KR20070120578A - Wet raw material drier and method of drying - Google Patents

Abstract

A wet raw material drier comprising fluidized-bed drier (8) for drying a wet raw material, gas supply piping (5) for supplying coke oven emission gas as not only a heat source but also a fluidizing gas to the fluidized-bed drier (8) and dust collector (11) for recovering dust-size particles discharged together with gas from the fluidized-bed drier (8), wherein there is provided binder adding unit (18) equipped with means capable of automatic or manual regulation so that the amount of binder added is a constant ratio to dust-size particles with respect to dust-size particles whose recovery rate by the dust collector (11) is varied in accordance with fluctuations of the drying level of wet raw material caused by fluctuations of the flow rate or temperature of supplied coke oven emission gas. A binder is added by the use of the binder adding unit (18). Thus, even if the amount of dust-size particles discharged together with gas from the fluidized-bed drier (8) and recovered is increased or decreased, any dust dispersal and carbon adhesion onto coke oven wall can be securely prevented.

Description

Drying Apparatus and Method of Drying the Wet Raw Material {WET RAW MATERIAL DRIER AND METHOD OF DRYING}

The present invention relates to a wet raw material drying apparatus and a drying method for drying wet raw materials such as coal charged into a coke oven with a fluid bed dryer.

In the production of coke, drying of the charged coal before charging the coke furnace is performed for the purpose of improving the quality of the coke and improving the productivity in the coke oven. The moisture content of the coke oven coal is usually about 9 to 13% before drying, but the coal is dried in a coal dryer at 5 to 6% moisture. In general, it is known that as the moisture in coal decreases, the amount of fine particles separated from coal increases.

It is conventionally known to use a fluidized bed dryer for drying this coal, and patent document 1 discloses the method of drying coal by introducing the flue exhaust gas of a coke oven as a heat source and fluidizing gas to a fluidized bed dryer. Most of the coal powder charged into the fluidized bed drier is discharged from the discharge chute communicating with the fluidized bed and returned to the coke oven. Further, fine powder is generated by drying the coal powder, which is discharged together with the exhaust gas from the exhaust gas outlet above the fluidized bed, and recovered by a dust collector provided in the exhaust gas pipe.

Here, the exhaust gas temperature to the coke oven used as a heat source and fluidizing gas of a fluidized bed dryer changes with the operation load situation, fuel property, and a combustion control situation to a coke oven. For example, when the production of coke oven is temporarily reduced, there may be a case where the exhaust gas which has become significantly hotter than the temperature condition at the time of dryer design flows in. As a result, the amount of fines generated from the coal is increased by drying the water in the coal more than necessary at the time of design, and the amount of fines recovered by the dust collector is also increased. In addition, when the calorific value of coke oven fuel is temporarily reduced, there may be a case where the exhaust gas which is significantly lower than the temperature condition at the time of dryer design flows in. As a result, the amount of fine powder generated from coal is reduced, and the amount of fine powder recovered by the dust collector is also reduced. Thus, when the exhaust gas to a coke oven is used as a heat source and fluidizing gas of a fluidized bed dryer, there exists a possibility that the temperature of gas may fluctuate. As a result, the amount of fines generated from coal varies with the change in the degree of drying of the wet raw material in the fluidized bed dryer, and the amount of fines recovered and discharged by the dust collector also varies.

In addition, as a coke, each combustion furnace system has two system | combustion gas systems normally, and when the use time in one system reaches a predetermined time, it switches to another system. Switching of the strain is usually performed once every 15 to 30 minutes. At the time of switching of a combustion gas system, as shown in FIG. 4, the flow rate of the combustion gas of the system (system A) used so far is reduced one by one, and when the flow volume becomes zero, the system (system B) of the next use will be reduced. The combustion gas flow rate is increased in turn. Therefore, at the time of switching of a combustion gas system, the amount of exhaust gas to a coke oven decreases, becomes zero, and increases again. The time for the fluctuation of the gas flow rate to accompany the switching of the combustion gas system is generally 0.5 to 3 minutes.

