WO2015045957A1

WO2015045957A1 - Air diffuser for seawater desulfurization and seawater desulfurization device provided with same

Info

Publication number: WO2015045957A1
Application number: PCT/JP2014/074409
Authority: WO
Inventors: 哲牛久; 康浩竹内; 岩下　浩一郎; 立人長安
Original assignee: 三菱日立パワーシステムズ株式会社
Priority date: 2013-09-30
Filing date: 2014-09-16
Publication date: 2015-04-02
Also published as: JP6313945B2; JP2015066526A; MY172570A

Abstract

An air diffuser (30) for seawater desulfurization is provided with air diffusing tubes (34) that are disposed within an oxidation tank (13) for seawater desulfurization, bring the sulfur component in exhaust gas (22) into contact with seawater, and supply air to acidic mixed seawater (24) that includes seawater (23) that has absorbed sulfur and that has arisen because of seawater desulfurization and an air supply tube (33) that feeds air from the outside by an air introduction means to the air diffusing tubes (34). The hole diameter (d) of holes (35) in the air diffusing tubes (34) is 5 mm or greater. The pitch (P₁) between holes (35, 35) in the air diffusing tubes (34) is 40 mm or greater, and the pitch (P₂) between the air diffusing tubes (34, 34) disposed on the air supply tube (33) is 500 mm or greater.

Description

Aeration device for seawater desulfurization and seawater desulfurization device provided with the same

The present invention relates to an aeration apparatus for seawater desulfurization and a seawater desulfurization apparatus including the same.

Conventionally, in a power plant using coal, crude oil or the like as fuel, combustion exhaust gas (hereinafter referred to as “exhaust gas”) discharged from a boiler is sulfur such as sulfur dioxide (SO ₂ ) contained in the exhaust gas. The oxide (SOx) is removed and then released to the atmosphere. As a desulfurization method of a flue gas desulfurization apparatus that performs such a desulfurization treatment, a lime gypsum method, a spray dryer method, a seawater method, and the like are known.

Among these, the flue gas desulfurization apparatus (hereinafter referred to as “seawater desulfurization apparatus”) employing the seawater method is a desulfurization system that uses seawater as an absorbent. In this system, for example, by supplying seawater and boiler exhaust gas into a desulfurization tower (absorption tower) having a cylindrical shape or a rectangular shape such as a substantially cylindrical shape, the seawater is used as an absorbing liquid to make a wet-based gas-liquid contact. Is generated to remove sulfur oxides.
The desulfurized seawater (spent seawater) used as the absorbent in the desulfurization tower described above is, for example, a part of the water channel when drained by flowing in a long water channel (Seawater Oxidation Treatment System; SOTS) with an open top. The carbon dioxide is deaerated (aerated) by aeration in which fine bubbles are discharged from an aeration apparatus (oxidation / aeration tank) installed on the bottom of the unit (Patent Documents 1 to 3).

JP 2006-055779 A JP 2009-028570 A JP 2009-028572 A

By the way, in plants with small boiler facilities, since the amount of SO _{2 in} the exhaust gas is small, the absorption of SO _{2 in} the sea water used in the flue gas desulfurization device is small, and oxygen in the air is supplied to the sea water. In order to dissolve it, air supply by a fine air supply means having fine holes (for example, 1.0 mm) for generating fine air is suitable.

However, when applying seawater desulfurization in a plant with a large boiler facility or a plant with a large amount of SO ₂ such as a large amount of sulfur (S) in the fuel, the pH of the seawater may not reach the optimum value for discharged seawater. is there.

Here, as a cause of lowering the pH, with S content in seawater is SO ₄ ^2-ions are the lysate of carbon dioxide generated by the seawater desulfurization (CO _2), the dissolved CO ₂ rapidly It needs to be removed.

