KR101349959B1 - Absorption tower having multi-reaction tank - Google Patents

Abstract

The present invention is to install a new reaction tank adjacent to the existing reaction tank so that a sufficient amount of acidic gas is collected by the slurry is recycled and sprayed, so that both reaction tanks are interconnected by a connecting pipe having a certain form and the movement of the slurry and A wet absorption tower having multiple reactors is characterized in that the circulation is smooth and the slurry is allowed to remain for a sufficient time in the increased reactor.
The wet absorption tower having the multiple reaction tank of the present invention comprises: a first reaction vessel containing a slurry for neutralizing oxides in exhaust gas and having a gypsum discharge port formed on a lower side thereof; A plurality of absorbent liquid supply nozzles and a plurality of absorbent liquid injection nozzles formed for each of the absorbent liquid supply pipes are disposed continuously in the upper portion of the first reaction tank, and an exhaust gas inlet is formed in a lower portion adjacent to the first reaction tank, and a process gas outlet is provided in the upper portion. An absorption chamber formed; A second reaction tank is formed adjacent to the first reaction tank, and the second reaction tank is connected to the first reaction tank by a connecting pipe, so that the slurry is moved from the first reaction tank to the second reaction tank.

Description

Absorption tower having multi-reaction tank

The present invention relates to a wet absorption tower having a multiple reaction tank, and more particularly, a new reaction tank is installed adjacent to an existing reaction tank so that a sufficient amount of acid gas is collected by a slurry that is recycled and sprayed, and both reactors are fixed. The present invention relates to a wet absorption tower having a multiple reaction tank, which is connected to each other by a connecting pipe having a form so as to smoothly move and circulate the slurry, and allow the slurry to stay in the increased reaction tank for a sufficient time.

Flue gas desulfurization equipment is a decontamination facility that removes sulfur oxides (SO _x ) and acid gases such as hydrogen chloride (HCl) and hydrogen fluoride (HF) contained in the exhaust gas using alkali chemicals. The desulfurization equipment is classified into dry, semi-dry or wet depending on whether water is used, and as an absorbent, limestone (CaCO ₃ ), calcareous lime (Ca (OH) ₂ ), ammonia (NH ₃ ), caustic soda (NaOH) or magnesium carbonate Alkali chemicals such as (MgCO ₃ ) are used.

As a method of treating sulfur oxide (SO _x ) and acidic gas contained in the exhaust gas, generally, a wet desulfurization system using limestone (CaCO ₃ ) is mainly used. The wet desulfurization method has a high initial investment cost. However, this method is mainly used in large facilities because of low operating maintenance costs. In addition, limestone (CaCO ₃ ) is used in a large amount of desulfurization equipment because it has an advantage that it can be used inexpensively unlike relatively expensive products such as caustic soda (NaOH) as a large amount of alkali material produced in Korea.

However, there is a situation in which the wet desulfurization facility needs to improve performance due to deterioration of fuel conditions and emission regulations due to strengthening environmental standards. 1 is a view showing an absorption tower according to the prior art, and shows that acid gas is absorbed through gas-liquid contact in the absorption chamber 30 after untreated gas enters the absorption tower. The absorbed acid gas is treated in the reaction tank 10 by the following reaction, and the slurry is supplied to the absorption liquid spray nozzle 63 by the recirculation pump 40 and re-injected to reabsorb the acid gas in the gas.

SO ₂ (g) + H ₂ O → H ₂ SO ₃ (aq) ... (1)

_{H 2 SO 3 (aq) ↔} H + + HSO 3 - ↔ 2H + + SO 3 2 - ................... (2)

Ca ^{2 +} + SO ₃ ^{2 -} ↔ CaSO ₃ ......................... (3)

In order to complete the reaction up to (3), a certain residence time is required. When the residence time is insufficient, a sufficient amount of acid gas cannot be collected when the slurry is recycled and injected. Therefore, in order to be able to recapture the acid gas, the slurry should be designed to be recycled after sufficiently remaining in the reaction tank 10, and the reaction tank residence time of the slurry depends on the capacity of the recycle pump 40 and the size of the reaction tank 10. Is determined. As such, the residence time, which is directly related to the absorption efficiency of sulfur oxides (SO _x ), is determined by the capacity of the recycle pump is called 'liquid residence time'.

