in actual production facilities for the contamination of toxic substances and water. Data derived from such measurements and observations are given herein as data, but other data or interpretations are well known, and it should be understood that the present invention is not limited by the given data. Regardless of the fiber tea process, in all manufacturing apparatus of integrated textile products, the pollutant will have a significant amount of effluent.

In a facility equipped with a device for thinning fibers by blowing, the material in the facility is converted to fibers by high energy injection, and the amount of toxic substances released into the air is determined by the following values. Have

-100 Nm 3 / kg (fiber) in the positive described in the US Pat. No. 2,133,236

-300 Nm3 / kg (fiber) in the Aeroco positive of US Patent No. 2,489,243 of Stego

In the supertel process of French Patent 1,124,489, US Patent 3,114,618 and US Patent 3,285,725, 70 Nm 3 / kg (fiber)

These are for large manufacturing bones with an output in the range of 500,000 to 1,000,000 Nm3 / hr (Nm3 is the volume at standard barometric room temperature). It is converted into fibers under the influence of mechanical forces, for example centrifugal forces, where the gaseous flow is used only as a medium for transporting the fiber product towards the vertical device (generally the flow is mainly in the horizontal direction, see Figure 14). The amount of toxic substances is slightly small but nevertheless very important: for example 30 Nm3 / kg fiber in the process described in US Pat. No. 2,577,431 which is data from a production plant with an output of 300,000 to 400,000 Nm3 / kg. The amount of contaminated water is equally large enough for all of the above processes and requires large industrial snow melting of 1000 m 3 / hr or more.

The amount of these contaminated effluents limits the concentration of tenol complexes in effluents that are first released into the atmosphere by law in some countries, and then the release of certain pollutants.

In addition, restrictions on the odor and opacity of effluents discharged are regulated in many countries. In addition, facilities for integrated fibrous products are polluting from another perspective. In addition, for toxic and severely odorous products, a significant amount of steam is emitted to these facilities, which amounts to 20 to 30 tons per hour in large plants, and these steams escape from the chimneys forming a very opaque umbrella. Noise is another form of pollution produced by a facility for the fabrication of textile aggregates. In these facilities, noise is mainly emitted by two sound sources. In other words, they come from equipment that produces fibers and fans used to extract toxic substances.

Indeed, all fiber manufacturing equipment installed in these facilities use gas spraying at high speeds, whether the material is drawn or finely processed into fibers or the fibers are produced directly. The level of acoustic intensity emitted by these injections is known to increase significantly with the injection speed. This level is known to exceed 100 decibels where the operator needs work in the vicinity of textile manufacturing equipment. This level is much higher than the level permitted by industry regulations in many countries.

Again, the acoustic intensity developed by the toxic extraction fan is transmitted along the conduit connected to the toxic exhaust chimney. The chimney is usually located outside the building, where it acts like an antenna, radiating this acoustic intensity around it. Discomfort in the neighborhood has resulted in orders to shut down certain facilities in various countries. There is an increasing need to reduce or eliminate pollution generation. And their costs should be made at a price low enough that they do not affect the price of the final product.

Many studies have been conducted on this issue and answers have been developed.

The characteristics of the process according to the invention are as follows. Toxic substances are the fact that they are recycled to repeatedly cross the molded mepo or mat, and that most of the gas distribution from the fibermaker and the finely processed fibrous material is converted into the wash water and also cools the wash water. It is also the fact that toxic substances are washed in water after crossing the fiber collecting device and blanket or mat to convert any pollutant into water, and also that the non-recirculated part of the toxic substance is purified before being released into the atmosphere. Some wash water is recycled, that is, the fractionable fraction of the pollutants contained in the wash water is extracted and the solid waste is purified before final discharge.

The process described above affects the cooling of the recycle gas and it is important to create such a recycle possibility. In addition to the cooling of the recirculating gas, it is preferable to spray water on the fiber and gas flow in the receiving chamber to cool the fiber and gas flow.

This water injection, in combination with the cooling of the recycle gas as a result of cooling the flow, reduces the temperature of the flow, thereby significantly reducing the induction of ambient air by the attenuating blast.

A particularly important feature of the present invention is that the amount of toxic substances generated in the atmosphere is approximately equal to the amount of gas flowing through the apparatus for processing fibers.

In particular, the present invention contemplates recycling of the main toxic material inside the facility and only minor parts of the toxic material are treated and released. That is, 95% of the total specific substances can be recycled, and the amount of toxic substances purified before discharge is only 5% of the total toxic substances, which can be used for costly purification, for example. There is no need to prevent the expenditure of energy such as combustion.

Another object of the present invention is to render the thermosetting resin contained in water insoluble. This resin is heat treated according to the present invention to make it insoluble. That is, it is suitable if the temperature is 100 ° C. or higher, and more preferably, a range between about 150 ° C. and 240 ° C. under pressure.

By applying the above process (insolubilization of resin) to some cooling water and washing water, it is convenient to insolubilize the dissolved binder component contained in water, and it is possible to extract the insoluble material by the well-known technique. The concentration of pollutants is maintained at a level sufficient for the continuous reuse of cooling water. The wash water thus circulates in the closed circuit, eliminating the external discharge of pollutants along with the wash water.

Another object of the present invention is in the heat treatment applied to the wash water, that is, to evaporate the wash water and to heat the steam to a sufficient temperature thereby converting the pollutant composition into a non-polluting component.

In addition, a sound insulation device is considered in the present invention. In other words, the device for transporting and guiding recycled toxic substances is adjusted to show a special form to reduce noise emission by these devices, and the device for discharging non-recycled toxic substances into the air is specially arranged by this device. This will reduce the noise emitted in the vicinity.

It is possible to extract insoluble materials by known techniques, thereby maintaining the concentration of the pollutants to a degree suitable for the continuous reuse of washing and cooling water in the facility. The wash water thus circulates in the closed circuit, omitting the external discharge of the material with the wash water.

Another object of the present invention is in the heat treatment applied to the washing tool, in other words, when the washing water is evaporated and the steam is heated to a sufficient temperature, thereby converting the pollutant composition into a non-polluting composition.

In addition, a sound insulation device is considered in the present invention. In other words, the device for transporting and guiding recycled toxic substances is adjusted to show a special form to reduce noise emission by these devices. This will reduce the noise emitted in the vicinity.

Other objects and advantages of the present invention will be described in more detail below, including various representative transfers of recycling of toxic substances.

The drawings of some suitable embodiments of the present invention are partially substantially graphical and are shown in side and vertical cross-sectional views.

Figure 1 shows a known fiber collection facility to which the present invention can be applied. The facility has a known fiber manufacturing device 11 which is generally used for facilities for integrated products or bonded fiberboards, in which the material is subjected to centrifugal motion, aerodynamics, or a combination of both. It is finely processed. The term aerodynamics is generally applied to thinning or fibrous material by gas phase injection at high temperatures and speeds.

