TW201339100A - Oxidation tank, seawater flue-gas desulfurization system and power generation system - Google Patents

Abstract

This oxidation tank (12) is characterized by comprising: a diluted seawater supply line (L14) which is coupled to a tank body in order to supply diluted seawater (13b) for dilution to sulfur content-absorbed seawater (14) containing sulfur content and discharged from a flue-gas desulfurization absorption tower (11); an aeration device (31) which is provided in the tank body and supplies air (33) to the sulfur content-absorbed seawater (14) discharged from the flue-gas desulfurization absorption tower (11); and a dissolved oxygen concentration measurement device (32) which is provided in the tank body and measures the dissolved oxygen concentration in the sulfur content-absorbed seawater (14), and adjusting the air quantity to be supplied from the aeration device (31) to the sulfur content-absorbed seawater (14) on the basis of the relation between the previously acquired length of the oxidation tank (12) and the dissolved oxygen concentration in the sulfur content-absorbed seawater (14).

Description

Oxidation tank, seawater flue gas desulfurization system and power generation system

The present invention relates to an oxidation tank, a seawater flue gas desulfurization system and a power generation system for oxidizing seawater containing sulfur components containing sulfur components which are desulphurized using seawater.

In a power generation facility that uses coal or crude oil as a fuel, a combustion component (hereinafter referred to as "exhaust gas") discharged from a boiler contains a sulfur component such as sulfur oxide (SOx) by burning a fossil fuel such as coal. Therefore, the exhaust gas is subjected to desulfurization treatment to remove sulfur oxides (SOx) such as sulfur dioxide (SO ₂ ) contained in the exhaust gas, and then is discharged to the atmosphere. As such a desulfurization treatment method, there are a lime gypsum method, a spray dryer method, a seawater method, and the like.

Power plants and the like are often built in places facing the sea due to the large amount of cooling water required. Therefore, from the viewpoint of suppressing the operation cost required for the desulfurization treatment, it is proposed to use a seawater flue gas desulfurization apparatus which uses seawater as an absorption liquid for absorbing sulfur oxides in exhaust gas to desulfurize seawater.

The seawater flue gas desulfurization device supplies seawater and boiler exhaust gas to the inside of a desulfurization tower (absorption tower) in which a cylindrical shape or an angular shape such as a substantially cylinder is longitudinally placed, so that seawater is subjected to gas-liquid contact as an absorption liquid. Remove SOx. The desulfurized seawater (the sulfur-absorbing component seawater) used as an absorbent in the desulfurization tower is supplied to the oxidation tank. The sulfur-absorbing component seawater flowing in the oxidation tank is diluted by mixing with seawater not used for desulfurization. In addition, the sulfur-absorbing component seawater is oxidized and decarboxylated (aerated) by fine bubbles flowing out from an aeration device (air distribution device) provided on the bottom surface of the oxidation tank (see, for example, Patent Document 1). Thereby, the sulfur-absorbing seawater is subjected to aeration treatment of SO ₃ and CO ₂ , and is discharged after satisfying the environmental standard.

[Previous Technical Literature] [Patent Literature]

[Patent Document 1] Japanese Patent Laid-Open Publication No. 2007-125474

The oxidation tank is usually a long water tank (Seawater Oxidation Treatment System) (SOTS) with a width of 20 m to 40 m and a length of 100 m to 200 m. It requires a wide area. In the oxidation tank, oxygen is supplied from the air distributing means provided at the bottom of the oxidation tank to the substantially entire surface of the bottom of the oxidation tank in the state of air.

The oxidation tank used in the prior art supplies oxygen to the seawater of the sulfur-absorbing component flowing in the oxidation tank from the entire surface of the bottom of the oxidation tank, and the power cost required for the operation of the oxidation tank is high. In addition, there is a place for supplying oxygen which is more than oxygen required for the oxidation of SO _{3 in} the seawater of the sulfur component and the aeration of the CO ₂ , and the oxygen is required to be supplied, and the sulfur component is not efficiently absorbed. Oxidation of SO ₃ and aeration of CO ₂ .

The present invention has been made in view of the above problems, and an object of the invention is to provide an oxidation tank, a seawater flue gas desulfurization system, and a power generation system that can efficiently treat seawater containing sulfur components and reduce the total amount of air supplied to the oxidation tank.

A first aspect of the present invention to solve the above problems is an oxidation tank comprising: a seawater supply mechanism for dilution, which is coupled to a tank body and absorbs sulfur containing components discharged from a flue gas desulfurization absorber. Sulfur component seawater is supplied to seawater for dilution; a plurality of air supply means are provided in the tank body, and air is supplied to the sulfur-absorbing component seawater discharged from the flue gas desulfurization absorption tower; and a dissolved oxygen concentration measuring device , its design Putting in the tank body, measuring the dissolved oxygen concentration in the seawater of the sulfur-absorbing component; and adjusting the supply from the air supply mechanism based on the relationship between the length of the oxidation tank obtained in advance and the dissolved oxygen concentration in the seawater of the sulfur-absorbing component The amount of air to the above-mentioned sulfur-absorbing seawater.

