JPS5843339B2 - Method and apparatus for producing fibers by gas spray elongation of thermoplastic materials - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION This invention relates to fibers of thermoplastic materials, in particular to the treatment of toxic, odor, and ecologically undesirable contamination contained within gaseous or liquid waste vehicles disposed of in mineral fiber manufacturing facilities. The present invention relates to a method of removing or suppressing at least a large portion of a substance and an apparatus for carrying out the method, and to reducing noise generated in a facility.

This invention relates to felts, mats, and fiberboards of fibers, especially those agglomerated with thermoplastic or thermosetting binders that coat the fibers in the final product and/or tightly bond the fibers together. This invention relates to methods and equipment for manufacturing glass fiber products.

The binders commonly used in this type of production are based on pure or modified phenolic or aminoplast resins.

The reason for this is that these binders have properties that are advantageous for the production of agglomerated fiber products.

These binders are thermosetting, soluble or emulsifiable in water, adhere well to fibers, and are relatively inexpensive.

Generally, these binders are dissolved or dispersed in water to which other ingredients are added to form the binder that is sprayed onto the fibers.

Due to the action of heat experienced during the textile manufacturing process, these binders are exposed to toxic volatile substances such as phenol, which have a perceivable pungent odor even in very low concentrations.
Releases formaldehyde, urea, ammonia, and decomposition products of organic substances.

Other binders are sometimes used because of their extremely low cost.

Extracts of various natural products are used which harden by oxidation and cross-linking, as occurs, for example, in the oxidation of linseed oil.

Still other binders are thermoplastic materials, such as asphalt.

During the fiber bonding process, all binders are heated to at least some extent sufficient to release volatile, toxic, or other malodorous components.

In the following description, binder refers to one or all binders that bind the aforementioned products, whether in liquid form or dissolved or suspended or emulsified in water or other liquids. do not have.

The present invention relates to a section called a fiber aggregation or forming section of an apparatus for producing agglomerated fiber materials. Said section is provided immediately after the apparatus for producing fibers, and the following operations are mainly performed within that section.

Transferring the fibers from the fiber production equipment to a mat or felting equipment; Applying a binder to the fibers (this binder is generally formulated with contaminants); - Forming a mat on a fiber gathering equipment (for this purpose - cooling the fibers and the gas used to attenuate and guide the fibers (such cooling is generally carried out by air attracted by the flow of said gas); separating the fibers from the attenuating gas and air by drawing a fluid consisting of the attenuating gas and the attracted air through the mat that is being formed; All materials are sucked out of the agglomerated fiber material manufacturing equipment.

In the fiber assembly or forming section, the binder containing contaminants comes into contact with large amounts of attenuating gas and water, which cause the fibers to coagulate with the binder to produce a felt, mat or board of fibers. It is this fiber gathering or forming section that is contaminated by the contamination steps common to known methods.

This contamination step will be explained below.

(a) Contamination of the gas effluent stream occurs as follows:

The binder is injected into the stream formed from the fibers and gas coming from the fiber manufacturing equipment (the binder is present in the form of a finely divided mist).

Some of this binder will be captured by the fibers, and it is inevitable that other parts of the binder will stick to the walls of the device, but
Eventually, some of it exists in the gas or fume in the form of fine droplets or vapor.

In this way, two types of fluid contamination modes coexist.

− is contamination in the form of binder droplets, and the others are contamination in the form of binder vapor.

When applying the binder, binder spraying or dispersing devices are used, which form the binder into particles or droplets of a very wide range of different diameters.

The finest droplet particles are not captured by the fibers, but are drawn through the produced mat by the gas stream and are present dispersed in the gas stream.

During binder application, the binder droplets deposited on the fibers are subjected to the dynamic action of the gas flow passing through the forming mat, and a large number of the droplets are extracted from the fibers and passed through the mat. and suspended in the exhaust gas body.

The binder is added to the fibers in an area near the fiber production equipment where the gas and fiber flow has a well-defined geometry and the gas is still kept at a sufficiently high temperature to evenly distribute the binder within the mat. It is necessary to disperse the binder in the flow of the binder and the gas so that a portion of the binder, or at least a large portion of the volatile components of the binder, evaporates into vapor.

This polluting vapor mixes with the gas streams, contaminating them and creating pollution.

In the following explanation, fume refers to the gas flow passing through the fiber mat and exiting the gathering device, i.e. the gas flow used to elongate and guide the fibers, the fluids attracted into the gas flow, and A gas stream that contains contaminants in the form of droplets or vapor suspended within the fluid.

Although various processing steps and equipment are used in the present invention to treat fumes containing a wide range of components and pollutants, it is important to treat not only pollutants generated from the fiber binder, but also pollutants in the gases used in the fiber manufacturing process. It is also intended to do so.

(b) The water used in the fiber gathering equipment is such that it is unavoidable to generate significant pollution in production equipment where binders are used.

Water is used as follows.

- (1) When the binder is in liquid form, it is used for dilution and as a carrier.

- (2) Used for the next operation of cleaning fume.

(2a) The maximum possible amount of contaminants present in the fume in the form of particles or vapors is captured by the wash water droplets.

-(2b) The fibers contained in the fume are caught on the wall of the collecting device and transported along with it.

- (3) Washing different parts of the gathering device (perforated belt, fume chimney, etc.) and discharging adhering binders and fibers.

During these operations, the wash water becomes contaminated with components of the binder in dissolved or undissolved or vapor form, the degree of contamination being considerable.

The above description of how water and fume contamination occurs is based on the state of fume and water contamination observed and measured in actual manufacturing equipment.

The data obtained from observations and measurements are shown here.
The invention is not limited to the data shown.

In most production systems for agglomerated fiber products, the effluent streams described above, regardless of the fiber production process, contain significant amounts of contaminants.

In devices equipped with devices in which the material is attenuated into fibers by means of high-energy jets, the amount of fumes emitted into the atmosphere is comparable to that of most known methods.

The AEROCOR process of U.S. Pat. No. 2,489,243 of 1100 N" starch for fiber I K9 using the method described in Slater U.S. Pat. 1st
, 124,489 and U.S. Pat. No. 3,114,618.
500,000 to 500,000 i, o o o, o o for a large manufacturing plant with 7 ONIT13 per kg of fiber.

The amount reaches Nm3/h.

Nm3 represents the amount in cubic meters at standard atmospheric pressure and room temperature.

A fiber attenuation device is provided in which the material to be attenuated is converted into fibers by mechanical force, e.g. When used only as (flowing horizontally),
The amount of fumes emitted is slightly less than above, but still large, with the process of Poell US Pat. No. 2,577,431 at 3 ON/Kg of fiber.
It reaches 300,000 to 400,00 ONm in m3.

The amount of contaminated water is almost the same for all methods, 1,000 m37h or more in large factories.

The amount of these emissions has led to the enactment of laws limiting the concentration of phenol emitted into the atmosphere, and then in at least some countries, emissions of the pollutant are completely prohibited.

Furthermore, restrictions on foul odors or turbidity in discharged fluids have been implemented in many countries.

Furthermore, equipment for producing agglomerated fiber products also tends to be a source of pollution in other ways, as in addition to producing noxious or malodorous emissions, these equipment also emit large amounts of steam, amounting to about 20 to 30 tons per hour in large factories. , emitted from the chimney as opaque smoke.

Noise is also another form of pollution generated by agglomerated fiber manufacturing plants.

Noise in these facilities is generated primarily from two sources: the fiber manufacturing equipment and the fume exhaust blowers.

In practice, the fiber manufacturing equipment in these facilities uses high velocity jet gases to transport material that is drawn or attenuated into fibers or to transport manufactured fibers.

The magnitude of the noise generated by these jets increases with the jet velocity.

This level may exceed 100 decibels near textile manufacturing equipment, and workers have to work in the noise.

This noise level is considerably higher than that permitted by industrial regulations in many countries.

Furthermore, the noise generated by the fume exhaust blower is transmitted along the chimney.

Chimneys are usually located on the outside of buildings and act as antennas, transmitting noise and disturbing the environment, and in some countries authorities have ordered some devices to be shut down.