Sulfur oxide (SO _x ) moved to the reactor 10 is regenerated into gypsum (CaSO ₄ · 2H ₂ O) through the following process.

O ₂ (g) → O ₂ (aq) ... 4)

^{_{HSO 3 - + ½O 2 → H}} + + SO 4 2 - .............................. (5)

^{_{SO 3 2 - + ½O 2 →}} SO 4 2 - ................................... (6)

CaCO ₃ (s) + 2H ⁺ → Ca ^{2 +} + H ₂ O + CO ₂ ... (7)

_{^{Ca 2 + + SO 3 2 -}} + ½H 2 O → CaSO 3 · ½H 2 O (s) ................... (8)

_{^{Ca 2 + + SO 4 2 -}} + 2H 2 O → CaSO 4 · 2H 2 O (s) .................... (9)

The process is also carried out in the reaction vessel 10 located below the absorption tower, the process requires a lot of time because it involves the dissolution of limestone and oxidation of sulfite. In this case, if the required residence time is not sufficient, the quality of the gypsum may be deteriorated, which may affect the rear end equipment or reduce the price of the gypsum. The time in which gypsum is made through the above process is referred to as a 'solid residence time', and the 'solid residence time' is determined according to a rate at which sulfur oxides are introduced.

The 'liquid residence time' or 'solid residence time' are all related to the size of the reactor 10, and if any of the residence time is insufficient, effective removal of acid gas is difficult to expect.

Recently, due to the deterioration of fuel quality, the proportion of acid gas in the exhaust gas flowing into the desulfurization facility is gradually increasing, and related laws that limit the allowable concentration of the acid gas contained in the exhaust gas continue to be strengthened. to be. The concentration of sulfur oxides (SO _x ) was only 300 ~ 400 ppm, but now, due to the deterioration of fuel quality, it is gradually increasing to 800 ~ 900 ppm, and environmental regulations are continuously strengthened, resulting in lower emission pollution standards. It is a reality.

Therefore, there is a need to improve the performance of the currently installed and operated desulfurization equipment, because it is expensive and time-consuming to replace the existing desulfurization equipment with a height of 30m and a reactor diameter of about 15m with new equipment. As a way of maintaining the method may be considered to increase the capacity of the recirculation pump (40). However, if the capacity of the recirculation pump is increased, the 'liquid residence time' decreases, which may reduce the absorption efficiency of sulfur oxides. The residence time 'also has a problem of decreasing.

As described above, the increase in the recirculation pump decreases the 'liquid residence time' and the 'solid residence time', thereby making it difficult to effectively remove sulfur oxides, thereby improving the desulfurization facility by extending the residence time. Consideration may be given to increasing the reactor of the desulfurization slurry in a manner. As a method of changing the size of the reactor 10, there may be a method of increasing the width of the existing desulfurization absorption tower or changing the height, but the method is to change the width or height of the absorption tower already installed. According to the company, all civil installations that have been done must be rebuilt, and the burden of changing all relevant ducts, pumps, foundations, etc. will be burdened.

Figure 2 is a view showing a reaction tank increase method of the conventional absorption tower, in the case of Figure 2 is to install a separate reaction tank to increase the reaction tank. According to FIG. 2, the existing reaction tank is configured as a circulation loop at the lower end, but the absorption chamber 30 in the upper part of the absorption tower is connected to the newly formed reaction tank so as to be configured as the upper circulation loop. In addition, in the case of the above technology, after the additional absorption chamber is formed on the upper side of the existing absorption tower, it is characterized in that the trap tray is further installed so that the slurry injected from the upper side may be introduced into the new reaction tank.

However, the above technique only looks as one absorption tower structure, and the absorption tower at the bottom and the top is substantially configured as two absorption towers connected in series. Therefore, in the case of the absorption tower according to the above technique, limestone should be separately introduced into each of the upper and lower ends, and accordingly, there is a problem that the work of checking the hydrogen ion concentration and taking out the gypsum must be separately performed.