One example of such a device is shown in US Pat. No. 3,285,723. The fiber manufacturing apparatus 11 is arranged in a gaseous fluid stream 12 formed by the injection of high energy and gas or air derived from the surrounding medium, the flow enclosing the fiber in the form of a perfectly regulated stream of flow. It is directed towards the collecting device. The apparatus also has an area for the application of a binder placed between the fiber manufacturing device 11 and the collecting device in the passage of the fiber and gas flow, in which the nebulizer 13 causes the binder to form a cloud of fine particles. Spray into the fiber and gas stream. Most of these microparticles are absorbed by the fibers and cling to the fibers, while the remainder is entrained in the gas and entrained in the gaseous form.

The fiber dispensing device is known and is shown graphically (14) and is formed between the manufacturing apparatus 11 and the binder application zone or between the binder application zone and the molding apparatus within the passage of the fiber and gas 12 as shown in FIG. Located between the three hands, this dispensing device 14 distributes the fibers on a vertical surface by causing vibrations in the fiber and gas streams or by deforming this flow, so that the weight per unit area is very uniform. The collecting surface is provided by an endless perforated belt 15 in which fibers are accumulated in the form of a blanket 23. Under the perforated reel of the side where the fibers are accumulated to form a blanket or mat. The chamber 16 located in the chamber extends into the molding zone or the molding section, the inside of which is reduced by compression or negative pressure by the fan 19, and all gases accompanying the fiber are perforated with the manufacturing apparatus 11. belt It passes through the blanket formed in connection with the passage between the 15, so that there is no fluid in the gas state absorbed by the fiber, and the blanket is molded on the outer side of the face. Vertical wall 21, which extends to a height approximating the height of the blanket and which marks the space in which the blanket is formed, regulates the chamber 22, surrounds the fiber and gas flow, and the upper end fiber manufacturing apparatus of the wall 21. It is open close to, which generally acts as a hood hood, while a fan 19 that provides negative pressure in the chamber 16 provides sufficient force to the gas entraining all the fibers passing through the formed fiber. And emits toxic substances into the atmosphere through the chimney (as they are measured on the molding section) The type set above is considered for the amount of toxic substances emitted from the molding section.

In fact, in the textile manufacturing apparatus of these facilities, drawing or pulverizing into fibers or guiding the material, or guiding the fiber, is achieved by gas phase injection, which has very high power and high speed. This speed is generally greater than 100 meters per second and is desirable for shaping the fibers, but this is much higher than the speed required for the fibers and gases reaching the perforated belt 15 to form suitable blankets, the latter being generally per second Do not exceed 10 meta.

In fact, there is a need to considerably reduce the injection speed introduced into the fiber making apparatus. This is accomplished by diverting some of the momentum of these injections to the surrounding fluid and flowing therein. Aspects of the surrounding fluid are guided and accelerated in the direction of injection and are combined with the injection.

This results in the injection from the fiber making device becoming a mixture and inducing a fluid consisting of the gas flow accompanying the fibers. Inducing ambient fluids by injection from a fiber making device is a well known physical property in injections or in chambers with open effluents or fluids retained. We have learned that in hydrodynamics, the effect of inducing a significant amount of ambient gas by such injection and the amount of this induced gas flow increase with the output of the injection, and the length of the injection depends on the ambient gas.

However, induced phenomena are forward phenomena, and the slowing down of induced dispersion is only severe after this injection has advanced enough distance through the surrounding gas.

In the above-described facility, in order to provide the velocity of the fiber and impingement half-gas flow to the value given above at the point of reaching the collecting belt 15, a value of up to 10 m or less from the fiber manufacturing apparatus 11 The length of the passage in which the flow to the belt 15 softens is generally 2 to 3 meters or more, and the amount of gas injected from the manufacturing apparatus 11 leads to this distance, and the amount of gas passing through the belt 15 is increased. Silver is at least 10 to 20 times the amount of injection gas blown out from the fiber production apparatus 11.

In addition, the slowing down of the fibers and the entrained gas flow must be brought about so that the blankets are formed under good conditions. It is necessary that the flow direction of the fiber and the gas be in the same direction generally parallel to the flow direction from the fiber manufacturing apparatus to the belt 15.

It will be explained further that the stream of fiber and entrained gas 12 is divided into strands and defined by a section that is perpendicular to the flow direction. That is, it is limited by the section which installed between the line segments M.N.0.P.

For some strands, for example, marked by the section of a segment, M. N., the flow maintains a well-measured direction and is subjected to a well-measured velocity decrease. These two factors, direction and speed reduction, will be necessary characteristics for each elementary wire, and if the flow is induced uniformly along the periphery of the elemental wire for all the fluids required, this is the fluid product contained in the horn at the inlet of line segment M. Since the elementary wire is transverse to the mass of, the proportional increase in the image velocity of the horn is increased. This relative velocity decrease is equal to the difference between the inlet horn speed of segment M and the outlet flow velocity of segment N and is related to the initial velocity.

If it is possible to supply the required amount of gas for the direction and deceleration of the flow with the desired characteristics of ambient air and gas, for each elementary stream between the textile manufacturing device and the collection belt, the induced ambient gas flow is the fiber and the accompanying gas flow. It will also be established in conjunction with the direction of the direction from the manufacturing apparatus 11 to the collecting belt 15. This flow is represented by the first degree line segment 27.

In the fiber forming bump collecting facility shown in FIG. 1, all gases induced by the flow 12 are introduced into the air inlet chamber 22 through the opening 28 having a large dimension near the fiber manufacturing apparatus 11. Is formed.

FIG. 2 shows the shape of the flow in the castle chamber when it is not possible to freely supply the jets from the thinner apparatus with all the gases for which ambient substitution is induced, which is given by way of example for clarity.

2 shows a part of a collecting device having a fiber manufacturing device 11, in which the flow of fibers and gas 12 from the device is applied to the binder applying device 13, the fiber splitting device 14, and the collecting belt 15. After passing through the formed blanket 23, the toxic substance 29 flows into the chamber 16 into which the toxic substance 29 is introduced. All these parts are the same as in FIG. However, in FIG. 2, the wall 21 regulating the receiving chamber 22 extends over the fiber making device 11 to extend between the openings 25 so that the cross section is reduced and communicates with the atmosphere through the openings. As a result, atmospheric air flows into this chamber.

It is thus located within a certain elementary stream 12, for example in the elementary wire M. N (in the region close to the fiber making apparatus 11. near the spraying orifice, where the material is guided or finely processed to be fibrous, or the guide of the fiber). The elementary stream (12) located downstream if the surrounding medium fails to supply the stream (12) with all the gases to which the flow will be induced. Will be short of supply (where flow 12 has a low speed).

The gas stream 30 emanating from the downstream region of the stream 12 rises in series with the wall 21 toward the upstream duct at high speed, and is captured by the stream and accelerated in this flow direction. This will cause a vortex 31 to develop between the flow 12 boundary and the chamber wall 21. The effect of this vortex will provide an increase in the amount of fluid that the surrounding medium could not perform. The direction of the circulation is such that the fibers extracted and transported from the molded blanket 23 are connected to the chamber wall 21 of the chamber toward the fiber distribution device 14 and the binder application device 13 or the fiber production device 11 to direct the direction. It's like catching.