There was an urgent need to reduce or eliminate the pollution generated, without seriously affecting the prices of the products produced.

Many experiments have been conducted on this problem and several different solutions have been developed.

The invention comprises: (a) introducing a stream of attenuating gas and attenuated fibers into a forming section having a perforated fiber aggregation device through which the attenuating gas passes but the fibers are collected to form a mat; (b) spraying the gas and fiber stream in the forming section with water and a resin binder; (C) recirculating the attenuation gas into the forming section from the downstream side of the apertured fiber gathering device;
(d) - During the flow path of the recirculating gas from the PL perforated fiber gathering device to the forming section, the recirculating gas stream is washed and cooled with water; (e) the solid material entrained in the M recirculating gas stream; and water from the recirculating gas stream; A method of producing fibers by gas blast attenuation of a thermoplastic material comprising reusing it to spray into a gas stream.

It is a feature of the present invention that the fumes, as previously defined, are largely recycled and repeatedly passed through the mat or felt product being formed, thereby significantly reducing the amount of air entering the forming section from the atmosphere. The objective is to reduce the amount of carbon dioxide and maintain a state suitable for forming a mat.

According to the invention, pregelling of the binder is prevented by spraying water into the gas and fiber streams in the forming section.

The method according to the invention is such that most of the heat from the fiber manufacturing equipment and the elongated fiber material is transferred to the wash water, the wash water is cooled, and the fume is washed with water after passing through the mat or felt and the fiber gathering equipment. It transfers some of the pollutants contained in the fume to the water, purifies only a small proportion of the fume that is not recycled before it is discharged into the atmosphere, and cleans at least a portion of the wash water. characterized in that it is recycled, a portion of which is treated to extract at least a significant portion of the pollutants contained in the wash water, and the solid material is subjected to a purification treatment prior to final disposal.

The method of this invention cools the recycle gas, which is important to enable recirculation.

Water is sprayed onto the fibers and gas stream within the forming section to cool the fibers and gas stream in combination with cooling the recirculated gas.

Such water spray cools the gas stream and lowers the temperature of the gas stream in conjunction with the cooling of the recirculated gas, despite the absence of entrainment of ambient air by the attenuating gas jet.

According to a feature of the invention, the amount of fume discharged to the atmosphere is substantially equal to the amount of gas flowing from the fiber attenuation device.

This invention relates to recycling a large portion of the fumes within the device and treating and discharging only a small portion of the fumes.

That is, the recirculated portion can amount to at least 95% of the total amount of fumes that are conventionally vented to the atmosphere.

The amount of fuyum that is purified prior to disposal is less than 5% of the total fuyum, which makes it even possible to carry out expensive purification treatments, the effectiveness of which can be reduced without prohibitive energy consumption, as for example in the case of combustion. is complete.

Another object of this invention is to make thermosetting resins contained in water insoluble.

These resins are rendered insoluble according to the invention by heat treatment under pressure, preferably at temperatures above 100 DEG C., more preferably at temperatures of about 1500 DEG to 240 DEG C.

The binder component contained in the water is made insoluble by carrying out the above-mentioned operation to make the resin insoluble using at least a portion of water for cooling and washing, and then the insoluble substances are extracted by a well-known method, The concentration of polluting components in the cooling and cleaning waters can be maintained at a level that is acceptable for continuous reuse of these waters within the device.

The cleaning steam water is circulated in a closed circuit to prevent pollutants from going outside together with the cleaning water.

Another object of the invention is to heat-treat washing water.

This heat treatment consists of evaporating the water and raising its vapor to a temperature sufficient to convert pollutants into non-polluting components.

The advantages of this invention also include the special configuration of these devices to reduce the noise generated by the recirculating fumes, the noise isolating devices of these devices, and the special arrangement of the devices for discharging non-circulating fumes to the atmosphere. The aim is to reduce the noise leaking from these devices to the surrounding environment.

Other objects and advantages of the present invention, particularly various special advantages of recycling fumes, are described in detail.

The accompanying drawings illustrate several embodiments of the invention, shown in partial arrangement and generally in vertical section.

PRIOR ART FIG. 1 shows a known fiber aggregation device, which includes a fiber production device 11, in which the material to be elongated is agglomerated or bonded by centrifugal force or aerodynamic action or both, to form a panel or a panel. Made of board material.

Aerodynamic action is generally carried out by subjecting the material or fibers to be attenuated to a high-temperature, high-velocity jet of gas.

An example of such a device is U.S. Pat. No. 3,285,723.
The produced fibers exit the apparatus 11 in a generally gas stream 12 formed by a high-energy jet and air or other gas that the jet draws in from the surroundings. The gas stream 12 directs the fibers in a uniformly shaped stream towards the concentrator while further elongating the fibers.

The present invention is applied to such a device.

The device further includes a fiber manufacturing device 1 for fiber and gas flow passages.
1 and the collecting device includes a binder supply zone in which an atomizer (binder supply device) 13 disperses atomized binder formed from small droplet particles into the fiber and gas stream.

Most of the droplets intersect with and adhere to the fibers, while the remaining part is either suspended as droplets in the gas stream accompanying the fibers or is contained in the form of vapor.

The fiber distribution device 14 is of a known type and is installed in the fiber and gas flow path 12 between the production device 11 and the binder supply zone or between the binder supply zone and the mat forming zone.
arranged as shown in the figure to vibrate or otherwise deform the flow of fibers and gas, causing the fibers to form a felt or mat of substantially uniform weight per unit area on the surface of the concentrator. let

The surface of the collecting device is formed by a perforated endless belt 15 on which the fibers are collected in the form of a felt or mat 23.

A chamber 16 is provided below the perforated belt, i.e. the area where the fibers are deposited and the felt or mat is formed, i.e. the forming area, and a blower 19 reduces the pressure in the chamber 16 to create a negative pressure. As a result, all gas flowing with the fibers between the production device 11 and the perforated belt 15 passes across the forming mat, so that no gaseous fluid is carried with the fibers out of the mat-forming section. .

A vertical wall 21 extending from the perforated belt 15 to a height near the fiber production apparatus 11 surrounds the area in which the mat is formed and forms a forming compartment or chamber 22 which is open at its upper end near the production apparatus 11. The so-called formation hood (HO
OD).

A blower 19 which creates a negative pressure in the chamber 16 causes the gas entrained with the fibers to pass through the mat that is being formed as all the fibers are being deposited in the mat forming area and releases the fumes into the atmosphere through the chimney 5.

The amount of fumes discharged from the forming section as described can be significant and, in fact, stretches or attenuates the fiber production material within the fiber production apparatus.

Alternatively, the guidance of this material and the fibers formed is carried out by means of gas jets, the quantity and velocity of which are extremely large.

The velocity of this gas jet is generally greater than 100 meters per second, which is preferred for fiber formation;
5 is much greater than the velocity required for the fibers and gas to arrive and form a mat.

Mat formation does not require more than 10 meters per second.

In fact, it is necessary to significantly reduce the velocity of the gas jet from the production device, and this is done by transferring part of the momentum of the gas jet to the surrounding fluid.

The surrounding fluid is attracted (inhaled) in the direction of the gas jet, mixes with the gas jet, and is accelerated.

This mixture of gas jet and suction fluid constitutes a gas stream that accompanies the fibers.

The attraction of ambient fluids by gas jets from textile manufacturing equipment is a well-known phenomenon of jets flowing in the atmosphere, and also in rooms containing fluid.

It is known that the flow mechanism attracts a large amount of gas from the surroundings by such a gas jet, and that the amount increases with the amount of the gas jet and the distance traveled through the surrounding gas body.

However, the attraction phenomenon is a continuous phenomenon, and the slowing down of the gas jet becomes noticeable only after the gas jet has passed a sufficient distance through the surrounding gas.

In an apparatus of the type described above, this flow from the textile production apparatus 11 to the belt 15 is controlled in order to provide a velocity of the fiber and gas stream on reaching the collecting belt 15 of the aforementioned approximately 10 meters per second or less. The distance is 2 meters or 3
meters, a gas jet from the production device 11 is attracted within this distance, so that the amount of gas crossing the belt 15 amounts to at least 10 to 20 times the amount of the gas jet.