In this case, in the case of decarboxylation by supplying from a conventional fine air supply means, it is necessary to supply a large amount of fine air, increasing in-house power and supplying a large amount of fine air. Therefore, there is a problem that a long passage for the oxidation tank is required and the equipment becomes enormous.

Therefore, when seawater desulfurization is applied to a plant with a large amount of SO ₂ in seawater desulfurization, the emergence of a seawater desulfurization apparatus capable of quickly removing CO ₂ is eagerly desired.

In view of the above problems, the present invention provides an aeration apparatus for seawater desulfurization that can quickly remove CO ₂ when applying seawater desulfurization in a plant with a large amount of SO ₂ , and a seawater desulfurization apparatus including the same. The task is to do.

The first invention of the present invention for solving the above-described problem is the absorption of sulfur content that is disposed in an oxidation tank for seawater desulfurization, and is produced by bringing the sulfur content in the exhaust gas into contact with seawater and desulfurizing the seawater. A diffuser pipe for supplying air to the oxidative mixed seawater containing seawater; and an air supply pipe for supplying air to the diffuser pipe from the outside by air introduction means, the hole diameter of the diffuser pipe being 5 mm or more, In the air diffuser for seawater desulfurization, the pitch between the holes of the trachea is 40 mm or more, and the pitch between the air diffusers arranged in the air supply pipe is 500 mm or more.

The second invention is an aeration apparatus for seawater desulfurization characterized in that, in the first invention, the flow velocity of the air discharged from the hole is 10 to 100 m / s.

The third invention is a seawater desulfurization device having the diffuser for seawater desulfurization of the first or second invention on the inlet side of the oxidation tank.

The fourth invention is a seawater desulfurization apparatus comprising the diffuser for seawater desulfurization according to the first or second invention on an inlet side and an outlet side of an oxidation tank.

According to the present invention, an aeration operation is performed in which a large amount of large air is supplied from a hole having a large pore diameter to expel dissolved CO ₂ in acidic mixed seawater in which desulfurization effluent and seawater are mixed from seawater. Therefore, in the case of applying seawater desulfurization in a plant in which decarbonation (aeration action) proceeds smoothly and has a high SO ₂ content, CO ₂ can be quickly removed.

FIG. 1 is a schematic diagram illustrating a configuration of a seawater desulfurization apparatus according to a first embodiment. FIG. 2 is a schematic view of a diffuser for seawater desulfurization. FIG. 3 is a cross-sectional view of an air supply pipe and a diffuser pipe disposed in the oxidation tank. FIG. 4 is a perspective view of the diffusing tube. FIG. 5A is a cross-sectional view of the diffusing tube. FIG. 5-2 is a cross-sectional view of the air diffuser. FIG. 6 is a perspective view of an air diffuser provided with a nozzle. FIG. 7 is a cross-sectional view of FIG. FIG. 8 is a schematic diagram illustrating the configuration of the desulfurization aeration apparatus according to the second embodiment. FIG. 9 is a graph showing the relationship between the amount of SO ₂ absorbed in the sulfur-absorbing seawater (ΔS) generated by seawater desulfurization / the amount of alkali (TA) in seawater used for seawater desulfurization and the amount of oxidized air. . FIG. 10 is a diagram showing the relationship between the air flow rate from the hole (horizontal axis), the oxidation rate (left vertical axis), and the oxidation rate per unit air amount (right vertical axis). FIG. 11 is a diagram showing the relationship between the pitch between the diffuser tubes and the oxidation rate.

Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings. In addition, this invention is not limited by this Example, Moreover, when there exists multiple Example, what comprises combining each Example is also included.

A seawater desulfurization apparatus provided with a diffuser for seawater desulfurization according to Embodiment 1 of the present invention will be described with reference to the drawings. FIG. 1 is a schematic diagram illustrating a configuration of a seawater desulfurization apparatus according to a first embodiment. As shown in FIG. 1, the seawater desulfurization apparatus 10 according to this embodiment includes a flue gas desulfurization absorption tower 11, an inlet side dilution mixing tank 12, an oxidation tank 13 that performs water quality recovery processing, and an outlet side dilution mixing tank 14. And have.

