KR102008364B1 - High-concentration fluegas desulfurization equipment using microbubble - Google Patents

Abstract

The present invention relates to a wet flue gas desulfurization facility. According to the present invention, the wet flue gas desulfurization facility comprises: a desulfurization reaction unit including a first desulfurization reactor where a desulfurization reaction for generating calcium sulfite takes place by having calcium carbonate-containing calcium carbonate slurry reacting with sulfur dioxide contained in exhaust gas, and an exhaust fan for discharging gas from the first desulfurization reactor; a calcium carbonate supply unit for supplying the calcium carbonate to the desulfurization reactor; and an oxidation reaction tank where an oxidation reaction for generating dihydrate gypsum takes place by having oxygen reacting with a liquid mixture containing the calcium sulfite discharged from the first desulfurization reactor. The first desulfurization reactor includes: a 1A^th storage space into which the calcium carbonate slurry and the exhaust gas are introduced; a 2A^th storage space having an exhaust port formed therein; and a first atomizing unit positioned in the 2A^th storage space, and communicating with the 1A^th storage space. A water level of the 2A^th storage space is increased by forming a negative pressure in the 2A^th storage space by an operation of the exhaust fan. Also, a water level of the 1A^th storage space is lowered so gas in the 1A^th storage space forms microbubbles by the first atomizing unit to spray the same to the 2A^th storage space.

Description

High concentration flue gas desulfurization equipment using micro bubble {HIGH-CONCENTRATION FLUEGAS DESULFURIZATION EQUIPMENT USING MICROBUBBLE}

The present invention relates to a flue gas desulfurization plant, and more particularly, to a wet flue gas desulfurization plant that absorbs sulfur dioxide in exhaust gas and softens the produced calcium sulfite to stable gypsum using calcium carbonate as an absorbent.

Flue gas desulfurization removes sulfur oxides (primarily sulfur dioxide) contained in combustion exhaust gases. Sulfur dioxide in exhaust gases emitted from factories, thermal power plants, and incinerators is a major source of air pollution, and research on flue gas desulfurization is being actively conducted in terms of prevention of environmental pollution and utilization of sulfur resources.

Flue gas desulfurization is classified into a dry method and a wet method according to the type and use form of the absorbent treatment agent of the exhaust gas.

The dry method is a method of removing particles and powders such as activated carbon and carbonates by contacting with exhaust gas to remove or adsorb sulfur dioxide by adsorbing or reacting sulfur absorbents. However, since equipment, such as an absorption tower or a scrubber, is not required, the installation cost is low and it is mainly used in small facilities.

The wet method is a method of removing the exhaust gas by contact reaction with liquid absorbent treatment agents such as ammonia water, sodium hydroxide solution, and lime oil, and is mainly used in large facilities such as thermal power plants due to its relatively high efficiency and stable operation of the equipment. Calcium carbonate is widely used, and a general wet flue gas desulfurization system is composed of a structure in which a slurry in which lime is dispersed in water is injected into the exhaust gas to remove sulfur dioxide and the slurry is injected downward into the absorption tower body. However, such a general wet flue gas desulfurization facility has a structure in which a slurry is divided into a downward space in a space through which exhaust gas passes, so that the slurry has a short air hole time and a short contact time with the exhaust gas. Due to the high concentration of sulfur dioxide is difficult to treat.

Republic of Korea Patent Registration No. 10-136372 (1998.04.25.)

It is an object of the present invention to provide a wet flue gas desulfurization plant with improved desulfurization efficiency.

It is another object of the present invention to provide a wet flue gas desulfurization plant suitable for the desulfurization treatment of a high concentration of sulfur dioxide containing exhaust gas.