If the amount of air flowing into the receiving chambers of the first and second solid lines is reduced to a value that is much less than the amount of air that the flow can induce, the vortex 31 is sufficient so that the fibers are fed to the fiber distribution device and the binder application device. Will cling to and interfere with the smooth functioning of these devices.

These vortices also disrupt the shaped blanket 23, as shown in FIG. The industrial application of this facility is that upstream fibers are employed, and the air flow into the chamber is 60 to 70% or more of the required amount. If it is below this value, there will be no industrial utility value.

If it is required to further reduce the amount of air entering the chamber or eliminate it as a whole, the mixing in the chamber will not be able to accumulate on the collecting belt.

One object of the present invention is to provide a process that can significantly reduce the amount of air entering the forming section, while preserving conditions suitable for forming the blanket. This process is not the atmosphere, but rather the use of some characteristic material taken from the exhaust fan outlet as the induction fluid, that is to recycle some of the toxic substances released from the molding section. The allowed device arrangement for this process is shown in FIG. The upper part of the receiving chamber 22 is closed by a cover 32 having a hopper piece through which the fiber flow 12 with the gas flowing from the fiberizing device 12 passes, and the molding section 22 protrudes. . The end 33 of the orifice is tangential to the flow 12 and has a convenient shape as a passage of the flow. The cover 32 is placed at a distance H from the fiberizer 11 for operational convenience.

In the arrangement shown in FIG. 3, the washing chamber 17 located downstream from the suction chamber 16 and larger in cross section than the chamber 16 is equipped with a device containing a toxic substance 29. As shown in FIG. In other words, the pollutant suspended in the gas entrained with the fiber between the manufacturing apparatus 11 and the collecting belt 15 is in contact with the washing fluid, in particular water. In this cleaning chamber 17, the toxic substances are separated from the elements that hold them. The elements pass mainly through the binder application zone and the fiber blanket forming area and consist of fibers and binders with those filled. In contact with the wash water, the fibers contained in the toxic substances are retained in the water particles and have a tendency to accumulate in the bottom of the chamber 17 by the omission, which is a phenomenon that the toxic substances are stored from the chamber 16 to the chamber 17. This phenomenon is further accelerated by drastically reducing the velocity of the toxic substances as a result of changing the flow cross section in connection with their passage to. Some particles or pollution vapors are absorbed by the particles in the wash water and are soluble in water. This is the function of both operations with the cleansing content of the toxin. Water with pollutants used for cleaning and converted to some toxic substances is discharged through the orifice 24.

This arrangement also has a cyclone or electrostatic sorting device (18), which is located between the cleaning chamber (17) and the suction fan (19), in which the droplets of toxic substances attached during the cleaning process are separated. In addition, it is important to remove toxic substances before entering the fan 19. The wash water extracted from the toxic substance in liquid form is discharged from the sorting device through the orifice 25. The collection device 26 directs the wash water discharged from the orifices 24 and 25 toward the treatment zone.

As described above, the fiber and gas flows through the binder device 13 and again through the fiber distribution device 14. The fibers are collected on the collecting belt 15, the toxic substance 29 passes through the formed fibrous blanket 23, passes through the chamber 16, passes through the water sorting device 18 and then to the fan 19. It flows into the chimney 34 upward. Some of these toxic substances are released from the device through orifices 35. The remainder is led to the forming section 22 through the chimney 34 and passes through the opening 36 in the region located near the fiber making apparatus 11 in the section 22. The amount of gas flowing into the molding section through the opening 33 is equal to the sum of the amount of gas coming out of the manufacturing apparatus 11 and the amount of air guided by the passage communicating with the atmosphere in connection with the length H. The amount of gas entering the chamber thus increases with the length H. For equilibrium of the fractionation device, the amount of toxic substances released from the device through the orifice 35 is equal to the amount of gas entering through the orifice 33. Therefore, the amount of toxic substances released decreases as distance H decreases.

4 shows a special embodiment according to the invention, where the distance H is zero. That is, the fibrous device 11 or at least the finely processed and guiding jet orifice of the guiding jet is located in the section 22 or chamber. The amount of toxic substances emitted from the device will be approximately equal to the amount of fluid exiting the manufacturing device 11. The share of recycle toxicant would thus reach a value of about 96-97% in this example.

In the installations shown in FIGS. 3 and 4 of the construction in accordance with the present invention, the amount of recycle gas is equal to the amount induced by the injection from the apparatus 11, and the fluid is finely processed through the section 22. It takes the direction of the flow of radiation, so that no vortex appears. The toxic material recycled will mainly follow the mammary gland indicated by arrow 37.

One advantage of the present invention is that the flow of specific material recycled by the fan 19 provides a slightly greater velocity than the atmospheric flow 27 where the fiber and gas flow 12 is induced in the facility shown in FIG. It is based on the fact that you can. These streams 37 have sufficient momentum to overcome the possibility of inducing reverse flow or backwind of the reversing fibers as described in the second diagram in the binder node 13 and the dispensing device 14.

One of the most important advantages of one process of the present invention is the fact that the amount of toxic substances emitted from the system is only 3 to 4% of the amount emitted in a typical installation (numbers indicating the magnitude of the amounts are mentioned above).

It is also the fact that with such a small amount of toxic substances, the purification process is carried out with high efficiency at a very low cost. In operation, the present invention treats toxic substances radiated through the orifice 35 by combustion, and this operation heats the toxic substances to a temperature above 600 ° C., which is sufficient and suitable for oils to burn, Beyond that, the pollution of toxic substances and especially phenol complexes are converted into non-polluting elements such as carbon dioxide and water by combustion. This treatment is also convenient for removing odors.

As shown in FIG. 3, the combustion process is taken in a known apparatus 38 and consists of a combustion chamber 39, a burner 40 which is a combustible mixture, and a grid or other flame safety ignition device 41. The treatment temperature may be reduced in the range of 300 ° C to 400 ° C by using a combustion catalyst. Purified toxic substances are discharged to the atmosphere through the chimney (42). At the exit of the chimney 42, the temperatures of the toxic substances are sufficiently high and their emissions are low due to recycling, so that the steam content contained in these toxic substances does not condense before the overall dilution of the toxic substances into the atmosphere. Therefore, the cloud umbrella does not occur at the exit of the chimney 42.

Another convenience store of the present invention is that the toxic substance is recycled and the entire purification process is performed, so that it is not necessary to perform a very complete primary washing, thereby eliminating the washing device 17 and the water only device upstream of the suction fan 19. 18) can reduce the dimensions and investment.

The facility constructed by the present invention and shown in FIG. 3 and FIG. 4 has a molding section 22 surrounding the binder and the fiber distribution device 13 and 14, and entering and exiting the fiber distribution device. It is difficult. It is necessary to enter and exit the binder nozzle 13 or the fiber distribution device 14 during operation. In order to do this work, it is necessary to observe the inspection window suited to the wall of the area chamber located near the fiber manufacturing apparatus 11.

In addition, the pressure in the forming section 22 should be kept deep at the same or several trillion millimeters lower than atmospheric pressure to prevent leakage from the chamber 22 during recycling of toxic substances that still have pollution.