In the present embodiment, the seawater 15 used in the flue gas desulfurization absorption tower 11 and the seawater 15 used for water quality reforming in the oxidation tank 13 for performing water quality recovery processing are separately pumped and a condenser (not shown) in the boiler 21. In this case, the seawater before being discharged into the sea 16 after being used for cooling is used.

The seawater 15 for dilution is pumped up through the seawater supply line L ₁ by the pump P ₁₁ from the sea 16, a portion of the seawater 15a the inlet side dilution mixing tank 12 through a seawater supply line L ₂ by a pump P ₁₁ To be supplied. If necessary, dilute seawater supply line L ₃ is provided for supplying the seawater 15b for dilution at the outlet side dilution mixing tank 14.
In this embodiment, seawater after cooling from a condenser (not shown) is used. However, the present invention is not limited to this, and seawater pumped directly from the sea 16 by the pump P ₁₁ is used. It may be.

The flue gas desulfurization absorption tower 11 is a tower that purifies the exhaust gas 22 by gas-liquid contact between the exhaust gas 22 from the boiler 21 and the seawater 15. In the flue gas desulfurization absorption tower 11, the seawater 15 is ejected in a liquid column shape above the spray nozzle 11a, and the exhaust gas 22 and the supplied seawater 15 are brought into gas-liquid contact to perform desulfurization of sulfur in the exhaust gas 22. Yes. In the present embodiment, the spray nozzle 11a is a spray nozzle that ejects upward in a liquid column shape, but is not limited thereto, and may be sprayed downward in a shower shape.

That is, the exhaust gas 22 and the seawater 15 are brought into gas-liquid contact in the flue gas desulfurization absorption tower 11 to cause a reaction as shown in the following formula (I), and are contained in the form of SO ₂ or the like in the exhaust gas 22. The sulfur content such as SOx is absorbed by the seawater 15, and the sulfur content in the exhaust gas 22 is removed using the seawater 15.
SO ₂ (G) + H ₂ O → H ₂ SO ₃ (L) → HSO ₃ ⁻ + H ⁺ (I)

Due to this seawater desulfurization, H ₂ SO ₃ generated by the gas-liquid contact between the sea water 15 and the exhaust gas 22 is dissociated and hydrogen ions (H ⁺ ) are liberated in the sea water 15, so that the pH is lowered, and the sulfur-absorbing sea water 23 A large amount of sulfur is absorbed. For this reason, sulfur content absorption seawater 23 contains sulfur content in high concentration.

At this time, the pH of the sulfur-absorbing seawater 23 is, for example, about 3 to 6. And the sulfur content absorption seawater 23 which absorbed the sulfur content in the flue gas desulfurization absorption tower 11 is stored in the tower bottom part of the flue gas desulfurization absorption tower 11. The sulfur-absorbing seawater 23 stored at the bottom of the flue gas desulfurization absorption tower 11 is fed to the inlet side dilution / mixing tank 12 via the sulfur-absorbing seawater discharge line L ₄ .
The sulfur-absorbing seawater 23 supplied to the inlet side dilution / mixing tank 12 is mixed with the seawater 15 from the condenser and the seawater 15a for dilution supplied to the inlet side dilution / mixing tank 12, and diluted to be acidic mixed. It becomes seawater 24.

Further, the purified gas 25 desulfurized in the flue gas desulfurization absorption tower 11 is released from the chimney 26 into the atmosphere. A dust collecting means 27 is provided between the boiler 21 and the flue gas desulfurization absorption tower 11 to remove dust and the like in the exhaust gas 22.