According to a second aspect of the invention, in the oxidation tank according to the first aspect of the invention, the relationship between the pH value of the sulfur-absorbing component seawater, the sulfuric acid concentration, the alkalinity, and the temperature, and the dissolved oxygen concentration are calculated in advance, and the dissolution is performed. The oxygen concentration can be determined based on any one of the pH value of the sulfur-absorbing component seawater, the sulfurous acid concentration, the alkalinity, and the temperature calculated in advance.

According to a third aspect of the invention, in the oxidizing tank according to the first aspect of the invention, the air supply means supplies the air to the sulfur-absorbing component seawater at intervals.

According to a fourth aspect of the invention, in the oxidizing tank according to the first aspect of the invention, the air supply means is supplied when the dissolved oxygen concentration of the sulfur-absorbing component seawater is equal to or lower than a specific value.

According to a fifth aspect of the invention, a seawater flue gas desulfurization system includes: a flue gas desulfurization absorption tower that cleans the exhaust gas by bringing gas and liquid gas into contact with seawater; and the oxidation tank according to the first aspect of the invention is provided in the above a flow side after the flue gas desulfurization absorption tower; a seawater supply line that supplies the seawater to the flue gas desulfurization absorption tower; and a sulfur component seawater discharge line that discharges the sulfur absorbed from the flue gas desulfurization absorption tower The component seawater is supplied to the oxidation tank; and the diluted seawater supply line supplies the seawater to either or both of the sulfur-absorbing component seawater discharge line and the oxidation tank.

A sixth aspect of the invention is a power generation system, comprising: a boiler; a steam turbine that uses exhaust gas discharged from the boiler as a heat source for steam generation, and uses the generated steam to drive a generator; and the fifth invention a seawater flue gas desulfurization system; and comprising: a condenser that recovers and circulates the condensed water in the steam turbine; a flue gas denitration device that performs denitration of the exhaust gas discharged from the boiler; and dust collection A device that removes coal dust from the exhaust gas.

According to the present invention, the treatment of the sulfur-absorbing component seawater can be efficiently performed, and the supply is lowered The total amount of air supplied to the oxidation tank.

10‧‧‧Seawater flue gas desulfurization system

11‧‧‧Exhaust flue gas desulfurization absorption tower

12‧‧‧oxidation tank

13‧‧‧ seawater

13a‧‧‧absorbing seawater

13b, 13c‧‧‧diluted seawater

14‧‧‧Sulphur-absorbing seawater

21‧‧‧Sea

22, 23‧‧‧ pump

25, 51‧‧‧ exhaust

26‧‧‧ spray nozzle

28‧‧‧ Purified gas

31‧‧‧Aeration device (air distribution device)

32‧‧‧Dissolved oxygen concentration measuring device

33‧‧‧ Air

34‧‧‧Oxidation air blower

35‧‧‧Distribution tube

36‧‧‧Oxidizing air nozzle

37‧‧‧Water quality restores seawater

38‧‧‧Control device

40‧‧‧Power Generation System

41‧‧‧Boiler

42‧‧‧Vapor turbine

43‧‧‧Condenser

44‧‧‧Exhaust smoke denitration device

45‧‧‧dust collection device

46‧‧‧fuel

47‧‧‧Air preheater (AH)

48‧‧‧ Air

49‧‧‧Into the fan

50‧‧‧Vapor

52‧‧‧ water

53‧‧‧Generator

55‧‧‧Exhaust fan

56‧‧‧ heat exchanger

57‧‧‧ chimney

L11, L12‧‧‧ seawater supply line

L13‧‧‧Sulphide-absorbing seawater discharge line

L14, L15, L18‧‧‧ diluted seawater supply line

L16‧‧‧ Purified gas exhaust passage

L17‧‧‧Seawater discharge line

Fig. 1 is a schematic view showing the configuration of a seawater flue gas desulfurization system to which an oxidation tank according to a first embodiment of the present invention is applied.

Fig. 2 is a view showing an example of the relationship between the length of the oxidation tank and the dissolved oxygen concentration in the sulfur-absorbing seawater.

Fig. 3 is an explanatory view showing an example of the relationship between the length of the oxidation tank and the SO ₃ ^- concentration and the dissolved oxygen concentration dissolved in the sulfur-absorbing seawater.

Fig. 4 is an explanatory view showing the relationship between the length of the oxidation tank and the amount of supplied air.

Fig. 5 is a schematic view showing the configuration of a power generation system according to a second embodiment of the present invention.

Hereinafter, the present invention will be described in detail with reference to the drawings. Further, the present invention is not limited by the following examples. Further, among the constituent elements in the following embodiments, those who can easily assume, substantially the same, and the so-called equal range are included. Further, the constituent elements disclosed in the following examples can be appropriately combined.