In addition to the reduction in velocity imparted to the flow of the gas stream and the fibers entrained therein, in order for the mat to form under good conditions, the fiber and gas flows must be parallel and the device 11
It must be oriented generally in the direction from to the belt 15.

To further illustrate, the fiber and gas flow stream 12 is plotted perpendicularly to the direction of flow by lines M, N, 0 . Consider partitioning as shown by P.

For example, in the section between lines M and N, the flow maintains a well-defined direction and the velocity reduction is constant.

These two factors, namely flow direction and velocity reduction, are favorable properties within each compartment for the flow to attract the required amount of fluid uniformly along the perimeter of the compartment, e.g. while passing through compartment MN. The decrease in relative velocity experienced by the flow of and the line M
The amount of fluid attracted is proportional to the product of the mass of fluid forming the entering flow.

This relative velocity reduction is equal to the ratio of the difference between the velocity of the flow entering line M and the velocity of the flow leaving line N to the initial velocity.

If each section of the flow between the textile manufacturing equipment and the collecting belt is supplied with the amount of fluid required by the surrounding air or gas to direct and slow the flow so that the flow between each section has the desired characteristics. An induced surrounding fluid flow is established from the manufacturing device 11 towards the collection belt 15 along the flow of the fibers and the gas associated therewith.

This flow is shown by line 27 in FIG.

In a fiber forming apparatus such as that shown in FIG.
1 is formed by the atmosphere entering through a large opening 28 near 1.

Figure 2 shows the pattern of fluid flow in the formation chamber when the gas jet coming from the elongating device cannot attract all the gas attracted from the surroundings into the jet; this pattern explains the action of the fluid. This is shown as an example.

Figure 2 shows a fiber manufacturing device 1 from which a flow 12 of fibers and gas is produced.
1, a binder supply device (binder nozzle) 13, a fiber distribution device 14, a gathering belt 15, and a suction chamber 16 into which the fume 29 after crossing the mat 23 to be formed is sucked. Show part.

These members are similar to those used in FIG.

However, in FIG. 2, the formation compartment (reception chamber or chamber) 22
The partitioning wall 21 extends up to the fiber manufacturing apparatus 11 and significantly reduces the size of the opening 28 through which the chamber 22 communicates with the atmosphere, thereby reducing the amount of atmosphere entering the chamber.

Therefore, the sections comprising the stream 12, in particular the sections MN, near the fiber production device 11, i.e. near the orifices of the elongating and guiding gas jets for the material to be fiberized, or near the fiber guiding jets, thus the gas In regions where the velocity of the jet stream is highest, the surrounding medium cannot supply stream 12 with all the gas it attracts, while downstream of stream 12, in sections such as section OP (where the velocity of stream 12 is (is small) cannot be supplied in sufficient quantity.

Gas stream 30 originating from the downstream area of stream 12 or stream 12 itself rises along wall 21 to the higher velocity upstream area, is captured by stream 12 and re-accelerated in the overall flow direction of stream 12.

A vortex flow 31 is thus generated between the boundary of the flow 12 and the chamber wall 21.

The strength of this vortex increases with the amount of fluid that the surrounding medium is unable to provide.

The direction of circulation of the vortex is such that it picks up fibers from the mat 23 and causes them to rise along the wall 21 in the direction of the fiber distribution device 14, the binder applicator nozzle 13 and the fiber production device 11.

If the amount of atmospheric air entering the receiving chamber 22 of the apparatus shown in FIGS. The transported fibers may adhere to the distribution device 14 and the binder supply device 13, preventing them from operating properly.

These swirls disrupt the mat that forms, causing it to take on the shape shown in FIG.

In devices of this kind, which are used in practical industrial applications, it is possible to carry the fibers upward by the phenomenon described, as long as the amount of air drawn into the room is at least 60-70% of the required amount. .

Below this amount, the operation becomes industrially impractical.

If the amount of air entering this chamber is further reduced or eliminated altogether, turbulence within the chamber will occur and the fibers will not be able to be deposited onto the collecting belt.

One of the objects of the invention is to significantly reduce the amount of air entering the formation zone from the atmosphere, while still maintaining conditions suitable for mat formation.

According to the invention, instead of air from the atmosphere as the induced fluid, a portion of the fume from the exhaust blower outlet is used, i.e. by recirculating a portion of the fume drawn from the forming section into the forming section. It is processed.

An apparatus for carrying out this method is shown in FIG.

The upper part of the forming section 22 is closed with a lid 32 through which the gas and entrained fiber stream 12 from the fiberizing device 11 enters the forming section 22 .

The edge 33 of this opening is made tangential to the flow 12 and
Facilitate the passage of 2.

For operational convenience, the lid 32 is located at a distance H from the fiberizing device 11.

The apparatus shown in FIG. 3 has a cleaning chamber 17 downstream of the suction chamber 16,
The cross section of the cleaning chamber 17 is generally larger than the cross section of the chamber 16;
A fume 29, i.e. a device is provided for bringing into contact the gas stream, which flows with the fibers and contains contaminants, with a cleaning fluid, in particular water, between the production device 11 and the collecting belt 15.

In the washing chamber 17, the fume is separated from a portion of the substances suspended therein, in particular consisting mainly of fibers and binders.

These materials are trapped and transported within the fume as it passes through the binder supply zone and mat forming zone.

When in contact with the wash water, water droplets settle on the fibers contained within the fume and fall by gravity to the bottom of the chamber 17; this phenomenon is a result of the change in the cross-sectional area of the flow passing from chamber 16 to chamber 17. is accelerated by a sudden decrease in the velocity of

Some of the droplets and contaminated vapor come into contact with the wash water droplets and are dissolved.

The fume is cleaned by these two actions.

The wash water, in which at least a portion of the fuyum contaminants have been transferred, is discharged from the drain 24.

In this device, a cyclone type or electrostatic type separation device 18 is disposed between a cleaning chamber 17 and a suction blower 19, and at least a portion of water droplets contained in the fume are separated from the fume during cleaning.

It is important that this separation takes place before entering the blower 19.

The cleaning water extracted from the fuyum is in liquid form at the outlet 25.
is removed from the separator 18 through.

A collection device 26 directs the wash water discharged from outlets 24 and 25 to a treatment area.

As previously discussed, the fiber and gas flow passes through a binder supply device 13 and then through a fiber distribution device 14.

The fibers are deposited on the collecting belt 15 and the fume 29 is passed through the forming fiber mat 23, the chamber 16, the (water) separator 18 and into the upper flue 34 by the blower 19.

A portion of the fume is discharged from the system via conduit 35.

The remainder of the fume passes through the flue 34 and enters the forming section 22 through an opening 36 close to the fiber production device 11.

The amount of gas entering the forming compartment through the opening surrounded by lip 33 is equal to the amount of gas from production device 11 and the amount of air drawn from the atmosphere during its passage along length H. is equal to the sum of

The amount of gas entering the chamber therefore increases with increasing length H.

In order for the system to be in equilibrium, the amount of fume leaving the system through the (exhaust) conduit 35 must be equal to the amount of gas entering the system through the opening surrounded by the rim 33.

The amount of fume to be ejected therefore decreases as the distance H decreases.

FIG. 4 shows a special embodiment in which the distance H is zero, that is, the fiber manufacturing apparatus 11. The case is shown in which at least the elongation and injection holes for the guide gas jet are located in the compartment 22 .

The amount of fume discharged from the system is very close to the amount of fluid coming from production equipment 11.

The percentage of recirculated fume is at least 96 in this example.
It reaches ~97.

In the device according to the invention shown in FIGS. 3 and 4, the amount of recirculating gas corresponds to the amount induced by the jet from the production device 11, and the fluid flowing through the forming section 22 is the flow of the attenuating jet. Therefore, no chaotic eddies occur.

The recirculating fumes primarily follow the direction of arrow 37.