In this way, when the exhaust gas to the coke oven is used as the heat source and the fluidizing gas of the fluidized bed dryer, the amount of the exhaust gas to the coke furnace is reduced at the time of switching the combustion gas system to the coke oven. Thus, in the technique of Patent Document 1, when the supply of the exhaust gas to the coke is stopped or reduced, the gas discharged from the fluidized bed dryer is circulated and used again as the fluidized gas of the fluidized bed dryer to maintain the fluidized state of the fluidized bed. Doing. However, since the gas discharged from the fluidized bed dryer is the gas after drying the coal powder, the temperature of the gas is, of course, significantly lower than the temperature of the exhaust gas to the coke, and at the time of switching the combustion gas system to the coke, As shown in 4, the gas temperature which flows into the fluidized bed of a fluidized bed drier will fall. As a result, the dryness of the wet raw material decreases, and the amount of fine powder generated by drying and recovered by the dust collector is reduced. On the other hand, it is also conceivable to separately install a hot air generating furnace and burn the combustion gas system to make up the heat amount of the shortage to make the amount of fines recovered to be constant, but to switch the combustion gas system to the coke oven. As described above, is usually once every 15 to 30 minutes, and the time taken for the fluctuation of the gas flow rate to accompany the switching is short as about 0.5 to 3 minutes. It is not realistic to replenish the calories needed for drying.

On the other hand, heavy oil is added to the collected fine powder for the purpose of preventing dust scattering by the fine powder discharged from the dust collector of the fluidized bed coal dryer for drying the coal charged into the coke oven, and carbon adhesion to the coke oven wall. The method of viii is devised as Patent Document 2. However, the above patent does not consider fluctuations in the gas flow rate or gas temperature of hot air as in the exhaust gas to the coke oven, and as described in the embodiment, the amount of the heavy oil added is about 95 t / hour. It is constant at about 250 kg / hour for the quantity.

Patent Document 1: Japanese Patent Application Laid-Open No. 2001-55582

Patent Document 2: Japanese Patent Application Publication No. 49-28241

The technical problem to be solved by the present invention is to stop, reduce or increase the supply of coke oven exhaust gas, which is a hot gas supplied to a fluidized bed dryer as a heat source and a fluidizing gas, or the temperature of the gas changes, Even if the amount of fine powder discharged and recovered with the gas from the fluidized bed dryer is increased or decreased, by maintaining the maintenance rate kneading with the binder necessary for kneading and assembling the fine powder, dust scattering and carbon adhesion to the coke oven wall are reliably ensured. To prevent it.

The present invention relates to a fluidized bed dryer for drying wet raw materials, a gas supply pipe (duct and blower) for supplying exhaust gas from a coke oven as a heat source and a fluidized gas to a fluidized bed dryer, and fine powder discharged together with gas from a fluidized bed dryer. In the drying apparatus of the wet raw material which has a dust collector which collect | recovers, the binder with respect to the fine powder which the amount of collection | recovery of a dust collector also fluctuates by the change of the dryness degree of the wet raw material accompanying the fluctuation | variation of the temperature or flow volume of the coke oven exhaust gas supplied, It is characterized by having the binder addition apparatus provided with the mechanism which can adjust automatically or manually so that addition amount may become a fixed ratio with respect to fine powder.

Moreover, in this drying apparatus, the binder addition amount control apparatus which detects the fluctuation | variation of the supply amount of the exhaust gas from a coke oven, or the fluctuation | variation of the temperature of exhaust gas, and adjusts a binder addition amount corresponding to the detection signal is provided. It is characterized by one.

In addition, in the drying apparatus, the present invention detects fluctuations in exhaust gas temperature and flow rate associated with fluctuations in the amount of production in the coke oven, and automatically or manually adjusts the amount of binder added to the fine powder collected according to the fluctuation amount. A binder addition control device having a mechanism capable of being provided is provided.

In addition, in the drying apparatus, the present invention is capable of detecting fluctuations in exhaust gas temperature and flow rate accompanying fluctuations in the calorific value of the coke oven fuel, and automatically or manually adjusting the amount of binder added to the fine powder collected according to the fluctuation amount. It is characterized by providing a binder addition control device having a mechanism therein.

