CA2512993A1 - A method and a plant for producing and treating wood fibres - Google Patents
A method and a plant for producing and treating wood fibres Download PDFInfo
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- CA2512993A1 CA2512993A1 CA002512993A CA2512993A CA2512993A1 CA 2512993 A1 CA2512993 A1 CA 2512993A1 CA 002512993 A CA002512993 A CA 002512993A CA 2512993 A CA2512993 A CA 2512993A CA 2512993 A1 CA2512993 A1 CA 2512993A1
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- scrubber
- chip
- flue gases
- air
- preheater
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- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21B—FIBROUS RAW MATERIALS OR THEIR MECHANICAL TREATMENT
- D21B1/00—Fibrous raw materials or their mechanical treatment
- D21B1/04—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres
- D21B1/12—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres by wet methods, by the use of steam
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- Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Mechanical Engineering (AREA)
- Drying Of Solid Materials (AREA)
- Dry Formation Of Fiberboard And The Like (AREA)
- Treating Waste Gases (AREA)
- Chemical And Physical Treatments For Wood And The Like (AREA)
Abstract
The present invention relates to a plant and a method for producing and treating wood fibres in a plant comprising a fibre-producing part having a chip preheater (1) and a beater (2) for freeing fibre from wood chips. Such a plant and such a method are included as parts in a continuous production process of board and the object is to reduce the emission discharges of foremost VOC and formaldehyde, during different parts of the process as well as from the finished product. The method comprises feeding of wood chips (A) into an upper part of the chip preheater (1), discharge of wood chips in the bottom of the chip preheater to a screw conveyor (12) for further transportation into the beater (2), compression of the wood chips in a compression zone (15) in the screw conveyor, supply of steam (B) into the lower part of the chip preheater for washing fed chips in the counterflow direction, disposal (8) of flue gases in the form of released organic emissions, steam and air in the upper part of the chip preheater, as well as disposal of flue gases generated during the compression through an outlet (13) arranged in the compression zone. The plant has the corresponding parts.
Description
A METHOD AND A PLANT FOR PRODUCING AND TREATING WOOD FIBRES
Technical Field of the Invention The present invention relates to a method for producing and treating wood fi-s byes in a plant comprising a fibre-producing part having a chip preheater and a beater used to free fibre from wood chips, according to the preamble of claim 1, as well as a corresponding plant according to the preamble of claim 9.
Background of the Invention io A continuous production process of board according to the dry and wet method, based on material containing lignocellulose such as wood, straw, bagasse etc., comprises, among other things, a disintegration of the raw material to free fibre or fibre aggregate, which in the subsequent steps is coated with glue, dried, formed and pressed to a finished product, so-called board or wood fibre board. The freeing is of fibre from the raw material is today preferably carried out in a so-called thermo-mechanical process in one step or in a fihermal and mechanical processing step in two separate phases.
The thermal part, heating of the raw material, takes place inter alia in an alka linizing device at a temperature of up to approx. 100 °C, under atmospheric pressure, 2o and then in a pressurized chip preheater at a fiemperature of approx. 150-190 °C un der a pressure of approx. 4-13 bar(e). The dwell time in the preheater may be be-tween 1-10 minutes depending on prevailing process conditions and may be ad-justed. The thermal heating in the chip preheater preferably takes place by means of steam. The mechanical processing takes place in a beater between beater discs 2s where the final fibre freeing takes place in a state where temperature and pressure is higher than in adjacent process stages. The dwell time of the wood chips raw mate-rial in the beater zone is very short. The power that is converted to mechanical en-ergy in connection with the mechanical processing transforms into heat in the beater zone and occurs as steam in the system, generated from the moisture in the raw ma-3o terial.
After the defibering in the beater, the fibre is transported to a pneumatic fibre drier where the drying process is performed by means of a large amount of air and a controlled entering air temperature of approx. 140-200 °C, depending on the current fibre moisture included. The dried fibre is then transported further to forming, pre-pressing and finally to final pressing of the board.
According to older prior art, the wood emissions released during the process, foremost in the chip preheater, are transported all the way from preheater via beater s together with the fibre bulk to the drier, where the majority is separated from the fibre and finally accompanies humid drying air leaving the drier and out into the atmos-phere. These emissions contain, above all, volatile organic substances, so-called VOC (Volatile Organic Compounds), as well as formaldehyde. The remaining amounts, which are not leaving the drier, follows the fibre flow to subsequent process to units where they successively are released to surrounding atmosphere or appear as residual product in the finished product, the board. Thus, also from the finished prod-uct, discharge of emissions to the atmosphere takes place.
From !NO 99/10594 it is, however, previously known to provide the chip pre heater with a top outlet for degassing of organic emissions released there.