One of the advantages of this invention is that the blower 19 imparts a slightly greater velocity to the recirculating fume stream 37 than the atmospheric air stream 27 that the fiber and gas stream 12 induces into the apparatus shown in FIG. It is.

In flow 3γ, the fibers flow through the binder supply device (binder nozzle).
13 and distribution device 14 to have sufficient momentum to overcome backflow or blowback as described with respect to FIG.

One of the most important advantages of the process of the invention is that the amount of fumes discharged from the system is only about 3 to 4% of the amount normally discharged (this amount has already been mentioned); It is possible to carry out highly effective purification treatment for small amounts of fumes without considering costs.

Fume treatment according to the present invention consists in heating the fume discharged from the discharge conduit 35 to a high enough temperature to burn out the organic compounds therein, preferably at a temperature of 600° C. or higher; pollutants,
In particular, phenolic compounds are converted into non-polluting substances by combustion, for example CO2 and H2O.

This treatment has the advantage of eliminating bad odors.

As shown in FIG. 3, combustion takes place in a device 38, which comprises a conventional combustion chamber 39, a burner 40 for supplying the combustion mixture, and is equipped with a grate 41 or similar element as a flame stabilizer. There is.

The treatment temperature is 3000-4000℃ when a combustion catalyst is used.
The temperature can be close to the 0°C range.

The purified fume is discharged into the atmosphere from the chimney 42.

At the exit of the chimney 42, the temperature of the fume is sufficiently high due to the low fume emissions due to recirculation, and the vapor contained within the fume does not condense until all of the fume is diffused into the atmosphere.

Therefore, the cloudy smoke that is expelled does not appear at the exit of the chimney 42.

Another advantage of this invention is that the fume is recycled and undergoes a full purification process, so there is no need for a complete preparatory cleaning.
This means that the size and equipment cost of the cleaning device 17 and water separation device 18 provided upstream of the blower can be reduced.

The apparatus of FIGS. 3 and 4 provided in accordance with the present invention is provided with a forming section 22 surrounding a binder supply device 13 and a fiber distribution device 14, making devices 13 and 14 difficult to access.

During operation, the binder supply device (nozzle) 13 or the fiber distribution device 14 may require servicing.

To accomplish this, it is advantageous to provide an inspection window in the wall of the room near the fiber manufacturing device 11.

A pressure equal to atmospheric pressure or a few millimeters of water column below is maintained in the forming section 22 to prevent fumes still containing pollutants from escaping from the forming section 22 during fume recirculation.

When the inspection window is closed, untimely fume leakage can be prevented due to the sealing effect.

In the embodiment shown in FIG.
The pressure inside is adjusted to the desired pressure.

In other methods, the fuyum is not placed in the recirculation flue 34 but in the fourth
As shown, this is done directly from the forming compartment 22 through an opening 43 in the chamber wall in the area necessary to maintain the pressure at the desired value.

The fumes are removed from the compartment 22 by a small auxiliary blower 44 and exhausted through the flue 35.

The blower 19 thereby only ensures recirculation of the fume.

This type of arrangement facilitates bringing the pressure within chamber 22 close to ambient atmospheric pressure.

One of the features of this invention is that the binder supply device (nozzle) 1
It is possible to control the flow of atomized binder from No. 3 as a function of the amount of binder component suspended within the recirculating fume.

The binder component is attached to the fibers as the fume passes through the mat.

During operation, the fume is repeatedly recirculated past the forming mat.

Although the mat has a limited ability to capture binder, the rate of fume passing through the mat is slow, so by continuously recirculating the fume through the mat approximately 15 times per minute, the binder components suspended within the fume can be reduced. A significant amount is captured and retained by the mat.

This reduces the amount of binder sprayed or dispersed by the binder supply device (nozzle) 13 to the same extent, which increases the binder efficiency by about 5% and is not negligible from an economical point of view.

In an apparatus such as that shown in FIG. 1, it is necessary to maintain a certain temperature within the forming section 22, so that the heat imparted by the fiber material to be attenuated and the attenuation and guiding fluid must be removed. No.

The binder used to bind the fibers is usually thermoset so that it gradually changes from a liquid state to a solid state during operation.

If the temperature within the forming section 22 is too high, during mat formation the binder reaches a hardened state in which its ability to bind fibers is reduced.

This state is called pre-gelation.

This is prevented by cooling the forming section 22.

In the apparatus shown in FIG. 1, such cooling is accomplished by introducing atmospheric air, which is generally lower than the minimum temperature desired in forming section 22.

The amount of heat introduced into the forming section by the material to be attenuated and the attenuation and guiding fluid is approximately 1500 to 1500 Kca/Kg of material depending on the fiberization method used.
l! This amount of heat is transferred to the attracted air and then to the fuyume, which transfers this heat to a small amount of washing water.
The rest is emitted into the atmosphere.

In the apparatus shown in FIGS. 3 and 4, since the amount of fumes released to the atmosphere is small, the amount of heat emitted is very small and, in accordance with the invention, other means are provided for cooling the forming section 22.

This cooling is accomplished by transferring at least a portion of the heat introduced into the forming section by the material being attenuated into the forming section 22 and the attenuating and guiding gas flow to the water; this heat transfer transfers the water to the fibers. This is done by contacting with an entrained gas or fume.

After absorbing heat within the forming section 22, this water is discharged outside the forming section and cooled by a suitable device outside the apparatus.

Heat exchange between the fibers and the entrained gas or fumes and the cooling water can take place directly or through heat exchange walls.

It is known that the amount of heat exchanged per unit area and unit time by such a heat exchanger is proportional to the temperature difference between the fluid being cooled and the cooling fluid, and also proportional to the area of the contact surface.

Since the velocity of the gas or fume is large compared to the size of the device, the time allowed for heat exchange is extremely short.

Therefore, the amount of heat exchanged per unit time must be large to achieve sufficient cooling.

The present invention provides a method and apparatus that achieves such objectives.

One method is to cool the material to be drawn and the heat carried in the elongation or guiding fluid to the fumes in the suction chamber 16 and wash chamber 17 outside the forming section 22; can utilize a large surface contact area between the fume and the cooling water.

This large contact surface can be obtained in several ways.

This is done by dispersing water in the form of fine droplets, by running it in the form of a very thin film, or by bubbling fume through the water.

In the arrangement shown in FIG. 3, the atomizer 45 distributes the cooling water in the form of a film or curtain of fine droplets, these films being carried out in a direction 29 approximately perpendicular to the direction of flow of the fume.

Once the fume has passed through the forming mat, it enters the suction chamber 16 at a temperature of approximately 800-100°C and is cooled within chamber 16 to approximately 30°C.

The temperature of the water at the inlet of the atomizer 45 is about 15° to 20° C., depending on the capacity of the cooling system for the atomizer 45.

Upon contact with the fume, the water is reheated to 30 DEG C. to 40 DEG C., depending on the flow rate of the cooling water through the atomizer 45.

After passing through the separator 18 and the blower 19, the recirculated portion of the cooled fume enters the forming section 22 again, where it is mixed with the gas stream from the fiber manufacturing apparatus, and the gas stream and the fibers are transferred to the apparatus of FIG. The recirculating fume cools the gas stream and fibers in the same way that air from the atmosphere cools the gas stream and fibers.

Another embodiment is shown in FIG. 4, where the water flows in a very thin film over the baffle 46.

The fume stream 29 flows along these bubbles and is cooled by contact with the water film.

Another embodiment is shown in FIG. 5, in which the fume stream 29 emerges from an orifice 47 located below the free surface of the water in a water tank 48 provided downstream of the suction chamber 16. to generate strong gas bubbles and obtain a large contact surface.

Another method is to inject water directly into the fiber and gas stream 12 to cool it directly and drain the water out of the forming section 22 to remove the material to be fiberized and the heat carried by the attenuation and guiding fluid. do.

The injection of water into stream 12 takes place where the contact surface is not too large due to the small area available, but where the temperature difference between the fluid to be cooled and the cooling fluid is large.

