JP2001246229A - Method and apparatus for treating exhaust gas - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a method and apparatus for treating exhaust gas using cross flow moving bed type reactor, capable of ensuring a desulfurization/ denitration ratio while suppressing the NH3/SO2 ratio on a carbonaceous catalyst after adsorbing treatment low. SOLUTION: The exhaust gas to be treated sent from a line L1 is guided to a first reactor 10 while ammonia is added to the exhaust gas through a line L2 to be subjected to desulfurization and denitration treatment and the treated gas is guided to a second reactor 20 while SOx recovered with a regenerator 30 is added to the treated gas through a line L22 to be treated with SOx. The carbonaceous catalyst is sent to the reactor 20 from the reactor 10 and regenerated with the regenerator 30 to be returned and circulated to the reactor 10.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

The present invention relates to an exhaust gas treatment method and apparatus for desulfurization and denitration, and more particularly to an exhaust gas treatment method and apparatus using a cross-flow moving bed reactor using a carbonaceous catalyst.

[0002]

2. Description of the Related Art There is known a desulfurization and denitration method for treating sulfur oxides (SOx) and nitrogen oxides (NOx) contained in exhaust gas using a carbonaceous catalyst such as activated carbon (which also functions as an adsorbent). ing. In this desulfurization and denitration method, the sulfur oxides in the exhaust gas are adsorbed on the carbonaceous catalyst as sulfuric acid, and further converted into ammonium sulfate by the reaction with the added ammonia to be adsorbed and removed. On the other hand, nitrogen oxides are decomposed and removed by reaction with ammonia added to exhaust gas.

[0003]

Since the carbonaceous catalyst is inactivated by the adsorption of sulfuric acid and ammonium salt, it needs to be heated and regenerated. At this time, the molar ratio of ammonia and SO ₂ present on the carbonaceous catalyst (NH ₃ / SO ₂ : actually NH ₄ ⁺ / SO ₄
When ²⁾ is high, the lower the decomposition rate of ammonia in the regenerator, As a result, a high concentration of SO ₂ will be a large amount of ammonia is mixed, closed and collected products of the device in the sub-product recovery step is recovered Problems such as a decrease in purity occur. Further, in a gas cleaning step by water washing or the like, it is dissolved in wastewater as an ammonium salt (such as ammonium sulfite), and its treatment is required. When the temperature of the exhaust gas is low (about 100 ° C. or lower), the pores of the catalyst may be broken by ammonium sulfate generated on the carbonaceous catalyst, and powder may be broken at a low temperature. As the amount of added ammonia is increased to improve the denitration performance,
These problems become significant.

[0004] In view of the above problems, the present invention provides a cross-flow moving bed reaction capable of securing a desulfurization / denitration rate while keeping the NH ₃ / SO ₂ ratio on the carbonaceous catalyst after the adsorption treatment low. An object of the present invention is to provide a method and an apparatus for treating exhaust gas using a vessel.

[0005]

In order to solve the above problems, an exhaust gas treatment method according to the present invention comprises: (1) a step of adding ammonia to at least a part of exhaust gas to be treated;
(2) a first treatment step of introducing and treating the ammonia-added and non-added exhaust gas to a first cross-flow moving bed reactor;
(3) A second treatment in which at least a part of the treated exhaust gas in the first treatment step is guided to a second cross-flow moving bed reactor to be treated.
(4) a step of heating the used carbonaceous catalyst in an inert gas to recover sulfur oxides and regenerate the carbonaceous catalyst, and (5) a step of treating the regenerated carbonaceous catalyst. (6) mixing a part of the sulfur oxide recovered in the regeneration step with the exhaust gas guided to the second cross-flow moving bed reactor And a step of performing