Here, the is steam is introduced in the lower part of the preheater and the wood chips, which en ter the upper part of the preheater, are washed in the counterflowing steam during condensation. This is achieved by means of the steam moving upwards through the wood chips column towards the colder wood chips in the top of the preheater, and re-leased emissions, air and steam being generated by evaporation of the moisture in 2o the wood chips are separated and disposed of through the outlet into a scrubber. Sy this publication, it is also known to transport the wood chips from the preheater into the beater by means of a screw conveyor, which also compresses and dewaters the wood chips during the transportation.
2s Summary ~t'the Inventi~n The object of the present invention is to provide a method and a plant that re-duce the emission discharges, foremost of VOC and formaldehyde, to the atmosphere, from the production process as well as from the finished product, the boards.
Simulta-neously, the capacity in the production plant should be maintained and so also the 3o quality of the final product.
This object is attained by a method having the new features that are defined in the characterizing clause of claim 1, as well as by a plant having the new features that are defined in the characterizing clause of claim 9.
Technical Field of the Invention The present invention relates to a method for producing and treating wood fi-s byes in a plant comprising a fibre-producing part having a chip preheater and a beater used to free fibre from wood chips, according to the preamble of claim 1, as well as a corresponding plant according to the preamble of claim 9.
Background of the Invention io A continuous production process of board according to the dry and wet method, based on material containing lignocellulose such as wood, straw, bagasse etc., comprises, among other things, a disintegration of the raw material to free fibre or fibre aggregate, which in the subsequent steps is coated with glue, dried, formed and pressed to a finished product, so-called board or wood fibre board. The freeing is of fibre from the raw material is today preferably carried out in a so-called thermo-mechanical process in one step or in a fihermal and mechanical processing step in two separate phases.
The thermal part, heating of the raw material, takes place inter alia in an alka linizing device at a temperature of up to approx. 100 °C, under atmospheric pressure, 2o and then in a pressurized chip preheater at a fiemperature of approx. 150-190 °C un der a pressure of approx. 4-13 bar(e). The dwell time in the preheater may be be-tween 1-10 minutes depending on prevailing process conditions and may be ad-justed. The thermal heating in the chip preheater preferably takes place by means of steam. The mechanical processing takes place in a beater between beater discs 2s where the final fibre freeing takes place in a state where temperature and pressure is higher than in adjacent process stages. The dwell time of the wood chips raw mate-rial in the beater zone is very short. The power that is converted to mechanical en-ergy in connection with the mechanical processing transforms into heat in the beater zone and occurs as steam in the system, generated from the moisture in the raw ma-3o terial.
After the defibering in the beater, the fibre is transported to a pneumatic fibre drier where the drying process is performed by means of a large amount of air and a controlled entering air temperature of approx. 140-200 °C, depending on the current fibre moisture included. The dried fibre is then transported further to forming, pre-pressing and finally to final pressing of the board.
According to older prior art, the wood emissions released during the process, foremost in the chip preheater, are transported all the way from preheater via beater s together with the fibre bulk to the drier, where the majority is separated from the fibre and finally accompanies humid drying air leaving the drier and out into the atmos-phere. These emissions contain, above all, volatile organic substances, so-called VOC (Volatile Organic Compounds), as well as formaldehyde. The remaining amounts, which are not leaving the drier, follows the fibre flow to subsequent process to units where they successively are released to surrounding atmosphere or appear as residual product in the finished product, the board. Thus, also from the finished prod-uct, discharge of emissions to the atmosphere takes place.
From !NO 99/10594 it is, however, previously known to provide the chip pre heater with a top outlet for degassing of organic emissions released there.
Here, the is steam is introduced in the lower part of the preheater and the wood chips, which en ter the upper part of the preheater, are washed in the counterflowing steam during condensation. This is achieved by means of the steam moving upwards through the wood chips column towards the colder wood chips in the top of the preheater, and re-leased emissions, air and steam being generated by evaporation of the moisture in 2o the wood chips are separated and disposed of through the outlet into a scrubber. Sy this publication, it is also known to transport the wood chips from the preheater into the beater by means of a screw conveyor, which also compresses and dewaters the wood chips during the transportation.
2s Summary ~t'the Inventi~n The object of the present invention is to provide a method and a plant that re-duce the emission discharges, foremost of VOC and formaldehyde, to the atmosphere, from the production process as well as from the finished product, the boards.
Simulta-neously, the capacity in the production plant should be maintained and so also the 3o quality of the final product.
This object is attained by a method having the new features that are defined in the characterizing clause of claim 1, as well as by a plant having the new features that are defined in the characterizing clause of claim 9.
Thus, the method according to the present invention is characterized in that flue gases generated during the compression are disposed of through an outlet ar-ranged in the compression zone. The plant according to the present invention is characterized in that in the compression zone a flue gas outlet is arranged for dis-c posal of evaporated moisture, which is generated upon the compression of the wood chips and which contains flue gases.