In order to achieve the above object of the present invention, according to an aspect of the present invention, a first desulfurization reactor in which a desulfurization reaction occurs in which a calcium carbonate slurry containing calcium carbonate and sulfur dioxide contained in the exhaust gas react to generate calcium sulfite And a desulfurization reaction unit including an exhaust fan for discharging gas from the first desulfurization reactor. A calcium carbonate supply unit for supplying the calcium carbonate to the desulfurization reaction unit; And an oxidation reaction tank in which an oxidation reaction occurs in which a liquid mixture containing oxygen and the calcium sulfite discharged from the first desulfurization reactor reacts to produce dihydrate gypsum, wherein the first desulfurization reactor comprises: the calcium carbonate slurry and the exhaust A first A storage space into which gas is introduced, a second A storage space in which an exhaust port is formed, and a first atomizing part located in the second A storage space and communicating with the first A storage space, and operated by the exhaust fan. When the negative pressure is formed in the second A storage space, the water level of the second A storage space is increased, and the water level of the first A storage space is lowered, whereby the gas in the first A storage space is microbubbles by the first atomizing unit. It is provided with a wet flue gas desulfurization facility is injected into the second A storage space.

According to the present invention, all the objects of the present invention described above can be achieved. Specifically, since the microbubbles are generated in the desulfurization reactor in which the desulfurization reaction occurs, the microbubbles generated in the desulfurization reactor are not extinguished and remain in the liquid mixture containing calcium sulfite generated during the desulfurization reaction and are supplied to the oxidation reaction tank. By further promoting the oxidation reaction in, the overall reaction efficiency is improved, so that desulfurization with a high concentration of sulfur dioxide becomes possible.

1 is a block diagram showing the configuration of a wet flue gas desulfurization facility according to an embodiment of the present invention.
FIG. 2 is a diagram illustrating a configuration of the first desulfurization reactor shown in FIG. 1.

Hereinafter, with reference to the drawings will be described in detail the configuration and operation of the embodiment of the present invention.

1 schematically shows the configuration of a wet flue gas desulfurization plant according to an embodiment of the present invention. Referring to FIG. 1, the wet flue gas desulfurization facility 100 according to an embodiment of the present invention is a facility for reducing the emission of sulfur dioxide (SO ₂ ), and supplies calcium carbonate (CaCO ₃ ) in a slurry form for the desulfurization reaction. Calcium carbonate supply unit 101, a first desulfurization reactor 110 to generate a microbubble and a first desulfurization reaction to the gas to be treated containing sulfur dioxide, and sulfur dioxide discharged from the first desulfurization reactor 110 The second desulfurization reaction 120 occurs to the gas containing and generates microbubbles, and the third desulfurization reaction to the gas containing sulfur dioxide discharged from the second desulfurization reactor 120 takes place and microbubbles The first mixture in which the third desulfurization reactor 130 and the liquid mixture discharged from the first desulfurization reactor 110 and the liquid mixture discharged from the second desulfurization reactor 120 are mixed. 140a, the liquid mixture discharged from the calcium carbonate slurry supplied from the calcium carbonate supply unit 101, the liquid mixture discharged from the third desulfurization reactor 130, and the liquid mixture discharged from the first mixing tank 140a is mixed and mixed Is supplied with the second mixing tank 140b for supplying the second desulfurization reactor 120 and the third desulfurization reactor 130 and the liquid mixture stored in the first desulfurization reactor 110 to undergo an oxidation reaction, Oxidation reaction tank 150 in which dihydrate gypsum (CaSO ₄ · 2H ₂ O) is generated, a first solid-liquid separator 160 for separating water from the gypsum slurry discharged from the oxidation reaction tank 150, and a first solid solution Before the second solid-liquid separator 170 separating the water from the gypsum slurry discharged from the separator 160 and the gypsum slurry discharged from the first solid-liquid separator 160 are supplied to the second solid-liquid separator 170. An intermediate reservoir 175 that is optionally stored and a first solid-liquid separator The water separated in the 160 is stored and includes a water reservoir 180 for supplying a portion of the stored water to the calcium carbonate supply unit 101.