On the other hand, an exhaust gas treatment apparatus according to the present invention
(1) A moving bed is formed by flowing the carbonaceous catalyst filled therein vertically downward, and the moving bed and the introduced exhaust gas are brought into contact with each other in a cross flow to treat the exhaust gas in the first and second columns. An AC moving bed type reactor, (2) an addition device for adding ammonia to at least a part of the exhaust gas led to the first cross flow moving bed type reactor, and (3) a first cross flow moving bed type reaction Exhaust gas transfer means for leading at least a part of the exhaust gas passing through the reactor to the second cross-flow moving bed reactor, and (4) heating the used carbonaceous catalyst in an inert gas to remove sulfur oxides. A regenerator that recovers and regenerates the carbonaceous catalyst, (5) a carbonaceous catalyst circulating means for returning and recycling the regenerated carbonaceous catalyst to each cross-flow moving bed reactor, and (6) a regenerator Of a part of the sulfur oxides recovered in the exhaust gas introduced to the second cross-flow moving bed reactor Characterized in that it comprises a means.

[0007] According to the exhaust gas treatment apparatus and method of the present invention, ammonia is added to a part of the exhaust gas and guided to the first cross-flow moving bed reactor for treatment. The catalyst is adsorbed and removed by the catalyst, and denitration is performed by a catalytic reaction between ammonia and NOx. Here, if the injection amount of ammonia is increased in order to enhance the denitration performance, the amount of ammonia leaked to the processing gas increases, but the SOx recovered by the regenerator is added to a part of the processing gas to perform the second cross-flow movement. By passing through the bed reactor, the leaked ammonia and the added SOx are adsorbed and removed by the carbonaceous catalyst. Thereby, NH ₃ / SO ₂ adsorbed on the carbonaceous catalyst
The ratio is kept low, and the decomposition rate of ammonia during regeneration in the regenerator is improved. And it becomes easy to increase the injection amount of ammonia, and it is possible to enhance the denitration performance.

[0008] In the circulation reuse step of the exhaust gas treatment method according to the present invention, the regenerated carbonaceous catalyst is guided to a first cross-flow moving bed reactor and discharged from the first cross-flow moving bed reactor. It is preferable to introduce the carbonaceous catalyst into the second cross-flow moving bed reactor. On the other hand, the carbonaceous catalyst circulating means of the exhaust gas treatment apparatus according to the present invention comprises: a carbonaceous catalyst returning means for introducing the regenerated carbonaceous catalyst into the first cross-flow moving bed reactor; A carbonaceous catalyst transfer means for introducing the carbonaceous catalyst discharged from the bed reactor into the second cross-flow moving bed reactor, and a carbonaceous catalyst discharged from the second cross-flow moving bed reactor. And a carbonaceous catalyst discharging means for leading to a regenerator.

As described above, by passing the carbonaceous catalyst in the order of the first reactor → the second reactor, the carbonaceous catalyst can be effectively used while ensuring the desulfurization and denitration performance in the first reactor. can do.

[0010] Alternatively, the regeneration step of the exhaust gas treatment method according to the present invention is a step of regenerating by mixing the carbonaceous catalyst discharged from each of the first and second cross-flow moving bed reactors. In the reuse step, it is preferable that the regenerated carbonaceous catalyst be bisected and introduced into each of the first and second cross-flow moving bed reactors. On the other hand, the carbonaceous catalyst circulating means of the exhaust gas treatment apparatus according to the present invention is a carbonaceous catalyst returning means for dividing the regenerated carbonaceous catalyst into two and introducing the bisected catalyst into each of the first and second cross-flow moving bed reactors. And a carbonaceous catalyst discharging means for guiding the carbonaceous catalyst discharged from each of the first and second cross-flow moving bed reactors to the same regenerator.

In this case, it is easy to independently adjust the flow rate of the moving bed of each of the first and second reactors and the residence time of the carbonaceous catalyst, while using the regenerator. Thus, the entire apparatus becomes compact.

[0012]

Preferred embodiments of the present invention will be described below in detail with reference to the accompanying drawings. In order to facilitate understanding of the description, the same constituent elements are denoted by the same reference numerals as much as possible in each drawing, and redundant description will be omitted.