In the compression of the wood chips in the screw conveyor, water is pressed out, which contains a great deal of remaining wood emissions. By providing an outlet in the compression zone, the water can evaporate and the released emis-sions can be discharged through the outlet. By catching and diverting the emissions that are released in the compression zone directly and on the spot, a considerably higher concentration of the emissions is obtained than if they instead had to be transported further with the fibre bulk and be mixed with the drying air, which repre-sents a very large flow of gas, and thereby provides low concentration, according to is prior art. Thus, a considerably more efficient handling of the flue gases from the pre-heating is obtained by means of the present invention.
According to one embodiment, the disposal of the flue gases that are gener-ated during the compression is achieved by conveying them back to the upper part of the chip preheater from which they then are disposed of together with other flue 2o gases. The flue gases may advantageously be conveyed to destruction, e.g., to in-cineration in a boiler, where the emissions transform to carbon dioxide and water.
According to another advantageous feature, upon the disposal of flue gases, the flow of flue gases can be controlled, and in this way, also the steam losses in the chip preheater can be controlled.
2s According to a further embodiment, a so-called catcher agent may be added to the wood chips upon the feeding thereof into the beater. A catcher agent is a chemical that is injected in order to bind some substance, in this case formaldehyde.
It is previously known to add catcher agents in other places in the process.
However, it is not previously known to add a catcher agent directly into the beater and at tests it 3o has turned out that this is particularly efficient as for binding formaldehyde. Test re-sults with a catcher agent added into the beater have demonstrated a reduction of formaldehyde content by 8-15 % and also a clear improvement of perforator values in the final board.
In the compression of the wood chips in the screw conveyor, water is pressed out, which contains a great deal of remaining wood emissions. By providing an outlet in the compression zone, the water can evaporate and the released emis-sions can be discharged through the outlet. By catching and diverting the emissions that are released in the compression zone directly and on the spot, a considerably higher concentration of the emissions is obtained than if they instead had to be transported further with the fibre bulk and be mixed with the drying air, which repre-sents a very large flow of gas, and thereby provides low concentration, according to is prior art. Thus, a considerably more efficient handling of the flue gases from the pre-heating is obtained by means of the present invention.
According to one embodiment, the disposal of the flue gases that are gener-ated during the compression is achieved by conveying them back to the upper part of the chip preheater from which they then are disposed of together with other flue 2o gases. The flue gases may advantageously be conveyed to destruction, e.g., to in-cineration in a boiler, where the emissions transform to carbon dioxide and water.
According to another advantageous feature, upon the disposal of flue gases, the flow of flue gases can be controlled, and in this way, also the steam losses in the chip preheater can be controlled.
2s According to a further embodiment, a so-called catcher agent may be added to the wood chips upon the feeding thereof into the beater. A catcher agent is a chemical that is injected in order to bind some substance, in this case formaldehyde.
It is previously known to add catcher agents in other places in the process.
However, it is not previously known to add a catcher agent directly into the beater and at tests it 3o has turned out that this is particularly efficient as for binding formaldehyde. Test re-sults with a catcher agent added into the beater have demonstrated a reduction of formaldehyde content by 8-15 % and also a clear improvement of perforator values in the final board.
According to a further embodiment, the wood fibres produced and treated in the beater are sent to a drier part and then to a scrubber, and air leaving the drier part, on the way to the scrubber, is conveyed through a heat exchanger for air enter-ing the drier part so that the air to the drier part is heated and the air to the scrubber s is cooled. Thereby, the advantage is gained of a certain heat recovery taking place for the air to the drier. Another important advantage is, however, that the air to the scrubber is cooled. Since the condensable hydrocarbons in the emissions originating from the previous stages in the process tend to be aerosols, this makes the purifica-tion effect of the scrubber more difficult. The equilibrium relationship between air and io water solution of said hydrocarbons is temperature dependent so that at higher tem-perature in the scrubber, it is difficult to bring the emissions into water phase. For this reason, it is advantageous to cool the air entering the scrubber.
Furthermore, water drops may advantageously be separated in the scrubber by a demister device. Additional cooling by supply of water is also possible.
is Thus, by means of the present invention, reduced discharges ofi foremost V~C and formaldehyde are obtained during the entire production process of board.
This results in important environmental improvements, both internally at the produc-tion line and externally, i.e., in the environment outside the plant.
Furthermore, the advantage is obtained of an improved final product in the form of a board that causes 20 less discharge in the environment where it is used.
Brief Description of tMe Drawings The invention will now be described in more detail in the form of embodiment examples and reference being made to the appended drawings, in which:
2s Figure 1 shows schematically a plant for production and treatment of wood fi-bras, comprising an embodiment example according to the present in-vention, Figure 2 shows an embodiment example of a first part of the plant according to the present invention, and 3o Figure 3 shows an embodiment example of a second part of the plant according to the present invention.
