JP2003164730A - Exhaust gas desulfurization equipment - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide an exhaust gas desulfurization equipment for removing sulfur oxide (SOx) in exhaust gas, for example, discharged from a boiler or an incinerator. <P>SOLUTION: An introducing port 5 of exhaust gas 100 containing sulfur oxide is provided to the side wall of a desulfurization column 4 of this exhaust gas desulfurization equipment and the discharge port 12 of the exhaust gas 100 is provided to the upper part of the desulfurization column 4. A water sprinkling nozzle 7 being a feeder of water for forming sulfuric acid is provided above a catalyst bed 6 comprising an activated carbon fiber bed provided in the desulfurization column 4 and a rectifier plate 42 having dispersing holes 41 for rectifying the exhaust gas 100 is arranged to the lower part of the desulfurization column 4 an the moisture quantity (moisture/humidifying exhaust gas) at the time of contact of the exhaust gas 100 supplied into the desulfurization column with the catalyst bed 6 is not less than saturated steam quantity. <P>COPYRIGHT: (C)2003,JPO

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a flue gas for removing sulfur oxides (SOx) in exhaust gas discharged from a boiler burning a fuel such as coal or heavy oil, a gas turbine, an engine or an incinerator. Regarding a processing device.

[0002]

BACKGROUND ART Conventionally, as a method for removing sulfur oxides in exhaust gas, a lime-gypsum method has been adopted in which limestone or slaked lime slurry is used as an absorbent and the sulfur content in the exhaust gas is recovered as gypsum. As another method, a dry method of adsorption with activated carbon is known.

In the above-mentioned conventional lime-gypsum method, limestone or slaked lime slurry is sprayed into the exhaust gas to simultaneously perform humidification cooling of the exhaust gas and absorption of SOx. Therefore, it is necessary to circulate a large amount of slurry, and power and a large amount of water for circulating the slurry are required.

On the other hand, in the dry method, a large amount of heat is required because the sulfur content adsorbed on the activated carbon is desorbed by heating. Moreover, in the case of this method, disposal of the generated dilute sulfuric acid, wear of the adsorbent, and the like pose problems. Therefore, it is possible to obtain a high concentration of sulfuric acid at the time of desulfurization without using a sulfur oxide absorbent and large-scale equipment, and to desulfurize to generate gypsum with a small amount of power using the same equipment as the lime gypsum method. The advent of devices is desired.

Therefore, as a device for removing SOx in exhaust gas, SOx in exhaust gas is adsorbed on a porous carbon material such as activated carbon fiber, and oxygen contained in the exhaust gas is utilized by utilizing the catalytic action of the porous carbon material. To oxidize the sulfur component,
It has been proposed to absorb this in water and remove it as sulfuric acid from the porous carbon material (JP-A-11-3473).
No. 50).

In a conventional flue gas treatment apparatus using this activated carbon fiber, an activated carbon fiber tank for adsorbing SOx in the exhaust gas is arranged in the adsorption tower, and the exhaust gas is supplied from below to activate the activated carbon fiber. SO ₂ is oxidized to SO ₃ on the surface of SO ₃ , and the generated SO ₃ reacts with the supplied water to generate sulfuric acid (H ₂ S
O ₄ ) is generated.

Here, the gas amount of the exhaust gas from the boiler that burns fuel such as coal and heavy oil is enormous, and it is necessary to improve the desulfurization efficiency when a large amount of this enormous exhaust gas is treated. Become. Therefore, simply increasing the size of the adsorption tower is essential, but it is desired that the desulfurization reaction of the activated carbon fibers be efficient and that the desulfurization system have a compact device configuration.

Further, in order to carry out the catalytic action efficiently, the reaction is optimized and S which is obtained by oxidizing SO ₂ in the exhaust gas is used.
O ₃ needs to be efficiently removed using water, and
In order to avoid increasing the size of auxiliary equipment for supplying the water, it is necessary to uniformly add water with the minimum necessary amount of water.

