阅读说明：本技术 有机性污泥的处理设备及处理方法 (Treatment equipment and treatment method for organic sludge ) 是由 长泽英和 河岸正泰 倭常郎 小林俊树 于 2019-08-30 设计创作，主要内容包括：本发明的有机性污泥的处理设备具备浓缩机(1)、脱水机(2)、焚烧炉(3)和排烟处理塔(12),排烟处理塔(12)在塔内下部具备向燃烧废气(E)供给第1冷却水(H1)来进行冷却、脱硫的第1冷却部(12A),并且在塔内上部具备向由第1冷却部(12A)冷却、脱硫后的燃烧废气(E)供给第2冷却水(H2)来进行冷却的第2冷却部(12B),该处理设备具备温水供给机构,该温水供给机构通过将在第2冷却部(12B)中对燃烧废气(E)进行冷却后的第2冷却水(H2)作为温水(I)供给向浓缩机(1)和脱水器(2)中的至少一方,从而对有机性污泥直接加温。(The organic sludge treatment facility of the present invention comprises a thickener (1), a dehydrator (2), an incinerator (3), and a flue gas treatment tower (12), wherein the flue gas treatment tower (12) is provided with a 1 st cooling part (12A) for supplying 1 st cooling water (H1) to combustion exhaust gas (E) at the lower part in the tower for cooling and desulfurizing, and a 2 nd cooling part (12B) for supplying a 2 nd cooling water (H2) to the combustion exhaust gas (E) cooled and desulfurized by the 1 st cooling part (12A) and cooling the combustion exhaust gas in the upper part of the tower, the treatment facility is provided with a hot water supply mechanism which directly heats the organic sludge by supplying 2 nd cooling water (H2) obtained by cooling the combustion exhaust gas (E) in the 2 nd cooling part (12B) to at least one of the thickener (1) and the dehydrator (2) as hot water (I).)

1. An organic sludge treatment facility comprising:

a thickener for thickening the organic sludge;

a dehydrator configured to dehydrate the organic sludge concentrated by the thickener;

an incinerator for incinerating the organic sludge dehydrated by the dehydrator; and

a flue gas treatment tower for treating the combustion exhaust gas generated by the incinerator,

wherein the content of the first and second substances,

the flue gas treatment tower is provided with:

a 1 st cooling unit which is located at a lower portion in the flue gas treatment tower and which supplies 1 st cooling water to the combustion exhaust gas to cool and desulfurize the combustion exhaust gas; and

a 2 nd cooling unit which is located at an upper portion in the flue gas treatment tower and which supplies 2 nd cooling water to the combustion exhaust gas cooled and desulfurized by the 1 st cooling unit to cool the combustion exhaust gas,

the treatment facility includes a hot water supply mechanism configured to supply the 2 nd cooling water obtained by cooling the combustion exhaust gas in the 2 nd cooling unit to at least one of the thickener and the dehydrator as hot water to directly warm the organic sludge.

2. The facility for treating organic sludge according to claim 1, wherein the hot water supply means includes a 1 st heat exchanger, and the 1 st heat exchanger indirectly exchanges heat between the 1 st cooling water obtained by cooling the combustion exhaust gas in the 1 st cooling unit and the 2 nd cooling water obtained by cooling the combustion exhaust gas in the 2 nd cooling unit.

3. The facility for treating organic sludge according to claim 1 or 2, wherein the hot water supply means includes a 2 nd heat exchanger, and the 2 nd heat exchanger indirectly exchanges heat between the combustion exhaust gas supplied to the flue gas treatment tower and the 2 nd cooling water obtained by cooling the combustion exhaust gas in the 2 nd cooling unit.

4. The facility for treating organic sludge according to any one of claims 1 to 3, wherein the hot water supply means supplies hot water having a temperature in a range of 50 ℃ or higher and less than 100 ℃ to at least one of the thickener and the dehydrator.