[Example 1]

The seawater flue gas desulfurization system to which the oxidation tank of the first embodiment of the present invention is applied will be described with reference to the drawings. Fig. 1 is a schematic view showing the configuration of a seawater flue gas desulfurization system to which an oxidation tank according to a first embodiment of the present invention is applied. As shown in Fig. 1, the seawater flue gas desulfurization system 10 includes: a flue gas desulfurization absorption tower 11; an oxidation tank 12 of the present embodiment; seawater supply lines L11, L12, which supply the seawater 13 to the flue gas desulfurization absorption Tower 11; a sulfur-absorbing component seawater discharge line L13 for supplying the sulfur-absorbing component seawater 14 containing sulfur components discharged from the exhaust gas desulfurization absorption tower 11 to the oxidation tank 12; and the diluted seawater supply lines L14 and L15, etc. The seawater 13 is supplied to the sulfur-absorbing component seawater discharge line L13 and the oxidation tank 12.

The seawater 13 is taken from the sea 21 by the pump 22 to the seawater supply line L11, and a part of the seawater 13 is supplied as the absorbing seawater 13a via the seawater supply line L12 by the pump 23 or gravity driving. The flue gas desulfurization absorption tower 11. One part of the remaining seawater 13 is sent to the sulfur-absorbing component seawater discharge line L13 via the diluted seawater supply line L14 as the diluted seawater 13b, and the remaining portion of the diluted seawater 13b is supplied to the oxidation tank 12 as the diluted seawater 13c via the diluted seawater supply line L15. The seawater 13 is a seawater directly taken from the sea 21 by the pump 22. However, the present invention is not limited thereto, and liquid discharging from seawater discharged from a condenser (not shown) may be used.

The flue gas desulfurization absorption tower 11 is a tower that purifies the exhaust gas 25 by bringing the exhaust gas 25 into gas-liquid contact with the absorbing seawater 13a. In the exhaust gas desulfurization absorption tower 11, the absorbing seawater 13a is ejected upward from the spray nozzle 26 in a liquid column shape, and the exhaust gas 25 is brought into gas-liquid contact with the absorbing seawater 13a supplied through the seawater supply line L12, and the exhaust gas 25 is discharged. Desulfurization of sulfur components. In the present embodiment, the spray nozzle 26 is a spray nozzle that is ejected in a liquid column shape upward. However, the spray nozzle 26 is not limited thereto, and may be sprayed downward in a shower shape.

In other words, in the exhaust gas desulfurization absorption tower 11, the exhaust gas 25 is brought into gas-liquid contact with the absorbing seawater 13a, and a reaction represented by the following formula (I) is generated, and sulfur such as SOx contained in the form of SO ₂ or the like in the exhaust gas 25 is generated. The component is absorbed by the absorbing seawater 13a, and the sulphur component in the exhaust gas 25 is removed using the absorbing seawater 13a.

SO ₂ (g)+H ₂ O → H ₂ SO ₃ (l)→HSO ₃ ^- +H ⁺ (I)

By desulfurizing the seawater, the H ₂ SO ₃ generated by the contact of the absorbing seawater 13a with the gas and liquid of the exhaust gas 25 dissociates, and the hydrogen ions (H ⁺ ) are released in the absorbing seawater 13a, so that the pH value is lowered to absorb the sulfur component seawater. 14 absorbs a large amount of sulfur components. Therefore, the sulfur-absorbing seawater 14 contains a sulfur component at a high concentration. In this case, the pH of the sulfur-absorbing seawater 14 is, for example, about 3 to 6. Further, the sulfur-absorbing component seawater 14 which absorbs the sulfur component in the flue gas desulfurization absorption tower 11 is accumulated in the bottom of the tower of the flue gas desulfurization absorption tower 11. The sulfur-absorbing component seawater 14 accumulated in the bottom of the tower of the exhaust gas desulfurization absorption tower 11 is sent to the oxidation tank 12 via the sulfur-absorbing component seawater discharge line L13.

Further, the purge gas 28 desulfurized in the flue gas desulfurization absorption tower 11 is discharged to the atmosphere through the purge gas discharge passage L16.

In addition, the diluted seawater supply line L14 is connected to the sulfur-absorbing seawater discharge line L13, and the sulfur-absorbing component seawater 14 in the sulfur-absorbing seawater discharge line L13 is mixed with the diluted seawater 13b and diluted. By mixing and diluting the sulfur-absorbing seawater 14 with the diluted seawater 13b, the pH of the sulfur-absorbing component seawater 14 in the sulfur-absorbing seawater discharge line L13 can be increased to prevent the SO ₂ gas from being diffused again. Further, by preventing the SO ₂ in the sulfur-absorbing seawater discharge line L13 from diffusing and leaking to the outside, it is possible to prevent the discharge of the irritating odor.

Further, a dilution mixing tank for diluting and mixing the sulfur-absorbing seawater 14 and the diluted seawater 13b may be provided on the sulfur-absorbing seawater discharge line L13. The sulfur-absorbing seawater 14 is mixed with the diluted seawater 13b in a dilution mixing tank and diluted. By mixing and diluting the sulfur-absorbing seawater 14 with the diluted seawater 13b, the pH of the sulfur-absorbing component seawater 14 in the dilution mixing tank can be increased to prevent re-diffusion of the SO ₂ gas. Further, by preventing the SO _{2 from} diffusing in the dilution mixing tank and leaking to the outside, it is possible to prevent the discharge of the irritating odor.