FIG. 1 is a schematic view showing a first embodiment of an exhaust gas treatment apparatus according to the present invention. This apparatus includes cross-flow moving bed reactors 10 and 20, a heating and regenerating unit 30, a washing tower 40, a separator 50, and an ammonia supply device 60.

In each of the reactors 10 and 20,
The moving layers 11 and 21 are formed by being filled with a carbonaceous catalyst such as activated carbon and descending at a predetermined speed in the vertical direction. The amount of the carbonaceous catalyst charged into and withdrawn from the reactor 10 (20) is controlled by the charging valve 12 (22) provided at the upper part of the reactor 10 (20) and the extraction valve 13 (23) provided at the lower part. Moving layer 11
The flow velocity of (21) can be adjusted. Hereinafter, they are referred to as the upstream side and the downstream side in accordance with the flow direction of the moving bed 11 (21).

The treated exhaust gas is supplied to these reactors 1
The structure is such that the carbonaceous catalysts are introduced so as to be orthogonal to the flow directions of the respective carbonaceous catalysts. Reactor 10 (20)
A gas inlet 14 (24) and an inlet louver 15 (25) for introducing gas and preventing the carbonaceous catalyst from flowing out of the moving bed 11 (21) are provided on the inlet side. Is a perforated plate 16 (26) and a gas outlet 17 (2
7) are provided.

A line L 1 for supplying the exhaust gas to be treated whose temperature has been adjusted to 60 to 180 ° C. is connected to the gas inlet 14 of the first reactor 10. Line L2 is connected. The line L3 is connected to the gas outlet 17 of the first reactor 10.
And the gas inlet 24 of the second reactor 20.
The gas outlet 27 of the second reactor 20 is connected to the line L4
Connected to the subsequent processing facility.

[0017] Withdrawal valve 1 at the bottom of the first reactor 10
3 is connected to a charging valve 22 on the upper part of the second reactor 20 via a line L13. On the other hand, the extraction valve 23 at the lower part of the second reactor 20 is connected to the inlet of the carbonaceous catalyst of the heating regenerator 30 via the line L10. The carbonaceous catalyst outlet of the heating regenerator 30 is connected to the line L1.
1 is connected to a separator 50, the separator 50 comprising:
Furthermore, it is connected to a charging valve 12 above the first reactor 10 via a line L12 so as to circulate the carbonaceous catalyst.

The degassing gas outlet of the heating and regenerator 30 is connected to a washing tower 40 via a line L20.
The desorbed gas passing through the washing tower 40 is supplied to the lines L21 and L22.
Is branched to The line L21 is connected to a by-product recovery device (not shown), and the line L22 is a line L for sending exhaust gas from the first reactor 10 to the second reactor 20.
3 is connected.

Next, the operation of this embodiment, that is, the exhaust gas treatment method according to the present invention will be described in detail. Ammonia is injected into the exhaust gas supplied from the line L1 from the ammonia supply device 60 via the line L2 and mixed. This gas is led into the first reactor 10 through the gas inlet 14, passes through the inlet louver 15, and comes into contact with the moving bed 11 inside the reactor 10. The descending speed of the moving bed 11 inside the first reactor 10 is adjusted mainly by adjusting the amount of the carbonaceous catalyst withdrawn from the valve 13 as described above.

Here, SOx in the exhaust gas is adsorbed and removed as sulfuric acid by the following reaction by contact with the carbonaceous catalyst.

SO ₂ + 1 / 2O ₂ + H ₂ O → H ₂ SO ₄ (1) SO ₃ + H ₂ O → H ₂ SO ₄ (2) A part of the ammonia mixed in the exhaust gas is It reacts with this sulfuric acid as follows to produce acidic ammonium sulfate and ammonium sulfate.

H ₂ SO ₄ + NH ₃ → NH ₄ HSO ₄ (3) NH ₄ HSO ₄ + NH ₃ → (NH ₄ ) ₂ SO ₄ (4) If the amount of sulfuric acid is large, Ammonium sulfate is decomposed into acidic ammonium sulfate by the reaction.