In view of the above problems, it is an object of the present invention to provide a flue gas desulfurization apparatus which is highly efficient in compacting a desulfurization reaction of activated carbon fibers, has a simple desulfurization system, and is highly efficient.

[0010]

A first invention for solving the above-mentioned problems is to provide a catalyst layer formed of an activated carbon fiber layer, which is provided in an apparatus tower through which exhaust gas containing sulfur oxide flows, In a flue gas treatment apparatus provided in the apparatus tower and comprising a water supply means for supplying water for sulfuric acid generation to the catalyst layer, the amount of water when the exhaust gas supplied into the apparatus tower and the catalyst layer come into contact with each other. In the flue gas desulfurization device, which is characterized by having a saturated steam amount or more.

A second invention is characterized in that, in the first invention, the water content (water content / humidified exhaust gas) when the exhaust gas comes into contact with the catalyst layer is a saturated water vapor content + 0.5 to 10% by volume. And the flue gas desulfurization equipment.

A third invention is the same as the first or second invention, wherein the saturated water vapor amount is 7.3% by volume at 40 ° C. and 50 ° C.
It is 12.2% by volume or 19.7% by volume at 60 ° C.

A fourth aspect of the present invention is the fuel cell system according to any one of the first to third aspects, wherein the cooling temperature of the above-mentioned humidification cooling is 40 to 60 ° C.
The flue gas desulfurization apparatus is characterized in that

A fifth invention is the flue gas desulfurization apparatus according to any one of the first to fourth inventions, wherein the mist particle size in the exhaust gas for the above-mentioned humidification cooling is 10 to 150 μm. is there.

A sixth invention is characterized in that, in any one of the first to fifth inventions, a flow rate of the humidified and cooled exhaust gas into the apparatus tower is 0.5 to 10 m / s. It is in a flue gas desulfurizer.

A seventh aspect of the present invention is the flue gas desulfurization apparatus according to any one of the first to sixth aspects, wherein the cooling water supplied from the water supply means has a particle size of 100 to 1000 μm.

An eighth invention is the exhaust gas according to any one of the first to seventh inventions, characterized in that the amount of the added water supplied from the water supply means is 5 to 50 ml / m ^{3 of} exhaust gas. It is in a smoke desulfurizer.

A ninth aspect of the present invention is the flue gas desulfurization apparatus according to the first aspect, characterized in that the catalyst layers are laminated in a plurality of stages by a supporting device.

A tenth aspect of the present invention is the fuel cell system according to any one of the first to ninth aspects, wherein the exhaust gas containing the sulfur oxide is provided in the upper and lower portions thereof and above the catalyst layer provided in the tower. It is a flue gas desulfurization device characterized by comprising a water supply device for producing sulfuric acid.

An eleventh aspect of the present invention is directed to a flue gas desulfurization apparatus according to any one of the first to tenth aspects, and a gypsum reaction tank for reacting dilute sulfuric acid from the flue gas desulfurization apparatus with lime slurry to obtain gypsum slurry. A flue gas desulfurization system comprising: a dehydrator for separating gypsum obtained from the gypsum reaction tank to obtain gypsum.

A twelfth invention is provided with a flue gas desulfurization system according to any one of the first to eleventh aspects and a concentration tank for concentrating the dilute sulfuric acid obtained by the desulfurization system. It is in.

A thirteenth invention is the fuel cell system according to the eleventh or twelfth invention, wherein the exhaust gas is a gas discharged from a boiler, a gas turbine, an engine and various incinerators, and is provided with a soot dust removing means for removing soot dust in the exhaust gas. The flue gas desulfurization system is characterized by the following.

[0023]

BEST MODE FOR CARRYING OUT THE INVENTION Embodiments of the flue gas desulfurization apparatus according to the present invention will be described below, but the present invention is not limited to these embodiments.

First, an exhaust gas treatment system equipped with a smoke treatment device will be described with reference to FIGS. 1 and 2.