The oxidation tank 12 is disposed on the flow side after the exhaust gas desulfurization absorption tower 11, and includes a dilution seawater supply line L15 as a dilution seawater supply mechanism, an aeration device (air distribution device) 31 as an air supply mechanism, and dissolved oxygen. The tank of the concentration measuring device 32. In the present embodiment, the diluted seawater supply line L15 is provided, and the diluted seawater 13c is supplied to the oxidation tank 12. However, the present invention is not limited thereto, and the diluted seawater supply line L15 may not be provided.

The diluted seawater supply line L15 connects the diluted seawater supply line L14 to the oxidation tank 12, and supplies the diluted seawater 13c to the sulfur-absorbing component seawater 14 in the oxidation tank 12.

The aeration device 31 is provided in the oxidation tank 12 and supplies air 33 to the sulfur-absorbing seawater 14 . In the present embodiment, the aeration device 31 includes an oxidizing air blower 34 that supplies air 33, a diffusing pipe 35 that transports the air 33, and an oxidizing air nozzle 36 that absorbs the sulfur-absorbing component seawater in the oxidizing tank 12. 14 supplies air 33. By the oxidizing air blower 34, the external air 33 is sent from the oxidizing air nozzle 36 to the oxidizing tank 12 via the diffusing pipe 35, and the oxygen is dissolved by the following formula (II). The sulfur component absorbed in the sulfur component seawater 14 in the oxidation tank 12 is brought into contact with the air 33 to generate an oxidation reaction of bisulfite ions (HSO ₃ ^- ) of the following formulas (III) to (V), and a bicarbonate ion. The decarboxylation reaction of (HCO ₃ ^- ), the sulfur-absorbing seawater 14 is recovered by water quality, and the water quality is restored to seawater 37. Further, the number of the oxidizing air nozzles 36 is not particularly limited, and is appropriately set depending on the size of the inside of the oxidation tank 12.

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)

Thereby, the pH value of the sulfur-absorbing seawater 14 can be raised and the chemical oxygen demand (COD: Chemical Oxygen Demand) can be lowered, and the water quality can be restored to the pH value of the seawater 37, the dissolved oxygen concentration, and the COD can be set as the dischargeable seawater. Discharged at the level. Further, even when the water in the sulfur-absorbing component seawater 14 is recovered in the oxidation tank 12, gas is generated, and the generated gas can be diffused into the oxidation tank 12 so as to satisfy the SO ₂ environment reference concentration. The water quality recovery seawater 37 is discharged to the sea 21 via the seawater discharge line L17.

Further, the dissolved oxygen concentration measuring device 32 is installed in the oxidation tank 12, and measures the dissolved oxygen concentration in the sulfur-absorbing seawater 14. The dissolved oxygen concentration measuring device 32 is provided in plural in the flow direction of the sulfur-absorbing component seawater 14 in the oxidation tank 12. Examples of the dissolved oxygen concentration measuring device 32 include a commercially available dissolved oxygen meter such as a portable type or a fixed type. The measurement result measured by the dissolved oxygen concentration measuring device 32 is transmitted to the control device 38.

In the present embodiment, the dissolved oxygen concentration can be determined based on the pH value of the sulfur-absorbing component seawater 14, the sulfuric acid concentration, the alkalinity, and the temperature. The relationship between the pH value, the sulfuric acid concentration, the alkalinity, and the temperature of the sulfur-absorbing component seawater 14 and the dissolved oxygen concentration is calculated in advance, and the control device 38 is based on the pH value of the sulfur-absorbing component seawater 14 calculated in advance, and sulfurous acid. The relationship between the concentration, the alkalinity, and the temperature and the dissolved oxygen concentration is determined based on the value of the pH value of the sulfur-absorbing component seawater 14, the sulfuric acid concentration, the alkalinity, and the temperature.

In the present embodiment, the control device 38 adjusts the relationship between the length of the oxidation tank 12 obtained in advance and the dissolved oxygen concentration in the sulfur-absorbing seawater 14, and adjusts the respective oxidizing air nozzles 36 supplied from the aeration device 31 to absorb sulfur. The amount of air in the air 33 of the component seawater 14.

An example of the relationship between the length of the oxidation tank 12 and the dissolved oxygen concentration in the sulfur-absorbing seawater 14 is shown in Fig. 2 . As shown in Fig. 2, the amount of air supplied from the respective aeration devices 31 to the air 33 absorbing the sulfur component seawater 14 can be adjusted using a relationship diagram showing the relationship between the length of the oxidation tank 12 and the dissolved oxygen concentration in the sulfur-absorbing seawater 14. .

The aeration device 31 preferably supplies the air 33 to the sulfur-absorbing component seawater 14 while being spaced apart from each other. In the present embodiment, the term "supply" is used to mean that the air is supplied from all of the oxidizing air nozzles 36 to the sulphur-insoluble seawater 14 and is in the longitudinal direction of the oxidizing tank 12. The air 33 is supplied to the sulfur-absorbing component seawater 14 from the limited oxidizing air nozzle 36 while maintaining the interval.