In addition, the present invention, in the drying device, the mechanism that can detect that the supply of the exhaust gas from the coke oven is stopped or reduced, and can automatically or manually adjust the amount of binder added to the fine powder collected in response to the detection signal It characterized in that the binder addition control device provided with a.

Further, the present invention, in the drying method of the wet raw material by the drying device, the fine powder in which the recovery amount of the dust collector also changes by the change in the dryness of the wet raw material accompanying the change in the temperature or flow rate of the coke oven exhaust gas supplied It is characterized by adjusting the addition amount of a binder with the binder addition apparatus provided with the mechanism which can adjust automatically or manually so that binder addition amount may become a fixed ratio with respect to fine powder.

Moreover, this invention is a binder to the fine powder which detected the fluctuation | variation of the exhaust gas temperature and flow rate accompanying the fluctuation | variation of the amount of production in a coke oven in the drying method of the wet raw material by the said drying apparatus, and collected it according to the fluctuation amount. It is characterized by adjusting the addition amount.

Moreover, this invention detects the fluctuation | variation of the exhaust gas temperature and flow volume accompanying the fluctuation | variation of the calorific value of coke oven fuel in the drying method of the wet raw material by the said drying apparatus, and adds the binder to the fine powder collected according to the fluctuation amount It characterized in that to adjust.

Moreover, this invention detects that supply of hot gas from a coke oven stops or decreases in the drying method of the wet raw material by the said drying apparatus, and adjusts the addition amount of the binder to the fine powder collected by responding to the detection signal. Characterized in that.

In the present invention, the signal from the coke oven can detect that the supply of the exhaust gas to the coke to be supplied to the fluidized bed dryer is stopped, reduced or increased, or the exhaust gas temperature fluctuates.

In the present invention, when the supply of the exhaust gas from the coke oven is stopped or reduced, the gas discharged from the fluidized bed dryer can be circulated and used again as the fluidized gas of the fluidized bed dryer. In addition, it is possible to detect that the supply of the exhaust gas to the coke is stopped or reduced by the prognosis signal or the start signal of the combustion system switching to the coke.

According to the present invention, with the stop, decrease or increase of the supply of coke oven exhaust gas supplied to a fluidized bed dryer as a heat source and fluidizing gas, or the temperature fluctuation of the coke oven exhaust gas, it is discharged | emitted with a gas from a fluidized bed dryer, and it collect | recovered Even if the amount of fines varies, the amount of binder added is determined after predicting or predicting stopping, decreasing or increasing the supply of coke oven exhaust gas or changing the temperature of the coke oven exhaust gas. By adjusting, the mixing ratio of the fine powder and the binder can always be maintained at the optimum ratio. Therefore, by adding a sufficient amount of binder to the fine powder, it is possible to prevent dust scattering and carbon adhesion to the coke oven wall, and to solve problems such as contamination of the conveyance path due to excessive binder and waste of the binder.

1 is a schematic configuration diagram showing an embodiment of a drying apparatus of the present invention.

Fig. 2 is a schematic configuration diagram showing another embodiment of the drying apparatus of the present invention.

3 is a view showing a switching state of the combustion exhaust gas system to the coke oven in the present invention.

4 is a view showing a switching state of the combustion exhaust gas system to the coke oven in the prior art.

EMBODIMENT OF THE INVENTION Hereinafter, embodiment of this invention is described based on the Example which applied this invention to the drying of the coke oven coal powder (it is only hereafter called "coal powder").

1 is a schematic configuration diagram showing an embodiment of a drying apparatus of the present invention. In the figure, combustion exhaust gas to the coke oven generated in the coke oven 1 passes through the flue 2 and is discharged from the coke oven chimney 3 to the atmosphere. The temperature of the flue exhaust gas (coke oven exhaust gas) 4 which passes through the flue 2 is about 150-250 degreeC. The coke oven exhaust gas 4 flows through the gas supply pipe 5 branched from the flue 2 to the coke furnace, and is boosted by the blower 6, and then the fluidized bed dryer 8 as the heat source and the fluidizing gas 7. Is supplied from the bottom of).

The exhaust gas 9 discharged from the fluidized bed dryer 8 is discharged from the chimney 13 into the atmosphere by the exhaust gas pipe 10 via the dust collector 11 and the blower 12.