The exhaust gas treatment system shown in FIG. 1 converts sulfur oxides in exhaust gas into sulfuric acid by desulfurization in a desulfurizer. As shown in FIG. 1, a boiler 1 for generating steam for driving a steam turbine and an exhaust gas 10 from the boiler 1 are generated.
The dust remover 2 for removing the soot and dust in the exhaust gas 0, the pushing fan 3 for supplying the exhaust gas from which dust has been removed into the desulfurization tower 4, and the exhaust gas 100 which has been cooled and increased in the preceding stage (or in the tower) for supplying to the desulfurization tower 4. A humidification / cooling device 16 for humidifying and a catalyst layer 6 are provided inside, and exhaust gas 100 is supplied from an inlet 5 on the lower side wall of the tower, and water is supplied from above the catalyst layer 6 by a water spray nozzle 7. A desulfurization tower 4 for performing a desulfurization reaction of SOx in exhaust gas to diluted sulfuric acid (H ₂ SO ₄ ), a chimney 13 for discharging the purified exhaust gas desulfurized to the outside from a discharge port 12 at the top of the tower, and a discharge from the desulfurization tower 4 A sulfuric acid tank 11 for storing dilute sulfuric acid via the pump 10 is provided. If necessary, a mist eliminator 19 may be provided in the line for discharging the purified exhaust gas discharged from the desulfurization tower 4 to separate water in the exhaust gas.

Here, in the boiler 1, for example, fuel f such as coal or heavy oil is burned in the furnace in order to generate steam for driving a steam turbine (not shown) of the thermal power generation facility. There is. The exhaust gas of the boiler 1 contains sulfur oxides (SOx), and the exhaust gas is denitrated by a denitration device (not shown), cooled by a gas gas heater, and then dedusted by a dust collector 2.

The dust-removed exhaust gas 100 is introduced into the desulfurization tower 4 from the inlet 5 of the lower side wall by the pushing fan 3. A catalyst layer 6 formed of an activated carbon fiber layer is provided inside the desulfurization tower 4, and water for sulfuric acid generation is supplied to the catalyst layer 6 from a water supply means 17. SOx is reacted and removed from the exhaust gas 100 by passing the exhaust gas from the lower part into the inside of the catalyst layer 6 supplied with water from the upper part. The exhaust gas that has passed through the catalyst layer 6 is discharged from the discharge port 12 and the stack 1
3 is released to the atmosphere.

The catalyst layer 6 has a catalyst composed of a plurality of activated carbon fiber layers, and the desulfurization reaction occurs on the surface of each activated carbon fiber layer, for example, by the following reaction. This reaction mechanism is shown in FIG. That is, as shown in FIG. 11, (1) Adsorption of sulfur dioxide SO ₂ in the exhaust gas 100 onto the activated carbon fiber layer 101 of the catalyst. (2) Adsorbed sulfur dioxide SO ₂ and oxygen O in exhaust gas
Oxidation to sulfur trioxide SO ₃ by reaction with ₂ (can be supplied separately). (3) Generation of sulfuric acid H ₂ SO ₄ by dissolving oxidized sulfur trioxide SO ₃ in water H ₂ O. (4) Activated carbon fiber layer 101 of generated sulfuric acid H ₂ SO ₄
Departure from.

The reaction formula at this time is as follows. SO ₂ + 1 / 2O ₂ + H ₂ O → H ₂ SO ₄

The sulfuric acid H ₂ SO _{4 which} has been removed by the above reaction becomes dilute sulfuric acid and is discharged to the sulfuric acid tank 11 via the discharge pump 10. In this way, sulfur dioxide SO ₂ in the exhaust gas 100 is adsorbed and oxidized in the activated carbon fiber layer of the catalyst layer 6 and reacted with water H ₂ O to generate sulfuric acid H ₂ SO ₄ and removed and removed. By doing so, the desulfurization of the exhaust gas flow is performed.