5. A method for treating organic sludge, which comprises dehydrating organic sludge concentrated by a thickener with a dehydrator, incinerating the organic sludge dehydrated by the dehydrator with an incinerator, and treating combustion exhaust gas generated from the incinerator with a flue gas treatment tower,

wherein the content of the first and second substances,

the flue gas treatment tower is provided with:

a 1 st cooling unit which is located at a lower portion in the flue gas treatment tower and which supplies 1 st cooling water to the combustion exhaust gas to cool and desulfurize the combustion exhaust gas; and

a 2 nd cooling unit which is located at an upper portion in the flue gas treatment tower and which supplies a 2 nd cooling water to the combustion exhaust gas cooled and desulfurized by the 1 st cooling unit to cool the combustion exhaust gas,

the 2 nd cooling water obtained by cooling the combustion exhaust gas in the 2 nd cooling unit is supplied as warm water to at least one of the thickener and the dehydrator by a warm water supply mechanism to directly warm the organic sludge.

6. The method for treating organic sludge according to claim 5, wherein the hot water supply means includes a 1 st heat exchanger, and the 1 st heat exchanger indirectly exchanges heat between the 1 st cooling water obtained by cooling the combustion exhaust gas in the 1 st cooling unit and the 2 nd cooling water obtained by cooling the combustion exhaust gas in the 2 nd cooling unit.

7. The method for treating organic sludge according to claim 5 or 6, wherein the hot water supply means includes a 2 nd heat exchanger, and the 2 nd heat exchanger indirectly exchanges heat between the combustion exhaust gas supplied to the flue gas treatment tower and the 2 nd cooling water obtained by cooling the combustion exhaust gas in the 2 nd cooling unit.

8. A method for treating organic sludge according to any one of claims 5 to 7, wherein the hot water supply means supplies hot water having a temperature in a range of 50 ℃ or higher and less than 100 ℃ to at least one of the thickener and the dehydrator.

[ technical field ] A method for producing a semiconductor device

The present invention relates to an apparatus and a method for treating organic sludge, comprising:

a thickener for concentrating organic sludge that is flocculated by adding a flocculant to sewage sludge or the like generated from a sewage treatment plant;

a dehydrator for dehydrating the organic sludge concentrated by the thickener;

an incinerator for incinerating the organic sludge dehydrated by the dehydrator; and

the flue gas treatment tower treats (removes dust, neutralizes and removes acid gases such as sulfur oxides, cools and dehumidifies) the combustion exhaust gas generated by the incinerator.

The present application claims priority based on japanese application No. 2019-037781, which was filed in japan on 3/1/2019, and the contents of which are incorporated herein by reference.

[ background of the invention ]

For example, patent document 1 describes an apparatus and a method for treating organic sludge, which includes:

a 1 st thickening unit that thickens sludge to produce thickened sludge;

a dewatering unit that receives the concentrated sludge generated in the 1 st concentrating unit as a sludge to be dewatered, and dewaters the sludge to be dewatered while heating the sludge by an indirect heating method such as a screw pressure type dewatering machine; and

an addition part for adding an inorganic flocculant to the concentrated sludge.

Wherein the temperature of a heating medium for heating sludge to be dehydrated in the dehydration section is lower than 100 ℃.

Patent document 1 discloses: according to the apparatus and the method for treating organic sludge, since sludge is heated and dewatered in the dewatering section, the viscosity of sludge is reduced, the water retention capacity of sludge is reduced by thermal denaturation, filtrate is easily separated, and the water content of dewatered sludge (dewatered sludge) can be reduced.