Detailed Description of the Invention The plant for producing and treating wood fibres, illustrated schematically in fig. 1, is included in the illustrated example as a part of a continuous process for pro-ducing board of material containing lignocellulose.
s Such a plant comprises a plurality of stages. The stages that are illustrated schematically in fig. 1 includes a first stage having a fibre-producing part comprising a chip preheater 1 and a beater 2 for freeing fibres of wood chips, a second stage having a drier part 3 comprising, for instance, a cyclone, and a third stage in connec-tion with the drier part and comprising a scrubber 4, foremost intended for efficient io particle separation in connection with the drying. It should be particularly mentioned that the drier part in itself may comprise a plurality of drying steps having a plurality of similar apparatuses and the plant may moreover also comprise additional intermedi-ate steps and details that have not been shown for reasons of clarity.
The fibre-producing part of the plant in fig. 1 is shown on a somewhat larger m scale in fig. ~. Via an inlet 6, wood chips A are fed into the preheater 1, usually from an alltalini~ing bin, which is not shown. In the lower part of the chip preheater, steam B is supplied via steam inlets 7. The chip preheater is also provided with a top outlet ~. In the chip preheater, the wood chips are heated by means of condensing heat from the steam, which is supplied at pressure, temperature and time having been 2o pre-set and adapted to the wood chips raw material. By the fact that the steam B is supplied into the lower part of the chip preheater, it will move up through the wood chips column C towards the colder entering wood chips in the top, and in this way the moisture in the wood chips is evaporated and forms steam containing released or-ganic emissions from the wood. Said emissions, foremost organic volatile substances as such as V~C and formaldehyde, are then separated at a high concentration in the top of the preheater via the top outlet 5. fVext, from the top outlet, the flue gases travel to some kind of destruction device, which is not shown. The destruction may, for instance, be effected by incineration or by evaporation.
As is seen in fig. 2, the flue gas line in the top of the preheater is provided 3o with temperature control device, TIC, and the supply line for steam is provided with a pressure control device, PIC. By setting a value of the pressure of the steam that cor-responds to a certain temperature, e.g., of the order of 170 °C, it is possible, by measuring the temperature of the leaving flue gases, to control these so that unnec-essary steam and energy losses are prevented. Thus, the temperature of the flue gases should not exceed the temperature of the entering steam. If this would take place, the flow of flue gases is automatically reduced, in order to thereby prevent that more steam is supplied than what can be utilized in the chip preheater.
In this connection! it may also be mentioned that the degassing in the top of s the preheater has a favourable impact on the heat transfer between the steam and the wood chips in the preheater. Normally, the air that is contained in the supplied cold wood chips A reduces said heat transfer, but by means of the present invention this air may instead be directly disposed of through the top outlet 8.
In the bottom of the chip preheater, there is a chip outlet 11. In connection with the same, there is a screw conveyor 12 arranged, which feeds the wood chips to the beater 2. The screw conveyor comprises a compression zone 15 where the water is pressed out of fibs chip mass and the formed moisture evaporates in the zone so that steam is generated. The compression zone 15 is formed by the shaft, of thafi part of the screw conveyor 12 fihat is closest to the beater 2, having an increasing diame-is ter, so that it obtains a conical shape. This results in the chip material in said part be-ing compressed and pushed out against the outer walls of the screw conveyor 12 where a so-called plug flow is formed, which partly plugs up the entrance to the beater. The formed plug separates the beater from the screw conveyor so that steam from the beater cannot travel rearwards into the compression zone. According to the 2o preferred embodiment, a flue gas outlet 13 is arranged in the compression zone so that it is possible to dispose of said evaporated moisture, which contains flue gases.
Furthermore, according to the preferred embodiment, said flue gas outlet is con-netted to a line 14 that conveys the flue gases back to the upper part of the chip pre-heater 1. Here, they can then be disposed of together with other flue gases via the 2s top outlet 8 and further away for destruction.
In the illustrated example, is also shown how a catcher agent D can be added into the beater 2. A catcher agent is a chemical, which is injected in order to bind some substance, in this case formaldehyde. The member 16 for addition of a catcher agent may, for instance, be formed so that the supply of the catcher agent D
3o takes place via the centre of the screw conveyor 12 into the beater 2. A
suitable catcher agent in this case may be urea or the like.
In fig. 3, an embodiment example is shown of a scrubber plant 4 according to the present invention, which is used in connection with a drier stage. Said scrubber plant may advantageously be used together with the above-described chip preheater 1 and the beater 2, but may also be used together with other types of chip preheaters and beaters and also in other types of plants, and may thus be regarded as an inven-tion in itself. In fig. 3, a scrubber 4 is shown that receives air E that travels from the drier part 3, via a line 28. Before the same air is allowed to pass into the scrubber, it s passes a heat exchanger device 20, for instance, a tube heat exchanger, for the air F
entering the drier. In this way, the heat that the air E leaving the drier contains is util-ized in order to preheat the air F, G entering the drier, at the same time as the air leaving the drier is cooled down before it enters the scrubber 4. The equilibrium rela-tionship between air temperature and the concentration of formaldehyde will conse-quently be altered and promotes the transfer of formaldehyde into water phase.