When the inspection window is closed, it prevents any accidental leakage by sealing engagement. The pressure in the section 22 is adjusted to the required value by adjusting the negative pressure formed in the chamber 16 by the fan 19 and is illustrated as an embodiment in FIG. Other processes of removing the amount of toxic substances are not emitted from the recirculation conduit 34 but directly from the forming section 22 (see FIG. 4) through the opening 43 located in the chamber wall. It is necessary for the pressure to be maintained at a desired value in the region. Toxic substances are extracted from the section 22 by a small auxiliary fan 44 and are emitted through the conduit 35. The fan 19 is thus only dependent on ensuring the recycling of toxic substances.

Such a facility should more accurately establish the pressure in the chamber 22 to a pressure near atmospheric pressure.

One feature of the present invention is the fact that it is possible to adjust the flow of the binder to be atomized through the nozzle 13 and when the toxic substance passes through the binder ash, by the function of the amount of binder component moored to recycle the toxic substance They accumulate on fibroblasts.

In operation, the recirculation process of toxic substances is repeated and passes very frequently through the formed fibrous follicles, and because of the low rate of toxic substances passing through these follicles, even though the tolerance of these vesicles is limited. The value of a typical pass (about 15 times per minute) is encompassed by the blanket of some amount of binder element mooring to the toxic substance. This reduces the extent to which the amount of binder sprayed and atomized by the application device 13 results in an increase in binder effect of 5% and an economic advantage.

In the facility shown in FIG. 1, it is necessary to maintain a specific temperature in the molding section 22, whereby the heat supplied by the material to be extracted and the heat supplied by the fluid to be processed or guided are radiated.

In operation, since the binder used to bond the fibers is usually thermosetting, the binder is sprayed in the liquid state by the thermal action, and the continuous solidification progress is made by the gradual change. If the temperature in the section 22 becomes excessively high, during binder formation, the binder will advance to a state where solidification progresses enough that the force is sufficient to bind the fibers.

This phenomenon is sometimes called pregelation. And. This is prevented by cooling the molding section 22. In the installation shown in FIG. 1 this cooling is achieved by inducing an atmosphere which is generally lower than the minimum temperature required in the section 20. The amount of heat introduced into the chamber by the material to be milled and by the fluid to be milled and guided depends on the fiberization process used, but is 1,500 to 15,000 kca1 per 1 k9 of material and is transferred to the induced air and is also toxic. A small amount of heat is transferred to the wash water and the rest is released to the atmosphere.

In the facilities shown in FIGS. 3 and 4, very small volumes of toxic substances remove very small amounts of heat, thus the present invention prepares other means for cooling the molding section 22.

The above-mentioned conversion of the heat entering the section 22 by at least partly by the material to be processed and by the fluid to be processed and guided by at least partly to a heat transfer fluid such as water or This is achieved by installing toxic substances in contact with this heat transfer fluid. After absorbing the heat entering the section 22, the weaning body is discharged out of the chamber and cooled by any suitable system installed outside the facility. The heat exchange between the gas or toxic substances and the cooling water accompanying the fiber flow is by direct contact between the fluids or by heat treatment or heat conversion walls.

The amount of heat converted per unit time by these exchange methods is proportional to the temperature difference between the fluid to be cooled and the cooling fluid and also to the area of the contact surface. The relatively high velocity of gas or toxic substances in the dimensions of the installation is only allowed for a short time for heat exchange to take place. Therefore, the amount of heat exchanged within the unit time requires that a large amount be cooled sufficiently.

The present invention is equipped with processes and politics to achieve this goal. One of the processes of discharging the amount of heat introduced by the material to be processed to the outside of the forming section 22 and by the fluid to be processed and guided to cool the toxic substances in the chamber 16 and the cleaning chamber 17, The contact area between the toxic material and the coolant is bulky to have a large surface area.

The large contact surface can be obtained in several ways. This can be done by dispersing water into fine particles, spilling them in the form of very thin films, or bubbling toxic substances in water.

In the arrangement shown in FIG. 3, for example, the atomizer 45 dissipates the coolant in the form of a plate or curtain of particulates, which are directed against the flow direction of the toxic substance as indicated by reference numeral 29. It is formed in the vertical direction. Toxic substances traverse the once formed fibrous blanket, which enters the chamber 16 at a temperature of about 80 ° C. to 100 ° C. and is cooled to a temperature of about 30 ° C. in contact with the water particle tube. The temperature of the water at the inlet of the atomizer 45 is between 15 ° C. and 20 ° C., depending on the ability of the chiller to feed the atomizer. In contact with the toxic material, the water is reheated to a temperature of 30 ° C. to 40 ° C., depending on the flow rate flowing through the atomizer 45.

The recycled fraction of the cooled toxic substance passes through the sorting device 18 and the fan 19, and then re-enters the molding section 22, where it is mixed with the gas from the fiber manufacturing device 11, and recycled toxic. The material cools these gases and fibers in the same way as air in the atmosphere in the apparatus shown in FIG.

Another embodiment is shown in FIG. 4, where water flows over the baffle 46 to form a very shallow film. The flow of toxic substances indicated by the sign 29 flows softly in this partition and is cooled in contact with water while licking the water film.

Another example is shown in FIG. 3, in which the flow of toxic substances indicated by reference numeral 29 is orifice 47 below the free surface of the water contained in the mat 48 downstream of the suction chamber 16. It escapes through and creates a fierce bubbling at the orifice 47 level in the water, creating a large contact surface of toxic substances between the liquid wall of the gaseous bubbles and the water.

There are other processes that directly cool the fiber and gas stream 12 by water injection and discharge this water outside of the forming section 22 to remove the heat to be introduced by the material to be fiberized and the fluid that is processed and guided. .

Spraying water over the stream is employed where the contact surface cannot be made very large when there is little space available but the temperature difference between the fluid to be cooled and the fluid to be cooled is large.

For example, in the embodiment shown in FIG. 3, the atomizer 49, located between the fiber manufacturing device 11 and the binder device 13, is made of fine particles with respect to finely processed fibers and gas flow to be cooled. Spray water clouds. The particles reach the flow of gases and fibers in the high temperature flow region, reaching a temperature of about 600 ° C., and evaporate immediately, thereby providing a high efficiency cooling effect. The large amount of heat required to evaporate 650 to 700 kcal of particles per kilogram of water is taken from the fiber and gas flows, resulting in quick cooling of every turn. This reduces the temperature of the flow at the binder apparatus 13 level to a value of 100 ° C to 120 ° C. The resulting steam is passed through the fibrous blanket 23 into the chamber 16 and into the cleaning chamber 17 where it contacts the curtain of water sprayed by the atomizer 45, whereby the steam condenses and The latent heat of vaporization of water is transmitted to the cooling water flowing out of the atomizer (45). This heat is discharged from the system along with the water from the atomizer 45. The place of installation of the injector 49 for injecting the coolant with respect to the flow 12 is between the fiber manufacturing device 11 and the binder nozzle 13, since this arrangement has some special convenience in operation. It is a suitable arrangement according to the invention.