1. As the addition of the absorption chamber with the injection nozzle 63 on the upper part of the existing absorption tower, during the renovation work is not possible to operate this facility, causing a large loss due to business suspension.

2. As the height increases to the top of the absorption tower, civil engineering design and construction must be redone and the structure itself must be changed, resulting in an increase in retrofit costs.

3. Trapout tray may cause clogging due to slurry, which may result in high pressure loss and higher retrofit costs.

4. The installation volume increases according to the complete separation of the top and bottom, and the investment cost increases and the operation of the equipment becomes complicated as the basic control such as the maintenance of pH, the injection of limestone, and the extraction of gypsum is performed separately.

5. The pressure loss of the gas increases and the number of recirculation pumps for supplying the slurry to the upper absorption chamber increases the energy cost and eventually the operating cost.

Japanese Patent Application Laid-Open No. 2004-209328 A (published date: 2004.07.29) of FIG. 3 further includes an absorption chamber at the top of an existing absorption tower, but in the case of the above technology, a civil engineering design is performed according to an increase in the height of the absorption tower. And the construction, etc. must be re-constructed, and accordingly the secondary equipment also has to be re-equipped, there is a problem that the increase in equipment and operating costs.

JP 2004-209328 A 2004.07.29.

The present invention was created to solve the problems of the prior art, the installation of a new reaction tank adjacent to the existing reactor to extend the residence time of the slurry while minimizing the number of days of change and downtime of the existing equipment, the conventional The present invention relates to a wet absorption tower having multiple reactors that can be used as is or by relocating from an existing reactor to a new reactor, thereby minimizing civil engineering or building redesign.

Wet absorption tower having a multiple reaction tank of the present invention for achieving the above object, the first reaction tank for receiving a slurry for neutralizing the oxide in the exhaust gas and the gypsum outlet is formed on the lower side; A plurality of absorbent liquid supply nozzles and a plurality of absorbent liquid injection nozzles formed for each of the absorbent liquid supply pipes are disposed continuously in the upper portion of the first reaction tank, and an exhaust gas inlet is formed in a lower portion adjacent to the first reaction tank, and a process gas outlet is provided in the upper portion. An absorption chamber formed; A second reaction tank is formed adjacent to the first reaction tank, and the second reaction tank is connected to the first reaction tank by a connecting pipe, so that the slurry is moved from the first reaction tank to the second reaction tank.

In addition, the connection pipe of the wet absorption tower having a multiple reaction tank of the present invention is characterized in that it is formed to protrude a predetermined length into the first reaction tank and the second reaction tank.

In addition, the vertical angle (θ) of the first reaction tank of the connection pipe of the wet absorption tower having a multiple reaction tank of the present invention is characterized in that it is formed below 75 °.

In addition, the horizontal angle (Φ) of the connection pipe of the wet absorption tower having a multiple reaction tank of the present invention is characterized in that it is formed to 80 ° or less with respect to the external tangential direction.

In addition, the slurry deposition preventing portion for preventing the deposition of the slurry is further provided on the upper portion of the connection pipe protruding into the first reaction tank of the wet absorption tower having a multiple reaction tank of the present invention.

In addition, the first or second reaction tank of the wet absorption tower having a multiple reaction tank of the present invention is characterized in that the recirculation pump for supplying the slurry discharged through the absorption liquid discharge pipe is further provided.

In addition, the slurry of the first reaction tank of the wet absorption tower having a multiple reaction tank of the present invention is to be injected from the injection nozzle of the absorption liquid supply pipe formed at the lower end in the absorption chamber, the slurry of the second reaction tank of the absorption liquid supply pipe formed at the upper end of the absorption chamber It characterized in that the injection from the injection nozzle.

In addition, the connection pipe of the wet absorption tower having a multiple reaction tank of the present invention is characterized in that the flow control valve for controlling the amount of movement of the slurry moved from the first reactor to the second reactor.

In addition, the connection pipe of the wet absorption tower having a multiple reaction tank of the present invention is characterized in that it is installed at a height of 1/3 or more of the slurry level of the first and second reaction tank.

According to the present invention, since a new reaction tank is installed separately from the existing reaction tank, it is possible to minimize the period of shutdown due to facility modifications, and to minimize changes, modifications, and civil engineering design of related equipment.