The desulfurization rate of the exhaust gas 22 is determined by the ratio of the inlet SO ₂ concentration to the outlet SO ₂ concentration in the exhaust gas 22 supplied to the flue gas desulfurization absorption tower 11 (outlet SO ₂ concentration / inlet SO ₂ concentration), The seawater 15 and the sulfur-absorbing seawater 23 are separately adjusted based on the seawater properties.

In the flue gas desulfurization absorption tower 11, SO ₂ concentration meters for measuring the inlet SO ₂ concentration and the outlet SO ₂ concentration of the exhaust gas 22 are provided at the inlet and outlet of the exhaust gas 22.

Then, the acidic mixed seawater 24 in which the sulfur-absorbing seawater 23 and the seawater 15 are mixed is supplied to the oxidation tank 13 provided on the downstream side of the inlet side dilution mixing tank 12. The oxidation tank 13 is provided with a seawater desulfurization air diffuser 30 which is an aeration means for performing water quality recovery processing of the acidic mixed seawater 24.

The seawater desulfurization aeration apparatus 30 includes an oxidation air blower 32 that is an air introduction means for supplying air 31, an air supply pipe 33 that supplies the air 31, and an air diffusion pipe 34 that is branched from the air supply pipe 33. , And an ejection hole (not shown in FIG. 1) 35 for supplying the air 31 to the acidic mixed seawater 24 in the oxidation tank 13.

The external air 31 is sent from the hole 35 into the oxidation tank 13 through the air diffuser 34 by the oxidizing air blower 32, and the oxygen is dissolved as shown in the following formula (II). In the oxidation tank 13, the sulfur content in the acidic mixed seawater 24 comes into contact with the air 31, and an oxidation reaction of bisulfite ions (HSO ₃ ⁻ ) as shown in the following formulas (III) to (V) and bicarbonate ions (HCO ₃ ^- ) Decarboxylation reaction occurs, and the acidic mixed seawater 24 is recovered in water quality to become water quality recovered seawater 29 and discharged into the sea 16 via the discharge line L7.
O ₂ (G) → O ₂ (L) (II)
HSO ₃ ⁻ + 1 / 2O ₂ → SO ₄ ²⁻ + H ⁺ (III)
HCO ₃ ⁻ + H ⁺ → CO ₂ (G) + H ₂ O (IV)
CO ₃ ^2- + 2H ⁺ → CO ₂ (G) + H ₂ O (V)

As a result, the pH of the acidic mixed seawater 24 can be raised and the chemical oxygen demand (COD) can be reduced, and the pH, dissolved oxygen (DO) concentration, chemical oxygen demand (COD) of the water quality recovery seawater 29 can be reduced. ) Can be released to the sea 16 as a level that can be released.

Next, the diffuser for seawater desulfurization according to the present embodiment will be described with reference to FIGS. FIG. 2 is a schematic view of a diffuser for seawater desulfurization. FIG. 3 is a cross-sectional view of an air supply pipe and a diffuser pipe disposed in the oxidation tank. FIG. 4 is a perspective view of the diffusing tube. 5A and 5B are cross-sectional views of the air diffuser. FIG. 6 is a perspective view of an air diffuser provided with a nozzle. FIG. 7 is a cross-sectional view of FIG.

As shown in FIGS. 2 and 3, the seawater desulfurization air diffuser 30 is disposed in the oxidation tank 13 for seawater desulfurization, and is generated by bringing the sulfur content in the exhaust gas into contact with seawater and desulfurizing the seawater. A diffuser pipe 34 for supplying air to the acidic mixed seawater 24 containing the sulfur-absorbing seawater 23, an air supply pipe 33 for supplying air to the diffuser pipe 34 from the outside by air introduction means, and (nozzles) of the diffuser pipe 34 The hole diameter (d) of the holes 35 is 5 mm or more, preferably 5 mm to 50 mm, the pitch (P ₁ ) between the

holes

35, 35 of the air diffuser 34 is 40 mm or more, preferably 40 mm to 2000 mm, and the air supply pipe 33. The pitch (P ₂ ) between the diffusing

tubes

34, 34 arranged in the above is 500 mm or more, preferably 500 mm to 4500 mm (the test is 750 mm).