The calcium carbonate supply unit 101 stores the calcium carbonate slurry, which is water in which calcium carbonate (CaCO ₃ ) is dispersed and mixed, and supplies the stored calcium carbonate slurry to the second mixing tank 140b for the desulfurization reaction. In this embodiment, the calcium carbonate supply unit will be described as supplying 15 ㎥ of calcium carbonate slurry to the second mixing tank 140b per day. In the present embodiment, the calcium carbonate supply unit 101 receives 14 m 3 of water per day from the water storage tank 180 and explains that 3.85 tons of calcium carbonate is supplied per hour.

In the first desulfurization reactor 110, a first desulfurization reaction occurs on a gas to be treated containing sulfur dioxide and microbubbles are generated. FIG. 2 shows the configuration of the first desulfurization reactor 110 shown in FIG. 1. Referring to FIG. 2, the first desulfurization reactor 110 provides an internal space 110a in which the desulfurization reaction occurs. The internal space 110a of the first desulfurization reactor 110 is partitioned into a first storage space 111a and a second storage space 111b by the partition wall 111. A connection passage 111c is formed below the partition wall 111 to communicate the first storage space 111a and the second storage space 111b. An inlet 112a is formed at the upper end of the first storage space 111a and communicates with the second storage space 111b at the upper end of the second storage space 111b. 112b is formed, and a drain hole 113a is formed below the second storage space 111b. Through the inlet 112a, the gas to be treated containing sulfur dioxide, the liquid mixture stored in the first mixing tank 140a, and the liquid mixture stored in the internal space 110a are circulated and supplied by the circulation pump 119a. The gas containing sulfur dioxide which is not removed by the desulfurization reaction is discharged to the outside through the exhaust port 112b and flows into the second desulfurization reactor 120. The liquid mixture stored in the internal space 110a is discharged to the outside by gravity through the drain hole 113a. Some of the liquid mixture discharged through the drain port 113a is supplied to the oxidation reaction tank 150, and the rest is supplied to the first mixing tank 140a. The amount supplied to the oxidation reaction tank 150 in the liquid mixture discharged through the drain port 113a is appropriately determined according to the oxidation reaction capacity of the oxidation reaction tank 150.

The first desulfurization reactor 110 includes a water tank 113 located in the first storage space 111a, a first water pipe 114 located in the first storage space 111a, and a first storage space 111a. Mixing cylinder 115 located in the second chamber, the second water pipe 116 located in the first storage space 111a, the atomizing unit 117 located in the second storage space 111b, and the second storage. A plurality of blocking plates 118 positioned in the space 111b and a droplet removing layer 119 positioned in the second storage space 111b are provided.

The water tank 113 is positioned adjacent to the inlet 112a in the first storage space 111a. The water tank 113 temporarily stores the liquid mixture flowing through the inlet 112a.

The first water pipe 114 is positioned below the water tank 113 in the first storage space 111a. The first water pipe 114 has a shape that becomes narrower toward the bottom thereof, and a first outlet 114a through which the liquid mixture and the gas to be treated is discharged is formed at the lower end of the first water pipe 114.

The mixing cylinder 115 is positioned below the first outlet 114a formed in the first water pipe 114 in the first storage space 111a. The mixing vessel 115 temporarily stores the liquid mixture discharged through the first outlet 114a.

The second water pipe 116 is positioned below the mixing cylinder 115 in the first storage space 111a. The second water pipe 116 has a shape that becomes narrower toward the bottom, and a second outlet 116a for discharging the liquid mixture and the gas to be treated is formed at the lower end of the second water pipe 116.

The water tank 113, the first water pipe 114, the mixing vessel 115, and the second water pipe 116 temporarily store the liquid mixture and allow the liquid mixture and the gas to be treated to contact each other.