FIG. 12 shows a comparison in the desulfurization reaction between the activated carbon fiber and the activated carbon according to the present invention. Here, FIG. 12 (A) shows activated carbon fibers, and FIG. 12 (B)
FIG. 3 is a schematic diagram showing SO ₂ gas adsorption and sulfuric acid desorption of activated carbon. As shown in FIG. 12 (A), the activated carbon fiber layer 10
1 has fine micropores 102 having a size (thickness) of 1 to 20 μm and a specific surface area of 700 to 25.
00 m ² / g, outer surface area 0.2 to 2.0 m ² / g, pore diameter of pore 102 is 2 nm or less. On the other hand, FIG.
As shown in (B), on the surface of the activated carbon 200, the mesopores 202 are formed inside the macropores 201, and the micropores 203 are slightly present inside the mesopores 202, and their size (thickness) is 1 to 3 mm. , The specific surface area is 900-1
200m ² / g, it is the external surface area ~0.001m ² / g.

The mechanism of desulfurization is shown in FIG. Here, in the activated carbon fiber layer 101 of FIG.
The gas phase is in direct contact with the micropore 102, and SO ₂
The gas diffusion / adsorption step and the generated sulfuric acid discharge step can be performed promptly. Also, there is little diffusion resistance,
The amount of sulfuric acid remaining on the surface is also extremely small. On the other hand, as shown in FIG. 13 (B), in the case of activated carbon 200, in addition to having a small number of micropores, in order to reach from the gas phase to the micropores 203, the macropores 201
It is necessary to pass through and Mesopore 202 in order,
Sulfuric acid passes through the mesopore 202 and the macropore 201 in order and is then discharged. In addition, micropore 20
Since it is not easy to desorb sulfuric acid from 3, the residual ratio becomes large and the desulfurization efficiency becomes poor.

Here, an example of the activated carbon fiber used in the present invention and an example of its production are shown below. Examples of the activated carbon fiber used in the present invention include pitch-based activated carbon fiber, polyacrylonitrile-based activated carbon fiber, phenol-based activated carbon fiber, and cellulose-based activated carbon fiber, but the present invention is not limited thereto. However, the activated carbon fiber is not limited as long as it is an activated carbon fiber having the above-mentioned catalytic action.

A specific production example is shown below. <Specific Example 1> Phenol-based activated carbon fiber ("Kractive-20", manufactured by Kuraray Chemical Co., Ltd.) was used in a nitrogen atmosphere at a temperature range of 900 to 1,200 ° C.
Bake for hours. <Specific Example 2> Using polyacrylonitrile-based activated carbon fiber ("FX-600", manufactured by Toho Rayon Co., Ltd.),
This is fired in a nitrogen atmosphere within a temperature range of 900 to 1,200 ° C. for 1 hour.

Next, another example of another exhaust gas treatment system is shown in FIG. The exhaust gas treatment system of FIG. 2 is for producing gypsum by converting sulfur oxides in the exhaust gas into sulfuric acid by desulfurization in a desulfurizer and supplying lime slurry to the sulfuric acid. As shown in FIG. 2, a boiler 1 that generates steam for driving a steam turbine, and an exhaust gas 100 from the boiler 1
A dust remover 2 that removes soot and dust therein, a pushing fan 3 that supplies the exhaust gas from which dust has been removed into the desulfurization tower 4, and a humidification that cools and humidifies the exhaust gas 100 before or within the desulfurization tower. The cooling device 16 and the catalyst layer 6 are provided inside, and the exhaust gas 100 is supplied from the inlet 5 on the lower side wall of the tower,
Water is supplied from above the catalyst layer 6 with a water sprinkling nozzle to desulfurize the SOx in the exhaust gas to desulfurize it to dilute sulfuric acid (H ₂ SO ₄ ), and the purified exhaust gas desulfurized from the outlet 12 at the top of the tower. A chimney 13 to be discharged to the outside, a gypsum reaction tank 52 for storing dilute sulfuric acid (H ₂ SO ₄ ) from the desulfurization tower 4 via the discharge pump 10 and supplying a lime slurry 51 to deposit gypsum, and a gypsum sedimentation Settling tank (thickener) 5
3 and a dehydrator 56 for removing water from the gypsum slurry 54 as drainage (filtrate) 57 to obtain gypsum 55.