For example, in the embodiment shown in FIG. 3, an atomizer 49 is positioned between the fiber production device 11 and the binder supply device 13 and injects a cloud of fine water droplets onto the elongated fibers and the stream of gas to be cooled.

The water droplets are fed into a high temperature zone of up to 600° C. of the fiber and gas stream and evaporate immediately, thus providing a highly efficient cooling.

This large amount of heat, about 650-700Kca per kg of water
/ heat is removed from the fiber and gas flow, causing the water droplets to evaporate.

This reduces the temperature of the stream to approximately 100° to 120° C. at the height of the binder feeder 13.

The generated steam is discharged together with fume through the fiber mat 23 to the suction chamber 16 and the cleaning chamber, and comes into contact with the curtain of water sprayed by the sprayer 45, where the steam condenses and transfers its steam latent heat to the cooling water from the sprayer 45. .

This heat is thus removed from the device along with the water from the atomizer 45.

The provision of a sprayer 49 for injecting cooling water onto the stream 12 between the fiber production device 11 and the binder supply nozzle 13 is a preferred arrangement according to the invention and has several advantages for operation. .

Firstly, this is because this region has the greatest temperature difference between the cooled fiber and gas flow and the water, and therefore the greatest heat exchange.

A binder is then applied to the fiber and gas stream, and the temperature of the stream is sufficiently low (100'-120'C) that evaporative degradation of the binder components is very limited or non-existent.

As a result, the efficiency of the binder is increased by about 5% and the pollution from fumes is therefore also reduced.

Another embodiment is shown in FIG. 4, where the fiber and gas flow 12
A cooling water injection device 50 for this purpose is arranged between the binder supply device (nozzle) 13 and the collecting belt 15.

Similar to the embodiment shown in FIG. 3, cooling water passes through the forming mat in the form of steam.

This vaporized water condenses on the baffle 46 of the cleaning chamber 17 and imparts heat to the water film flowing over the baffle.

Water is discharged to the outside of the device through holes 24 and 25 provided at the bottom of the washing chamber 17 and the bottom of the water separation device 18, respectively.
Filtration device 5 for separating solid substances, especially fibers, suspended in water
Sent to 1.

The filtration device 51 may be a known rotating or vibrating mesh filter or a decanter or centrifugal device.

The water, free of suspended solids, is collected in a basin or tank 52 in the embodiment of FIG. 3 and then pumped by gravity or pump 5.
3 to the cooling device 54.

This device 54 can be discharged to the outside or reused.

As shown in FIG. 3, the cooling system 54 includes a cooling tower 106 in which the water is cooled by contact with air in a known manner.

Cooling water is circulated and sprayed within the tower 106 by a pump 107.

The water from the water tank (tank) 52 is indirectly heat exchanged with the cooled water in the device 54 through the heat exchanger 105, cooled, and returned to the water tank 52.

Make-up water may be introduced through supply pipe 111.

The wash water may be passed through cooling tower 106 for indirect heat exchange with cooling water (or other cooling fluid).

This can completely avoid contaminating the air with evaporative pollutants remaining in the wash water.

The amount of residual pollutants is often very small (eg, less than 5% is emitted from the outlet of the non-recirculating facility shown in Figure 1).

The wash water may be cooled directly in the spray cooling tower.

One advantage of this invention is that the water is not drained from the device in liquid form;
Even when there are few pollutants contained in the water, the surrounding environment should not be contaminated.

This means that the water introduced from the cooling water injection device (nozzle) 49 or 50 and the cleaning water are circulated in a closed circuit within the facility.

In the apparatus shown in FIGS. 3, 4 and 5, the closed circuit for producing cooling and washing water is as follows.

Water exiting the cooling system 54 is pumped by a pump 55 to a cooling water injection system 49 and/or 50 in the forming section 22 and a steam condensing and fume cleaning system in the cleaning chamber 17, including a sprayer 45, as shown in FIG. or includes a water film bubble 46 as shown in FIG. 4, or a water tank or tank 48 as shown in FIG.
sent to.

The cleaning water and condensed steam containing pollutants, fibers and binder components are discharged through the outlet 24 at the bottom of the cleaning chamber 17 and the separator 18.
It flows through an outlet 25 at the bottom of the water to a collection device 26 and is led to a filtration device 51 to separate and remove suspended solid waste 56, fibers and insoluble binder components, from the wash water.

These solid wastes 56 are collected on a conveyor 57.

The filtered wash water, containing only dissolved binder components and contaminants, is conveyed by gravity or by pump 53 to cooling device 54 .

It has been observed that when the wash water is circulated in a closed circuit it is necessary to maintain the amount of dissolved or suspended matter contained in the filtered water below a certain amount consisting of units of water. Approximately 3 to 4 units of dry material relative to the amount
% is better.

In this case, materials dissolved or suspended in the wash water (particularly microscopic fibers and binder particles not captured by the filtration device 51) will adhere to various parts of the device.

The binder component polymerizes and forms a viscous or solid layer which gradually closes the holes in the collecting belt 15 through which the nozzles of the atomizer 45 and the fume 29 pass.

As a result, the amount of fume discharged from the formation section and wash chamber and the amount of fume cooling are reduced, causing the entire system to be closed.

It is necessary to remove a large amount of material from the wash water in order to reduce the concentration of the material carried into the water so that spraying of the water onto the fume or removal from the fume is not impeded.

During operation, a quantity of 20-30% of the binder sprayed onto the fibers by the binder supply device (nozzle) 13 is carried into the wash water as explained above.

In large factories it is unavoidable that 3,000 to 5,000 to 90% of binders are introduced into the wash water circuit every day, and an equal amount of binder is introduced into the water in order to keep the concentration of these substances in the water in equilibrium. It is necessary to extract the binder from the water.

Several extraction methods are possible.

One method is to subject at least a portion of the wash water to a centrifuge, in which case small suspended solids that cannot be processed by the filter 51 can also be separated.

The water treated by the centrifugal separator 58 is preferably returned to the water tank 52 as shown in FIG. 3, or sent to the cooling water injection device 49.

Another method involves adding a coagulant to the water and treating it to separate the coagulated material.

These two methods have the disadvantage of separating only the undissolved substances contained in the water; the dissolved binder component, which constitutes the majority that must be removed, is not separated or is only slightly affected. Only.

The present invention provides a number of methods for extracting the binder dissolved within the wash water.

One method consists in using filtered or centrifuged wash water to dilute the binder during preparation of the binder for application to the fibers by the binder feeder 13.

The filtered water may be taken at any point downstream of the cooling device 54 or by a valve 59 downstream of the centrifugal device 58 as shown in FIG.

Another method consists in using wash water in the forming section 22 as a cooling fluid for the fiber and gas stream 12.

The wash water is injected into the stream 12 by a (cooling water) injector 49 as shown in FIG. 3 or by a (cooling water) injector 50 as shown in FIG.

These two methods have the advantage that a part of the binder contained in the cleaning water can be reused. According to the present invention, the amount of binder sprayed by the binder supply device 13 is reduced by the mat 23 being formed (cooling water ) control as a function of the amount of binder retained by the forming mat without being washed away by the water injected by the injectors 49 or 50;

Although this improves binder efficiency, these methods do not allow for the removal of dissolved binder from the wash water and reduce the concentration in the wash water below the desired amount.

For this reason, the invention provides two methods for extracting large amounts of binder from water circulating in a closed circuit.

One of these methods consists in burning a small portion of the wash water flowing in the circuit, about 1 to 5%, in a suitable device such as device 60.

A device 60, shown in FIG. 4, is a known device and comprises the following elements: a burner 61 supplied with combustion air and fuel; - water coming from a pipe 63 in the form of pressurized droplets into the flame of the burner 61; an atomizer 62 which is injected under the action of a jet air 64; a reaction chamber 65 in which the wash water is treated with heat from the N11-s 61; to about 800° C., converting binders and contaminants into non-polluting substances such as CO2 and H2O).

The treated non-contaminated steam is discharged from the chimney 66 at a high temperature to prevent cloud-like white smoke from being discharged.

The point where water is to be treated is removed from a point between pump 55 and devices 50 and 46 as shown in FIG.