The atomizing unit 117 is located in the second storage space (111b) and the gas supplied from the first storage space (111a) is a micro bubble in the liquid mixture stored in the second storage space (111b) micro-bubble (micro-) It is formed into a bubble (B) and sprayed. Microbubbles (B) are not easily extinguished but are present for a long time and have a property of dwelling for a fairly long time in the liquid mixture. The atomizing portion 117 includes a nozzle 117a extending from the partition wall 111 and an impingement plate 117b positioned at the end of the nozzle 117a.

The nozzle 117a is located at a relatively lower portion of the second storage space 111a and is formed by protruding from the partition wall 111. The end of the nozzle 117a extends generally upwardly upward. The nozzle 117a is formed to have a narrower inner diameter toward the end, so that the sulfurous acid gas of the first storage space 111a flows to the end of the nozzle 117a to increase the speed. The inlet side 1171a of the nozzle 117a connected to the first storage space 111a is located below the second outlet 116a formed in the second water pipe 116. The impingement plate 117b is adjacent to the end which forms the exit 117c of the nozzle 117a.

The impingement plate 117b is located adjacent to the end of the nozzle 117a. The gas injected from the nozzle 117a collides with the impingement plate 117b to form micro bubbles. In the present embodiment, the collision plate 117b is described as having a two-stage structure in which two 1171b and 1172b are disposed in the vertical direction as shown, but the present invention is not limited thereto. The above structure is also within the scope of the present invention. In the case of the multi-stage structure, the collision plate 1172b positioned above is larger to cover the collision plate 1171b positioned below, and at least one passage 1173b is preferably formed between the collision plate 1172b.

The plurality of blocking plates 118 are arranged in layers on the impingement plate 117b in the second storage space 111b. Sudden rise of liquid mixing is blocked by the plurality of blocking plates 118.

The droplet removing layer 119 is positioned between the exhaust pipe 112b and the uppermost blocking plate 118 of the plurality of blocking plates 118 in the second storage space 111b. The droplet removing layer 119 is made of a stainless steel net.

In the first desulfurization reactor 110, the desulfurization reaction is mainly performed as in the following [Scheme 1].

Scheme 1

CaCO ₃ + SO ₂ + H ₂ O → CaSO ₃ 2H ₂ O + CO ₂

That is, sulfur dioxide (SO ₂ ) and calcium carbonate (CaCO ₃ ) react to form calcium sulfite (CaSO ₃ ) to remove sulfur. Calcium carbonate is contained in the liquid mixture supplied from the first mixing tank 140a. In the present embodiment, it will be described that sulfur dioxide gas having a concentration of 30,000 ppm is introduced into the first desulfurization reactor 110 and sulfur dioxide gas having a concentration of 20,000 ppm is discharged.

In the first desulfurization reactor 110, an oxidation reaction as shown in [Scheme 2] is also performed.

Scheme 2

CaSO ₃ 2H ₂ O + 1 / 2O ₂ + H ₂ O → CaSO ₄ 2H ₂ O + H ₂ O

That is, sulfur sulphite produced through [Scheme 1] is produced through the oxidation reaction. Oxygen supplied in [Scheme 2] is partially included in the gas to be treated together with sulfur dioxide. In this embodiment, 11 tonnes of dihydrate gypsum is introduced into the first desulfurization reactor 110 through the liquid mixture supplied in an amount of 125 m 3 per hour from the first mixing tank 140a, and in the first desulfurization reactor 110, [ 1.2 tonnes of dihydrate gypsum is further generated by the oxidation reaction of Scheme 2, so that 12.2 tonnes of dihydrate gypsum is introduced and generated in the first desulfurization reactor 110, and discharged in an amount of 125 m 3 per hour through the drain 113a. 12.2 tons of gypsum per hour contained in the liquid mixture to be discharged to the outside through the drain port 113a. 3 tons of hydrated gypsum per hour of 12.2 tons of hydrated gypsum discharged to the outside through the drainage port 113a is contained in the liquid mixture discharged in an amount of 17㎥ per hour and discharged to the oxidation reactor 150, and the remaining 9.2 tons The dihydrate gypsum is combined with the liquid mixture discharged in an amount of 105 m 3 per hour and discharged into the first mixing tank 140a. The liquid mixture discharged through the drain port 113a includes a microbubble B formed by the atomizing unit 117.