In addition, according to the present invention, even if the reaction tank is increased to two or more, since the control of the pH control, limestone injection amount, gypsum circulation amount, etc. is carried out in the existing reactor, the operation of the equipment can be maintained as it is, thus adding the cost of equipment for new control It is economical because it does not occur, and it requires only the minimum cost according to the connection cost between the new reactor and the existing reactor.

In addition, according to the present invention, even if the recirculation pump is moved to a new reactor, the additional cost of power due to the level difference can be minimized because the level difference between the existing reactor and the new reactor is maintained only as necessary.

1 is a view showing an absorption tower according to the prior art.
Figure 2 is a view showing a reaction vessel increase method of the conventional absorption tower.
Figure 3 is a view showing the absorption chamber increasing method of the conventional absorption tower.
Figure 4 is a view showing a first embodiment of the present invention showing an absorption tower in which the reaction vessel is increased.
5 is a view showing a second embodiment of the present invention showing an absorption tower with increased reactor.
6 and 7 show a third embodiment of the present invention showing an absorption tower with increased reaction vessel.
Figure 8 is a view showing a planar cross-sectional view of the connecting pipe connecting the first reactor and the second reactor of the absorption tower is increased in accordance with the present invention.

Hereinafter, with reference to the accompanying drawings will be described in detail a preferred embodiment of the present invention.

Figure 4 is a view showing a first embodiment of the present invention showing an absorption tower with an increased reaction tank, the present invention is not installed or changed to the absorption chamber at the top of the absorption tower, but additionally installed a second reaction tank (20) Construction of equipment can proceed. According to the present invention, the slurry sprayed from the absorption tower falls to the first reaction tank 10, which is an existing reaction tank, and the slurry exceeding the highest level of the first reaction tank 10 is moved to the second reaction tank 20, which is a new reaction tank. Thereby increasing the reaction tank residence time of the slurry, and the existing recirculation pump 40 is relocated to the second reactor 20 so that the high-quality slurry having the increased residence time is re-injected through the absorption liquid spray nozzle 63. do.

According to the present invention, since the capacity of the recycle pump 40 is much larger than the amount of limestone supplied or the amount of gypsum taken out, the pipe to which limestone is supplied or the pump from which gypsum is taken out does not move to the second reactor 20. It is to be positioned as it is in the first reaction tank 10 without.

The second reaction tank 20 is located as close as possible from the first reaction tank 10 to prevent deposition and wear of the connecting pipe 50 due to the movement of the slurry. Slurry movement from the first reaction tank 10 to the second reaction tank 20 is made through the connecting pipe 50. If the moving speed of the slurry is too fast, the inside of the connecting pipe 50 is easily worn out and the service life is increased. Since it becomes short, the maximum moving speed of the slurry flowing through the connecting pipe 50 does not exceed 2.5m / s.

In addition, the connection pipe 50 is a vertical angle (θ) relative to the first reaction tank 10 to be 75 ° or less to prevent the deposition of slurry in the pipe to the second reaction tank 20 from the first reaction tank (10) In order to smoothly move the slurry, and to protrude a portion of the first reaction tank 10 and the second reaction tank 20 to the extent that does not impair the performance of the stirrer (14). When the protrusion of the connecting pipe 50 is not formed in the reaction tank, the slurry of the first reaction tank 10 does not stay in the first reaction tank 10 for a predetermined time while the slurry rotates according to the stirring of the stirrer 14. Since there may be a case in which the connection to the second reaction tank 20 directly through the connection pipe, the connection pipe 50 by protruding a predetermined portion into the interior of the reaction tank by the stirring action of the stirrer 14 for a certain time It is to be prevented from moving to another reactor without staying.

The connection pipe 50 protrudes into the first reaction tank 10, and the slurry moves in a downward direction of 75 ° or less from the first reaction tank 10 to the second reaction tank 20 through the connection pipe 50. Due to the structure, deposits of slurry may accumulate on an upper portion of the connection pipe 50 protruding from the first reaction tank 10. In order to prevent this by forming a slurry deposition prevention portion 52 on the upper portion of the connection pipe 50 protruding to the first reaction tank 10 of the present invention to prevent the deposition of slurry, the slurry deposition prevention portion 52 For example, to prevent the slurry deposition by forming a closed surface toward the top of the inner surface of the first reaction tank 10 from the upper end of the protrusion of the connection pipe 50.