Above all, the temperature difference between the water to be cooled and the water to be cooled in this region is the largest, where the heat transfer is the highest. The binder is then sprayed on the cooled fiber and gas stream at a sufficiently low temperature (100 ° C. to 120 ° C.), thereby limiting or not destroying the binder due to evaporation of the component. This results in an increase in binder efficiency of about 5%, resulting in a reduction in pollution from toxic substances.

In other embodiments shown in FIG. 4, an apparatus 50 for injecting cooling water onto the fiber and gas stream 12 is located between the binder apparatus 13 and the collecting belt 15. As shown in FIG.

As in the embodiment shown in FIG. 3, the cooling water passes through the blanket 23 shaped in the form of steam. This water transfers heat to the film of water flowing over the partition 46 of the cleaning chamber 17 and condenses. This water is discharged out of the facility by the orifices (24) and (25) installed at the lower positions of the chambers (16) and (17) and the water sorting device (18) and flows into the device (51), where The suspended solids mainly fibers are separated. The device 51 may be a filter having a known rotating or vibrating gold mesh, a known decanter or a centrifuge. The solids removed are collected in the tank 52, and in FIG. 3, the water is directed into the cooling station 54 by gravity or by the pump 53. By leaving this station, the coolant may be drained out and reused in the system.

Station 54 may have a known cooling tower 106, as shown in FIG. 3, in which water is cooled by contact with air. The cooling water is circulated through the spray cooling tower by the pump 107. Water from the tank 52 is in an indirect heat exchange relationship with the cooling water of the tower 54 by a heat exchanger indicated by reference numeral 105, in which the cooling water may return to the tank 52. The treated water is led by the water supply connection pipe 111 as specified in FIG. It is suitable to circulate through the cooling tower 106 to cool the wash water by means of an indirect thermal bridge with cooling water (or other cooling fluid), because it completely avoids contaminating the air with any volatile pollutants in the wash water. do. In many installations such residual pollutant holdings are very low (eg less than 5% of the emissions from the non-recirculating new gas outlets shown in Figure 1). The washing water in the water spray cooling tower 106 may be considered directly.

One advantage of the present invention is that there is no liquid water discharged out of the facility, thereby avoiding contaminating the surroundings by the small amount of pollutants still contained in the water. This includes the water drawn through the furnaces 49 and 50 and the wash water circulating in the closed circuit in the facility.

In the facilities shown in FIG. 3, FIG. 4, and FIG. 5, the closed circuit formed by the cooling water and the washing water is as follows. The water leaving the coolant rotation 54 is sent to the cooling device 49 or 50 in the chamber 22 via the pump 55, and simultaneously to the steam condenser and the toxic substance cleaning device installed in the chamber 17. Is sent. In the chamber 17, the inaccuracy device 45 shown in FIG. 3 or the baffle 46 with the water film shown in FIG. 4 or the tanks 48 which are to send water as shown in FIG. Have one of Pollutant fibers, wash water and steam condensate loaded with binder elements are introduced into the collecting device 26 through orifices 24 and 25 installed at the lower positions of the washing chamber 17 and the material sorting site 18. The collecting device leads them to the filtration device 51. Here, solids consisting of fibers and insoluble binder elements are classified from the wash water. These waste solids are collected in the conveyor 57. Since the filtered wash water only contains dissolved binder elements and pollutants, it is sent to the cooling station 54 by gravity or via a pump 53. When the wash water circulated in the closed circuit, the inventors contemplated that the concentration of the mooring or dissolved material in the filtered water needs to be kept below a certain value, which is a unit mass evaluation of dry material per unit mass of water. Is 3 to 4%.

If this value is exceeded, any substance dissolved or moored in the wash water (especially, the fine fibers or the fine particles of the binder collected by the filtration device 51) is deposited in other parts of the facility. The binder is made of a polymer and forms a viscous or solid layer, which gradually closes the orifices in the water spray orifices 45, 49 and 50 and also in the collecting belt 15 for the passage of toxic substances. do. This reduces the amount of toxins emitted from the hood and, in cooling these toxins, leads directly to closure of the facility.

In order to maintain the concentration of the substance below the values that will persecute spraying or toxic emissions, it is necessary to extract much of the substance from the wash water.

In operation, the method described above has been followed to ensure that the washing water contains a large amount of 20-30% of the binder sprayed onto the fibers by the nodules 13. In large plants, this means that 3,000 to 5,000 kg of binder (dry material basis) per day is introduced into the closed circuit for the wash water circulation, which approximates the amount of binder extracted from the water to maintain the equilibrium of concentration. You need to do it. Several extraction processes are possible.

Firstly, this process treats some amount of wash water in a centrifuge, which is much less capable of separating the moored solids from the water than can be manipulated by the filter 51. As shown in FIG. 3, the water is treated by centrifuge 58 and returned to bat 52, or, more conveniently, to chiller 49.

Next, this process is to treat the water by the additive of the villi, the separation is made by the material of the villi.

Both processes have the inconvenience of mainly extracting only insoluble materials from water.

The dissolved binder, which constitutes the majority of the material to be extracted, has little or only little effect.

The present invention provides several processes for extracting the binder dissolved in the wash water.

One process is to dilute the binder drug as a preparatory step to act on the fiber by the applicator 13 using filtered or centrifuged wash water. The filtered water can be withdrawn from cooling station 54 at any point downstream of the circuit, or more conveniently, with a valve as shown in FIG. 3 downstream of the centrifuge.

Another process is to use wash water, such as a fluid, for the cooling flow 22 of fibers and gases in the chamber 22. Washing water is sprayed against the flow 12 by the cooling device 59 in the illustration of FIG. 3 or by the cooling device 50 in the illustration of FIG.

These two processes have the advantage of being able to reuse some of the binder contained in the wash water, which is caused by the fact that the blanket 23 produced by the present invention retains the water sprayed by the devices 49 and 50. Adjusting the amount of binder injected by the application device 13 by the function of the binder content has been considered in the center, which leads to an improvement in the binder efficiency rate. However, this process is not allowed to sufficiently extract the amount of binder dissolved in the wash water, so the concentration of this water is kept below the required value. For this reason, the present invention provides for the complete extraction of the large amount of binder dissolved in the circulator in the closed circuit in the above two processes. One of these processes is to burn about 1 to 5% of the small fraction of the wash water entering the circuit in the occupancy device 60. This apparatus is known as shown in FIG. 4 and is configured as follows.

Burners fed with a combustible air fuel mixture (61)

Atomizing atom 62 in which the water in which the particle form condensed into the expanding flame of the burner 61 is injected through the pipe 63 by the effect of the atomizing air 64;

-The reaction chamber 65 in which the washing water treatment is effected by the effect of heat generated by the burner 61.

It firstly evaporates the wash water and afterwards gives a temperature of 800 ° C. so that the binder elements are also produced as steam.

This will allow the conversion of these binders and pollutants to non-polluting elements such as CO ₂ or H ₂ O. Non-polluting steam is discharged at high temperature through the chimney 66 outside the facility, thereby preventing the formation of cloud umbrellas.

The point at which the treated water is removed is generally between the pump 55 and the devices 50, 46, as shown in FIG. 4.