The second desulfurization reactor 120 has the same configuration and function as the first desulfurizer 110 described above. The second desulfurization reactor 120 is circulated and supplied with the gas discharged from the first desulfurization unit 110, the liquid mixture stored in the second mixing tank 140b and the liquid mixture in the second desulfurization reactor 120, and the second desulfurization The gas discharged from the reactor 120 is supplied to the third desulfurization reactor 130. In the present exemplary embodiment, sulfur dioxide gas having a concentration of 20,000 ppm is introduced through the second desulfurization reactor 120 and sulfur dioxide gas having a concentration of 1,000 ppm is discharged. In this embodiment, 21.3 tons of dihydrate gypsum per hour is introduced into the second desulfurization reactor 120 through the liquid mixture supplied in an amount of 250 m 3 per hour from the second mixing tank 140b, and in the second desulfurization reactor 120, [ In the second desulfurization reactor 110, 22.4 tonnes of dihydrate gypsum is introduced and generated, and 22.4 tonnes of dihydrate gypsum are discharged to the outside through the drainage hole by the oxidation reaction of Scheme 2]. It explains. 22.4 tonnes of dihydrate gypsum contained in the liquid mixture of 250 m 3 per hour discharged to the outside through the drainage port of the second desulfurization reactor is supplied to the first mixing tank 140a.

The third desulfurization reactor 130 has the same configuration and function as the first desulfurization unit 110 described above. The third desulfurization reactor 130 is circulated and supplied with the gas discharged from the second desulfurization unit 120, the liquid mixture stored in the second mixing tank 140b, and the liquid mixture in the third desulfurization reactor 130, and the third desulfurization Gas discharged from the reactor 130 is discharged to the electric dust collector 190. In this embodiment, the sulfur dioxide gas having a concentration of 100 to 5,000 ppm is introduced through the third desulfurization reactor 130 and the sulfur dioxide gas having a concentration of 0 to 50 ppm is discharged. In this embodiment, 21.3 tonnes of dihydrate gypsum per hour is introduced into the third desulfurization reactor 130 through the liquid mixture supplied in an amount of 250 m 3 per hour from the second mixing tank 140b, and in the third desulfurization reactor 130, [ In the third desulfurization reactor 130, 22 tonnes of dihydrate gypsum is introduced and generated in the third desulfurization reactor 130, and 22 tonnes of dihydrate gypsum are discharged to the outside through the drain. It explains. 22 tons of dihydrate gypsum contained in the liquid mixture of 250 m 3 per hour discharged to the outside through the drainage port of the third desulfurization reactor is supplied to the second mixing tank 140b.

An exhaust fan F is installed in the exhaust line connected to the exhaust port of the third desulfurization reactor 130. When the exhaust fan F is operated, a negative pressure is formed in the second storage space of the third desulfurization reactor 130 and the second and second dehydration reactors 120 and 110 are continuously shown in FIG. 2. Likewise, the level of the second storage space is increased and the level of the first storage space is lowered, so that the microbubbles are formed and sprayed in the second storage space.

Referring to the desulfurization reactor 110 shown in FIG. 2, the action of forming microbubbles in the first, second, and third desulfurization reactors 110, 120, and 130 will be described in more detail. When the exhaust fan F is operated, a water level difference occurs between the two storage spaces 111a and 111b in the first desulfurization reactor 110 (the water level before the exhaust fan F is operated is (S1) and The same). As shown in FIG. 2, in the first desulfurization reactor 110, as the pressure of the second storage space 111b is lowered, the level of the second storage space 111b rises above the impingement plate 117b and the first storage space. The water level of 111a is lowered and the inlet 1171a of the nozzle 117a is opened. Accordingly, gas containing sulfur dioxide in the first storage space 111a is strongly injected upward from the second storage space 111b through the nozzle 117a. The gas injected from the nozzle 117a collides with the plurality of impingement plates 117b to form micro bubbles, thereby significantly improving the gas-liquid contact efficiency. Although not shown, the second desulfurization reactor 120 and the third desulfurization reactor 130 also generate microbubbles with the same action.