The air E leaving the drier may have a temperature of the order of +60 °C, the drying air F
entering the heat exchanger is as a rule taken from outside and may then have a temperature of +10 °C, and the preheated air G entering the drier may then have a temperature of +30 °G.
is The scrubber is also provided with a number of water sprayers 21, which ac-cordingly spray out water that cools and absorbs the emissions that are in the drying air into water phase. Vl/ater sprayers 22 may advantageously also be positioned in the inlet line 25 to the scrubber. In the lower part of the scrubber, there is a water out-let 23, where water is drawn off in order to be conveyed to purification. In the top of 2o the scrubber, there is an outlet 24 for leaving air. The scrubber is suitably also pro-vided with a so-called demister or droplet separator 25 in connection with the upper air outlet, in order to separate water drops.
The supplied spray water may possibly be chemically treated with NaHS~3 and NaOH in order to optimise the function of the emission reduction. Thus, the 2s scrubber 4 is provided with a device 27 for supply of said additives to the water. Test results have shown that in this way, a 75 °/~ reduction of the formaldehyde content in the leaving air is achieved, already without connection of a heat exchanger.
The present invention should not be regarded as limited to the above-described embodiment examples, but may be modified and varied in a multiple of 3o ways, as is realized by a person skilled in the art, within the scope of the accompa-nying claims.
Furthermore, water drops may advantageously be separated in the scrubber by a demister device. Additional cooling by supply of water is also possible.
is Thus, by means of the present invention, reduced discharges ofi foremost V~C and formaldehyde are obtained during the entire production process of board.
This results in important environmental improvements, both internally at the produc-tion line and externally, i.e., in the environment outside the plant.
Furthermore, the advantage is obtained of an improved final product in the form of a board that causes 20 less discharge in the environment where it is used.
Brief Description of tMe Drawings The invention will now be described in more detail in the form of embodiment examples and reference being made to the appended drawings, in which:
2s Figure 1 shows schematically a plant for production and treatment of wood fi-bras, comprising an embodiment example according to the present in-vention, Figure 2 shows an embodiment example of a first part of the plant according to the present invention, and 3o Figure 3 shows an embodiment example of a second part of the plant according to the present invention.
Detailed Description of the Invention The plant for producing and treating wood fibres, illustrated schematically in fig. 1, is included in the illustrated example as a part of a continuous process for pro-ducing board of material containing lignocellulose.
s Such a plant comprises a plurality of stages. The stages that are illustrated schematically in fig. 1 includes a first stage having a fibre-producing part comprising a chip preheater 1 and a beater 2 for freeing fibres of wood chips, a second stage having a drier part 3 comprising, for instance, a cyclone, and a third stage in connec-tion with the drier part and comprising a scrubber 4, foremost intended for efficient io particle separation in connection with the drying. It should be particularly mentioned that the drier part in itself may comprise a plurality of drying steps having a plurality of similar apparatuses and the plant may moreover also comprise additional intermedi-ate steps and details that have not been shown for reasons of clarity.
The fibre-producing part of the plant in fig. 1 is shown on a somewhat larger m scale in fig. ~. Via an inlet 6, wood chips A are fed into the preheater 1, usually from an alltalini~ing bin, which is not shown. In the lower part of the chip preheater, steam B is supplied via steam inlets 7. The chip preheater is also provided with a top outlet ~. In the chip preheater, the wood chips are heated by means of condensing heat from the steam, which is supplied at pressure, temperature and time having been 2o pre-set and adapted to the wood chips raw material. By the fact that the steam B is supplied into the lower part of the chip preheater, it will move up through the wood chips column C towards the colder entering wood chips in the top, and in this way the moisture in the wood chips is evaporated and forms steam containing released or-ganic emissions from the wood. Said emissions, foremost organic volatile substances as such as V~C and formaldehyde, are then separated at a high concentration in the top of the preheater via the top outlet 5. fVext, from the top outlet, the flue gases travel to some kind of destruction device, which is not shown. The destruction may, for instance, be effected by incineration or by evaporation.
As is seen in fig. 2, the flue gas line in the top of the preheater is provided 3o with temperature control device, TIC, and the supply line for steam is provided with a pressure control device, PIC. By setting a value of the pressure of the steam that cor-responds to a certain temperature, e.g., of the order of 170 °C, it is possible, by measuring the temperature of the leaving flue gases, to control these so that unnec-essary steam and energy losses are prevented. Thus, the temperature of the flue gases should not exceed the temperature of the entering steam. If this would take place, the flow of flue gases is automatically reduced, in order to thereby prevent that more steam is supplied than what can be utilized in the chip preheater.