The connecting pipe 50 connecting the first reaction vessel 10 and the second reaction vessel 20 is installed at a height higher than 1/3 of the slurry level of both reaction vessels so that the operation of the stirrer formed at the bottom thereof is not disturbed. The stirrer 14 prevents the deposition of the slurry while the stirrer blade 14a rotates in the reaction tank, and the maximum effect of the gypsum production reaction can be obtained by the rotary stirring action of the stirrer 14. According to the present invention, the efficiency and reliability of the desulfurization plant operation are improved because the consumption of air introduced by the scattering action by the stirrer 14 is reduced.

Therefore, the connection pipe 50 of both reaction tanks according to the present invention is formed at the height of 1/3 of the slurry level of both reactors so as not to interfere with the rotation operation of the stirrer 14, and is installed in the first reactor 10 The upper end of the connection pipe 50 is selected based on the lowest water level of the first reactor. According to the present invention, the difference in the water level between the first reactor 10 and the second reactor 20 during operation depends on the operation speed of the recirculation pump 40 and the slurry movement speed in the connecting pipe 50 connecting both reaction tanks. It happens naturally.

FIG. 5 is a view showing a second embodiment of the present invention showing an absorption tower with increased reaction tanks. Unlike the first embodiment, the recirculation pump 40 is divided into the first reaction tank 10 and the second reaction tank 20. And the slurry supplied to the absorbent liquid supply pipe 62 of the absorption chamber 30 may be supplied from both reaction tanks. The second embodiment of the present invention corresponds to a case where the capacity of the newly established second reactor 20 is significantly smaller than that of the first reaction tank 10, and the capacity of the second reaction tank 20 is smaller than that of the absorption chamber 30. Since the amount of the slurry to be supplied) is small, the recirculation pump 40 is arranged to be distributed so that the slurry can be supplied even in the first reactor 10.

According to the second embodiment of the present invention, the absorbent liquid supply pipe 62 formed at the lower end of the absorption chamber 30 by the recirculation pump 40 formed in the first reaction tank 10 is stored in the first reaction tank (10) And the slurry stored in the second reaction tank 20 is the absorption liquid supply pipe formed at the upper end in the absorption chamber 30 by the recirculation pump 40 formed in the second reaction tank 20. It is injected through the injection nozzle 63 of (62). The exhaust gas flowing into the absorption tower is processed while rising to the upper part, but is partially processed through the lower injection nozzle, but is substantially processed through the upper injection nozzle.

According to the second embodiment of the present invention, the slurry of the first reaction tank 10 having a short residence time of the reaction tank is to be injected from the injection nozzle of the absorption liquid supply pipe 62 formed at the lower end in the absorption chamber 30, the second reaction tank The slurry of 20 is sprayed from the injection nozzle of the absorbent liquid supply pipe 62 formed at the top to maximize the treatment efficiency of sulfur oxides or acid gases. Referring to Figure 5, it can be seen that the slurry of the first reaction tank 10 is supplied to the lower two stages of the absorption liquid supply pipe 62 in the absorption chamber 30, the upper two stages of the second reaction tank 20 It can be seen that the slurry is supplied.

The second embodiment of the present invention has a smaller capacity of the second reactor 20, so that the recirculation pump 40 is divided into and installed in the first reactor 10 and the second reactor 20 in the first embodiment. Since it is the same as the detailed description thereof will be omitted.

6 and 7 are views showing a third embodiment of the present invention showing an absorption tower with increased reaction tanks, such that the flow control valve 51 is located above the first reaction tank 10 of the connection pipe 50. And, it is characterized in that to adjust the water level of the newly formed second reaction tank 20 by allowing the flow control valve 51 to be opened and closed as necessary.