(NH ₄ ) ₂ SO ₄ + H ₂ SO ₄ → 2NH ₄ HSO ₄ (5) On the other hand, NOx in the exhaust gas is decomposed by reacting with ammonia using a carbonaceous catalyst as follows. .

4NH ₃ + 4NO + O ₂ → 4N ₂ + 6H ₂ O (6) On the side of the moving bed 11 near the gas inlet 14, NH is added to the carbonaceous catalyst.
₃ and sulfuric acid are adsorbed to produce ammonium sulfate. Then, in the region on the exhaust gas outlet side, NH ₃ and sulfuric acid are adsorbed as acidic ammonium sulfate. In regions after SOx has been substantially removed in these zones, denitration is performed by the remaining NH ₃ . Therefore, in consideration of the amount of ammonia consumed by the neutralization reaction of sulfuric acid, it is necessary to introduce ammonia supplied via the line L2 so as to be larger than the sum of the molar amounts of NOx and SOx in the exhaust gas. The exhaust gas thus denitrated is discharged from the exhaust gas outlet 17 through the line L3 to the second
To the reactor 20.

The SO ₂ recovered in the regenerator 30 via the line L22 is mixed with the exhaust gas sent to the second reactor 20 via the line L3. Second reactor 2
Even at 0, the descending speed of the internal moving bed 21 is adjusted mainly by adjusting the amount of the carbonaceous catalyst pulled out from the valve 23. Here, by setting the addition amount so that the SO ₂ concentration of the gas after SO ₂ addition becomes higher than the concentration of ammonia remaining without contributing to the reaction in the first reactor 10, Is mainly a sulfuric acid adsorption reaction. Then, the remaining ammonia is adsorbed and removed by the chemical reaction shown in equations (3) to (5). Further, since the denitration reaction is further performed in the second reactor 20 by the unreacted and unadsorbed ammonia, the denitration rate is improved. Further, since the exhaust gas containing ammonia is passed through the second reactor 20 for treatment, the amount of leaked ammonia can be reduced. Therefore, the amount of ammonia added via the line L2 can be increased, so that the denitration rate in the first reactor 10 can also be improved. The exhaust gas thus desulfurized and denitrated is sent to a subsequent processing facility via a line L4.

The carbonaceous catalyst of the moving bed 11 which has been subjected to the exhaust gas treatment in the first reactor 10 is pulled out by a predetermined amount from the valve 13 at the bottom, and the second reaction is carried out through the line L 13 and the charging valve 22. To the vessel 20. Second reactor 20
The carbonaceous catalyst of the moving bed 21 further subjected to the exhaust gas treatment is pulled out by a predetermined amount from the valve 23 at the bottom and sent to the regenerator 30 via the line L10. In the regenerator 30, the carbonaceous catalyst is heated and regenerated in a high-temperature inert gas atmosphere at about 300 to 600 ° C. Then, the regenerated carbonaceous catalyst is sent to a separator 50 composed of a vibrating screen or the like via a line L11 to remove dust and powdered carbonaceous catalyst. Is returned to the moving bed 11 through the charging valve 12 provided at the upper part of the tank, and is circulated and reused.

[0027] In the carbonaceous catalyst is withdrawn from the bottom of the second reactor 20, are adsorbed as easy acidic ammonium sulfate many are decomposed from ammonium sulfate NH _3, further, NH ₃ / SO
_{The two} ratio is also reduced to about 0.7 to 1 as described later. Therefore, the ratio of NH ₃ present in the desorbed gas can be greatly reduced, and the regeneration treatment of SO ₂ contained in the desorbed gas at a high concentration becomes easy. Further, when the heat regeneration is performed in a state where a large amount of sulfuric acid and ammonia are present on the carbonaceous catalyst, there is also an effect of increasing the activity of the carbonaceous catalyst.