The aeration device 31 is preferably supplied when the dissolved oxygen concentration of the sulfur-absorbing seawater 14 is equal to or lower than a specific value. The specific value refers to an amount that can ensure a sufficient oxidation rate, and is supplied, for example, when the dissolved oxygen concentration of the sulfur-absorbing seawater 14 is equal to or less than 1/3 of the saturated concentration. Furthermore, the specific value is not limited to the case where the dissolved oxygen concentration is 1/3 of the saturated concentration.

In the aeration device 31, when the air 33 is supplied to the sulfur-absorbing seawater 14, the air 33 is supplied to the upstream side of the oxidation tank 12, and the amount of the air 33 is reduced toward the downstream side of the oxidation tank 12. This is because the air 33 supplied to the oxidation tank 12 is not immediately dissolved by the oxidation of the sulfite ions (SO ₃ ^- ) in the sulfur-absorbing seawater 14 or the CO ₂ aeration, so that the sulfur component seawater 14 is absorbed. The downstream side of the oxidation tank 12 flows. Further, since the upstream side of the oxidation tank 12 is easily oxidized due to the high concentration of SO ₃ ^- , the dissolved oxygen in the sulfur-absorbing seawater 14 tends to be small. Therefore, in consideration of absorbing sulfur component is dissolved in the seawater SO ₃ 14 ^- oxidized by the reaction time, the time required for the aeration of CO _2, air 33 is supplied to the more upstream of the oxidation tank 12 side, downstream of the oxidation tank 12 The side reduces the supply amount of the air 33, whereby the SO ₃ ^{-concentration} concentration of the sulfur-absorbing seawater 14 can be reliably reduced in the oxidation tank 12.

3 is an explanatory view showing an example of the relationship between the length of the oxidation tank 12 and the SO ₃ ^- concentration and the dissolved oxygen concentration dissolved in the sulfur-absorbing seawater 14 . As shown in Fig. 3, even when the air 33 is supplied to the oxidation tank 12 at intervals, the air 33 can be separated by the concentration of dissolved oxygen of the sulfur-containing seawater 14 being set to a specific set value α. The supply to the oxidation tank 12 is intermittently supplied and the supply amount thereof is adjusted, and the SO ₃ ^- concentration in the sulfur-absorbing seawater 14 is reduced to be substantially equal to the case where the air 33 is supplied all the way to the oxidation tank 12 .

Further, by supplying the air 33 to the oxidation tank 12 at intervals, the length of the oxidation tank 12 required to be equal to or lower than the SO ₃ ^- concentration dissolved in the sulfur-absorbing seawater 14 is a specific value or less. In the case of adjusting the depth of the oxidation tank 12 and the width of the flow path, and adjusting the flow rate of the sulfur-absorbing seawater 14 to be slow, it is adjusted to regenerate and discharge the sulfur-containing seawater 14 The length of the oxidation tank 12 is equal to the length of the oxidation tank 12 required to supply the air 33 to the oxidation tank 12 and regenerate and discharge the sulfur-containing seawater 14 as previously.

Fig. 4 is an explanatory view showing the relationship between the length of the oxidation tank 12 and the amount of supplied air. As shown in FIG. 4, when the length of the oxidation tank 12 in the longitudinal direction is 1.0, and the air 33 is equally supplied to each of the five sections which are equally divided in the longitudinal direction of the oxidation tank 12, the supply is oxidized. The total air amount ratio in the tank 12 was set to 1.0 (refer to Comparative Example 1). At this time, as in Experimental Example 1, the length of each region when the oxidation tank 12 was divided into five portions was changed, and the amount of air supplied to each region was adjusted. Specifically, the length of the region where the air 33 is supplied to the oxidation tank 12 is slightly longer, the length of the region where the air 33 is not supplied is shortened, and the amount of air supplied into the oxidation tank 12 is increased toward the upstream side of the oxidation tank 12. In many cases, the adjustment is performed so as to become smaller toward the downstream side of the oxidation tank 12.

As a result, in Experimental Example 1, as compared with the case where the air 33 is uniformly supplied to the respective regions in the oxidation tank 12 as in Comparative Example 1, the total amount of air supplied to the oxidation tank 12 can be reduced by, for example, about 20%. . Therefore, by adjusting the oxidation groove 12 into a plurality of regions The length of each region and the amount of air supplied to each region can efficiently perform the treatment of absorbing the sulfur component seawater 14, so that the aeration device 31 can be provided at an excessive position in the oxidation vessel 12, and the supply to the oxidation can be reduced. The total amount of air in the tank 12 reduces the amount of oxygen required for the supply to the oxidation tank 12.