The first mixing tank 140a is supplied with a liquid mixture discharged from each of the first desulfurization reactor 110 and the second desulfurization reactor 120, and is evenly mixed using a stirrer. Dihydrate gypsum is included in both the liquid mixture supplied from the first desulfurization reactor 110 and the liquid mixture supplied from the second desulfurization reactor 120. The first mixing tank 140a is positioned below the first desulfurization reactor 110 and the second desulfurization reactor 120, so that the liquid mixture from the first desulfurization reactor 110 and the second desulfurization reactor 120 may be self-weighted. It moves to the 1st mixing tank 140a by this. In this embodiment, the liquid mixture is supplied in an amount of 108 m 3 per hour from the first desulfurization reactor 110, so that 9.2 tons of dihydrate gypsum is supplied in an hour, and the liquid mixture is supplied in an amount of 250 m 3 per hour from the second desulfurization reactor 120. It is explained that 22.4 tons of gypsum is supplied per hour. Some of the liquid mixture mixed in the first mixing tank 140a is moved and supplied by the weight to the second mixing tank 140b, and the other is moved by the pump P1 and supplied to the first desulfurization reactor 110. do. In this embodiment, the liquid mixture is supplied to the second mixing tank 140b in an amount of 233 m 3 per hour from the first mixing tank 140a so that 20.6 tons of gypsum is supplied to the second mixing tank 140b per hour, It will be described that the liquid mixture is supplied to the first desulfurization reactor 110 in an amount of 125 m 3 so that 11 tons of dihydrate gypsum is fed to the first desulfurization reactor 110 per hour. In this embodiment, the first mixing tank 140a will be described as maintaining pH 4-5.

The second mixing tank 140b is supplied with the calcium carbonate slurry discharged from the calcium carbonate supply unit 101, the liquid mixture discharged from the third desulfurization unit 130, and the liquid mixture discharged from the first mixing tank 140a. Mix evenly using a stirrer. Dihydrate gypsum is included in both the liquid mixture supplied from the third desulfurization reactor 130 and the liquid mixture supplied from the first mixing tank 140a. The second mixing tank 140b is located below the third desulfurization reactor 130 and the first mixing tank 140a, so that the liquid mixture from the third desulfurization reactor 130 and the first mixing tank 140a is self-weighted. It moves to the 2nd mixing tank 140b by this. In addition, as shown to move the calcium carbonate slurry from the calcium carbonate supply unit 101 to the second mixing tank 140b by its own weight, the calcium carbonate supply unit 101 is located below the calcium carbonate supply unit 101 as well. desirable. In this embodiment, the liquid mixture is supplied in an amount of 250 m 3 per hour from the third desulfurization reactor 130, and 22 tons of dihydrate gypsum is supplied in an hour, and the liquid mixture is supplied in an amount of 233 m 3 per hour from the first mixing tank 140a. It will be described that 20.6 tons of hydrated gypsum per hour is supplied, and the calcium carbonate slurry is supplied from the calcium carbonate supply portion 101 in an amount of 15 m 3 per hour. Some of the liquid mixture mixed in the second mixing tank 140b is moved and supplied by the pump P2 to the second desulfurization reactor 120, and the rest is moved by the pump P3 to the third desulfurization reactor 130. Is supplied. In this embodiment, the liquid mixture is supplied to the second desulfurization reactor 120 in an amount of 250 m 3 per hour from the second mixing tank 140b so that 21.3 tons of hydrated gypsum is supplied to the second desulfurization reactor 120 per hour, It will be described that the liquid mixture is supplied to the third desulfurization reactor 130 in an amount of 250 m 3 so that 21.3 tons of dihydrate gypsum is fed to the third desulfurization reactor 130 per hour. In the present embodiment, the second mixing tank 140b will be described as maintaining a pH of 4.5 to 5.5.