This method has the advantage of converting all of the binder components contained in the treated wash water into non-polluting substances.

However, it has the drawback of requiring a large amount of energy and being expensive.

However, the processing cost impact on the manufactured textile product can be reduced by recovering heat from the hot steam in a heat exchanger to produce superheated steam for multi-purpose use.

Another method involves heat treating a small portion of the wash water containing dissolved binder, approximately 1-5%, circulating in a closed circuit to render the binder insoluble and then separating it from the water by a suitable method such as filtration centrifugation or coagulation. .

In operation, the inventors found that if the water used for cooling and washing the fume and thus containing binder or dissolved binder components after filtration is maintained at a certain temperature for a certain period of time, as the temperature increases and the time increases, the molten binder becomes free. It was observed that it turned into dissolved particles and became suspended in water and could be easily separated from the water.

The efficiency of this heat treatment is determined by the rate at which the molten material is insolubilized by the heat treatment.

Processing temperature has a very large effect on processing efficiency.

For example, the treatment efficiency of water containing 1% binder content is - 40% if the water is kept at 40°C for 8 days; - 40% if the water is kept at 70°C for 3 days;
40% if kept at 0°C for 3 minutes; - if water is kept at 180°C
60% if water is kept at 240°C for 3 minutes;
It was 95% when maintained for minutes.

FIG. 6 shows the variation in processing efficiency as a function of temperature and processing time.

In a large factory that manufactures cohesive fiber panels, the amount of water to be treated is 5.
0 m3/h, and in order to avoid installing a water treatment plant of considerable size, the shortest treatment time is therefore 10 m3/h.
It is necessary to process at a temperature higher than 0°C.

This means that the process is carried out under pressure at a temperature that is maintained approximately 5°C below the boiling point of the water under pressure so as to maintain the water in the liquid phase during the process.

This solution has the advantage that only a small amount of energy is required for waste disposal, which corresponds to an increase in the amount of heat imparted to the water due to the increase in its temperature.

It therefore requires one-fourth the cost compared to the previously described combustion method with the same amount of dissolved binder extracted.

A common disadvantage when heating water containing binder or dissolved binder components indoors is that deposits of undissolved binder, even at low concentrations, form on the walls of the chamber and quickly thicken and block the chamber's drainage holes. or the chamber itself may become impaired.

If the heat required for treatment is applied to the water to be treated and the temperature of the walls of the chamber is kept lower than the temperature of the water to be treated during treatment, no binder deposits will form on the walls and the insolubilized binder will remain in the water. was observed to remain suspended in the water.

This can be done by mixing a hot fluid such as superheat steam with the water or by blowing combustion burner gas into the water or by placing an electric spark into the water to localize the energy.

A wide range of operating conditions is possible, for example pressures between 6 and 40 bars absolute, temperatures between 1500 and 240° C., and treatment times between 3 and 10 minutes.

The following conditions result in a satisfactory compromise between energy costs and equipment maintenance costs: Temperature 200°C Pressure 16 bar absolute Duration 5 minutes Efficiency 70 to 80% This process is a discontinuous process. Alternatively, it can be applied to any continuous processing method.

FIG. 7 shows a discontinuous processing apparatus for carrying out this processing method.

The water to be treated is introduced into the container 68 through a motor-operated valve 67, the amount introduced being between 70 and 8 of the volume of the chamber 68.
At 0%, heated fluid or steam, preferably superheated steam, is injected into the water through the injection tube 69.

The amount of steam is regulated by controlling a motor-operated valve 70 with a controller 71.

The processing cycle is performed as follows.

The chamber 68 is initially filled with the water to be treated at atmospheric pressure and is then pressurized by the controller 71 to the required pressure, for example 16 bar absolute.

The valve 70 is opened and steam is injected through the injection pipe 69 to mix with the water to be treated (this steam condenses and transfers its sensible and latent heat to the water), the temperature in the chamber 68 is set to 200°C, and the pressure is set to 16% absolute pressure. Continue introducing steam until it rises to the crowbar.

At this time, the introduction of steam is stopped, but the injection of steam from the injection pipe 69 is adjusted so that this increase in temperature and pressure occurs within one minute.

The water is kept at 200° C. and 16 bar for 2 to 4 minutes.

At the end of this period pump 72 is operated and jacket 74
New water to be treated is supplied to the water tank 73 through the process.

This new treated water is at about 40° C. at the jacket temperature and cools the treated water in chamber 68 as it passes through the jacket.

The size of the jacket 74 is adjusted so that the water to be treated reaches a temperature of about 80° C. when it reaches the water tank 73.

Auxiliary cooling fluid circulates through jacket 75 to complete cooling of the water to be treated within chamber 68 .

This cooling is considered complete when the temperature of the water to be treated is below 100°C and preferably between 40°C and 50°C.

At this point, motor operated valve 76 is gradually opened to reduce the pressure in chamber 68.

The treated water flows to a filtration device 51, a coagulation device, a decanter device, or a centrifuge device, and the binder component insolubilized by the above treatment is separated from the treated water.

The filtered water flows into a water tank 52 and the separated waste 56 is conveyed to a conveyor 57.

When the chamber 68 is empty, the valve 76 is closed, the valve 67 is opened, the water in the preheated water tank 73 flows into the chamber 68 by gravity, and the gas in the chamber is discharged by the exhaust valve 67a.

A new cycle can be restarted.

FIG. 8 shows the arrangement of a continuous processing apparatus for the processing method according to the present invention.

The pump 77 sends the water to be treated under the treatment pressure to a mixing device 78. A jet pipe 79 is disposed in the mixing device 78, and a heating fluid made of steam is introduced into the mixing device 78.

This steam mixes with the water to be treated and, upon condensation, transfers all of its heat to the water.

The flow rate of this steam is regulated by a motor operated valve 80 controlled by a controller 81 to maintain the desired process temperature at the outlet of the mixing device 78.

After residence in mixer T8 for 10 seconds, the water to be treated passes through reactor 82, where the binder is insolubilized.

The size of the reactor 82 is such that the residence time of the water to be treated is, for example, 2
The size is adjusted to correspond to a processing time of 4 to 4 minutes.

The water leaving the reactor 82 is cooled in a heat exchanger 83 to below 100°C, preferably to 400-50°C.

Part of this cooling is performed by the water to be treated itself, which is heated within the coiled tube 84 from about 40°C to about 80°C.

The remaining cooling is provided by fluid flowing within coiled tube 85.

The treated cooled water leaving heat exchanger 83 is routed to controller 8
The pressure is reduced to atmospheric pressure by a pressure reducing valve 86 which is controlled by 7 and maintains the processing pressure in the apparatus.

The reduced pressure water is sent to a filtration device 51, a coagulation-decantation device, or a centrifugal separator to separate the insolubilized binder component from the treated water.

The filtered water is sent to a water tank 52, and the waste 56 produced by the treatment is sent to a conveyor 57.

The continuous operation type apparatus shown in FIG. 8 is more flexible than the apparatus shown in FIG. 7 and can be processed at a lower cost.

Another method may be to treat a portion of the wash water containing contaminants with bacteria in an aeration tank.

In the aeration tank, bacteria act to destroy yeast on the phenolic compounds present in the water.

The phenolic compounds are converted, in particular, into the non-polluting substances CO2 and H2O by an operation corresponding to a complete oxidation reaction.

In order for the reaction to take place completely, it is necessary to aerate the tank, supply bacteria, and supply oxygen to carry out the oxidation reaction.

Equipment for producing cohesive fiber panels produces large amounts of waste of varying compositions, but always containing binders and polluting binder components.

First, industrial waste removed through quality control has pollutants widely dispersed and is large in volume.

The waste resulting from the filtration of cooling and wash water contains fibers and large amounts of binder and binder components.

Traditionally, these wastes were usually stored in storage sites.

However, this created a pollution problem.

This invention is to convert waste into non-polluting materials.

After pre-treatment, the waste is subjected to heat treatment combustion to convert pollutants into non-polluting substances such as CO2 and H2O.