The desorbed gas generated in the regenerator 30 is supplied to the line L
After being sent to the washing tower 40 via the water washing | cleaning 20 and being wash | cleaned by water, most are sent to the by-product collection | recovery process via the line L21. Then, a part of the desorbed gas (mostly SO ₂ ) is mixed with the exhaust gas flowing through the line L3 via the line L22. Here, the amount of SO ₂ returned through the line L22 is adjusted so that the adsorption NH ₃ / SO ₂ ratio of the carbonaceous catalyst withdrawn from the lower part of the second reactor 20 is about 0.7 to 1. are doing. The SO ₂ return line L2
2 may be provided so as to connect the regenerator 30 to the line L3.

Next, second to fourth embodiments of the exhaust gas treatment apparatus according to the present invention will be described with reference to FIGS.
The processing apparatus 1a according to the second embodiment shown in FIG.
Only a part of the gas (here, the gas discharged from the outlet 17u on the upstream side) processed in the reactor 10 is supplied to the second reactor 2
0, and the rest (here, the gas discharged from the downstream outlet 17l) is sent directly to the subsequent processing device via the line L5, which is different from the first embodiment.

In this apparatus 1a, the first reactor 1
Although only a part of the gas treated at 0 is sent to the second reactor 20, the treatment apparatus can be made compact when the amount of leaked ammonia is smaller than that of the apparatus 1 of the first embodiment. The proportion of the exhaust gas sent to the second reactor 20 among the exhaust gas processed in the first reactor 10 is appropriately determined according to the target value of the amount of leaked ammonia and the like.

The processing apparatus 1b according to the third embodiment shown in FIG. 3 divides the inlet of the first reactor 10 into two parts, and supplies ammonia to only one exhaust gas (here, supplied to the upstream side). Is added. That is, the first reactor 10 has an upstream exhaust gas inlet 14u and a downstream exhaust gas inlet 14l. The exhaust gas inlet 14u receives the exhaust gas mixed with ammonia via the line L2 in the line L2.
1 and exhaust gas not mixed with ammonia is introduced into the exhaust gas inlet 141 via a line L6.

In this device 1b, since the exhaust gas introduced into the lower part of the first reactor is not mixed with ammonia,
Although the denitration reaction does not proceed in this region, the same effect can be obtained because the denitration reaction proceeds with the ammonia remaining in the second reactor.

The processing apparatus 1c of the fourth embodiment shown in FIG. 4 is different from the processing apparatus 1 of the first embodiment shown in FIG. 1 only in the circulation line of the carbonaceous catalyst. In particular,
While the processing apparatus 1 sends out the carbonaceous catalyst from the first reactor 10 to the second reactor 20, the processing apparatus 1c
Then, the carbonaceous catalyst discharged from the first reactor 10 and the second reactor 20 is directly sent to the regenerator 30 via the line L14 and the line L10. After the regeneration, the regenerated activated carbon from which unnecessary components have been removed by the separator 50 is supplied to the line L1.
2, the first reactor 10, the second reactor 2 via L15
Returned to each of the zeros.

In this apparatus 1c, since the carbonaceous catalyst not adsorbed with SO ₂ is supplied to the second reactor, the amount of SO ₂ returned via line L22 is required to efficiently remove the leaked ammonia. Is required to be larger than that of the device 1, but the same effect as that of the device 1 can be obtained. On the other hand, it is easier to independently adjust the flow velocity of the moving bed and the residence time of the carbonaceous catalyst in the first reactor 10 and the second reactor 20 as compared with the first to third embodiments. There is an advantage of becoming.

As the carbonaceous catalyst of the present invention, activated carbon, activated coke, activated char, etc. obtained by oxidizing, heat-treating or activating coal with steam or the like are generally used. And those carrying a metal compound such as manganese can also be used. The ammonia supply device may be configured to inject ammonia water or the like in addition to the ammonia gas.

[0036]

EXAMPLES The present inventors conducted comparative experiments to confirm the effects of the exhaust gas treatment method of the present invention. Hereinafter, the experimental results will be described.