Here, the hole diameter (d) of the holes 35 of the diffuser tube 34 is 5 to 50 mm, the pitch (P ₁ ) between the

holes

35 and 35 is 40 to 2000 mm, and the pitch (P ₂ ) between the

diffuser tubes

34 and 34 is 500 to 500 mm. By setting the length to 4500 mm, large-diameter air can be discharged from the holes 35 into the acidic mixed seawater 24 in the oxidation tank 13.

In FIG. 2, the hole 35 is formed on the upper side of the diffuser tube 34, but in FIGS. 3 and 4, the hole 35 is formed on the lower side of the diffuser tube 34. As shown in FIG. 3, by forming the hole 35 on the lower side of the air diffuser 34, an upward flow is formed, which is more preferable.

Further, as shown in FIGS. 5-1 and 5-2, not only one hole 35 but also a plurality (three in FIG. 5-2) may be formed.

Further, as shown in FIGS. 6 and 7, a nozzle 36 may be installed in the hole 35, and the air 31 may be supplied into the oxidation tank 13 from the tip of the nozzle 36.

FIG. 9 is a diagram showing the relationship between the amount of SO ₂ absorbed in the sulfur-absorbing seawater 23 (ΔS) generated by seawater desulfurization / the amount of alkali (TA) in seawater 15 used for seawater desulfurization and the amount of oxidized air. It is.

As shown in FIG. 9, the relationship between the seawater properties of the sulfur-absorbing seawater 23 and the amount of alkali in the seawater 15 supplied for water quality modification (absorbed SO ₂ amount (ΔS) / alkaline amount in seawater (TA)). However, in the case of 0.2 or more, it is preferable to apply the diffuser of the present configuration for the decarboxylation treatment.

Here, the amount of alkali is obtained from the alkalinity in seawater 15 and seawater (amount). This alkalinity is obtained by separately collecting seawater 15 introduced from the condenser, and a value obtained by multiplying the obtained alkalinity by the amount of seawater introduced into the oxidation tank 13 is defined as the alkali amount.
The alkalinity refers to carbonate (H ₂ CO ₃ ), carbonate ion (CO ₃ ²⁻ ), bicarbonate ion (HCO ₃ ⁻ ), OH ⁻ , organic acid or weak acid salt (silica) contained in seawater 15. Acid, phosphoric acid, boric acid) and the like.

Therefore, as shown in FIG. 9, when the S concentration in the sulfur-absorbing seawater 23 is high, such as ΔS / TA = 0.2 or higher, the seawater desulfurization diffuser 30 of this embodiment is used to oxidize. By supplying a large amount of air into the acidic mixed seawater 24 in the tank 13, decarboxylation proceeds well.
Here, in the present invention, ΔS / TA = 0.2 or more is defined in order to satisfy predetermined seawater property required values such as pH and dissolved oxygen at the discharge point to the open sea. When the S concentration is low, it is often decisive to increase the dissolved oxygen concentration. In order to increase the dissolved oxygen concentration, the amount of required oxidized air is less because the fine air supply can refine the air. It will be over. On the other hand, when the S content concentration in the sulfur-absorbing seawater 23 is high, it often becomes decisive to decarboxylate the CO ₂ produced by the neutralization reaction from the seawater. Large diameter air supply that can send air at a time is more efficient. The relationship of the required air quantity between the fine air supply and the large-diameter air supply is reversed in the vicinity of ΔS / TA = 0.2.