[ Prior art documents ]

[ patent document ]

Patent document 1: japanese patent laid-open publication No. 2017-213479

[ summary of the invention ]

[ problem to be solved by the invention ]

However, in the treatment facility and the treatment method disclosed in patent document 1, the heat medium is heated by waste heat of combustion generated when the dewatered sludge is incinerated in the incinerator, scrubber drain water after cooling is made a heat medium by bringing combustion exhaust gas into contact with cooling water in a scrubber (flue gas treatment tower), or the heat medium is supplied to the screw pressure type dehydrator or the like as described above by using warm water after heat exchange with the scrubber drain water as the heat medium, and the concentrated sludge as the sludge to be dewatered is heated by an indirect heating method. However, for example, it is also conceivable to heat (warm) the sludge by directly supplying warm water to the concentrated sludge of the thickener or the dewatered sludge of the dehydrator and mixing the warm water with the sludge.

Here, when the hot water heated by the combustion waste heat of the incinerator and the hot water heat-exchanged with the scrubber drain water are directly supplied as heat media to the concentrated sludge of the thickener and the dewatered sludge of the dehydrator and mixed, the supplied hot water and the sludge directly contact each other, and therefore cannot be recycled. Therefore, the amount of warm water (heat medium) used is significantly increased.

Further, even if the scrubber waste water cooled by bringing the combustion exhaust gas into contact with the cooling water in the scrubber is directly supplied as warm water (heat medium) to the concentrated sludge of the thickener or the dewatered sludge of the dehydrator, the scrubber waste water is in direct contact with the dust in the combustion exhaust gas, so that the insoluble solid content (SS content) is large, and the unreacted alkali component is contained to treat the acidic gas in the combustion exhaust gas, so that the concentrated sludge or the dewatered sludge may be deteriorated. Further, since the unreacted alkali component cannot be recycled, the amount of the alkali component used also increases.

The present invention has been made under such circumstances, and an object of the present invention is to provide an apparatus and a method for treating organic sludge, which can supply the drain water of a flue gas treatment tower (scrubber) as warm water having a small insoluble solid content (SS component) and a small unreacted alkali content without causing deterioration of concentrated sludge and dewatered sludge, and can prevent an increase in the amount of alkali content used in the flue gas treatment tower, in the case where the warm water is directly supplied to the concentrated sludge of a thickener and the dewatered sludge of a dehydrator for warming up.

[ MEANS FOR SOLVING PROBLEMS ] to solve the problems

The organic sludge treatment facility of the present invention comprises:

a thickener for thickening the organic sludge;

a dehydrator for dehydrating the organic sludge concentrated by the thickener;

an incinerator for incinerating the organic sludge dehydrated by the dehydrator; and

a flue gas treatment tower for treating the combustion exhaust gas generated by the incinerator;

wherein the content of the first and second substances,

the flue gas treatment tower is provided with a 1 st cooling part for supplying 1 st cooling water to the combustion flue gas to cool and desulfurize the combustion flue gas at the lower part in the flue gas treatment tower,

and a 2 nd cooling unit for supplying a 2 nd cooling water to the combustion exhaust gas cooled and desulfurized by the 1 st cooling unit to cool the combustion exhaust gas, the 2 nd cooling unit being provided in an upper portion of the flue gas treatment tower,

and a hot water supply mechanism for supplying the 2 nd cooling water obtained by cooling the combustion exhaust gas in the 2 nd cooling unit to at least one of the thickener and the dehydrator as hot water to directly warm the organic sludge.

The method for treating organic sludge according to the present invention is a method for treating organic sludge in which organic sludge concentrated by a thickener is dewatered by a dewaterer, the organic sludge dewatered by the dewaterer is incinerated by an incinerator, and combustion exhaust gas generated by the incinerator is treated by a flue gas treatment tower, wherein the flue gas treatment tower is provided with a 1 st cooling part for supplying 1 st cooling water to the combustion exhaust gas to cool and desulfurize the combustion exhaust gas at a lower part in the flue gas treatment tower, and is provided with a 2 nd cooling part for supplying 2 nd cooling water to the combustion exhaust gas cooled and desulfurized by the 1 st cooling part at an upper part in the flue gas treatment tower, and the 2 nd cooling water cooled by the combustion exhaust gas in the 2 nd cooling part is supplied as warm water to at least one of the thickener and the dewaterer by a warm water supply mechanism to directly treat the organic sludge in the dewaterer And heating.