In this connection! it may also be mentioned that the degassing in the top of s the preheater has a favourable impact on the heat transfer between the steam and the wood chips in the preheater. Normally, the air that is contained in the supplied cold wood chips A reduces said heat transfer, but by means of the present invention this air may instead be directly disposed of through the top outlet 8.
In the bottom of the chip preheater, there is a chip outlet 11. In connection with the same, there is a screw conveyor 12 arranged, which feeds the wood chips to the beater 2. The screw conveyor comprises a compression zone 15 where the water is pressed out of fibs chip mass and the formed moisture evaporates in the zone so that steam is generated. The compression zone 15 is formed by the shaft, of thafi part of the screw conveyor 12 fihat is closest to the beater 2, having an increasing diame-is ter, so that it obtains a conical shape. This results in the chip material in said part be-ing compressed and pushed out against the outer walls of the screw conveyor 12 where a so-called plug flow is formed, which partly plugs up the entrance to the beater. The formed plug separates the beater from the screw conveyor so that steam from the beater cannot travel rearwards into the compression zone. According to the 2o preferred embodiment, a flue gas outlet 13 is arranged in the compression zone so that it is possible to dispose of said evaporated moisture, which contains flue gases.
Furthermore, according to the preferred embodiment, said flue gas outlet is con-netted to a line 14 that conveys the flue gases back to the upper part of the chip pre-heater 1. Here, they can then be disposed of together with other flue gases via the 2s top outlet 8 and further away for destruction.
In the illustrated example, is also shown how a catcher agent D can be added into the beater 2. A catcher agent is a chemical, which is injected in order to bind some substance, in this case formaldehyde. The member 16 for addition of a catcher agent may, for instance, be formed so that the supply of the catcher agent D
3o takes place via the centre of the screw conveyor 12 into the beater 2. A
suitable catcher agent in this case may be urea or the like.
In fig. 3, an embodiment example is shown of a scrubber plant 4 according to the present invention, which is used in connection with a drier stage. Said scrubber plant may advantageously be used together with the above-described chip preheater 1 and the beater 2, but may also be used together with other types of chip preheaters and beaters and also in other types of plants, and may thus be regarded as an inven-tion in itself. In fig. 3, a scrubber 4 is shown that receives air E that travels from the drier part 3, via a line 28. Before the same air is allowed to pass into the scrubber, it s passes a heat exchanger device 20, for instance, a tube heat exchanger, for the air F
entering the drier. In this way, the heat that the air E leaving the drier contains is util-ized in order to preheat the air F, G entering the drier, at the same time as the air leaving the drier is cooled down before it enters the scrubber 4. The equilibrium rela-tionship between air temperature and the concentration of formaldehyde will conse-quently be altered and promotes the transfer of formaldehyde into water phase.
The air E leaving the drier may have a temperature of the order of +60 °C, the drying air F
entering the heat exchanger is as a rule taken from outside and may then have a temperature of +10 °C, and the preheated air G entering the drier may then have a temperature of +30 °G.
is The scrubber is also provided with a number of water sprayers 21, which ac-cordingly spray out water that cools and absorbs the emissions that are in the drying air into water phase. Vl/ater sprayers 22 may advantageously also be positioned in the inlet line 25 to the scrubber. In the lower part of the scrubber, there is a water out-let 23, where water is drawn off in order to be conveyed to purification. In the top of 2o the scrubber, there is an outlet 24 for leaving air. The scrubber is suitably also pro-vided with a so-called demister or droplet separator 25 in connection with the upper air outlet, in order to separate water drops.
The supplied spray water may possibly be chemically treated with NaHS~3 and NaOH in order to optimise the function of the emission reduction. Thus, the 2s scrubber 4 is provided with a device 27 for supply of said additives to the water. Test results have shown that in this way, a 75 °/~ reduction of the formaldehyde content in the leaving air is achieved, already without connection of a heat exchanger.
The present invention should not be regarded as limited to the above-described embodiment examples, but may be modified and varied in a multiple of 3o ways, as is realized by a person skilled in the art, within the scope of the accompa-nying claims.
Claims (19)
1. A method for producing and treating wood fibres in a plant comprising a fibre-pro-ducing part having a chip preheater and a beater for freeing fibre from wood chips, comprising the following steps:
- feeding wood chips into an upper part of the chip preheater, - discharging wood chips in the bottom of the chip preheater to a screw con-veyor for further transport to the beater, - compression of the wood chips in a compression zone in the screw con-veyor, - supply of steam into the lower part of the chip preheater for washing fed wood chips in the counterflow direction, - disposal of flue gases in the form of released organic emissions, steam and air in the upper part of the chip preheater, characterized in that flue gases generated during the compression are disposed of through an outlet arranged in the compression zone.