FIG. 10 is a diagram showing the relationship between the air flow rate from the hole (horizontal axis), the oxidation rate (left vertical axis), and the oxidation rate per unit air amount (right vertical axis). Here, the dotted line and the solid line in FIG. 10 indicate the case of large-diameter air supply. In FIG. 10, the solid line represents the oxidation rate per unit air on the right vertical axis, and the dotted line represents the oxidation rate on the left vertical axis.
As shown in FIG. 10, the oxidation rate (left vertical axis) increases as the air flow rate from the hole increases, but the oxidation rate per unit air amount (right vertical axis) exceeds 100 m / s. And the oxidation rate decreases.

Therefore, as shown in FIG. 10, the flow velocity from the hole 35 of the air diffuser 34 is 10 m / s or more, preferably 10 m / s to 100 m / s.

FIG. 11 is a diagram showing the relationship between the pitch (P ₂ ) between the diffusing

tubes

34 and 34 and the oxidation rate. Here, the solid line in FIG. 11 shows the case of large-diameter air supply.
When the pitch (P ₂ ) between the

air diffusers

34 and 34 is too narrow, large air that rises interferes with each other and the aeration effect is reduced. Therefore, it is preferable to separate at least 500 mm or more.

Further, when the air ascending flow rate is determined and the hole diameter of the holes 35 and the pitch (P ₁ ) between the

holes

35 and 35 are determined, the pitch (P ₂ ) between the

air diffusers

34 and 34 is determined, but the maximum. It is good to be about 4500 mm.

As an example, the hole diameter (d) of the (nozzle) hole 35 of the air diffuser 34 is 15 mm, the pitch (P ₁ ) between the

holes

35 and 35 of the air diffuser 34 is 187.5 mm, and the air supply pipe 33 is disposed. When the pitch (P ₂ ) between the

air diffusers

34 and 34 is 750 mm and the flow rate is 10 m / s, the size of the oxidation tank 13 (the length of the passage) can be made smaller than before, and the hole 35 having a larger hole diameter. The large air 31 ejected from the air facilitates the decarboxylation in the acidic mixed seawater 24 in the oxidation tank 13.

That is, according to the present embodiment, since a large amount of large air 31 is supplied from the hole 35 having a large hole diameter, the aeration operation for expelling the dissolved CO ₂ in the acidic mixed seawater 24 from the seawater is performed. Carbonic acid (aeration action) proceeds smoothly.

In this embodiment, the water quality is not restored with fine air as in the past, but large air bubbles with a large capacity are supplied to recover the water quality by decarboxylating CO ₂ in seawater at once. Can be achieved.

Table 1 shows the aeration evaluation of the size of the hole diameter and the size of the oxidation tank when the air flow rate is 10 m / s and the absorbed SO ₂ amount (ΔS) / alkaline amount in seawater (TA) is 0.3.

As shown in Table 1, when the hole diameter is 5 mm or more, the size of the oxidation tank 13 (the length of the water channel) is large, and when the hole diameter is 10 mm or more, the size of the oxidation tank 13 is medium and the compactness is reduced. I was able to plan. When the hole diameter was 3 mm or less, the size of the oxidation tank 13 (the length of the water channel) became extra large, and it was not possible to reduce the size.
Here, as an example, the length and width of a large water channel are illustrated.
When acidic seawater having an absorbed SO ₂ amount (ΔS) / seawater alkali amount (TA) of 0.3 is treated in an oxidation tank having a width of 25 m to a pH of 6.0 and a dissolved oxygen saturation of 70% or more, the pore diameter is 5 mm. The length of the oxidation tank was 80 m, but when the hole diameter was 10 mm, the oxidation tank length could be reduced to 20 m. However, it has been found that if the hole diameter is 3 mm, the required oxidation tank length is 200 m, which makes it impossible to achieve compactness.

As a result, in the case of seawater desulfurization in a plant with a large amount of S, even if the dissolved oxygen (DO) consumed is returned to about 70% of the original seawater, the pH of the seawater does not reach the optimum value for the discharged seawater, When decarboxylation is performed by supplying fine air as in the past, it is necessary to supply a large amount of fine air, which increases the internal power of the air blower, and also supplies a large amount of fine air. However, the use of the seawater desulfurization air diffuser 30 as in this embodiment avoids an enormous amount of equipment.