In the organic sludge treatment facility and the treatment method, the 1 st cooling water used for the acid gas treatment of the flue gas is contained in the 1 st cooling water used for desulfurization of the flue gas, and the 1 st cooling water is recycled in the 1 st cooling part at the lower part in the flue gas treatment tower, whereby the unreacted alkali component can be prevented from being discharged, and the use amount of the alkali component can be prevented from increasing.

Further, since the combustion exhaust gas is cooled by the 2 nd cooling unit in the upper part of the flue gas treatment tower and cooled by the 2 nd cooling unit in the upper part of the flue gas treatment tower, the 2 nd cooling water which becomes warm water is supplied to at least one of the thickener and the dehydrator by the warm water supply means to directly warm the organic sludge, it is possible to avoid deterioration of the insoluble solid content (SS component) and the unreacted alkali component in the dust, or the concentrated organic sludge and the dehydrated organic sludge due to the acid gas component.

The amount of the 2 nd cooling water supplied to the 2 nd cooling unit is about several times to ten times the amount of the 1 st cooling water circulated in the 1 st cooling unit, and it is not necessary to circulate and reuse the hot water supplied to the thickener and the dehydrator and directly contacted with the organic sludge.

Here, the 2 nd cooling water after cooling the combustion exhaust gas may be directly supplied to the thickener or dehydrator to be mixed with the organic sludge, but in the case where the temperature of the 2 nd cooling water discharged from the 2 nd cooling unit is so low that it is difficult to sufficiently reduce the water content of the organic sludge, the 1 st hot water supply means may include a 1 st heat exchanger in which the 1 st cooling water after cooling the combustion exhaust gas in the 1 st cooling unit and the 2 nd cooling water after cooling the combustion exhaust gas in the 2 nd cooling unit indirectly exchange heat with each other, and the temperature of the 2 nd cooling water supplied as hot water is raised by the heat exchange of the 1 st heat exchanger.

Similarly, when the temperature of the 2 nd cooling water discharged from the 2 nd cooling unit is low, the 2 nd hot water supply means may include a 2 nd heat exchanger, and the temperature of the 2 nd cooling water supplied as hot water may be raised by heat exchange performed by the 2 nd heat exchanger by indirectly performing heat exchange between the combustion exhaust gas supplied to the exhaust gas treatment tower and the 2 nd cooling water in which the combustion exhaust gas is cooled in the 2 nd cooling unit.

The temperature of the 2 nd cooling water supplied as hot water by the hot water supply means is preferably in the range of 50 ℃ or more and less than 100 ℃. If the temperature of the 2 nd cooling water is less than 50 ℃, the above-mentioned reduction in viscosity of the organic sludge and the reduction in water content by the separation of water cannot be sufficiently achieved. In addition, if the temperature of the hot water is 100 ℃ or higher, it may be difficult to handle the hot water.

[ Effect of the invention ]

As described above, according to the present invention, when warm water is directly supplied to the concentrated sludge of the thickener and the dehydrated sludge of the dehydrator for heating, it is possible to supply the drain water from the 2 nd cooling unit of the flue gas treatment tower, which is large in amount and does not need to be recycled, as warm water, and it is possible to prevent the concentrated sludge and the dehydrated sludge from being deteriorated and to prevent the amount of alkali components of the acid gas used for treating the combustion exhaust gas from being increased.

[ description of the drawings ]

FIG. 1 is a schematic view showing an embodiment of an apparatus for treating organic sludge according to the present invention.

Fig. 2 is a sectional view of the flue gas treatment tower in the embodiment shown in fig. 1.

[ detailed description ] embodiments

Fig. 1 and 2 show an embodiment of the organic sludge treatment facility according to the present invention, and the organic sludge treatment facility according to this embodiment will be described below, as well as an embodiment of the organic sludge treatment method according to the present invention.