- feeding wood chips into an upper part of the chip preheater, - discharging wood chips in the bottom of the chip preheater to a screw con-veyor for further transport to the beater, - compression of the wood chips in a compression zone in the screw con-veyor, - supply of steam into the lower part of the chip preheater for washing fed wood chips in the counterflow direction, - disposal of flue gases in the form of released organic emissions, steam and air in the upper part of the chip preheater, characterized in that flue gases generated during the compression are disposed of through an outlet arranged in the compression zone.
2.~A method according to claim 1, characterized in that the disposal of the flue gases generated during the compression is achieved by conveying them back to the upper part of the chip preheater from which they then are disposed of together with other flue gases.
3. A method according to claim 1 or claim 2, characterized in that the flue gases disposed of are conveyed to a destruction device where they are destructed.
4. A method according to any one of the preceding claims, characterized in that the steam losses from the chip preheater are controlled by means of measuring the tem-perature of the flue gases disposed of from the upper part of the chip preheater, measuring and controlling the pressure of the entering steam, comparison of the same values and controlling the flow of flue gases from the top outlet based on the same comparison.
5. A method according to any one of the preceding claims, characterized in that a catcher agent is added to the wood chips upon their feeding into the beater.
6. A method according to any one of the preceding claims, characterized in that the wood fibres produced and treated in the beater are sent to a drier part and then to a scrubber, air leaving the drier part being cooled before it is treated in the scrubber.
7. A method according to claim 6, characterized in that the air leaving the drier part for the scrubber passes a heat exchanger for air entering the drier part so that the air conveyed to the drier part is heated and the air conveyed to the scrubber is cooled.
8. A method according to claim 6 or 7, characterized in that water drops are sepa-rated in the scrubber by means of a demister device arranged at the air outlet of the scrubber.
9. A plant for producing and treating wood fibres, comprising a fibre-producing part having a chip preheater and a beater for freeing fibre from wood chips, the chip pre-heater being provided with a chip inlet in the upper part thereof and a chip outlet in the lower part thereof, and further with a steam inlet in the lower part thereof and a top outlet for generated flue gases in the form of released organic emissions, steam and air, so that ships fed into the preheater through said chip inlet are washed in the counterflow direction by means of steam supplied through said steam inlet, and the chip outlet being in connection with the beater via a screw conveyor that comprises a compression zone, characterized in that a flue gas outlet is arranged in the com-pression zone for disposal of evaporated moisture that is generated upon the com-pression of the wood chips and that contains flue gases.
10. A plant according to claim 9, characterized in that said flue gas outlet in the compression zone is connected to a connection line arranged between the compres-sion zone and the upper part of the chip preheater.
11. A plant according to claim 9 or claim 10, characterized in that it comprises a de-struction arrangement to which the generated flue gases are sent and destructed.
12. A plant according to any one of claims 9-11, characterized in that it comprises a temperature control device that measures the temperature of the flue gases disposed of, during prevailing partial mixing volume and partial pressure for the gases con-tained in the chip preheater, and a pressure control device which measures and con-trols the pressure of the entering steam, and by comparison of said values the steam losses in the chip preheater are controlled by means of control of the flow of flue gases from the top outlet.
13. A plant according to any one of claims 9-12, characterized in that it comprises a device for addition of a catcher agent to the wood chips upon the feeding thereof into the beater.
14. A plant according to any one of claims 9-13, characterized in that it comprises a drier part to which the wood fibres produced and treated in the beater are brought, a scrubber located after the drier part and lines that convey air leaving the drier part into the scrubber, as well as a cooling device in order to cool the air entering the scrubber from the drier part.
15. A plant according to claim 14, characterized in that the cooling device comprises a heat exchanger for air entering the drier part and that said lines that convey air leaving the drier part into the scrubber, convey the leaving air through said heat ex-changer so that the air entering the drier part is heated and the air that is conveyed to the scrubber is cooled.
16. A plant according to any one of claims 14-15, characterized in that the scrubber comprises means for supply of water that cools and absorbs existing flue gases into water phase.
17. A plant according to any one of claims 14-16, characterized in that means are arranged in the lines between the drier part and the scrubber for supply of water that cools and absorbs existing flue gases into water phase.
18. A plant according to claim 16 or claim 17, characterized in that it comprises at least one device for supply of additives for chemical treatment of the supplied water.