This process is convenient for extracting and enlarging all binder elements contained in the treated wash water as non-polluting elements. This requires a lot of energy consumption and is very costly.

The effect of the processing cost on the price of the manufactured textile products can be reduced by recovering some heat from the production of superheated steam in the heat exchanger for various purposes from high temperature steam.

In other processes, the dissolved binder circulating in the circuit is heat treated for a small amount of 1 to 5% of the load of the wash water stream, resulting in an insoluble binder, and then the binder is separated from the water by a suitable sorting device such as filtration and villi. The process is classified by centrifugal treatment.

In operation, the inventors have found that the width of the dissolved binder, together with the temperature and time, if the binder or dissolved binder element contained after filtration, where water was used to cool and wash the toxins, was kept under constant temperature for a given period of time. It has been found that the conversion to insoluble particles is increased, and gradually the mooring in water is increased, thereby making it easier to classify from water.

The rate of insolubilization by treatment of the dissolved material characterizes the treatment efficiency. Treatment temperature has a very significant effect on efficiency. For example, when water had a dissolved binder element of 1%, the treatment efficiency was as follows.

40% if water temperature is maintained at 40 ℃ for 8 days

40% if water temperature is maintained at 70 ° C for 3 days

40% when water temperature is maintained at 160 ° C for 3 minutes

60% when water temperature is maintained at 180 ° C for 3 minutes

95% if water temperature is kept at 240 ° C for 3 minutes

In FIG. 6, the state of the treatment efficiency with respect to the temperature and the treatment time relationship is shown. In a fiber integrated manufacturing panel of a large-scale facility plant, 50 m 3 of water must be treated per hour. Therefore, in order to reduce a considerable size of the treatment plant facility, it is necessary to measure the shortest treatment time and work at a high temperature of 100 ° C. or more.

The apparatus is processed in a compression chamber, which maintains a temperature of about 5 ° C. below the boiling temperature of water under pressure in the chamber, thereby maintaining the liquid phase throughout the treatment period. This solution also has the advantage of only a small amount of energy consumption and only depends on the increase in the heat added to the water to increase its temperature with respect to the waste.

Thus, on the basis of the same amount from which the dissolved binder is extracted, this process is about 1/4 the cost of the combustion process described above.

One inconvenience generally considered is that when heating water in a chamber containing a binder or dissolved binder element, even at low concentrations, insoluble binders deposited on the chamber wall prevent the spinning of the orifice of the chamber at a very high rate. It is thick enough to do so or thick in the chamber itself.

The inventors note that the heat required for the treatment is released into the water to be treated and that the walls of the chamber are kept at a lower temperature than the water to be treated throughout the treatment, so that no deposits are formed on the walls and the insoluble binder remains mooring in the water. Was observed. This can be done by mixing the heating of the heat with a suitable hot fluid such as steam, by immersing the burner combustion gas, or by installing something like an electric arc in the water to give energy.

A wide range of operating conditions are possible, such as a treatment time of 3 to 10 minutes with an absolute pressure of 6 to 40 bars at temperatures of 150 ° C to 240 ° C.

The following conditions are the result of a good compromise between energy and equipment maintenance costs.

Temperature: 200 ℃ Pressure: Absolute pressure 16 bar

Time: 5 minutes Efficiency: 70% to 80%

This treatment method is applicable to non-continuous operation or continuous operation. 7 shows a discontinuous operating device for the application of this treatment process. The water to be treated is led to the chamber 68 through the motor actuating valve 67.

The amount of water derived is represented by about 70-80% of the capacity of this chamber.

The superheated fluid, suitably superheated, is injected into the chamber through the injector 69 and the outlet orifice of the injector is submerged. The amount of steam or fluid is regulated by valve 70 and controlled by regulator 71.

The processing cycle performed is as follows.

The chamber 68 is essentially filled with water to be treated below atmospheric pressure. The processing pressure is, for example, required to be 16 bar absolute and recorded in the regulator 71. The valve 70 is opened and steam enters through the injector 69, mixes with the water to be treated and condenses so that all these steam transfers all of the latent heat and swell to the water. The temperature and pressure in the chamber 68 rise to about 200 ° C absolute pressure 16 bar. The induction of steam ends hereby. The injector 69 is adjusted such that the temperature and pressure rise occurs within one minute and ends. Water is maintained at 200 ° C. for 2-4 minutes at 16 bar absolute. At the end of this period, pump 72 is activated to supply fresh charge of water to be culled through jacket 74 into bat 74.

As the water to be treated passes through the jacket, the temperature of the water at the inlet is about 40 ° C. and causes cooling of the treated water retained in the chamber 68. The size of the jacket 74 is adjusted to the size at which the water to be treated enters the bat 73 at a temperature of about 80 ° C. The supplementary cooling fluid circulates in the jacket 75 and completes cooling of the treated water retained in the chamber 68. This cooling should be considered to be complete when the treated water drops to a temperature below 100 ° C., with 40 ° C. to 50 ° C. being suitable. At this time, the valve 76 is gradually opened to depressurize the chamber 68. The treated water flows to the filtration station 51, the bridging device, the decantation device, or the centrifugal device, and the treated water is treated therein to separate the insoluble binder.

The filtered water enters the bat 52 and the extracted waste 56 is supplied to the conveyor 57. When the chamber 68 is empty, the valve 76 is closed and the valve 67 is opened, thereby. Heated water to be filled in bat 73 is introduced into chamber 68 by gravity. The outlet 67a is provided. This restarts the new cycle.

In FIG. 8, a continuous operating facility for the application of the treatment process is shown.

Under the treatment pressure, the pump 77 sends water to be treated to the mixer 78, in which the injector 79 is non-heated, and introduces a heating fluid composed of steam through the injector 79.

This steam is mixed with the water to be treated and condensed to transfer steam and total heat to the water. The steam flow allows the motor to be controlled by the copper valve 80, controlled by the regulator 81 and to maintain the processing temperature at the outlet of the mixer 78 at the required value. The water to be treated after leaving for 10 seconds in the mixer 78 is passed through the reactor 78, where the insolubilization of the binder takes place.

The size of the reactor is adjusted so that the residence time of the water to be treated is for example a treatment time of 2 to 4 minutes.

After leaving the reactor, the water is cooled to a temperature of 100 ° C. or lower in the heat exchanger 83, and preferably cooled to 40 ° C. to 50 ° C. Part of the cooling is treated with water and the cooling water is preheated to a temperature of about 40 ° C. to 80 ° C. in the coil 84. The remaining cooling is provided by the cooling fluid circulating in the coil 85.

After leaving the heat exchanger 83, the treated and cooled water is decompressed to atmospheric pressure through the pressure reducing valve 86.

The pressure reducing valve 86 is controlled by the regulator 87 to maintain the processing pressure in the facility. The depressurized water is flowed to the filtration device 51, the villi, the decantation device, or the centrifuge device, and the insoluble binder is separated from the treated water by treatment.

The filtered water is flowed towards the batt 52 and the waste 56 is fed to the conveyor 57. The facility shown in FIG. 8 represents a continuous operation type that is more flexible and less expensive than the facility of FIG.