The organic sludge treatment facility of the present embodiment includes:

a flocculant machine (not shown) for adding a polymer flocculant to organic sludge such as sewage sludge such as mixed raw sludge generated and supplied from a sewage treatment plant to perform flocculation;

a thickener 1 for thickening the flocculated sludge A in which the solid content is flocculated to some extent by the flocculant; and

and a dehydrator 2 for dehydrating the concentrated sludge B having a sludge concentration of 5 wt% or more, preferably 8 wt% to 10 wt% by the thickener 1.

Further, an inorganic flocculant such as ferric Polysulfate (PFS) or a flocculant such as a polymer flocculant may be added to the concentrated sludge B supplied to the dewatering machine 2.

In the dewatering machine 2, the concentrated sludge B is dewatered to about 70 to 74 wt% of water to become dewatered sludge C, and the dewatered sludge C thus dewatered is supplied to the incinerator 3 and incinerated. The incinerator 3 is a supercharged flow incinerator in the present embodiment, and the dewatered sludge C supplied to the incinerator 3 is combusted by flowing together with the fluidizing medium by high-temperature and high-pressure combustion air D of about 130 ℃ supplied from a supercharger described later, thereby generating high-temperature combustion exhaust gas E of about 850 ℃.

The combustion exhaust gas E is supplied to the waste heat boiler 4, cooled to about 500 ℃ by heat exchange with the heat medium F supplied from the heat utilization equipment 5, further supplied to the dust collector 6, collected and cooled to about 470 ℃, and then supplied to the supercharger 7 to pressurize the combustion air D supplied to the incinerator 3. The heat utilization equipment 5 includes, for example, a dryer and a generator.

The combustion exhaust gas E of about 400 ℃ discharged from the supercharger 7 is supplied to the white smoke prevention preheater 8, and the combustion exhaust gas E is cooled to about 320 ℃ by preheating the white smoke prevention air G supplied from the fan 9 to the white smoke prevention preheater 8.

The combustion exhaust gas E cooled in the white smoke prevention preheater 8 is supplied to a hot water boiler 11 as a 2 nd heat exchanger in the present embodiment, is further cooled to about 200 ℃, and is supplied to a 1 st cooling unit (adiabatic cooling unit/desulfurization unit) 12A at the lower part in the tower inside the flue gas treatment tower 12 shown in fig. 2. The flue gas treatment tower 12 is provided with a circulation tank 13 of the 1 st cooling water H1 at the bottom, a funnel-shaped water collection unit 14 is provided at the upper part of the circulation tank 13, and the combustion exhaust gas E discharged from the hot water boiler 11 is supplied into the flue gas treatment tower 12 from a supply unit 15 provided above the water collection unit 14.

Above the supply unit 15, a 1 st nozzle 16A and a 2 nd nozzle 16B for spraying the 1 st cooling water H1 into the 1 st cooling unit 12A of the flue gas treatment tower 12 are arranged at a vertical interval, and a space from the 2 nd nozzle 16B above to the water collecting unit 14 is the 1 st cooling unit 12A. Between the 1 st nozzle 16A and the 2 nd nozzle 16B, a 1 st filler 17 is disposed at an interval from the 2 nd nozzle 16B in the upper direction, and a propeller-shaped blade (vane) 18 is provided below the 1 st filler 17 around the center line of the exhaust gas treatment tower 12.

In the present embodiment, the 1 st cooling water H1 stored in the circulation tank 13 passes through the 1 st heat exchanger 20 by the 1 st pump 19, and is sprayed from the 1 st and 2 nd nozzles 16A and 16B into the 1 st cooling unit 12A, thereby adiabatically cooling the combustion exhaust gas E supplied into the exhaust gas treatment tower 12. Further, an alkaline component (for example, sodium hydroxide or the like) is added to the 1 st cooling water H1, and the acidic gas contained in the combustion exhaust gas E is treated to be desulfurized, and the dust that has not been collected by the dust collector 6 is also removed by the 1 st cooling water H1.