As described above, the aeration apparatus 30 for seawater desulfurization as in the embodiment is disposed in the oxidation tank 13 and the

holes

35 and 35 are disposed at a constant pitch (P ₁ ), thereby oxidizing the oxidation air 31. It can be dispersed inside the tank 13. Further, by setting the oxidation air ejection flow rate and the installation interval to the predetermined ranges as in the present embodiment, the dispersion of the oxidation air 31 due to the flow in the oxidation tank 13 caused by the ejected air 31 and Diffusion can be promoted and the oxidation capacity of the entire oxidation tank 13 can be improved.

As a result, even in the case of seawater desulfurization in a plant with a large amount of S, the oxidation tank 13 can be made compact, the equipment cost can be reduced, and the air flow rate for oxidation can be reduced.

An aeration apparatus for seawater desulfurization according to a second embodiment of the present invention will be described with reference to the drawings. FIG. 8 is a schematic diagram illustrating the configuration of the diffuser for seawater desulfurization according to the second embodiment. In addition, about the component same as the apparatus structure of Example 1, the same code | symbol is attached | subjected and the overlapping description is abbreviate | omitted.
As shown in FIG. 8, the diffuser for seawater desulfurization according to the present embodiment is installed on both the inlet side and the outlet side of the oxidation tank 13 for seawater desulfurization.

Although the length of the oxidation tank 13 can be reduced according to the present invention, when the existing water channel is applied to an oxidation tank having a long length, the discharge point to seawater is separated.

For example, when the pH regulation value of the discharged seawater at the discharge point is pH 6.0, the seawater passage is long when the seawater desulfurization air diffuser 30A is provided only on the inlet side of the oxidation tank 13 having a long water channel. The recovered seawater 29 is oxidized and lowered to a water quality recovered seawater 29A having a pH of 5.9. The water quality recovery seawater 29A having a low pH cannot be discharged at the same pH value (5.9).

Accordingly, a diffuser 30B for seawater desulfurization is also provided in the vicinity of the outlet side of the oxidation tank 13, and the air 31 is introduced to raise the pH, so that the water quality is pH 6.0 or higher, which is the pH value of the discharge regulation value. The recovered seawater 29 can be discharged.

DESCRIPTION OF SYMBOLS 10 Seawater desulfurization apparatus 11 Flue gas desulfurization absorption tower 12 Inlet side dilution mixing tank 13 Oxidation tank 14 Outlet side dilution mixing tank 15 Seawater 23 Sulfur content absorption seawater 24 Acid mixed seawater 30 Seawater desulfurization diffuser 31 Air 33 Air supply pipe 34 Air diffuser 35 hole 36 nozzle

Claims

A diffuser pipe disposed in an oxidation tank for seawater desulfurization, supplying air to oxidized mixed seawater containing sulfur-absorbed seawater produced by contacting sulfur in the exhaust gas with seawater and desulfurizing seawater;
An air supply pipe for supplying air from the outside to the diffuser pipe by air introduction means,
The hole diameter of the air diffuser is 5 mm or more,
The pitch between the holes of the air diffuser is 40 mm or more,
An air diffuser for seawater desulfurization, wherein a pitch between air diffusers arranged in the air supply pipe is 500 mm or more.
In claim 1,
An air diffuser for seawater desulfurization, wherein the flow velocity of air discharged from the hole is 10 to 100 m / s.
A seawater desulfurization apparatus comprising the diffuser for seawater desulfurization according to claim 1 or 2 on an inlet side of an oxidation tank.
A seawater desulfurization apparatus comprising the diffuser for seawater desulfurization according to claim 1 or 2 on an inlet side and an outlet side of an oxidation tank.