Another process is the bacterial treatment of pollutants containing pollutants in an oxidation pond.

The presence of bacteriological yeast in such ponds is certain to ferment decay, especially in the presence of waste product in water. By reacting to the total oxidation reaction, the treatment results in the reduction of phenol products, in particular, to non-polluting substances such as CO ₂ and H ₂ O. In order for this reaction to take place as a whole, it is necessary to feed the germicidal yeast to oxidize the pond and to oxidize with the necessary oxygen. First of all, the production of plate scraps is rejected by quality control. Such wastes are widely scattered and have very bulky pollutants. Waste from filtration of cooling and washing water retains fibers or very large concentrations of binders or binder particles.

So far, all of this waste has been stored in sediments. This method can be used for pollution purposes.

The present invention provides a process for converting waste to non-polluting elements. After the primary preparation, the waste is treated by combustion heat treatment to convert pollutants into non-pollutants such as CO ₂ and H ₂ O.

In Figure 9, the facility to which this process is applied is shown. Waste 56 from the heat treatment and water filtration station is conveyed by a conveyor 57 to be fed to the mill 88 where it is mixed with the aggregated textile waste 87 from the manufacturing process.

While leaving the mill 88, the mixture is injected into the incinerator 90 by a combiner 89. Heat is released by the burner 91 to heat the waste to a temperature of 1000 ° C or higher. At this temperature, the binder and binder particles are converted into non-polluting elements such as CO ₂ and H ₂ O, and are discharged through the chimney 93 together with the combustion gas coming from the burner 91.

A material composed of heat softened fibers accumulates at the bottom of the furnace 90 and is released in the furnace in the form of viscous flow via drain 92 and cooled in a bat 94 filled with water. The cooled material appears in the form of granules, which in turn can be processed into fibers.

Figure 10 shows a facility that allows other treatment of waste. The waste mixtures 56 and 87 leaving the separator 88 are deposited on the belt 94 extending through the furnace 95 by the conveyor 89.

By the heat emitted by the reflector or the periodic resistance 96, this raises the temperature of the waste to 600 ° C to 700 ° C. At this temperature, the binder or binder particles contained in the waste are converted into non-polluting elements such as CO ₂ and H ₂ O. The fiber, which is a major component in the waste volume, is softened by the effect of heat, hardens and aggregates in the form of a plate 98 by sintering, and becomes a greatly reduced volume compared to the original volume of the waste. These plates can be reinjected into the textile manufacturer.

Another important feature of the present invention is to reduce the noise emitted by the facilities according to the invention. In these facilities, the most important noise source is the fiber making device, and more precisely it is emitted from a high speed fluid jet. The sound level around the fabric making apparatus will generally exceed 100 decibels where the operator is engaged in work.

The shape of the area surrounding the sound source in the open facility as shown in FIG. 1 makes it impossible to effectively soundproof the sound source to the outside. Therefore, there is a need to provide a large size free space for the air passages to be introduced.

Closed wall with orifice 33 through which orifice 33 is introduced into chamber 22 through orifice 33 in the construction of the facility according to the invention and in FIGS. 3 and 4 32 and the wall 21 of the chamber 22 are given a shape suitable for installing a shock absorbing plate 99 inside the chamber 22 and a soundproofing plate 100 outside the chamber 22. The reduction in sound levels obtained by installing these plates results in 20-30 decibels in the area surrounding the fiber manufacturing apparatus 11, which considerably improves the operator's working conditions.

The other sound source is a toxic exhaust fan 19. Acoustic intensity radiated from the fan is transmitted through a conduit connected to the chimney and radiates sound when surrounding by the chimney installed outside the facility.

In the facility shown in FIG. 1, a large volume of radiation is emitted through the chimney 35, and a chimney having a large diameter is installed directly at the outlet of the fan 19 due to the limitation of the pressure drop of the chimney. In this way, almost all of the sound intensity emitted by the fan is emitted.

In a facility constructed in accordance with the present invention and indicated by FIGS. 3 and 4, a small amount of toxic material is emitted and the location of the toxic material at a certain distance from the fan 19 is determined.

In FIG. 3, the advantage is provided on the recirculation conduit 34 at a distance of at least one bend from the fan 19, and because the length of the conduit is sufficient, a part of the sound radiated by the fan 19 is reduced to conduit. 34).

In the arrangement of FIG. 4 the emissions are also low and the discharge point is away from the fan 19. The reduction in sound level in the area surrounding the chimney 35 is reduced to 10 decimils or less.

11 shows a facility according to the present invention, the structure of which is as follows. The fiberizing device 101 is a device in which the material 102 dissolved therein is guided to a high speed rotating device. The device 101 has a certain number of orifices at its periphery, through which materials are passed by centrifugal force. As a result, the fiber yarn is subjected to the action of concentric annular injection of the high-speed heat gas toward the white, which is finely processed into fine fiber yarn. A fiber distribution device made of a vibrating two-winder (wind hole), (e.g., described in US Pat. No. 3,134,145) surrounds the fiber and gas stream 12 supplied from the fiberizing device. There is a chiller with atomizer 50 for spraying coolant on stream 12. This device is located between the dispensing device 14 and the binder applying device 13.

There is a blanket collecting device 15 having a perforated belt. The shaping section 22 is a parallel hexahedron with a vertical wall 21 in the transverse direction, an upper horizontal wall 32 of the section 22 at a distance of 200 mm below the fibrous device 101, and a circular orifice A flow 12 passes through 33, and the end of the orifice is shaped to be convenient for the flow 12 to flow in, and is tangential to this flow, and the vertical wall 21 is a perforated belt ( 15) partition the area of the follicle formed on it. In the region where the blanket is formed, there is a partition chamber 16 in the lower part of the belt which is punched out and has a pressure drop fan 19. The suction and wash chamber 17 is downstream of the compartment 16, which has an atomizer 45 arranged to form a plate of water particles, to which the toxic substance 29 flows. Downstream of the chamber 17 is a cyclone-type water separator 18. The fan 12 blows all the gas accompanying the fiber through the belt 15 and also operates to introduce the gas into the conduit 34. The conduit 35 installed on the conduit 34 releases 5 to 10% of the toxic substances passing through the belt 15 toward the combustion device 39 and passes through the combustion device. Heated toxic substances are released into the atmosphere.

The sound absorbing plate 49 and the soundproof plate 100 are provided in the vicinity of the fiber manufacturing apparatus 101 on the wall 21 and the wall 32.

The thumb 103, which collects fibers and binders and binder particles loaded with washing and cooling water, flows in from orifices 24 and 25 provided at the lower positions of the chamber 17 and the cyclone 18. Pump 104 supplies water in the thumb to filtration device 51. Vibratory filtration device 51 with a screen separates insoluble waste from the wash water.

The batt 52 installed under the filter 51 stores the filtered water.