In addition, by branching the gas circulation pipe 14 from the exhaust gas pipe 10 and connecting the front end thereof to the gas supply pipe 5, the exhaust gas 9 of the fluidized bed dryer 8 is circulated, and the fluidized bed dryer is again. It can be used as the fluidizing gas of (8).

The coal powder, which is a wet raw material, is charged into the fluidized bed dryer 8 by the charging chute 15, and is fluidized by the upward flow by the above-described heat source and fluidized gas 7 introduced from the fluidized bed dryer 8. ). In this fluidized bed 16, coal powder is dried, and the coal powder is adjusted to a predetermined temperature and water content, and most of the coal powder is discharged by the discharge chute 17. The coal powder discharged | emitted from the discharge chute 17 is conveyed to a coke oven by the conveyance path which is not shown in figure. On the other hand, although fine powder is produced by drying coal powder in the fluidized bed 16, this fine powder is discharged | emitted with gas from the upper part of the fluidized bed dryer 8, and the dust collector 11 provided in the exhaust-gas piping 10 was carried out. Is recovered by.

A binder such as heavy oil is added to the collected fine powder by the binder adding device 18, and kneaded and assembled in the kneading granulator 19 and then conveyed to the coke oven by a conveying path (not shown). The amount of the binder added by the binder addition device 18 is adjusted by the binder addition control device 20. Of course, the binder addition control device 20 can also be incorporated in the binder addition device 18. In addition, when adjusting the binder addition apparatus 18 manually, the binder addition control apparatus 20 is unnecessary.

The flue gas flowmeter 21 is provided in the flue 2 of the coke oven mentioned above, the flowmeter 23 and the 1st control valve 24 are installed in the gas supply piping 5, and the exhaust gas pipe 10 The 2nd control valve 25 is provided and the 3rd control valve 26 is provided in the gas circulation piping 14. The exhaust gas flowmeter 21 is not essential, and the exhaust gas flow rate may be estimated by the combustion calculation to the coke oven. The first to third regulating valves 24 to 26 can adjust the opening degree or the flow rate by the regulating valve control devices 27 to 29, respectively.

In this embodiment, the mixing ratio of the fine powder recovered by the dust collector 11 and the binder is always the optimum ratio by adjusting the binder adding device 18 with the change of the exhaust gas temperature or the flow rate to the coke oven. . A concrete description with reference to FIG. 1 is as follows.

In the steady state, since the amount of fine powder discharged from the dust collector 11 is constant, the amount of binder added is constant, and a mechanism for adjusting the binder adding device 18 is not necessary. As a result of earnestly examining the optimum mixing ratio of a fine powder and a binder, this inventor turned out that the optimum ratio is 0.1 to 15% of a binder with respect to fine powder 1.

On the other hand, when the flow rate or temperature of the coke oven exhaust gas 4 introduced into the fluidized-bed drier 8 changes for some reason, such as a sudden change of a production quantity in a coke oven, a fluctuation of the calorific value of coke oven fuel, and the like, it is mentioned above. For one reason, the amount of fines recovered by the dust collector 11 also changes. As described above, a binder necessary for kneading and assembling is added to the recovered fine powder, but if the same amount of binder is added as in the normal operation when the exhaust gas properties of the coke oven are changed, the binder becomes excessive or the binder is insufficient. On the other hand, in the present invention, by grasping the amount of fines recovered by the dust collector 11, which changes with the change in the flow rate or the temperature of the coke oven exhaust gas, according to the change in the flow rate or the temperature of the coke oven exhaust gas, By adjusting the binder addition apparatus 18 manually or automatically, the mixing ratio of the fine amount discharged from the dust collector 11 and a binder can be kept constant. This can prevent problems such as contamination of the conveyance path due to excessive binder, oscillation in the conveyance path due to insufficient binder, or carbon adhesion in the coke oven.

As the adjustment method of the binder addition apparatus 18 mentioned above, although the property change of the coke oven exhaust gas can be detected or predicted and performed manually, the signal of the change of the property of the coke oven exhaust gas sent from a coke oven (coke) It is also possible to automatically adjust the amount of binder added by detecting a signal indicating an increase or decrease of furnace production amount, a signal indicating an increase or decrease of calorific value of coke oven fuel, etc. with the binder addition control device 20 shown in the drawing.