Here, the combustion exhaust gas E rising above the 1 st nozzle 16A is turned into a swirling flow by the vanes 18, and the contact efficiency with the 1 st cooling water H1 sprayed from the 2 nd nozzle 16B is improved, and then, when passing through the 1 st filler 17, the combustion exhaust gas E further contacts the 1 st cooling water H1 stored in the 1 st filler 17, is cooled to about 74 to 85 ℃, rises in the flue gas treatment tower 12, and is supplied to the 2 nd cooling unit (supercooling unit) 12B at the upper portion in the flue gas treatment tower 12. The 1 st cooling water H1 sprayed from the 1 st and 2 nd nozzles 16A and 16B is collected in the water collection unit 14 to the circulation tank 13 and recycled.

In the 2 nd cooling unit 12B, above the 2 nd nozzle 16B of the 1 st cooling unit 12A, there are provided:

a bottom 21A joined to the inner wall of the flue gas treatment tower 12 in a ring plate shape;

a cylindrical wall portion 21B joined to extend upward from the inner peripheral edge of the bottom portion 21A; and

a conical plate-shaped umbrella part 21C which is arranged above the wall part 21B and has an outer diameter larger than that of the wall part 21B;

a space surrounded by the bottom 21A, the wall 21B, and the inner wall of the flue gas treatment tower 12 is a drain separator 21. Further, a 2 nd filler 22 is disposed above the umbrella part 21C, and a 3 rd nozzle 23 for spraying a 2 nd cooling water H2 into the 2 nd cooling part 12B is disposed further above the 2 nd filler 22.

The combustion exhaust gas E which rises from the 1 st cooling unit 12A and passes through the wall portion 21B of the drain separating unit 21 to be supplied to the 2 nd cooling unit 12B is brought into contact with the 2 nd cooling water H2 sprayed from the 3 rd nozzle 23 and stored in the 2 nd filler 22, and is supercooled to about 40 ℃. The combustion exhaust gas E thus cooled is discharged to a stack 12C at the upper end of the exhaust gas treatment tower 12, and as shown in fig. 1, is mixed with white smoke preventing air G supplied from the white smoke preventing preheater 8 to the 2 nd heat extraction boiler 10, thereby preventing generation of white smoke and discharging the mixture into the atmosphere.

On the other hand, the 2 nd cooling water H2 after cooling the combustion exhaust gas E is heated to about 70 ℃, drips from the 2 nd filler 22 and is stored in the drain separator 21, or falls on the upper surface of the umbrella part 21C and flows to the outer peripheral side and is stored in the drain separator 21. Note that, a 1 st discharge pipe 24A is connected to the inner wall of the flue gas processing tower 12 at a position slightly lower than the upper end edge of the wall portion 21B of the drain separation portion 21, and when the water level of the 2 nd cooling water H2 held in the drain separation portion 21 reaches a position connected to the 1 st discharge pipe 24A, the 2 nd cooling water H2 is discharged to the drain tank 25.

Further, a 2 nd drain pipe 24C including a valve 24B is connected to the inner wall of the flue gas treatment tower 12 at a position slightly above the bottom 21A of the drain separator 21, and the 2 nd cooling water H2 stored in the drain separator 21 can be drained between the 1 st packing 17 and the vane 18 of the 1 st cooling unit 12A with the opening of the valve 24B. Further, on the inner wall of the flue gas treatment tower 12, a 3 rd drain pipe 24D is connected to a part of the circulation tank 13, and when the water level of the 1 st cooling water H1 in the circulation tank 13 reaches the connection position of the 3 rd drain pipe 24D, the 1 st cooling water H1 is discharged into the drain tank 25.

