KR20200059119A - Exhaust gas treatment apparatus - Google Patents

Abstract

Disclosed is an exhaust gas treatment apparatus to simultaneously remove sulfur oxides and nitrogen oxides from exhaust gas. The exhaust gas treatment apparatus according to one embodiment of the present invention includes: a reactor into which exhaust gas is introduced; a reducing agent supply unit which mixes a reducing agent or a reducing agent precursor, which becomes the reducing agent, with the exhaust gas before the exhaust gas is introduced into the reactor; and a regenerating agent supply unit which supplies a regenerating agent into the reactor after the exhaust gas is introduced into the reactor.

Description

Exhaust gas treatment system {EXHAUST GAS TREATMENT APPARATUS}

The present invention relates to an exhaust gas treatment apparatus for treating exhaust gas.

The exhaust gas treatment device is a device that treats exhaust gas discharged from an exhaust gas discharge device such as an engine and then discharges it to the outside.

Examples of the exhaust gas treatment apparatus include a scrubber to remove sulfur oxides from exhaust gas, and a selective catalyst reduction device called SCR (Selective Catalyst Reduction) to remove nitrogen oxides from exhaust gas.

Conventionally, in order to remove both sulfur oxides and nitrogen oxides from exhaust gas, both the scrubber and the selective catalytic reduction device described above had to be provided. In addition, in some cases, in the case of removing sulfur oxides or nitrogen oxides from exhaust gas, both the scrubber and the selective catalytic reduction device described above had to be provided.

Therefore, in places where there is not much free space, such as a ship, it is not easy to install both a scrubber and a selective catalytic reduction device, thereby simultaneously removing sulfur oxides and nitrogen oxides from exhaust gas, or, if necessary, sulfur oxides from exhaust gas Or it was not easy to remove nitrogen oxides.

In addition, in the conventional scrubber, treated water such as seawater or fresh water is injected into the exhaust gas to remove sulfur oxides from the exhaust gas. In this case, since the amount of the treated water used is large, in addition to the scrubber, the treated water is supplied to the scrubber. The structure and the structure for removing the sulfur oxides from the exhaust gas and treating the treated water containing sulfur oxides had to be provided separately.

The present invention has been made by recognizing at least one of the above-described demands or problems occurring in the related art.

One aspect of the object of the present invention is to enable simultaneous removal of sulfur oxides and nitrogen oxides from exhaust gas with a single exhaust gas treatment device.

Another aspect of the object of the present invention is to mix a reducing agent or a reducing agent precursor that becomes the reducing agent in the exhaust gas before the exhaust gas enters the reactor, and after the exhaust gas enters the reactor, to supply a regenerant inside the reactor will be.

An exhaust gas processing apparatus related to one embodiment for realizing at least one of the above-described problems may include the following features.

Exhaust gas processing apparatus according to an embodiment of the present invention is a reactor in which the exhaust gas is introduced; A reducing agent supply unit for mixing a reducing agent or a reducing agent precursor that becomes the reducing agent in the exhaust gas before the exhaust gas enters the reactor; And a regenerant supply unit for supplying a regenerant into the reactor after the exhaust gas flows into the reactor. It may include.

In this case, the reactor is provided with an exhaust gas inlet through which the exhaust gas is introduced, and the regenerant supply unit is capable of supplying the regenerant to a portion inside the reactor that is a predetermined distance away from the exhaust gas inlet in the exhaust gas flow direction. have.

In addition, the reactor is provided with an exhaust gas outlet through which treated exhaust gas is discharged, and the regenerant supply unit can supply the regenerant to a portion inside the reactor at the exhaust gas outlet side.

And, the adsorption catalyst member provided inside the reactor; It may further include.

In addition, the nitrogen oxide contained in the exhaust gas is removed by the reducing agent and the adsorption catalyst attached to the adsorption catalyst member, and the sulfur oxide contained in the exhaust gas is adsorbed by the adsorption catalyst and the nitrogen oxide contained in the exhaust gas These can be removed sequentially.

In addition, the adsorption catalyst is adsorbed so that the sulfur oxides contained in the exhaust gas is adsorbed and the nitrogen oxides are sequentially removed, and the nitrogen oxides contained in the exhaust gas are reduced to nitrogen by the reducing agent and help to be removed from the exhaust gas. It may include a catalyst.

In addition, the adsorbent catalyst is a powder form in which the adsorbent and the catalyst are mixed, and may be attached to the adsorbent catalyst member by extrusion molding or an adhesive material.

Then, after the catalyst in powder form is first attached to the adsorption catalyst member by extrusion molding or an adhesive material, the adsorbent in powder form may be attached to the adsorption catalyst member by adhesive material or extrusion molding.

In addition, the sulfur oxides contained in the exhaust gas are removed from the exhaust gas by being adsorbed to the adsorbent by a chemical reaction to become desulfurization by-products, and nitrogen oxides contained in the exhaust gas are chemically reacted with the desulfurization by-products to become denitrification by-products. It can be removed from.

Then, the regenerant is chemically reacted with the nitrogen oxides, sulfur oxides, desulfurization by-products, and denitrification by-products contained in the exhaust gas to make an adsorbent precursor, and the adsorbent precursor is thermally decomposed by the heat of the exhaust gas and can be regenerated with the adsorbent. .

In addition, the regenerant may be an aqueous alkali solution.

In addition, the temperature of the exhaust gas in the reactor may be 200 ° C or more and less than 500 ° C so that thermal decomposition of the adsorbent precursor and reduction of nitrogen oxide by the reducing agent and the catalyst are possible.

In addition, the adsorbent may include at least one of iron oxide (Fe ₂ O ₃ ), copper oxide (CuO), and cerium oxide (CeO).