Fig. 2 is a schematic configuration diagram showing another embodiment of the drying apparatus of the present invention. In the figure, combustion exhaust gas to the coke oven generated in the coke oven 1 passes through the flue 2 and is discharged from the coke oven chimney 3 to the atmosphere. The temperature of the coke oven exhaust gas 4 passing through the flue 2 is about 150 to 250 ° C. The coke oven exhaust gas 4 flows through the gas supply pipe 5 branched from the flue 2 of the coke oven, and is boosted by the blower 6, and then the fluidized bed dryer 8 as a heat source and a fluidizing gas 7. It is supplied from the bottom of.

The exhaust gas 9 discharged from the fluidized bed dryer 8 is discharged from the chimney 13 into the atmosphere by the exhaust gas pipe 10 via the dust collector 11 and the blower 12.

In addition, by branching the gas circulation pipe 14 from the exhaust gas pipe 10 and connecting the front end thereof to the gas supply pipe 5, the exhaust gas 9 of the fluidized bed dryer 8 is circulated, and the fluidized bed dryer is again. It can be used as the fluidizing gas of (8).

The coal powder, which is a wet raw material, is charged into the fluidized bed dryer 8 by the charging chute 15, and is fluidized by the upward flow by the above-described heat source and fluidized gas 7 introduced from the fluidized bed dryer 8. ). In this fluidized bed 16, coal powder is dried, and the coal powder is adjusted to a predetermined temperature and moisture content, and most of the coal powder is discharged by the discharge chute 17. The coal powder discharged | emitted from the discharge chute 17 is conveyed to a coke oven by the conveyance path which is not shown in figure. On the other hand, although fine powder is produced by drying coal powder in the fluidized bed 16, this coal powder is discharged | emitted with gas from the upper part of the fluidized bed dryer 8, and the dust collector 11 provided in the exhaust-gas piping 10 was carried out. ) Is recovered.

A binder such as heavy oil is added to the collected fine powder by the binder adding device 18, and kneaded and assembled in the kneading granulator 19 and then conveyed to the coke oven by a conveying path (not shown). The amount of the binder added by the binder addition device 18 is adjusted by the binder addition control device 20. Of course, the binder addition control device 20 can also be incorporated in the binder addition device 18.

The flue gas flowmeter 21 is provided in the flue 2 of the coke oven mentioned above, the flowmeter 23 and the 1st control valve 24 are installed in the gas supply piping 5, and the exhaust gas pipe 10 The 2nd control valve 25 is provided and the 3rd control valve 26 is provided in the gas circulation piping 14. The exhaust gas flowmeter 21 is not essential, and the exhaust gas flow rate may be estimated by the combustion calculation to the coke oven. The first to third regulating valves 24 to 26 can adjust the opening degree or the flow rate by the regulating valve control devices 27 to 29, respectively. Moreover, the gas circulation system control apparatus 30 is provided, and the control command is given to each control apparatus 27-29 of the 1st-3rd control valves 24-26, and it is made to control the amount of circulating gas.

As described in the column of the background art, the coke oven 1 normally has two combustion gas systems for each furnace stage, and when the use time in one system reaches a predetermined time, the coke oven 1 is switched to the other system. . Switching of the strain is usually performed once every 15 to 30 minutes.

At the time of switching of a combustion gas system, as shown in FIG. 4, the flow rate of the combustion gas of the system (system A) used so far is reduced one by one, and when the flow volume becomes zero, the combustion gas of the system (system B) to be used next will be reduced. Increase the flow rate in turn. Therefore, at the time of switching of a combustion gas system, the amount of exhaust gas to coke reduces and increases again. The time required for switching the combustion gas system is generally 0.5 to 3 minutes.

In the present embodiment, when the supply of the exhaust gas to the coke is stopped or reduced, the exhaust gas discharged from the fluidized bed dryer 8 is circulated through the gas circulation pipe 14 to fluidize the fluidized bed dryer 8. Use again as gas. A detailed description with reference to FIGS. 2 and 3 is as follows.