In the system of FIG. 1, the sulfuric acid obtained by desulfurization is used as it is, but in the system of FIG. 2, lime slurry is supplied to sulfuric acid to obtain gypsum slurry, and then dehydration is performed. It is then used as plaster.

The desulfurization apparatus used in FIGS. 1 and 2 is common, and the structure of the flue gas desulfurization apparatus will be described below with reference to FIG.

[Structure of Flue Gas Desulfurization Device] As shown in FIG. 3, the flue gas desulfurization device includes an exhaust gas 10 containing sulfur oxides.
0 has an inlet port 5 of 0 on the side wall (or lower part) of the above apparatus tower,
A sprinkler nozzle 7 serving as a water supply device for producing sulfuric acid is provided above a catalyst layer 6 formed of an activated carbon fiber layer provided in the desulfurization tower 4, and exhaust gas supplied upstream of the catalyst. Rectifier plate 42 having dispersion holes 41 for rectifying 100
Is provided.

The structure of the catalyst layer 6 is shown in FIGS. 4 is a perspective view of the catalyst layer, FIG. 5 is a front view of the catalyst layer, and FIG. 6 is a plan view of the catalyst layer. As shown in these drawings, in the activated carbon fiber layer 20 forming one unit of the catalyst layer 6, a flat plate-shaped active carbon fiber sheet 21 and a corrugated corrugated plate activated carbon fiber sheet 22 are alternately laminated. Thus, the linear space formed therebetween becomes the passage 15 and the passage 15 extends vertically. The flat plate activated carbon fiber sheet 21 and the corrugated plate activated carbon fiber sheet 22 are plate-shaped, and the corrugated plate activated carbon fiber sheet 22 is corrugated by, for example, a corrugator. Alternatively, the exhaust gas may be formed into a shape such that the exhaust gas passes in parallel to the activated carbon fiber sheet, such as a honeycomb shape.

Then, water is sprayed and supplied from the water spray nozzle 7 and the exhaust gas 100 is sent from below, and the water flowing through the activated carbon fiber layer 20 has a particle size of about several mm and falls to the lower part. Since the exhaust gas 100 flows through the relatively small passage 15 formed by alternately stacking the flat plate activated carbon fiber sheets 21 and the corrugated plate activated carbon fiber sheets 22, an increase in pressure loss is suppressed. There is.

The activated carbon fiber layer 2 shown in FIGS.
No. 0 has a V-shaped corrugated plate shape because the corrugated plate activated carbon fiber sheet 22 has a V-shaped cross-sectional shape, but the present invention is not limited to this. For example, as shown in FIG. As shown, a U-shaped corrugated plate activated carbon fiber sheet 31 may be formed by continuously forming a U-shaped corrugation. In addition, FIG.
As shown in FIG. 7, the flat-plate activated carbon fiber sheet 21 and the U-shaped corrugated activated carbon fiber sheet 31 may have the corrugated convex portions laminated in the same direction, and as shown in FIG. The U-shaped corrugated plate activated carbon fiber sheet 31 may be laminated on both sides of the flat plate activated carbon fiber sheet 21 so that the convex portions protrude. Instead of the flat plate and the corrugated shape, the corrugated parts may be adhered and laminated.

Further, as shown in FIG.
The V-shaped corrugated sheet activated carbon fiber sheet 31 may be provided with finer irregularities 32.

The catalyst layer is arranged in the desulfurization tower as follows. For example, as shown in FIG.
The activated carbon fiber layer 20 laminated inside is filled to form a catalyst layer (for example, height is 0.5 m to 4 m) 42, and the catalyst layer 42 is installed in the desulfurization tower 4 by a lifting means such as a crane or the like. I am trying.