Further, a 4 th drain pipe 26 provided with a valve 26A is connected to the inner wall of the flue gas treatment tower 12 between the connection positions of the 1 st and 2 nd drain pipes 24A and 24C in the drain separation section 21, and the 2 nd cooling water H2 discharged from the 4 th drain pipe 26 is indirectly heated by the 1 st cooling water H1 in the 1 st heat exchanger 20 in the present embodiment in accordance with the opening of the valve 26A.

The 2 nd cooling water H2 heated by the 1 st heat exchanger 20 in this way passes through the 2 nd pump 27, is indirectly heated again by the combustion exhaust gas E in the hot water boiler 11 as the 2 nd heat exchanger in the present embodiment, and is supplied as hot water I of about 70 to 87 ℃ to at least one of the thickener 1 and the dehydrator 2. In the present embodiment, the hot water I is supplied to both the thickener 1 and the dehydrator 2, and is mixed with, for example, the concentrated sludge B and the dehydrated sludge C, which are organic sludge, and directly heated. That is, in the present embodiment, the 4 th drain pipe 26, the 2 nd pump 27, the 1 st heat exchanger 20, and the hot water boiler 11 as the 2 nd heat exchanger constitute a hot water supply means. The direct heating of the organic sludge with the hot water I may be performed by supplying the hot water I to a space between the strainer and the casing, for example, in the case where the dehydrator 2 is a screw press.

As described above, the organic sludge of the concentrated sludge B and the dewatered sludge C is heated by the hot water I, so that the viscosity of the organic sludge is reduced and the water contained in the organic sludge is separated by thermal denaturation of proteins. In addition, since the water separated from the organic sludge is discharged together with the water discharged from the thickener 1 and the dehydrator 2, the water content of the organic sludge can be reduced. In addition, since the viscosity of the organic sludge decreases and the filtration resistance decreases, the water separated from the organic sludge can be easily discharged.

In the organic sludge treatment facility and the treatment method configured as described above, since the hot water I supplied to the thickener 1 and the dehydrator 2 is the 2 nd cooling water H2 obtained by cooling and desulfurizing the combustion exhaust gas E, which has been treated with the acidic gas by the 1 st cooling water H1 and collected with the dust, in the 1 st cooling section 12A in the flue gas treatment tower 12 in the 2 nd cooling section 12B, it is possible to avoid mixing the insoluble solid content (SS content) in the dust of the combustion exhaust gas E, the unreacted alkali content in the 1 st cooling water H1, or the acidic gas component with the concentrated sludge B and the dehydrated sludge C. Therefore, the condensed sludge B and the dewatered sludge C can be prevented from being deteriorated by insoluble solid components (SS components), unreacted alkali components, and acidic gas components.

Further, the alkaline component used for the acid gas treatment of the combustion exhaust gas E is contained in the 1 st cooling water H1 for cooling and desulfurizing the combustion exhaust gas E in the 1 st cooling unit 12A. Further, since the 1 st cooling water H1 is circulated and used in the 1 st cooling part 12A in the lower part of the flue gas treatment tower 12, it is possible to prevent unreacted alkali components from being discharged and to prevent the amount of alkali components used from increasing.

Further, since the supply amount of the 2 nd cooling water H2 in the 2 nd cooling unit 12B is about several times to ten times larger than the circulation amount of the 1 st cooling water H1 in the 1 st cooling unit 12A, it is not necessary to circulate and reuse the hot water I supplied to the thickener 1 and the dehydrator 2 and directly contacted with the organic sludge of the concentrated sludge B and the dehydrated sludge C. Therefore, the amount of the hot water I (2 nd cooling water H2) used can be prevented from increasing more than necessary.

In the present embodiment, the temperature of the 2 nd cooling water H2 which is retained in the drain water separation section 21 and discharged from the 4 th drain pipe 26 is about 70 ℃ which is a sufficiently high temperature, and therefore, it is also possible to directly supply the same to the thickener 1 and the dehydrator 2 by the 2 nd pump 27, but when the temperature of the combustion exhaust gas E generated in the incinerator 3 is low, the 2 nd cooling water H2 having such a high temperature cannot be supplied as the hot water I, and it may be difficult to effectively reduce the water content of the concentrated sludge B and the dehydrated sludge C.