The 3rd control valve 26 arrange | positioned at the gas circulation piping 14 is fully closed or slightly open at the time of normal operation. That is, when the exhaust gas temperature to coke oven is too high at the time of normal operation, it is effective to mix a low temperature circulating gas and to lower gas temperature, and the drying ability when the moisture of the coal powder to be supplied fluctuates. The circulating gas can also be used for the adjustment of.

At the start of combustion gas system switching to the coke, the third control valve 26 is opened from a fully closed or slightly open state to a certain opening degree. As a result, the circulating gas 31 flows through the gas circulation piping 14 by the action of the blower 6 and the blower 12, and a recycle flow is produced | generated. The opening degree of the 1st control valve 24 is gradually made small at the timing by which the fixed flow volume of the circulating gas 31 was secured. As a result, the coke oven exhaust gas 4 which was supplied to the fluidized-bed dryer 8 until then gradually decreases, and the flow volume to the coke oven chimney 3 increases on the contrary. The opening and closing operation speed of the first regulating valve 24 is not necessarily constant, and the amount of combustion exhaust gas (the amount of flue gas) fluctuates depending on the operation degree of the coke oven 1 or the combustion state of the coke oven 1, so that the coke oven ( It is necessary to decide on the basis of the operation status of 1).

Control of the first to third regulating valves 24 to 26 is performed by the respective regulating valve control devices 27 to 29 controlling the respective regulating valves based on the instructions from the gas circulation system control device 30. Of course, it is also possible to integrate some or all of the gas circulation system control device 30 and each regulating valve control device 27 to 29 into a single control device. Moreover, each regulating valve control apparatus can also be incorporated in each regulating valve.

The start of the control for changing the supply gas to the fluidized bed dryer 8 at the time of the combustion gas system switching to the coke oven receives the start signal of the combustion gas system switching from the coke oven 1, and the method of the year (2). The method of starting based on the flow volume change of the exhaust-gas flowmeter 21, etc. can be used.

Further, as shown in Fig. 3, a prediction signal is received from the coke oven 1 for a predetermined time before starting the combustion gas system switching, and the control of supply gas change to the fluidized bed dryer 8 is started based on this prediction signal. It may be. For example, the prediction signal is received one minute before the exhaust gas flow rate becomes zero, and gas recycling via the gas circulation pipe 14 is started. Thereby, the gas recycling is delayed and the situation where the supply gas amount (heat source and fluidizing gas amount) to the fluidized bed dryer 8 is insufficient can be avoided.

Since the circulating gas 31 used at the time of switching the combustion gas system to the coke is the gas after used for drying the coal powder in the fluidized bed dryer 8, the temperature of the gas is naturally higher than that of the coke oven exhaust gas 4. low. Therefore, when switching the combustion gas system to coke, as shown in FIG. 3, the gas temperature which flows into the fluidized bed of a fluidized bed dryer will fall. As a result, the dryness of the wet raw material decreases, and the amount of fine powder generated by drying and recovered by the dust collector is reduced.

As described above, the binder required for kneading and assembling is added to the recovered fine powder. However, when the amount of fine powder decreases during the switching of the combustion gas system to the coke oven, adding the same amount of binder as in normal operation results in excessive binder. . In contrast, in the present invention, the switching of the combustion gas system to the coke is detected, and the amount of binder added is reduced after predicting a decrease in the amount of fines (see the bottom of FIG. 3). Detection of switching of the combustion gas system can be performed by receiving a foresight signal from a coke oven a predetermined time before starting combustion gas system switching, as shown in FIG. When the binder addition control device 20 receives this predictive signal, it predicts that the amount of fine powder decreases every t seconds, and the binder by the binder addition device 18 makes the ratio between the fine powder and the binder equal to that in normal operation. Reduce the amount of addition. Thereby, fine powder and a binder can always be mixed by a fixed ratio, and the problem of contamination of the conveyance path by excess binder does not arise.

Detection of switching of the combustion gas system can also be performed by receiving the start signal of combustion gas system switching from the coke oven 1. In this case, the time until the adjustment of the binder addition amount is shortened as compared with the detection by the prediction signal, but in actual operation, it can be sufficiently coped.