9 and 10 show a case 43 in which two layers of the catalyst layers 42 are packed in two layers. Furthermore, you may make it laminate | stack a 3-5 layer and multiple layers. 9 shows a plan view and FIG. 10 shows a side view thereof.

Here, in the present invention, the amount of water (moisture / humidified exhaust gas) when the exhaust gas in the desulfurization tower 4 of the exhaust gas desulfurization apparatus comes into contact with the catalyst layer is saturated steam amount + 0.5 to 10, preferably It is preferable that the saturated water vapor amount + 1.0 to 1.5% by volume. The saturated water vapor amount is, for example, 12.2% by volume (50 ° C.) at 50 ° C. The saturated steam amount at 40 ° C. is 7.3% by volume, and the saturated steam amount at 60 ° C. is 19.7% by volume. This is because the desorption of sulfuric acid in the desulfurization action as described above is not favorably performed at a saturated amount or less.

The cooling temperature for the humidification cooling may be appropriately determined depending on the relationship between the temperature of the exhaust gas and the water content, but is preferably 40 to 60 ° C., for example. This is because when the temperature exceeds 60 ° C., the evaporation amount of water increases, the amount of water supplied increases, the treatment cost increases, and when the water is insufficient, the desulfurization performance decreases. On the other hand, when the temperature is lower than 40 ° C., it is substantially impossible to lower the temperature below this by general humidification cooling of exhaust gas.

That is, when the exhaust gas 100 is supplied into the desulfurization tower 4 in a state where the moisture is saturated by the humidification cooling of the humidification cooling device 10, and when the exhaust gas 100 comes into contact with the catalyst layer 6, the exhaust gas moisture amount is saturated. By setting the amount of water vapor + 0.5 to 10 (preferably the amount of saturated water vapor + 1.0 to 1.5% by volume), the desorption of SO ₃ generated by the oxidation of SO _{2 on} the catalyst surface proceeds rapidly. Since sulfuric acid does not remain on the surface of the activated carbon fiber, the active sites are effectively used and the desulfurization efficiency is improved.

On the other hand, unlike FIG. 3, when the exhaust gas 100 is lowered from above the tower, the mist is also supplied to the catalyst layer 6, so the amount of sprinkling should be made smaller than in the case shown in FIG. You may be able to In any case, it is essential that the exhaust gas be saturated steam or more, and in particular, by setting the saturated steam amount +1.0 to 1.5% by volume, extremely efficient water replenishment can be achieved by the activity of the catalyst. It can be applied to the surface of carbon fibers. That is, it is insufficient to desorb SO _{3 obtained} by oxidizing SO ₂ as sulfuric acid by water with the above-mentioned saturated steam amount alone, and when the saturated steam amount + 1.5% by volume is exceeded, the water amount becomes excessive. As a result, the diluted sulfuric acid becomes thinner, and the amount of water used increases, which is not preferable.

Although the relationship between saturated steam and steam mist is not clear, when SO _{3 obtained} by oxidizing SO _{2 on the} surface of activated carbon fiber is discharged as sulfuric acid due to water, if the water content is insufficient, it is discharged as sulfuric acid. And the subsequent oxidation of SO ₂ becomes insufficient. On the other hand, if the water content is excessive, the sulfuric acid will be diluted. Furthermore, if the water content becomes excessive and, for example, if a water film or water wall is formed on the surface of the activated carbon fiber, it will cover the active sites of the activated carbon fiber, and it will not be able to catalyze the oxidation of SO ₂ and will not be desulfurized. However, the desulfurization efficiency will be reduced. Therefore, by setting the water content (water content / humidified exhaust gas) when the exhaust gas comes into contact with the catalyst layer to be the saturated water vapor content + 1.0 to 1.5% by volume as in the present invention, water droplets are intermittently formed into beads. As a result, the water is supplied to the surface of the activated carbon fiber in an appropriate amount, the sulfuric acid is desorbed efficiently, and as a result, the exhaust gas is desulfurized effectively.