In contrast, in the present embodiment, the 1 st heat exchanger 20 is provided in the hot water supply mechanism, and the 1 st heat exchanger 20 indirectly exchanges heat between the 1 st cooling water H1 that cools the combustion exhaust gas E in the 1 st cooling unit 12A and the 2 nd cooling water H2 that cools the combustion exhaust gas E in the 2 nd cooling unit 12B and supplies the cooled combustion exhaust gas E as the hot water I to the thickener 1 and the dehydrator 2. Therefore, the 1 st cooling water having a high temperature after cooling the combustion exhaust gas E supplied to the 1 st cooling unit 12A in a state of a higher temperature than the 2 nd cooling unit 12B can increase the temperature of the 2 nd cooling water H2 supplied as the hot water I by 1.

In the present embodiment, the 2 nd hot water supply means also includes a hot water boiler 11 as the 2 nd heat exchanger in the above-described hot water supply means, and the hot water boiler 11 indirectly exchanges heat between the combustion exhaust gas E supplied to the flue gas treatment tower 12 and the 2 nd cooling water H2 that cools the combustion exhaust gas E in the 2 nd cooling unit 12B, so that the temperature of the 2 nd cooling water H2 supplied as the hot water I to the thickener 1 or the dehydrator 2 can be raised by the 2 nd heat exchanger.

The temperature of the 2 nd cooling water H2 supplied as the hot water I to the thickener 1 or dehydrator 2 by the hot water supply means is preferably 50 ℃ or higher and less than 100 ℃. If the temperature of the 2 nd cooling water H2 is less than 50 ℃, there is a possibility that the viscosity of the organic sludge is lowered and the water content is lowered by the water separation, and on the other hand, if the temperature of the hot water I exceeds 100 ℃, the treatment may be difficult. The temperature of the 2 nd cooling water H2 supplied as the hot water I is more preferably in the range of 60 ℃ to 90 ℃.

In the present embodiment, the hot water I is supplied to both the thickener 1 and the dehydrator 2, but may be supplied to only one of them. Further, when the temperature of the hot water I is sufficiently high, etc., the hot water I may be supplied to both the thickener 1 and the dehydrator 2, and the moisture (filtrate) separated from the dewatered sludge C by the dehydrator 2 together with the hot water I may be supplied to the thickener 1, or when the hot water I is supplied only to the dehydrator 2 without being supplied to the thickener 1, the moisture (filtrate) separated from the dewatered sludge C by the dehydrator 2 together with the hot water I may be supplied to the thickener 1.

[ INDUSTRIAL APPLICABILITY ]

By applying the apparatus and method for treating organic sludge of the present invention to this field, when warm water is directly supplied to the thickener and dehydrator for heating, the wastewater discharged from the flue gas treatment tower can be supplied as warm water, and the sludge is not deteriorated by the warm water, and an increase in the amount of alkali used in the flue gas treatment tower can be prevented.

[ notation ] to show

1 thickener

2 dewaterer

3 incinerator

4 waste heat boiler

5 Heat utilization apparatus

6 dust collector

7 supercharger

8-preheater for preventing white smoke

9 Fan

11 Warm water boiler (2 nd heat exchanger)

12 flue gas treatment tower

12A 1 st Cooling section

12B 2 nd cooling part

12C chimney

13 circulation tank

14 water collecting part

15 supply part

19 st pump

20 st 1 heat exchanger

21 drainage separation part

25 drainage tank

26 th 4 water discharge pipe

27 nd 2 nd pump

A coagulated sludge

B concentrated sludge

C dewatered sludge

D air for combustion

E combustion exhaust gas

H1 cooling water No. 1

H2 No. 2 cooling water

I warm water