The present invention can be applied not only to drying of coal powder charged into a coke oven, but also to drying of other wet raw materials such as crushed slag and limestone.

Claims (22)

A fluidized bed dryer for drying the wet raw material, a duct and a blower for introducing exhaust gas into the fluidized bed dryer, and a dust collector for recovering fine powder accompanying the exhaust gas of the fluidized bed dryer, the heat source of the fluidized bed dryer It is a drying device of a wet raw material using the exhaust gas to the coke oven as the cumulative gas, Having a binder addition apparatus provided with the mechanism which adjusts binder addition amount to become a fixed ratio with respect to fine amount according to the fluctuation of the fine amount discharged from the said dust collector accompanying the change of the temperature or flow volume of the exhaust gas to coke oven Drying apparatus for wet raw material characterized by the above-mentioned. The binder addition amount control apparatus which detects the fluctuation | variation of the supply amount of the exhaust gas from the coke oven, or the fluctuation | variation of the temperature of exhaust gas, and adjusts the binder addition amount according to the detection signal, It characterized by the above-mentioned. Drying device for wet raw materials. The wet material drying apparatus according to claim 1, wherein a binder addition amount control device is provided which detects the increase or decrease of the production amount by coke and adjusts the binder addition amount according to changes in the exhaust gas temperature and flow rate accompanying the increase and decrease. . The wet material drying apparatus according to claim 1, wherein a binder addition amount control device is provided which detects the increase or decrease of the calorific value of the fuel by coke and adjusts the binder addition amount according to the exhaust gas temperature and flow rate accompanying the increase and decrease. Device. The wet material drying apparatus according to claim 1, wherein a binder addition amount control device is provided for detecting that supply of exhaust gas to the coke is stopped or reduced, and adjusting a binder addition amount in response to the detection signal. 2. The gas circulating pipe for circulating the gas discharged from the fluidized bed dryer again to be supplied to the fluidized bed dryer, and the gas discharged from the fluidized bed dryer when the supply of the exhaust gas from the coke oven is stopped or reduced. And a gas circulation system control device configured to control the gas circulation system so as to be circulated and reused as the fluidizing gas of the fluidized bed dryer. 3. The wet raw material drying apparatus according to claim 2, wherein the amount of supply of the exhaust gas from the coke oven is reduced or increased or the fluctuation of the exhaust gas temperature is detected by a signal sent from the coke oven. 4. The wet raw material drying apparatus according to claim 3, wherein the amount of supply of the exhaust gas from the coke oven is reduced or increased or the fluctuation of the exhaust gas temperature is detected by a signal sent from the coke oven. 5. The wet raw material drying apparatus according to claim 4, wherein the amount of exhaust gas supplied from the coke oven is reduced or increased or the fluctuation of the exhaust gas temperature is detected by a signal sent from the coke oven. 6. The wet raw material drying apparatus according to claim 5, wherein the supply signal of the exhaust gas to the coke is stopped or reduced by a prognosis signal or a start signal of the combustion system switching to the coke. A fluidized bed dryer for drying the wet raw material, a duct and a blower for introducing exhaust gas into the fluidized bed dryer, and a dust collector for recovering fine powder accompanying the exhaust gas of the fluidized bed dryer, the heat source of the fluidized bed dryer A wet raw material drying apparatus using an exhaust gas of coke oven as a fluidizing gas, wherein the amount of binder added to the fine powder is changed in accordance with the variation of the fine amount discharged from the dust collector, which is accompanied by a change in temperature or flow rate of the exhaust gas of the coke oven. It is a drying method of a wet raw material by the drying apparatus of the wet raw material which has a binder addition apparatus provided with the mechanism which adjusts so that it may become a fixed ratio with respect to, A fluctuation in the supply amount of the exhaust gas from the coke oven or a fluctuation in the temperature of the exhaust gas is detected, and the amount of binder added is adjusted in response to the detection signal. A fluidized bed dryer for drying the wet raw material, a duct and a blower for introducing exhaust gas into the fluidized bed dryer, and a dust collector for recovering fine powder accompanying the exhaust gas of the fluidized bed dryer, the heat source of the