The mist particle size in the exhaust gas that has been humidified and cooled is preferably 10 to 150 μm. This is 1
If it is less than 0 μm, high water pressure, high air pressure, and large amount of air are required, which is not preferable. On the other hand, if it exceeds 150 μm, moisture is attached to the inside of the pipe, which is not preferable.

Here, a mist catcher (not shown) for replenishing the mist may be provided. By providing this catcher, it is possible to prevent water from being brought into the desulfurization tower, and the sulfuric acid produced by desulfurization in the catalyst layer will not be diluted.

The flow rate of the above-mentioned humidified and cooled exhaust gas 100 into the apparatus tower is 0.5 to 10 m / s, preferably 1 to
3m / s is recommended. This is because pressure loss increases when the flow velocity is faster than 10 m / s, while 0.5 m / s.
If it is less than 1, the installation area becomes large and both are not preferable.

The particle size of the cooling water supplied from the water spray nozzle 7 which is the water supply means is preferably 100 to 1000 μm. This is because when the amount exceeds the above range, it is not possible to effectively supply water on the surface of the activated carbon fiber and the desorption action of sulfuric acid does not proceed well, which is not preferable. Especially, when the exhaust gas is supplied from the lower side, mist-like water from the sprinkling nozzle rises, and good water supply cannot be performed. On the other hand, if the water particle size is too large, a water wall state is formed, and although sulfuric acid can be desorbed, the desulfurization reaction does not proceed because the active sites do not surface, which is not preferable.

For this purpose, the amount of added water supplied from the water supply means is preferably 5 to 1 when the flow rate of the exhaust gas 100 into the apparatus tower is 0.5 to 10 m / s.
It is recommended to use exhaust gas of 00 ml / m ³ .

[0055]

As described above, according to the present invention, the catalyst formed by the activated carbon fiber layer is provided in the apparatus tower through which the exhaust gas containing sulfur oxide flows, and the inside of the apparatus tower. In the flue gas treatment device provided with a water supply means for supplying water for producing sulfuric acid to the catalyst layer, the amount of water when the exhaust gas supplied into the device tower and the catalyst layer come into contact with saturated steam. Since the amount is at least the amount, the desulfurization reaction with the activated carbon fiber proceeds properly and the supply of water used is extremely small.

[Brief description of drawings]

FIG. 1 is a schematic diagram of an exhaust gas treatment system (sulfuric acid production) including a flue gas treatment apparatus according to the present embodiment.

FIG. 2 is a schematic diagram of an exhaust gas treatment system (gypsum production) including the smoke emission treatment device according to the present embodiment.

FIG. 3 is a configuration diagram of a flue gas desulfurization apparatus according to the present embodiment.

FIG. 4 is a perspective view of a catalyst layer.

FIG. 5 is a plan view of a catalyst layer.

FIG. 6 is a front view of a catalyst layer.

FIG. 7 is a schematic sectional view of a catalyst layer.

FIG. 8 is a perspective view of a catalyst layer supported by a frame.

FIG. 9 is a plan view in which a catalyst layer supported by a frame is housed in a case.

FIG. 10 is a side view in which a catalyst layer supported by a frame is housed in a case.

FIG. 11 is a view showing a mechanism of desulfurization of activated carbon fiber.

FIG. 12 is a configuration diagram of activated carbon fibers (A) and activated carbon (B).

FIG. 13 is a diagram showing a mechanism of desulfurization of activated carbon fiber (A) and activated carbon (B).