Therefore, according to the relationship diagram showing the relationship between the length of the oxidation tank 12 obtained in advance and the dissolved oxygen concentration in the sulfur-absorbing seawater 14 according to the oxidation tank 12 of the present embodiment, the respective nozzles for oxidizing air from the aeration device 31 are adjusted. The amount of air supplied to the air 33 absorbing the sulfur component seawater 14 is adjusted to the length of each region when the oxidation tank 12 is divided into a plurality of regions and the amount of air supplied to each region. Therefore, the oxidation tank 12 of the present embodiment can reduce the amount of the aeration device 31 disposed in the oxidation tank 12 without increasing the oxidation tank 12 by efficiently performing the treatment of absorbing the sulfur component seawater 14, and can reduce the self-exposure. The gas device 31 supplies the total amount of air to the air 33 in the oxidation tank 12 and reduces the power required to supply the air 33.

Thus, the seawater flue gas desulfurization system 10 to which the oxidation tank 12 of the present embodiment is applied can reduce the number of the oxidizing air nozzles 36 of the aeration device 31 disposed in the oxidation tank 12, and can reduce the supply to the oxidation tank 12. Since the total amount of air is reduced and the power required to supply the air 33 is reduced, the sulfur-absorbing component seawater 14 flowing through the open-type oxidation tank 12 can be efficiently oxidized and subjected to water quality recovery treatment.

Therefore, according to the seawater flue gas desulfurization system 10 to which the oxidation tank 12 of the present embodiment is applied, the inside of the oxidation tank 12 is efficiently supplied while reducing the number of the oxidizing air nozzles 36 of the aeration device 31 in the oxidation tank 12. The air 33 can efficiently treat the sulfur-absorbing seawater 14 from the sulfur-absorbing component seawater 14 discharged from the flue gas desulfurization absorption tower 11 and perform water quality recovery treatment, thereby providing a highly reliable seawater flue gas desulfurization process. system.

Further, in the present embodiment, the seawater flue gas desulfurization system for treating the seawater 13a for seawater desulfurization in the flue gas desulfurization absorption tower 11 has been described, but the present invention is not limited thereto. The seawater flue gas desulfurization system can also be applied to power plants such as factories in various industries, large and medium-sized thermal power plants, large-scale boilers for electric power enterprises, or general production. A seawater flue gas desulfurization device for seawater desulfurization by using sulfur oxides contained in exhaust gas discharged from boilers, ironworks, refineries, and the like.

Further, in the present embodiment, the flue gas desulfurization absorption tower 11 and the oxidation tank 12 are independent of the respective tanks, and the flue gas desulfurization absorption tower 11 and the oxidation tank 12 are connected by the sulfur absorption component seawater discharge line L13. However, the present embodiment is not limited thereto, and the exhaust gas desulfurization absorption tower 11 and the oxidation tank 12 may be integrally formed as one groove.

[Embodiment 2]

The power generation system of the second embodiment of the present invention will be described with reference to the drawings. The seawater flue gas desulfurization system of the first embodiment is used for the seawater flue gas desulfurization system applied to the power generation system of the present embodiment. The same members as those in the first embodiment are denoted by the same reference numerals, and their description will be omitted.

Fig. 5 is a schematic view showing the configuration of a power generation system according to a second embodiment of the present invention. As shown in FIG. 5, the power generation system 40 of the present embodiment includes a boiler 41, a steam turbine 42, a condenser 43, a smoke exhausting and denitrating device 44, a dust collecting device 45, and a seawater flue gas desulfurization system 10. Further, in the present embodiment, as described above, the sulphur-absorbing component seawater 14 refers to seawater that has been used in the seawater flue gas desulfurization system 10 to absorb sulfur components such as SO ₂ .

The boiler 41 is configured to inject and burn a fuel 46 supplied from an oil tank or a coal grinder together with air 48 preheated by an air preheater (AH, Air Heater) 47 from a burner (not shown). The air 48 supplied from the outside is preheated by the press-in fan 49 to the air preheater 47. The fuel 46 and the air 48 preheated by the air preheater 47 are supplied to a burner (not shown), and the fuel 46 is combusted in the boiler 41. Thereby, a vapor 50 for driving the steam turbine 42 is generated.

The exhaust gas 51 generated by combustion in the boiler 41 is sent to the exhaust gas denitration device 44. Further, the exhaust gas 51 exchanges heat with the water 52 discharged from the condenser 43 to serve as a heat source for generating the vapor 50. The steam turbine 42 drives the generator 53 using the generated steam 50. Moreover, the condenser 43 recovers the water 52 condensed in the steam turbine 42 and returns it to the boiler 41 again to follow ring.

The exhaust gas 51 discharged from the boiler 41 is denitrated in the exhaust gas denitration device 44, and is exchanged with the air 48 by the air preheater 47, and then sent to the dust collecting device 45 to remove the coal dust in the exhaust gas 51. Then, the exhaust gas 51 dedusted by the dust collecting device 45 is supplied to the exhaust gas desulfurization absorption tower 11 by the air suction fan 55. At this time, the exhaust gas 51 is supplied to the heat exchanger 56, and is subjected to heat exchange with the purge gas 28 that has been desulfurized and discharged through the flue gas desulfurization absorption tower 11, and then supplied to the flue gas desulfurization absorption tower 11. Further, the exhaust gas 51 may be directly supplied to the exhaust gas desulfurization absorption tower 11 without being exchanged with the purge gas 28 in the heat exchanger 56.