fluidized bed dryer A wet material drying apparatus using an exhaust gas of coke oven as a fluidizing gas, wherein the amount of binder added is fine in accordance with a variation in the amount of fines discharged from the dust collector accompanied by a change in temperature or flow rate of the exhaust gas of the coke oven. It is a drying method of a wet raw material by the drying apparatus of the wet raw material which has a binder addition apparatus provided with the mechanism which adjusts so that it may become a fixed ratio with respect to, A method for drying a wet raw material characterized by detecting the increase or decrease of the production amount by coke and adjusting the binder addition amount in accordance with the change of the exhaust gas temperature and the flow rate accompanying the increase and decrease. A fluidized bed dryer for drying the wet raw material, a duct and a blower for introducing exhaust gas into the fluidized bed dryer, and a dust collector for recovering fine powder accompanying the exhaust gas of the fluidized bed dryer, the heat source of the fluidized bed dryer A wet material drying apparatus using an exhaust gas of coke oven as a fluidizing gas, wherein the amount of binder added is fine in accordance with a variation in the amount of fines discharged from the dust collector accompanied by a change in temperature or flow rate of the exhaust gas of the coke oven. It is a drying method of the wet raw material by the drying apparatus of the wet raw material which has a binder addition apparatus provided with the mechanism which adjusts so that it may become a fixed ratio with respect to, A method for drying a wet raw material characterized by detecting the increase or decrease of the calorific value of fuel by coke and adjusting the amount of binder added in accordance with the exhaust gas temperature and flow rate accompanying the increase and decrease. 12. The method of drying a wet raw material according to claim 11, wherein the amount of exhaust gas supplied from the coke oven is reduced or increased or a fluctuation in exhaust gas temperature is detected by a signal sent from the coke oven. 13. The method of drying a wet raw material according to claim 12, wherein the supply amount of the exhaust gas from the coke oven is detected by a signal sent from the coke oven to reduce or increase the flue gas temperature. The method for drying a wet raw material according to claim 13, wherein the amount of exhaust gas supplied from the coke oven is reduced or increased or a fluctuation in exhaust gas temperature is detected by a signal sent from the coke oven. A fluidized bed dryer for drying the wet raw material, a duct and a blower for introducing exhaust gas into the fluidized bed dryer, and a dust collector for recovering fine powder accompanying the exhaust gas of the fluidized bed dryer, the heat source of the fluidized bed dryer A wet raw material drying apparatus using an exhaust gas of coke oven as a combined fluidization gas, and the amount of binder added is small in accordance with the variation in the amount of fines discharged from the dust collector accompanying the change of the temperature or flow rate of the exhaust gas of the coke oven. It is a drying method of a wet raw material by the drying apparatus of the wet raw material which has a binder addition apparatus provided with the mechanism which adjusts to a fixed ratio with respect to quantity, A method for drying a wet raw material characterized by detecting that supply of exhaust gas from a coke oven is stopped or reduced, and adjusting the amount of binder added in response to the detection signal. The method of drying a wet raw material according to claim 11, wherein when the supply of the exhaust gas from the coke oven is stopped or reduced, the gas discharged from the fluidized bed dryer is circulated and used again as the fluidized gas of the fluidized bed dryer. The method of drying a wet raw material according to claim 12, wherein when the supply of the exhaust gas from the coke oven is stopped or reduced, the gas discharged from the fluidized bed dryer is circulated and used again as the fluidized gas of the fluidized bed dryer. The method of drying a wet raw material according to claim 13, wherein when the supply of the exhaust gas from the coke oven is stopped or reduced, the gas discharged from the fluidized bed dryer is circulated and used again as the fluidized gas of the fluidized bed dryer. 18. The method of drying a wet raw material according to claim 17, wherein when the supply of the exhaust gas from the coke oven is stopped or reduced, the gas discharged from the fluidized bed dryer is circulated and used again as the fluidized gas of the fluidized bed dryer. 18. The method of drying a wet raw material according to claim 17, wherein the supply signal of the exhaust gas to the coke is stopped or reduced by a prognosis signal or a start signal of combustion system switching to the coke.

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