[Explanation of symbols]

1 boiler 100 exhaust gas 2 dust remover 3 push fan 4 Desulfurization tower 5 entrance 6 Catalyst layer 7 watering nozzle 10 discharge pump 11 Sulfuric acid tank 12 outlet 13 chimney 16 Humidification cooling device 19 Mist Eliminator

   ─────────────────────────────────────────────────── ─── Continued front page    (72) Inventor Takashi Kurisaki             1-1 Satinoura Town, Nagasaki City, Nagasaki Prefecture Mitsubishi Heavy Industries             Nagasaki Shipyard Co., Ltd. (72) Inventor Keiko Kobayashi             2-5-3 Marunouchi, Chiyoda-ku, Tokyo             Hishi Heavy Industries Ltd. F term (reference) 3K070 DA03 DA23 DA25 DA37 DA37 DA42                 4D002 AA02 AC01 AC04 BA02 BA14                       CA01 CA07 DA35 DA44 EA09                       FA08                 4D048 AA02 AB01 AC10 BA05X                       BB02 BB03 BB08 CC32 CC36                       CC38 CC51 CC61 CD03 CD10                       DA01 DA05 DA06 DA08 DA13                       DA20                 4G076 AA14 AB02 AB26 BA24 BB02

Claims (13)

[Claims] 1. A catalyst layer provided in an apparatus tower through which an exhaust gas containing sulfur oxide flows and formed of an activated carbon fiber layer; and a catalyst layer provided in the apparatus tower, for producing sulfuric acid in the catalyst layer. In a flue gas treatment apparatus comprising water supply means for supplying water, the flue gas desulfurization is characterized in that the amount of water when the exhaust gas supplied into the apparatus tower and the catalyst layer come into contact with each other is equal to or more than the amount of saturated steam. apparatus. 2. The flue gas desulfurization according to claim 1, wherein the amount of water (moisture / humidified exhaust gas) when the exhaust gas comes into contact with the catalyst layer is a saturated steam amount +0.5 to 10% by volume. apparatus. 3. The method according to claim 1, wherein the saturated water vapor content is 7.3% by volume at 40 ° C. and 1 at 50 ° C.
2. A flue gas desulfurization apparatus which is 2.2% by volume or 19.7% by volume at 60 ° C. 4. The flue gas desulfurization device according to claim 1, wherein a cooling temperature of the humidification cooling is 40 to 60 ° C. 5. The mist particle size in the exhaust gas for the above-mentioned humidification cooling according to claim 1, wherein the mist particle size is 10 to 10.
A flue gas desulfurization device having a size of 150 μm. 6. The flue gas desulfurization apparatus according to claim 1, wherein a flow rate of the humidified and cooled exhaust gas into the apparatus tower is 0.5 to 10 m / s. . 7. The additive water supplied from the water supply means according to claim 1, wherein the particle size is 100 to 10
A flue gas desulfurization device characterized by having a diameter of 00 μm. 8. The supply amount of the additive water supplied from the water supply means according to claim 1, wherein the supply amount is 5 to 50.
Flue gas desulfurization equipment characterized by being ml / m ³ exhaust gas. 9. The flue gas desulfurization device according to claim 1, wherein the catalyst layers are laminated in a plurality of stages by a supporting device. 10. The water for generating sulfuric acid according to claim 1, wherein the exhaust gas containing sulfur oxide has inlets and outlets in the upper and lower portions and above the catalyst layer provided in the tower. A flue gas desulfurization device, characterized in that it is equipped with a feeder. 11. A gypsum reaction tank for obtaining a gypsum slurry by reacting the flue gas desulfurization device according to claim 1 with dilute sulfuric acid from the flue gas desulfurization device and lime slurry, and the gypsum reaction. A flue gas desulfurization system comprising: a dehydrator for separating water from gypsum obtained in a tank to obtain gypsum. 12. A flue gas desulfurization system comprising: the flue gas desulfurization device according to any one of claims 1 to 11; and a concentration tank for concentrating the dilute sulfuric acid obtained by the desulfurization device. 13. The exhaust gas according to claim 11 or 12, wherein the exhaust gas is a gas discharged from a boiler, a gas turbine, an engine and various incinerators, and a soot removing means for removing soot dust in the exhaust gas is provided. Flue gas desulfurization system.