The first, second, and third desulfurization reactors 110, 120, and 130, the exhaust fan F, the first and second mixing tanks 140a and the transfer pumps P1, P2, and P3 are the desulfurization reactions of the present invention. Construct wealth.

In the oxidation reactor 150, a liquid mixture containing calcium sulfite discharged from the first desulfurization reactor 110 is supplied, and an oxidation reaction occurs as shown in [Scheme 2]. According to the oxidation reaction, dihydrate gypsum (CaSO ₄ · 2H ₂ O) is produced. ) Occurs. The oxidation reactor 150 is provided with an air supply unit 151 for the oxidation reaction. The liquid mixture discharged from the first desulfurization reactor 110 includes a microbubble, and the microbubble promotes the oxidation reaction in the oxidation reaction tank 150, thereby improving the efficiency of generating the gypsum. In this embodiment, the liquid mixture is supplied from the first desulfurization reactor 110 in an amount of 17 m 3 per hour, so that 3 tonnes of dihydrate gypsum is supplied to the oxidation reactor 150 per hour, and the hydrated gypsum is oxidized by the oxidation reaction in the oxidation reactor 150. It is described that a large amount is generated, and the dihydrate gypsum in the oxidation reactor 150 is increased to 6.62 tons per hour, and the dihydrate gypsum in the oxidation reactor 150 is discharged as the primary gypsum slurry and supplied to the first solid-liquid separator 160. In the present embodiment, the primary gypsum slurry is discharged from the oxidation reaction tank 150 in an amount of 17 m 3 per hour, and the primary gypsum slurry is included and discharged together with 6.62 tons of gypsum per hour. In the present embodiment, the oxidation reaction tank 150 will be described as maintaining a pH of 3.5 to 4.5.

The first solid-liquid separator 160 separates water from the first gypsum slurry discharged from the oxidation reactor 150. In the present embodiment, it will be described that the first solid-liquid separator 160 is a hydrocyclone device. The water separated from the first solid-liquid separator 160 is supplied to the water storage tank 180, and the remaining secondary gypsum slurry is supplied to the second solid-liquid separator 170.

The second solid-liquid separator 170 separates the water from the second gypsum slurry discharged from the first solid-liquid separator 160. In the present embodiment, the second solid-liquid separator 170 is described as a vacuum belt filter (VBF). The water separated in the second solid-liquid separator 170 is advanced to the water reservoir 180.

The intermediate reservoir 175 selectively stores the first gypsum slurry discharged from the first solid-liquid separator 160 before supplying it to the second solid-liquid separator 170.

The water reservoir 180 stores water separated from the first solid-liquid separator 160 and the second solid-liquid separator 170 and supplies a portion of the stored water to the calcium carbonate supply unit 101. In this embodiment, the water storage tank 180 will be described as supplying 14 ㎥ of water to the calcium carbonate supply unit 101 per day.

Although the present invention has been described through the above embodiments, the present invention is not limited thereto. The above embodiments may be modified or changed without departing from the spirit and scope of the present invention, and those skilled in the art will recognize that such modifications and changes also belong to the present invention.