Example Using the processing apparatus shown in FIG. 1, 150 ppm SOx, 220 ppm
140 ° C exhaust gas 1000 containing NOx, 10% moisture and 15% oxygen
m ³ / h (Normal) was processed. The amount of ammonia added via the line L2 was set such that the concentration in the exhaust gas after the addition became 450 ppm. The carbonaceous catalyst is activated carbon having a diameter of about 7 mm and a length of about 8 mm. The first reactor 10 is filled with 2.50 m ³ and the second reactor 20 with 1.25 m ^3, and the residence time is 120 hours and 60 hours, respectively.
The withdrawal amount and the input amount were adjusted so that the time was reached. Then, the SO ₂ concentration of the exhaust gas introduced into the second reactor 20 becomes 190
The supply amount of the desorbed gas via the line L22 was adjusted to be ppm.

As a result, the desulfurization rate in the first reactor 10 was almost 100%, the denitration rate was 82%, and the NH ₃ concentration in the exhaust gas after passing was 49 ppm. And the second reactor 2
At 0, the desulfurization rate was almost 100%, the denitration rate was 3%, and the NH ₃ concentration in the exhaust gas after passing was 2 ppm. That is, the desulfurization rate of the entire apparatus 1 was almost 100%, the denitration rate was 82.5%, and the leak NH ₃ concentration was 2 ppm. The decomposition rate of ammonia in the regenerator 30 was 96%.

COMPARATIVE EXAMPLE In the processing apparatus of FIG. 1, the same exhaust gas treatment as in the example was performed without returning the desorbed gas from the line L22. All other conditions are the same as in the embodiment.

As a result, the desulfurization rate in the first reactor 10 was almost 100%, the denitration rate was 81%, and the NH ₃ concentration in the exhaust gas after passing was 51 ppm. And the second reactor 2
At 0, the denitration ratio was 6%, and the NH ₃ concentration in the exhaust gas after passing was 4 ppm. That is, the desulfurization rate in the entire apparatus 1 was almost 100%, the denitration rate was 82%, and the leak NH ₃ concentration was 4 ppm. The decomposition rate of ammonia in the regenerator 30 was 45%.

According to the exhaust gas treatment apparatus and method of the present invention, NH ₃ / SO adsorbed on activated carbon by reducing the amount of ammonia leaking into the exhaust gas while maintaining the denitration rate is maintained.
_The effect of reducing the ratio of ₂ and improving the decomposition rate of ammonia was confirmed. Since the amount of leaked ammonia is reduced, it is possible to further improve the denitration rate by further injecting ammonia.

The exhaust gas treatment apparatus and method according to the present invention are applicable to SOx, N2, etc. of boiler exhaust gas, sintering exhaust gas, waste incinerator exhaust gas, etc.
It can be suitably applied to the treatment of exhaust gas containing harmful substances such as Ox, dioxin, and Hg.

[0043]

As described above, according to the present invention, desorbed gas containing SO ₂ is added to a part of the exhaust gas desulfurized and denitrified in the first reactor, and is introduced into the second reactor. Thus, leak ammonia can be efficiently removed. Therefore, the first
The denitration rate can be improved by increasing the amount of ammonia added to the exhaust gas guided to the reactor.

[Brief description of the drawings]

FIG. 1 is an overall schematic diagram showing a first embodiment of an exhaust gas treatment apparatus according to the present invention.

FIG. 2 is an overall schematic diagram showing a second embodiment of the exhaust gas treatment apparatus according to the present invention.

FIG. 3 is an overall schematic diagram showing a third embodiment of the exhaust gas treatment apparatus according to the present invention.

FIG. 4 is an overall schematic diagram showing a fourth embodiment of the exhaust gas treatment apparatus according to the present invention.

[Explanation of symbols]

10, 20 ... cross-flow moving bed reactor, 11, 21 ... moving bed, 12, 13, 22, 23 ... valve, 14, 24 ... exhaust gas inlet, 17, 27 ... exhaust gas outlet, 30 ... regenerator, 4
0: separator, 50: washing tower, 60: ammonia supply device, L1 to L6: gas pipe, L10 to L15: carbonaceous catalyst supply line, L20 to L22: desorption gas pipe.