FIG. 9 shows the arrangement of equipment for carrying out this method.

The waste 56 is transferred to the conveyor 5 from the heat treatment equipment and water filtration equipment.
7 and placed in a crusher 88 where it is mixed with waste agglomerated fiber product waste from the manufacturing stage.

The mixture discharged from the crusher 8B is conveyed to an incinerator 90 by a conveyor 89, and heated to a temperature of 1000° C. or more by a burner 91.

At this temperature, the binder and binder components are H2O and CO
It is converted into a non-polluting substance such as No. 2, and is discharged into the atmosphere from a chimney 93 together with combustion gas from a burner 91.

The material made of fibers softened by the heat accumulates at the bottom of the furnace 90;
It is discharged as a viscous stream from an outlet 92 and cooled in a tank 94 filled with water.

The cooled material is removed in the form of particles, which may be used again for fiber production.

FIG. 10 shows another arrangement for waste treatment, in which a mixture of wastes 56 and 87 is conveyed from a crusher 88 on a belt 94 to a furnace 95 and is heated to 600 m
The temperature can be increased from 0 to 700°C.

In this process, the binder and its components contained in the waste are converted into non-polluting substances such as H2O and CO2,
It is discharged from the chimney 97.

The fibers, which constitute the bulk of the waste volume, are softened by heat and agglomerated by combustion into the form of plates 98 whose volume is much smaller than the original volume of the waste.

This plate 98 is reintroduced into the textile manufacturing circuit.

Another important feature of the invention is that it reduces the noise generated by the device.

The most important source of noise in these facilities is the textile manufacturing equipment, and more precisely due to its high-velocity jets.

The noise surrounding the textile manufacturing equipment exceeds 100 decibels at the worker's position.

In an open facility like the one shown in FIG. 1, a structure that surrounds the noise source cannot provide effective sound insulation because a free space is required to allow the induced air to pass through.

In the apparatus shown in FIGS. 3 and 4, the shape of the vertical walls 21 of the forming section 22 and the closing wall 32 with openings 33 allowing the passage of the fiber and gas flow 12 is such that an acoustic absorbing panel is provided in the forming section 22. 99 and the acoustic insulation panel 1 on the outside of the forming section 22
00 installation can be performed.

Providing these insulating plates around the fiber manufacturing equipment 11 reduces the noise in the area where the workers work by 20-30 decibels, representing a considerable improvement.

Another source of noise is the blower 19, the noise generated is transmitted through the flue to a chimney installed on the outside of the building, transmitting the noise to the environment.

In the device shown in FIG. 1, a large amount of air is discharged through the chimney 5, and due to the problem of limiting the pressure drop in the chimney, the blower 19 is
In order to install a large diameter chimney directly at the outlet of the air blower 19
Almost all of the noise from the

In the device according to the invention shown in FIGS. 3 and 4, the amount of fume discharged is small, and the point from which the fume is discharged can be located at a distance from the blower 19.

In FIG. 3, the chimney is connected to the circulation flue 34 at a point remote from the blower 19 through at least one curved pipe and a sufficient flue length, so that at least a portion of the noise generated by the fan 19 is transferred to the circulation flue 34. be absorbed into.

In the arrangement of FIG. 4, the outlet 43 is small and quite far away from the blower 19.

The noise reduction around the flue 35 is 10 decibels or more.

FIG. 11 shows an arrangement according to the invention and includes the following devices:

A fiberizing device 101. A molten material 102 is introduced into the device rotating at high speed. It has a number of orifices around its periphery and material is ejected by centrifugal force.

Fibers are formed and elongated into fine fibers by a focused annular jet of high velocity hot gas.

The jet is generally directed downward.

One-vibration air outlet 14 (e.g., U.S. Pat. No. 3,134,145
A fiber distribution device made of a fiber distribution device (as shown in the above), which surrounds the fiber and gas stream 12 from the fiber manufacturing device.

- a cooling device comprising a sprayer 50 for injecting cooling water into the stream 12;

This device is arranged between the distribution device 14 and the binder supply device 13.

A mat gathering device 15 is provided with a perforated belt.

The fiberizing device 10 has a perforated belt 15 at the bottom, a vertical wall 21 in the lateral direction, and a horizontal wall 32 at the top at an interval of about 200111 degrees.
1, there is a circular opening 33 through which the stream 12 passes, the edge of the opening is tangential to the stream in a shape that facilitates the entry of the stream 12, and the vertical wall 21 is connected to the perforated belt 15.
A parallelepiped formation area 22 on which a mat is formed, located below the mat formation area on the partially perforated belt 15;
The pressure is reduced by a suction chamber 16 with a blower 19, a cleaning chamber 17 located downstream of the suction chamber 16 and forming a film of water droplets in the passage of the fume 29, and a cyclone installed downstream of the cleaning chamber 17. water separator 18 of the type, passing the entire gaseous body with the fibers through the belt 15;
A blower 19 feeding the flue 34 - the downstream end through an opening 36 in the upper part of the forming section 22;
A recirculation flue 34 conducting into the peripheral zone of the fiber distribution device 14 an amount of about 90-95% of the gaseous material passing through the perforated belt 15 and being conducted into the forming section 22 - about 5-95% of the fumes passing through the belt 15 A discharge pipe 35 is provided in the flue 34 to lead 10% of the fume to the combustion device 39.
- Noise absorbing panels 99 and insulating panels 100 installed on walls 21 and 32 near the fiber manufacturing equipment 101, - Washing room 1
7 and a water sump 103 that collects cleaning cooling water containing fibers, binder, and binder components flowing through drains 24 and 25 provided near the bottom of the cyclone separator 18; a pump 104, a vibrating filter 51° with a screen to separate insoluble waste from the wash water; a water tank 52 provided below the filter 51 to collect filtered water; a water tank 52; is circulated by a pump 53 to the compartments 22.
An indirect heat exchanger 105 that is cooled by releasing the heat absorbed by contact with the fume 29 that has passed through the heat exchanger 105, a cooling tower 106 in which cooling water from the heat exchanger 105 is circulated by a pump 107, and a water tank. The water from 52 is recirculated and supplied in the direction of the spray cooling device for the fiber and gas stream 12, in the direction of the condensation and cleaning spray device 45 for the fume 29, and also to the binder preparation device 108 and the water treatment device 109. pump 55
, one water treatment device 109, this treatment device or treatment plant 109
The water is pressurized to an absolute pressure of 16 bar with a pump 77 and heated to approximately 80° C. while passing through a heat exchanger 83. On leaving this heat exchanger 83, the water to be treated enters a mixing device 78 where it is superheated. The treated water exiting the reactor 882 is contacted with steam, such that the temperature is raised to 200° C., and remains in the reactor 82 connected to the mixing device 78 for 2 to 4 minutes. Passes through heat exchanger 83 and temperature 4
00 to 50 degrees Celsius, the pressure reducing valve 86 is opened to reduce the pressure to atmospheric pressure, the water is sent to a centrifuge 110 to separate the binder made insoluble by the treatment from the treated water, and the treated water is placed in a water tank. It is returned to 52.

A water supply pipe 111° for supplying fresh water to the water tank 52 to maintain constant the amount of water in the device - conveyors 57 and 112, which carry waste from the filtration device 51 and the water treatment device 109 and from the production equipment; sending the waste to the waste treatment device 113; - the waste treatment device 113;
This device 113 is equipped with a combustion gas pipe or electrical resistance and heats the waste to approximately 600'-700°C, burns the binder and binder components, burns the fibers into thin plates, and the fired fibers are returned to the fiber manufacturing circuit.

FIG. 12 shows another arrangement of the invention, comprising:

A high velocity hot gas jet 117 is introduced into the molten material, particularly the glass material, from the crucible 114 in the form of a small stream 115, normally perpendicularly as practical, into the solidified filament or rod material before it comes into contact with the pulling roller 116. A fiber manufacturing device is used, so that the ends of the rod-like stream are heated and softened, elongated and fiberized by the jet stream, and the fibers are conveyed in the form of a stream 12 of fibers and gas to a mat or felt-forming belt 15.