Further, the heat exchanger 56 includes a heat recovery unit and a reheater, and the heat medium circulates between the heat recovery unit and the reheater. The heat recovery device is disposed between the extraction fan 55 and the exhaust gas desulfurization absorption tower 11, and exchanges heat between the exhaust gas 51 discharged from the boiler 41 and the heat medium. The reheater is disposed on the flow side after the exhaust gas desulfurization absorption tower 11, and exchanges heat between the purge gas 28 discharged from the flue gas desulfurization absorption tower 11 and the heat medium, and reheats the purge gas 28.

The seawater flue gas desulfurization system 10 is the seawater flue gas desulfurization device of the above first embodiment. That is, the seawater flue gas desulfurization system 10 includes the flue gas desulfurization absorption tower 11, the oxidation tank 12, the seawater supply lines L11 and L12, the sulfur-absorbing component seawater discharge line L13, and the diluted seawater supply lines L14 and L15.

In the seawater flue gas desulfurization system 10, as described above, seawater desulfurization is performed on the sulfur component contained in the exhaust gas 51 using the seawater 13 from the sea. Further, after the seawater 13 is branched from the sea 21 by the pump 22 and heat-exchanged in the condenser 43, a part of the absorbed seawater 13a is sent to the seawater flue gas desulfurization system 10 via the seawater supply line L12 via the pump 23. . Further, the remaining diluted seawater 13b is sent to the upstream side of the oxidation tank 12 via the diluted seawater supply line L14. In the seawater flue gas desulfurization system 10, the exhaust gas 51 is brought into gas-liquid contact with the absorbing seawater 13a, and the sulfur component in the exhaust gas 51 is absorbed into the absorbing seawater 13a. The seawater 14 which absorbs the sulfur component and absorbs the sulfur component is discharged from the flue gas desulfurization absorption tower 11, and the diluted seawater 13b The mixture is mixed and diluted and delivered to the upstream side of the oxidation tank 12. Moreover, the exhaust gas 51 purified by the seawater flue gas desulfurization system 10 becomes the purge gas 28 and is discharged to the outside from the chimney 57 via the purge gas discharge passage L16.

Further, the power generation system 40 of the present embodiment supplies a part of the diluted seawater 13b to the upstream side in the oxidation tank 12 via the diluted seawater supply line L15. However, the present invention is not limited thereto, and a part of the diluted seawater 13b may not be supplied via the diluted seawater. The line L15 is supplied to the upstream side in the oxidation tank 12.

Further, the seawater 13 from the sea 21 is subjected to heat exchange in the condenser 43, and then sent to the seawater flue gas desulfurization system 10 for seawater desulfurization, but it is also possible not to condense the seawater 13 from the sea 21 The heat exchange in the unit 43 is carried out directly to the seawater flue gas desulfurization system 10 for seawater desulfurization.

The sulfur-absorbing seawater 14 is mixed with the diluted seawater 13b in a dilution mixing tank, and then sent to the oxidation tank 12. In the present embodiment, the oxidation tank 12 includes a diluted seawater supply line L15, an aeration device 31, and a dissolved oxygen concentration measuring device 32. The control device 38 adjusts the oxidation from each aeration device 31 based on the measurement result measured by the dissolved oxygen concentration measuring device 32 based on the relationship between the length of the oxidation tank 12 obtained in advance and the dissolved oxygen concentration in the sulfur-absorbing seawater 14. The air nozzle 36 supplies the amount of air to the air 33 that absorbs the sulfur component seawater 14. By adjusting the length of each region when the oxidation tank 12 is divided into a plurality of regions and the amount of air supplied to each region, the treatment of the sulfur-absorbing seawater 14 can be efficiently performed, and the oxidation tank 12 can be reduced without being increased in oxidation. The number of aeration devices 31 in the tank 12 can reduce the total amount of air supplied from the aeration device 31 to the air 33 in the oxidation tank 12 and reduce the power required to supply the air 33.

The water content of the sulfur-absorbing seawater 14 is recovered in the oxidation tank 12 in the above manner, and the water quality recovery seawater 37 is obtained. The water quality recovery seawater 37 obtained in the oxidation tank 12 discharges the pH value, the dissolved oxygen concentration, and the COD to the level of the seawater to be released from the oxidation tank 12 via the seawater discharge line L17.

Further, the power generation system 40 of the present embodiment includes the diluted seawater supply line L18 on the flow side after the seawater supply line 13 is supplied to the oxidation tank 12 from the seawater supply line L11 except for the absorption seawater 13a and the diluted seawater 13b. The power generation system 40 of the present embodiment supplies a part of the seawater 13 from the seawater supply line L11 to the flow side after the water quality recovery seawater 37 in the oxidation tank 12 via the diluted seawater supply line L18. Thereby, the water quality recovery seawater 37 can be further diluted. As a result, the pH value of the seawater recovery seawater 37 can be increased, and the pH value of the seawater discharge liquid can be raised to a pH value close to the seawater 21, and the drainage standard (pH value 6.0 or more) which satisfies the pH value of the seawater discharge liquid can be satisfied, and The COD is lowered, and the water quality is restored to the pH value of the seawater 37, and the COD is discharged to the level of the seawater that can be discharged. In the present embodiment, the diluted seawater supply line L18 is supplied to the downstream side in the oxidation tank 12, but the present invention is not limited thereto, and a part of the diluted seawater 13b may not be supplied to the oxidation tank via the diluted seawater supply line L18. The downstream side of the 12th.