The indirect heat exchanger 105 circulates the water stored in the bat 52 and returns to the bat 52 by the operation of the pump 53, which causes the chambers 22, 17 and the compartment 16 to be separated. As it passes through, it comes into contact with the toxic substance 29, releasing the absorbed heat and cooling. Cooling tower 106 is circulated in the operation of the pump 107, the cooling water from the heat exchanger 105. The pump 55 circulates water from the bet 52 to supply water towards the spray cooler 50 and to the condenser for fiber and gas flow and to provide a spray device 45 for the toxic material 29. It is also washed and fed to the binder preparation plant 108 and to the water treatment plant 109. The water treatment plant 109 is operated to increase the pressure to 16 bar absolute through the pump 77 to the water to be treated, and then heated to about 80 ° C. or more in the heat exchanger 83 to pass through the exchange unit. By leaving this exchanger, the water to be treated enters the mixer 78 where the water to be treated is brought into contact with a suitable superheated steam stream, and consequently heated to a temperature of 200 ° C. And it is maintained for 2 to 4 minutes in the reactor 82 connected to the outlet of the mixer 78.

By leaving the reactor 82, the treated water passes through the heat exchanger 83, which separates the insoluble binder from the treated water at a temperature of 40 ° C to 50 ° C. The treated water is returned to the bat 52.

The new water supply line 111 supplies water to the bat 52 to maintain a constant amount of water in the facility. The conveyors 57 and 112 carry waste from the filtration plant 51 and water treatment plant 109 and also waste from the manufacturing line toward the waste treatment plant 113.

The waste treatment plant 113 had a volatile gas stove or a furnace equipped with electrical resistance, where the waste was heated to a temperature of 600 ° C. to 700 ° C., which allowed the binder and binder particles to burn, and also reduced the fiber to reduced dimensions. It may be sintered into a plate and then returned to the fiber manufacturing circuit.

In figure 12 other facilities for the invention are indicated. The structure is as follows. In the fiberizing apparatus, the material to be melted, in particular, glass, flows out of the container 114 to form a fine primary flow 115, and hardens before entering into contact with the traction roller 116, and the roller passes the hardened filament or rod into the furnace gas spray 117. Will lead to). In this way, the injection 117 processes the fibers into thinner fibers, and transports the fibers to the blanket or the mat forming apparatus 15 in the form of a stream 12 composed of fibers and gases.

There is a chiller with atomizer 50 for injecting coolant into the stream 12. There is a binder applicator 13 for injecting a binder onto the stream 12, which is installed downstream from the chiller in the flow direction of the stream 12. The blanket forming apparatus 15 is provided with a perforated belt.

The equilibrium hexagonal shaping section 22 is bounded by a perforated belt at the bottom, with a vertical wall 21 traversed, a wall 32 at the top, and a vertical wall 118 at the rear. It is positioned about 200 mm from the jet orifice of 117 and flow 12 passes through the quadrilateral orifice 33. The end of this orifice is shaped so as to be convenient as the inlet of the flow 12 and is tangential to this flow. The vertical wall 21 borders the area of the blanket which is formed on the perforated belt 15.

Figure 12 also includes: There is a suction compartment 16 in the lower blanket forming region of the perforated belt 15. There is a washing chamber (17) located below the compartment (16), which has an open orifice (47) at the bottom of the water surface (48), through which the toxic substances indicated by reference (29) flow out. The atomizer 45 spreads the wash water, and the water is supplied to the collecting device 26 by overflowing the pipe 24. Downstream of the chamber 17 is a cyclone-type water separator 18. The fan 19 blows all the gas accompanying the fiber passing through the fiber collecting device and supplies gas into the conduit 34. The recirculation conduit 34 is radiated into the chamber 22 through two openings in its two vertical walls 21 whose downstream ends are provided on both sides of the fiberizer. The amount of toxic material that is recycled reaches more than 95% of the amount that passes through the perforated belt 15 and is led into the chamber 22 through these openings.

The conduit 43, which is in communication with the chamber 22 and provided in an upstream region of the chamber, radiates toxic substances which are not recycled to the combustion device 39 through the fan 44. The sound absorbing plate 99 and the soundproof plate 100 are provided on the walls 21, 32, and 118 in the vicinity of the fiberizer.

The thumb 103 collects the washing and cooling water loaded with the binder and binder particles dissolved or moored with fibers through the orifices 24 and 25 provided at the lower positions of the chamber 17 and the cyclone 18. The pump 104 directs the water retained in the thumb to the filtration device 51.

Vibratory filtration device 51 with a screen separates insoluble waste from the wash water. The bat 52 located below the filtration device 51 collects filtered water. Under the operation of the pump 53, the heat exchanger 105 circulates and the water retained in the bat 52 is circulated and the toxic substance passes through the chambers 22 and 17 to release and absorb the heat absorbed.

The facility also has a water treatment plant and a waste treatment plant as described in FIG.

Figure 13 shows another facility according to the present invention and the structure is as follows. In the fiberizing device, the molten material flows from the converter section 118 of the furnace through an orifice of one or a number of tips provided on the bushing 119, and produces a large number of strands of material and enters into an area to be finely processed. Passes between the high-speed convergence device and the gas injection. Injector 120 is installed in close proximity to the glass fiber, the injection is directed downwards and parallel to the direction of movement of the glass fiber.

Injection is usually composed of high pressure steam. The fibers are produced by the blasting and the surrounding surrounding fluid inducing a flow 12. The cooling spray device sprays cooling water onto the stream 12. The fiber doubling device 14 is made of two pressurized air jet devices such as those shown in US Pat. No. 3,020,585 to guide the fiber in the required direction.

The remaining facilities shown in FIG. 13 are similar to FIG. Another facility for the present invention is shown in FIG. 14 and the structure is as follows. In the fiberizer, the molten material and the fluid 121 are injected from the orifice 123 at high speed to face the periphery of the rotor 122 which rotates at high speed.

Under the influence of the centrifugal force, the rotary device 122 fiberizes a part of the material he receives and sends the remaining material to the second rotor 124, and the second rotor also fiberizes some material he received in the same manner. The number of rotors, such as 122, is generally limited to two to three. By means of a ring with an orifice 125 provided around the rotor, such as 122 and 124, the fluid is ejected at a high speed as well, which acts on the fabric produced to direct the fiber to the receiving device. These injections consist of high pressure air and steam.

Orifice 125 is also generally used to spray a binder onto the fibers. The stream 12 consists of fibers, intraocular injection and the surrounding fluid in which they are directed. A cooling spray device 50 for spraying cooling water on the stream 12 is located downstream of the orifice 125 and the binder is atomized via these orifices.

The remaining facilities in FIG. 14 are as indicated in FIG.

Claims (1)

A fiber collecting device with a drawing gas flow and a small pore fiber collecting device forms a boundary of the forming section, the gas flow passes through the collecting device and the fibers are collected on the collecting device to form a branch, water and dendritic fiber. A method of producing fibers from a thermoplastic material by a gas spray drawing method adapted to inject a binder into the gas and fiber flow in a molding section, the method comprising: passing them through a molding section and a collecting device from a downstream side of the collecting device, The gas is recycled, the water is separated from the recycled gas stream together with the solids contained therein, the solids are separated from the separated water, and the water from which the solids are separated is reused for injection into the gas and fiber streams in the forming section. Of pollutants released during the production of mineral fiber, characterized by And purification methods.

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