In the case of the first embodiment of Figure 4, since the flow of the slurry is formed according to the natural water level difference between the first reactor 10 and the second reactor 20, the connecting pipe 50 is the upper portion of the first reactor (10) At the bottom of the second reaction vessel 20 is configured to be maintained in a straight line, thereby preventing the slurry deposition portion 52 for preventing the slurry deposition on the upper end of the connection pipe 50 protruding into the first reaction vessel 10. However, since the third embodiment of the present invention can control the flow of the slurry in both reaction tanks using the flow control valve 51, it is not necessary to keep the connecting pipe 50 in a straight line. 6 and 7, it can be seen that the connection pipe 50 is formed by bending to the left and right of the flow control valve 51, and thus the connection pipe protruding into the first reaction tank 10. At the top of the configuration of the slurry deposition prevention portion required in the first embodiment of Figure 4 can be omitted.

According to the third embodiment of the present invention, the bottom surface of the second reaction vessel 20 may be located on the same horizontal plane as the first reaction vessel 10, or be formed below a certain depth underground. 6 shows that the bottom surface of the second reaction vessel 20 is located on the same horizontal plane as the first bottom surface, and FIG. 7 shows that the bottom surface of the second reaction vessel 20 is located below the basement depth. . However, the height of the upper end of the second reaction tank 20 is equal to or higher than the highest level of the slurry stored in the first reaction tank 10 so that the slurry of the first reaction tank 10 is not saturated in the second reaction tank 20. To be accepted.

According to the present invention, when the water level difference between the first reactor 10 and the second reactor 20 is 2 m, a slurry flow of about 5 m / s may occur, so that the flow control valve 51 is connected to the connecting pipe 50. It can be installed in to prevent the wear of the connecting pipe 50 due to the over-flow of the slurry, the flow control valve 51, for example, by using the Knife Gate Type to maintain the opening and closing of the connecting pipe 50 according to the flow rate Do it. The flow control valve is a necessary configuration when the height of the second reactor 20 is to be kept constant, and since the slurry may be deposited around the valve due to the installation of the valve, it is necessary to prevent the deposition of the slurry if necessary. It is also possible to provide a separate configuration around the flow control valve.

6 and 7 show a state in which the recirculation pump 40 is divided into a first reaction tank 10 which is an existing reaction tank and a second reaction tank 20 which is a new reaction tank, and according to the present invention, The slurry is supplied and sprayed through the recirculation pump installed in the second reaction tank 20, so that the slurry may be supplied by the recirculation pump installed in the first reaction tank 10 as necessary. Also in the third embodiment of the present invention, the slurry of the first reaction tank 10 having a short residence time of the reaction tank is to be injected from the injection nozzle of the absorption liquid supply pipe 62 formed at the lower end in the absorption chamber 30, the second reaction tank The slurry of 20 may be injected from the injection nozzle of the absorbent liquid supply pipe 62 formed at the upper end in the absorption chamber 30 to increase the treatment efficiency of the exhaust gas.

8 is a connection pipe 50 connecting the first reactor 10, the second reactor 20, and the first reactor 10 and the second reactor 20 of the absorption tower with increased reaction tank according to the present invention. As a view showing a planar cross section of the slurry slurry 60 is rotated in accordance with the rotation of the stirrer 14, it can be seen that the connection pipe 50 is formed at a predetermined angle with respect to the rotation of the slurry (60). have. According to the present invention, the agitator 14 is separately formed in the first reactor 10 and the second reactor 20, respectively, and the internal slurry maintains the flow according to the driving of the agitator 14.

In the case of the present invention, the flow of the slurry may be interrupted by the end of the protruding connecting pipe 50 due to the characteristic that a portion of the connecting pipe 50 protrudes into both reactors. Therefore, according to the present invention, the connecting pipe 50 protruding in the reaction tank is formed to be 80 ° or less with respect to the flow direction so as not to interfere with the circulation of the slurry.

8 shows a structure in which the horizontal rotation flow of the slurry according to the operation of the stirrer 14 is not affected by the connection pipe 50 protruding inside the reactor. Referring to FIG. 8, the horizontal angle Φ of the connection pipe is an angle made with respect to a tangential direction outside the reaction tank, and the horizontal angle Φ in the present invention is formed to be 80 ° or less.