 ────────────────────────────────────────────────── ─── Continuing on the front page (72) Inventor Kazuyoshi Takahashi 63-30 Yuigaoka, Hiratsuka-shi, Kanagawa F-term in Hiratsuka Works of Sumitomo Heavy Industries, Ltd. 4D048 AA02 AA06 AB02 AB05 AC04 BA05X BB01 BD01 CB03 4G069 AA02 BA08A BA08B CA04 CA08 CA12 CA13 EA02Y GA01

Claims (6)

[Claims] 1. An exhaust gas treatment method for subjecting an exhaust gas to desulfurization and denitrification treatment by contacting the exhaust gas with a carbonaceous catalyst in a cross-flow moving bed reactor, wherein ammonia is added to at least a part of the exhaust gas to be treated, Guiding the added and unadded exhaust gas to a first cross-flow moving bed reactor, and treating at least a part of the treated exhaust gas in the first processing step in a second cross-flow moving bed reactor A step of heating the used carbonaceous catalyst in an inert gas to recover sulfur oxides and regenerate the carbonaceous catalyst; and a step of applying the regenerated carbonaceous catalyst to the crossflow. Returning to the moving-bed reactor and circulating and reusing the sulfur oxide;
Mixing with the exhaust gas guided to the cross-flow moving bed type reactor. 2. The circulating reuse step includes: introducing a regenerated carbonaceous catalyst into the first cross-flow moving bed reactor, and removing the carbonaceous material discharged from the first cross-flow moving bed reactor. The exhaust gas treatment method according to claim 1, wherein a catalyst is led to the second cross-flow moving bed reactor. 3. The regenerating step is a step of mixing and regenerating the carbonaceous catalyst discharged from each of the first and second cross-flow moving bed reactors, and the recirculating reuse step includes: The exhaust gas treatment method according to claim 1, wherein the regenerated carbonaceous catalyst is bisected and introduced into each of the first and second cross-flow moving bed reactors. 4. A method for desulfurizing exhaust gas by contacting the exhaust gas with a carbonaceous catalyst.
In an exhaust gas treatment apparatus for denitrification treatment, a carbonaceous catalyst filled therein is caused to flow vertically downward to form a moving bed, and the moving bed and the introduced exhaust gas are brought into contact with each other in a cross flow to treat the exhaust gas. And a second cross-flow moving bed reactor, an addition device for adding ammonia to at least a part of the exhaust gas guided to the first cross-flow moving bed reactor, and the first cross-flow moving bed reactor An exhaust gas transfer means for leading at least a part of the exhaust gas passing through the reactor to the second cross-flow moving bed reactor; and heating the used carbonaceous catalyst in an inert gas to recover sulfur oxides. A regenerator that regenerates the carbonaceous catalyst by means of: a carbonaceous catalyst circulating means for returning the regenerated carbonaceous catalyst to each of the cross-flow moving bed reactors for recycling and reuse; Part of the oxide is cross-linked to the second cross-flow Exhaust gas treatment device comprising a sulfur oxide returning means for mixing the exhaust gas is guided to the moving bed reactor, a. 5. The carbonaceous catalyst circulating means includes: a carbonaceous catalyst returning means for introducing a regenerated carbonaceous catalyst into the first cross-flow moving bed reactor; A carbonaceous catalyst transfer means for introducing the carbonaceous catalyst discharged from the reactor into the second cross-flow moving bed reactor; and a carbonaceous catalyst discharged from the second cross-flow moving bed reactor. The exhaust gas treatment device according to claim 4, further comprising: a carbonaceous catalyst discharge unit that leads to the regenerator. 6. The carbonaceous catalyst circulating means, wherein the regenerated carbonaceous catalyst is bisected and introduced into each of the first and second crossflow moving bed reactors; The exhaust gas treatment device according to claim 4, further comprising: a carbonaceous catalyst discharging unit that guides the carbonaceous catalyst discharged from each of the first and second cross-flow moving bed reactors to the same regenerator. .