19. A plant according to any one of claims 14-18, characterized in that the scrubber comprises a device for separation of water drops.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| SE0300385-2 | 2003-02-11 | ||
| SE0300385A SE524788C2 (en) | 2003-02-11 | 2003-02-11 | Method and apparatus for producing and treating wood fibers |
| PCT/SE2004/000180 WO2004072362A1 (en) | 2003-02-11 | 2004-02-11 | A method and a plant for producing and treating wood fibres |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2512993A1 true CA2512993A1 (en) | 2004-08-26 |
Family
ID=20290392
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002512993A Abandoned CA2512993A1 (en) | 2003-02-11 | 2004-02-11 | A method and a plant for producing and treating wood fibres |
Country Status (8)
| Country | Link |
|---|---|
| US (1) | US20060151133A1 (en) |
| EP (1) | EP1597427A1 (en) |
| CN (1) | CN1748057A (en) |
| BR (1) | BRPI0407339A (en) |
| CA (1) | CA2512993A1 (en) |
| RU (1) | RU2345186C2 (en) |
| SE (1) | SE524788C2 (en) |
| WO (1) | WO2004072362A1 (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SE528116C2 (en) * | 2005-12-02 | 2006-09-05 | Kvaerner Pulping Tech | Wood chip steaming system for chemical pulp production, has chip bin dilution pipe extending between atmosphere and valve regulated by sensor for measuring process parameter |
| PT3872256T (en) * | 2020-02-28 | 2022-03-25 | Fiberboard Gmbh | Method for reducing volatile organic compounds from wood chips |
| EP4122662B1 (en) | 2021-07-23 | 2024-02-28 | Fiberboard GmbH | Method for producing fibreboard with reduced voc emissions |
Family Cites Families (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4037792A (en) | 1972-10-23 | 1977-07-26 | Sca Development Aktiebolag | Continuously refining raw fibrous material to produce mechanical refiner pulp |
| US4059237A (en) | 1974-02-15 | 1977-11-22 | Oy Keskuslaboratorio - Centrallaboratorium, Ab | System for feeding a double disc refiner |
| SE403916B (en) * | 1975-06-04 | 1978-09-11 | Rolf Bertil Reinhall | DEVICE FOR MILLING APPARATUS FOR LIGNOCELLULOSE-MATERIAL |
| SE413784B (en) * | 1976-08-06 | 1980-06-23 | Isel Sa | SET AND DEVICE TO USE IN DEFIBRATION ZONE DEVELOPED HEAT TO MINIMIZE CONSUMPTION WHEN PREPARING MASS FOR FIBER DISC |
| SE413522B (en) | 1977-01-03 | 1980-06-02 | Reinhall Rolf Bertil | DEVICE FOR THE PREPARATION OF FIBER MASS OF LIGNOCELLULOSALLY MATERIAL |
| US4129166A (en) | 1977-07-18 | 1978-12-12 | General Electric Company | Nb3 Ge superconductive films grown with air |
| SE422089B (en) | 1978-05-03 | 1982-02-15 | Defibrator Ab | SET AND DEVICE FOR MANUFACTURING FIBER MASS OF LIGNOCELLULOSALLY MATERIAL |
| FI62687C (en) * | 1978-05-26 | 1983-02-10 | Enso Gutzeit Oy | SKIVRAFFINOER |
| FI62149C (en) * | 1979-01-12 | 1984-03-20 | Yhtyneet Paperitehtaat Oy | FOERFARANDE FOER FRAMSTAELLNING AV VARMSLIPMASSA |
| US4555254A (en) * | 1982-11-30 | 1985-11-26 | Koppers Company, Inc. | Material collector and discharger apparatus |
| SE461962B (en) * | 1987-12-16 | 1990-04-23 | Sunds Defibrator Ind Ab | SET AND DEVICE FOR MANUFACTURING FIBER BOARD DISKS |
| FI106223B (en) * | 1996-06-07 | 2000-12-15 | Valmet Corp | Heat exchanger |
| SE521593C2 (en) * | 1997-08-25 | 2003-11-18 | Valmet Fibertech Ab | Plant for the production and treatment of wood fibers |
-
2003
- 2003-02-11 SE SE0300385A patent/SE524788C2/en not_active IP Right Cessation
-
2004
- 2004-02-11 CN CNA2004800037195A patent/CN1748057A/en active Pending
- 2004-02-11 EP EP04710138A patent/EP1597427A1/en not_active Withdrawn
- 2004-02-11 US US10/544,699 patent/US20060151133A1/en not_active Abandoned
- 2004-02-11 BR BR0407339-8A patent/BRPI0407339A/en not_active IP Right Cessation
- 2004-02-11 CA CA002512993A patent/CA2512993A1/en not_active Abandoned
- 2004-02-11 WO PCT/SE2004/000180 patent/WO2004072362A1/en active Application Filing
- 2004-02-11 RU RU2005128278/11A patent/RU2345186C2/en not_active IP Right Cessation
Also Published As
| Publication number | Publication date |
|---|---|
| CN1748057A (en) | 2006-03-15 |
| RU2345186C2 (en) | 2009-01-27 |
| RU2005128278A (en) | 2006-01-27 |
| US20060151133A1 (en) | 2006-07-13 |
| WO2004072362A1 (en) | 2004-08-26 |
| SE0300385D0 (en) | 2003-02-11 |
| SE524788C2 (en) | 2004-10-05 |
| EP1597427A1 (en) | 2005-11-23 |
| SE0300385L (en) | 2004-08-12 |
| BRPI0407339A (en) | 2006-01-10 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EEER | Examination request | ||
| FZDE | Discontinued |