When the protrusion inside the reactor of the connecting pipe 50 is formed close to 90 ° with respect to the rotational direction of the slurry or is formed at 90 ° or more, the flow of the slurry may not be made smoothly or stays in the reactor for a certain time. There is a possibility that the slurry moves to another reactor through the connecting pipe 50. In order to prevent this, in the present invention, by maintaining the angle of the connection pipe 50 in the slurry rotation direction to 80 ° or less, it does not interfere with the rotation flow of the slurry and at the same time to maintain a stable reaction tank residence time of the slurry.

While the present invention has been particularly shown and described with reference to exemplary embodiments thereof, it is to be understood that the invention is not limited to the disclosed exemplary embodiments, but, on the contrary, It will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the spirit and scope of the invention as defined by the appended claims. That is, in the present invention, the embodiment has been described above with one example of a new reaction tank. However, when there is room in the surrounding space or an extension of the residence time is required, it is also possible to install and operate two or more new reaction tanks.

10: first reactor 11: exhaust gas inlet
12: process gas outlet 13: gypsum outlet
14: stirrer 14a: stirring blade
20: second reactor 30: absorption chamber
40: recirculation pump 50: connection piping
51: flow control valve 52: slurry deposition prevention portion
60: slurry 61: absorption liquid discharge pipe
62: absorbent liquid supply pipe 63: absorbent liquid spray nozzle
100: absorption tower
v: moving speed θ: vertical angle
Φ: horizontal angle

Claims (9)

A first reactor (10) containing a slurry for neutralizing the oxide in the exhaust gas and having a gypsum outlet (13) formed at a lower side thereof;
Continuously positioned in the upper portion of the first reaction tank 10 and provided with a plurality of absorbent liquid supply pipe 62 and a plurality of absorbent liquid spray nozzles 63 formed for each of the absorbent liquid supply pipe 62, in the first reaction tank (10) An exhaust chamber inlet 11 formed at an adjacent lower portion, and an absorption chamber 30 in which a processing gas outlet 12 is formed at an upper portion thereof;
A second reaction tank 20 is formed adjacent to the first reaction tank 10, and the second reaction tank 20 is connected to the first reaction tank 10 by a connecting pipe 50 so that the slurry 60 is formed. To move from the first reaction tank 10 to the second reaction tank 20,
The connection pipe 50 is a wet absorption tower having a multiple reaction tank, characterized in that formed by protruding a predetermined length into the interior of the first reaction vessel (10) and the second reaction vessel (20).
delete The method of claim 1,
Vertical absorption angle (θ) of the first reaction tank (10) of the connecting pipe 50 is a wet absorption tower having a multiple reaction tank, characterized in that formed in less than 75 °.
The method of claim 1,
Horizontal angle (Φ) with respect to the rotation direction of the slurry 60 of the connecting pipe 50 is a wet absorption tower having a multiple reaction tank, characterized in that formed in less than 80 °.
The method of claim 1,
Wet absorption tower having a multi-reactor, characterized in that the slurry deposition prevention portion 52 for preventing the deposition of the slurry is further provided on the upper portion of the connecting pipe 50 protruding into the first reaction tank (10).
The method of claim 1,
The first absorption tank 10 or the second reaction tank 20 is a wet absorption having a multiple reaction tank, characterized in that the recirculation pump 40 for supplying the slurry 60 discharged through the absorbent liquid discharge pipe 61 is further provided. tower.
The method according to claim 6,
The slurry of the first reaction tank 10 is to be injected from the injection nozzle of the absorbent liquid supply pipe 62 formed at the lower end in the absorption chamber 30, the slurry of the second reaction tank 20 is formed at the upper end in the absorption chamber 30 Wet absorption tower having a multiple reaction tank, characterized in that to be injected from the injection nozzle of the absorbent liquid supply pipe (62).
The method of claim 1,
The connection pipe 50 is wet absorption having a multiple reaction tank further comprises a flow control valve 51 for adjusting the amount of movement of the slurry moved from the first reaction tank 10 to the second reaction tank 20 tower.
The method of claim 1,
The connection pipe 50 is a wet absorption tower having a multiple reaction tank, characterized in that installed in the height of 1/3 or more of the slurry level of the first, second reaction tank (10, 20).

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