100: wet flue gas desulfurization equipment 101: calcium carbonate supply unit
110: first desulfurization reactor 120: second desulfurization reactor
130: third desulfurization reactor 140a: first mixing tank
140b: second mixing tank 150: oxidation reaction tank
160: first solid-liquid separator 170: second solid-liquid separator
175: intermediate reservoir 180: water reservoir

Claims (15)

A first desulfurization reactor in which a desulfurization reaction occurs in which a calcium carbonate slurry containing calcium carbonate and sulfur dioxide contained in exhaust gas react to form calcium sulfite, and a calcium carbonate slurry containing calcium carbonate and discharged from the first desulfurization reactor. The second desulfurization reactor in which the sulfur dioxide contained in the gas reacts to produce calcium sulfite occurs, the calcium carbonate slurry containing calcium carbonate, and the sulfur dioxide contained in the gas discharged from the second desulfurization reactor react with calcium sulfite. A desulfurization reactor including a third desulfurization reactor for generating a desulfurization reaction, an exhaust fan for discharging gas from the third desulfurization reactor, a first mixing tank, and a second mixing tank;
A calcium carbonate supply unit for supplying the calcium carbonate to the desulfurization reaction unit; And
A oxidation reaction tank in which an oxidation reaction in which a liquid mixture containing oxygen and the calcium sulfite discharged from the first desulfurization reactor reacts to produce dihydrate gypsum occurs,
The first mixing tank mixes the liquid mixture discharged from the second desulfurization reactor with the remainder except for the amount supplied to the oxidation reaction tank among the liquid mixture discharged from the first desulfurization reactor,
The second mixing tank mixes a part of the calcium carbonate slurry supplied from the calcium carbonate supply unit, the liquid mixture discharged from the third desulfurization reactor, and the liquid mixture discharged from the first mixing tank,
Except for the amount of the liquid mixture discharged from the first mixing tank except the amount supplied to the second mixing tank is supplied to the first desulfurization reactor,
The liquid mixture discharged from the second mixing tank is respectively supplied to the second desulfurization reactor and the third desulfurization reactor,
Each of the first desulfurization reactor, the second desulfurization reactor, and the third desulfurization reactor may include a first storage space in which an inlet is formed, a second storage space in which an exhaust port is formed, and the second storage space. It has an atomizing part in communication with the storage space,
Sulfur dioxide contained in the calcium carbonate slurry and the exhaust gas is introduced through the inlet port of the first desulfurization reactor,
The exhaust port of the first desulfurization reactor and the inlet port of the second desulfurization reactor are in communication, the exhaust port of the second desulfurization reactor and the inlet port of the third desulfurization reactor are in communication,
By the operation of the exhaust fan, in each of the first desulfurization reactor, the second desulfurization reactor, and the third desulfurization reactor, a negative pressure is formed in the second storage space, so that the water level of the second storage space is increased, 1 As the water level of the storage space is lowered, the gas in the first storage space to form a microbubble by the atomizing portion and the wet flue gas desulfurization facility is injected into the second storage space. delete delete delete delete The method according to claim 1,
In the first desulfurization reactor, the second desulfurization reactor, and the third desulfurization reactor, the wet flue gas desulfurization also occurs along with an oxidation reaction in which oxygen contained in the exhaust gas reacts with the calcium sulfite produced by the desulfurization reaction to generate dihydrate gypsum. equipment. delete The method according to claim 1,
The amount of the liquid mixture supplied from the first desulfurization reactor to the first mixing tank is controlled in accordance with the oxidation reaction capacity of the oxidation reactor. The method according to claim 1,
Wet flue gas desulfurization facility is installed in the oxidation reaction tank air supply. The method according to claim 1,
And a first solid-liquid separator for separating water from the gypsum slurry discharged from the oxidation reactor. The method according to claim 10,
The first solid-liquid separator is a hydro cyclone (Hydro Cyclone) wet flue gas desulfurization facility. The method according to claim 10,
And a second solid-liquid separator for separating water from the gypsum slurry discharged from the first solid-liquid separator. The method according to claim 12,
The second solid-liquid separator is a vacuum flue gas filter (Vacuum Belt Filter). The method according to claim 13,
And an intermediate reservoir in which the gypsum slurry discharged from the first solid-liquid separator is selectively stored before being supplied to the second solid-liquid separator. The method according to claim 13,
And a water reservoir for storing water separated from the first solid-liquid separator and the second solid-liquid separator and supplying the stored water to the calcium carbonate supply unit.

Images