As described above, according to the power generation system 40 of the present embodiment, the air 33 is efficiently supplied to the oxidation tank 12 while reducing the number of the aeration devices 31 provided in the oxidation tank 12 in the oxidation tank 12, so that the absorption can be efficiently performed. Since the sulfur component seawater 14 reduces the total amount of air supplied into the oxidation tank 12, the power for supplying the air 33 to the sulfur-absorbing seawater 14 in the oxidation tank 12 can be reduced, and the operation cost can be suppressed. Therefore, the power generation system 40 of the present embodiment can efficiently and stably treat the sulfur-absorbing seawater 14 and perform the water quality recovery process, thereby providing a power generation system having high safety and reliability.

Further, the seawater flue gas desulfurization system 10 of the present embodiment can be used, for example, for discharging power plants such as factories, large and medium-sized thermal power plants, and large-scale boilers or general industrial boilers in various industries. The sulfur component contained in the exhaust gas is subjected to removal of sulfur component in the sulfur-absorbing component solution generated by seawater desulfurization.

10‧‧‧Seawater flue gas desulfurization system

11‧‧‧Exhaust flue gas desulfurization absorption tower

12‧‧‧oxidation tank

13‧‧‧ seawater

13a‧‧‧absorbing seawater

13b, 13c‧‧‧diluted seawater

14‧‧‧Sulphur-absorbing seawater

21‧‧‧Sea

22, 23‧‧‧ pump

25‧‧‧Exhaust

26‧‧‧ spray nozzle

28‧‧‧ Purified gas

31‧‧‧Aeration device (air distribution device)

32‧‧‧Dissolved oxygen concentration measuring device

33‧‧‧ Air

34‧‧‧Oxidation air blower

35‧‧‧Distribution tube

36‧‧‧Oxidizing air nozzle

37‧‧‧Water quality restores seawater

38‧‧‧Control device

L11, L12‧‧‧ seawater supply line

L13‧‧‧Sulphide-absorbing seawater discharge line

L14, L15‧‧‧ diluted seawater supply line

L16‧‧‧ Purified gas exhaust passage

L17‧‧‧Seawater discharge line

Claims (6)

An oxidizing tank, comprising: a seawater supply mechanism for dilution, which is connected to a tank body, and supplies seawater for dilution to seawater containing sulfur which is discharged from a flue gas desulfurization absorption tower and contains a sulfur component; and an air supply mechanism; Provided in the tank body, and supplying air to the sulfur-absorbing component seawater discharged from the exhaust gas desulfurization absorption tower; and a dissolved oxygen concentration measuring device installed in the tank body and measuring the sulfur-absorbing component seawater The dissolved oxygen concentration in the medium is adjusted based on the relationship between the length of the oxidation tank obtained in advance and the dissolved oxygen concentration in the seawater of the sulfur-absorbing component, and the supply amount of the air supplied from the air supply means to the sulfur-absorbing component seawater is adjusted. In the oxidation tank of claim 1, wherein the relationship between the pH value of the sulfur-absorbing component seawater, the sulfuric acid concentration, the alkalinity, and the temperature and the dissolved oxygen concentration is calculated in advance, and the dissolved oxygen concentration can be calculated based on the calculation. The pH value of the sulfur-absorbing component seawater, the sulfuric acid concentration, the alkalinity, and the temperature are determined. The oxidation tank according to claim 1, wherein the air supply means supplies the air to the sulfur-absorbing component seawater while being spaced apart from each other. The oxidation tank according to claim 1, wherein the air supply means is supplied when the dissolved oxygen concentration of the sulfur-absorbing component seawater is equal to or lower than a specific value. A seawater flue gas desulfurization system, comprising: a flue gas desulfurization absorption tower, which washes the exhaust gas by gas-liquid contact with the seawater; The oxidation tank of claim 1, which is disposed on the flow side after the exhaust gas desulfurization absorption tower; the seawater supply line supplies the seawater to the exhaust gas desulfurization absorption tower; and absorbs the sulfur component seawater discharge line, which will be The sulfur-absorbing component seawater discharged from the flue gas desulfurization absorption tower is supplied to the oxidation tank; and the diluted seawater supply line supplies the seawater to either or both of the sulfur-absorbing component seawater discharge line and the oxidation tank. . A power generation system, comprising: a boiler; a steam turbine that uses exhaust gas discharged from the boiler as a heat source for steam generation, and uses the generated steam to drive a generator; and desulfurization of seawater flue gas as claimed in claim 5 a system comprising: a condenser that recovers and circulates water condensed in the steam turbine; a flue gas denitration device that performs denitration of exhaust gas discharged from the boiler; and a dust collecting device that removes the above Coal dust in the exhaust gas.