- a cooling device with a sprayer 50 for injecting a jet of cooling water into the stream 12; - a binder supply device 13 downstream of the cooling device and injecting binder in the flow direction into the stream 12; - a mat-forming perforated belt 15. device, - perforated belt 15 at the bottom;
Vertical wall 21° in the lateral direction, lid 32 at the top, jet stream 11 at the back
It is located approximately 200111 distance from the outlet of flow 12.
A forming section 22 having a vertical wall 118 with a rectangular opening 33 through which the edges of the rectangular opening 33 are tangential to the flow 12 to facilitate the inflow of the flow 12, the vertical wall 21 forming a mat on the perforated belt 15; A suction chamber 16 located below the mat formation zone of the partially perforated belt 15, which forms the boundary between the mat formation zones; - A jet located below the suction chamber 16 and which opens below the liquid level of the water tank 48 to eject a flow of fume 29; It has a suction chamber 16 having an outlet 47 and a sprayer 45 that sprays cleaning water,
Water overflows into the drain 24 and flows into the collection device 26 in the cleaning chamber 1
7. Cyclone-type water separation device 1 located downstream of the cleaning chamber 17
8. A blower 19 which passes the gaseous body with the fibers through the fiber gathering device and sends the gaseous body to the flue 34, - a vertical blower 19 whose downstream end is located in the forming section 22, one on each side of the fiberizing device; In the upper part of the forming section 22 is a circulation flue 34 which has an opening in the wall 21 and introduces a large amount of circulating fumes, amounting to up to 95% of the amount of gas passing through the belt 15, in the vicinity of the fiber forming device. - a conduit 43 discharging non-circulating fumes to the combustion device 39; - noise absorbing panels 99 and insulating panels 100 arranged on the vertical walls 21, 32, 118 in the area near the fiberizing device;
, contains one fiber, a binder, and a binder component in a dissolved or suspended state, and has a washing chamber 17 and an outlet 2 of the cyclone separation device.
A water reservoir 103 that collects cleaning cooling water from water reservoirs 4 and 25, and a pump 1 that sends water in the water reservoir 103 to the filtration device 51.
04. A vibrating filter 51° with a screen to separate undissolved waste from the wash water - A water tank 52 placed below the filtration device 51 to collect the filtered water; A pump to pump the water in the water tank 52; Cycles in 53, fuyum 29
A heat exchanger 105 for releasing and cooling the heat absorbed during passage through the cleaning chamber 17 and the forming section 22.The apparatus of FIG. Contains material handling equipment or locations.

FIG. 13 shows another arrangement according to the invention, comprising: a.

- The molten material is transferred from the front end hearth 118 of the furnace to the bushing 619.
A fiberizing device in which thread-like material is produced from one or more rows of orifices in an elongated zone and passed between converging high-velocity jets of gas.

The jet injector 120 is placed very close to the glass fibers and the jet is directed downwardly and practically parallel to the direction of flow of the glass fibers.

Usually, the jet stream is high pressure steam, and the fiber to be manufactured,
The elongated jet and the attracted ambient fluid constitute flow 12.

- a cooling spray device 50 for injecting cooling water into stream 12; - a binder spray device 13 for injecting binder into stream 12; U.S. Pat. The remainder of the arrangement of FIG. 13 is similar to that shown in FIG. 11, with the remainder of the arrangement of FIG.

FIG. 14 shows yet another arrangement of the invention, comprising the following:

A fiberizing device in which a stream 121 of molten material is directed around a rotor 122 rotating at high speed with a high velocity jet from an orifice 123.

The centrifugal force of rotor 122 transforms a portion of the material into fibers, and the remaining material is directed to a twentieth rotor 124 and similarly fiberized, although the number of rotors 122, 124 is generally limited to two or three. be done.

Orifice 1 is provided surrounding the rotors 122 and 124.
A high velocity fluid jet is ejected by an annulus having 25;
The produced fibers are directed towards the forming section (receiving device).

These jets are high pressure air or steam.

Orifice 125 is also commonly used to inject binder onto the fibers.

Stream 12 consists of a fiber guiding jet and a fluid drawn from the surroundings.

A spray device 50 for injecting cooling water into the stream 12 is provided downstream of the orifice 125 and the binder is injected into the orifice 125.
It is sprayed through a portion of the water.

The remainder of the arrangement shown in FIG. 14 is similar to that shown in FIG. 12.

[Brief explanation of drawings]

FIG. 1 shows a forming section of a conventional fiber manufacturing apparatus to which the present invention can be applied, and FIG. 2 shows an apparatus similar to that shown in FIG. 1, but with walls forming the forming section. FIG. 3 shows a modified device by adding the device according to the present invention to the device shown in FIGS. 1 and 2, and FIG. 4 shows another device according to the present invention. FIG. 5 shows another embodiment of the fume cleaning device, FIG. 6 shows a curve of insolubilization efficiency versus time and temperature, and FIG. Figure 8 shows a continuous operation equipment for water treatment, Figure 9 shows an example of a solid waste treatment equipment, and Figure 10 shows an example of a solid waste treatment equipment. 11 shows the overall arrangement of the fiber gathering device of the present invention used for manufacturing glass fiber boards, and FIG.
Figure 2 shows another embodiment of the glass fiber manufacturing apparatus, and the 13th
The figures show another embodiment of the invention used in the production of mineral fibers by spraying, and FIG. 14 shows another embodiment used in the production of mineral fibers, in particular from slag. In the figure, 5... Chimney, 11... Fiber manufacturing equipment, 12... Fiber and gas flow, 13...
... Binder supply nozzle, 14 ... Fiber distribution device, 15 ... Perforated belt, 16 ...
Suction chamber, 17... Washing chamber, 18... Separation device, 19... Blower, 21... Vertical wall, 22... Formation Section, 23... Mat, 14, 15... Drain port, 26...
- Collection device, 27... Induced gas flow, 29...
... fuyum, 34... flue, 38...
... Combustion device, 39... Combustion chamber, 40...
... Burner, 42 ... Chimney, 44 ...
Auxiliary blower, 45... Sprayer, 46...
Baffle, 49, 50... (cooling water) injection device,
51... Filtration device, 52... Water tank, 5
3...Pump, 54...Cooling device, 5
5...Pump, 56...Waste, 60
... Combustion device, 61 ... Burner, 65
...Reaction chamber, 68...Reaction chamber, 73.
...Water tank, 78...Mixing device, 82...
... Reactor, 83 ... Heat exchanger, 88.
...Crusher, 90...Incineration device, 94.
...Aquarium, 97...Chimney, 99...
...Noise absorption panel, 100...Insulation panel,
105... Heat exchanger, 106... Cooling tower.

Claims (1)

[Scope of Claims] 1(a) A forming section having a perforated fiber aggregation device in which the attenuating gas and the attenuated fibers flow through which the attenuating gas passes but the fibers are collected to form a mat. (b) spraying water and a resin binder to the flow of gas and fibers in the forming section; (C) recirculating the attenuating gas into the forming section from a downstream side of the perforated fiber concentrator; (d) washing and cooling the recirculating gas stream with water in the flow path of the recirculating gas from the perforated fiber gathering device to the forming section; (e) washing and cooling the recirculating gas stream with water; (f) for cooling the separated water; (g) for spraying the recycled water into the gas and fiber streams in the forming section; A method for the production of fibers by gas-blown attenuation of thermoplastic materials, comprising reusing them for spraying into a stream. (b) a suction chamber; (C) a perforated fiber gathering device separating the suction chamber from the formation zone; (d) (e) a device for spraying water and a resin binder into the stream of attenuating gas and attenuated fibers in the forming section;
An inlet communicating with the suction chamber and a forming section from the suction chamber. (f) a suction fan with an outlet connected to recirculate the attenuation gas to the forming section; (g) a device for separating water from the cooled and washed recycle gas stream; (h) a device for cooling the separated water; (i) a device for cooling the separated water; (i) a device for cooling the separated water; a device for recirculating water into at least one of said atomizing devices; manufacturing equipment.