In addition, the adsorbent may be iron oxide (Fe ₂ O ₃ ) and the adsorbent precursor may be iron hydroxide (Fe (OH) ₃ ).

In addition, the catalyst may include at least one of vanadium (V) and tungsten (W) and titanium oxide (TiO ₂ ).

As described above, according to the embodiment of the present invention, it is possible to simultaneously remove sulfur oxides and nitrogen oxides from exhaust gas with one exhaust gas treatment device.

In addition, according to an embodiment of the present invention, before the exhaust gas flows into the reactor, a reducing agent or a reducing agent precursor serving as the reducing agent is mixed with the exhaust gas, and after the exhaust gas flows into the reactor, regenerant is supplied to the reactor. Can

1 is a perspective view of an embodiment of an exhaust gas treatment apparatus according to the present invention.
2 is a view showing that the exhaust gas is treated in an embodiment of the exhaust gas treatment apparatus according to the present invention.
3 is a view showing other embodiments of the exhaust gas treatment apparatus according to the present invention.
4 and 5 are views showing a case in which the exhaust gas treatment apparatus according to the present invention is installed on a ship.
6 and 7 are graphs showing the results of experiments of the performance of the adsorption catalyst attached to the adsorption catalyst member included in the exhaust gas treatment apparatus according to the present invention.
8 is a view showing a related chemical reaction equation in which nitrogen oxide and sulfur oxide are respectively removed from the exhaust gas in the exhaust gas treatment apparatus and the exhaust gas treatment method according to the present invention.
9 is a view showing an example showing the process of removing nitrogen oxides and sulfur oxides from the exhaust gas in the exhaust gas treatment apparatus and exhaust gas treatment method according to the present invention.
10 is a view showing a process in which the adsorbent of the adsorbent catalyst attached to the adsorbent catalyst member is regenerated by the adsorbent regenerant in the exhaust gas treating apparatus and the exhaust gas treating method according to the present invention.

In order to help understanding of the features of the present invention as described above, it will be described in more detail with respect to the exhaust gas treatment apparatus and exhaust gas treatment method according to an embodiment of the present invention.

The embodiments described below will be described based on the most suitable embodiments for understanding the technical features of the present invention, and the technical features of the present invention are not limited by the embodiments described, It is to illustrate that the present invention can be implemented as in the embodiments. Accordingly, the present invention can be implemented in various modifications within the technical scope of the present invention through the embodiments described below, and such modified embodiments will fall within the technical scope of the present invention. In addition, in order to help understanding of the embodiments described below, in the reference numerals in the accompanying drawings, among the components that have the same function in each embodiment, related components are indicated by the same or extended line numbers.

Hereinafter, an exhaust gas processing apparatus and an exhaust gas processing method according to the present invention will be described with reference to FIGS. 1 to 10.

1 is a perspective view of an embodiment of an exhaust gas processing apparatus according to the present invention, Figure 2 is a view showing that the exhaust gas is processed in an embodiment of the exhaust gas processing apparatus according to the present invention, Figure 3 is the present invention It is a diagram showing other embodiments of the exhaust gas treatment device according to the drawings, and FIGS. 4 and 5 are views showing a case where the exhaust gas treatment device according to the present invention is installed on a ship.

6 and 7 are graphs showing the results of testing the performance of the adsorption catalyst attached to the adsorption catalyst member included in the exhaust gas treatment apparatus according to the present invention.

And, Figure 8 is a view showing a related chemical reaction equation in which nitrogen oxides and sulfur oxides are respectively removed from the exhaust gas in the exhaust gas treatment apparatus and exhaust gas treatment method according to the present invention, Figure 9 is an exhaust gas treatment apparatus according to the present invention And an example showing the process of removing nitrogen oxides and sulfur oxides from the exhaust gas in the exhaust gas treatment method, and FIG. 10 is an adsorption attached to the adsorption catalyst member in the exhaust gas treatment apparatus and the exhaust gas treatment method according to the present invention. It is a diagram showing the process in which the adsorbent of the catalyst is regenerated by the adsorbent regenerant.

Exhaust gas treatment system

The exhaust gas treatment apparatus 100 according to the present invention may include a reactor 200, an adsorption catalyst member 300, a reducing agent supply unit 400, and a regenerant supply unit 500.

Exhaust gas may be introduced into the reactor 200. To this end, the reactor 200 may be connected to an exhaust gas discharge device (ED) through which exhaust gas is discharged. For example, the reactor 200 may be connected to an exhaust gas discharge device (ED) such as a main engine (ME) or a power generation engine (GE) provided on a ship as shown in FIGS. 4 and 5. However, the exhaust gas discharge device ED connected to the reactor 200 is not particularly limited, and any exhaust gas, such as a boiler (not shown), may be used as long as the exhaust gas is discharged.

The reactor 200 may have a long shape in the height direction as shown in FIGS. 1 and 2 and 3 (b) or a long shape in the length direction or the width direction as shown in FIG. 3 (a). . However, the shape of the reactor 200 is not particularly limited, and is connected to the exhaust gas discharge device ED and the exhaust gas discharged from the exhaust gas discharge device ED flows in and the adsorption catalyst member 300 is inside. Any shape can be provided as long as it can be provided.

The reactor 200 may be provided with an exhaust gas inlet 210, an exhaust gas outlet 220, and a treatment by-product outlet 230 as shown in FIG. 1.

Exhaust gas may be introduced into the reactor 200 through the exhaust gas inlet 210. To this end, an exhaust pipe PE connected to the exhaust gas discharge device ED may be connected to the exhaust gas inlet 210. And, the exhaust gas discharged from the exhaust gas discharge device (ED), such as the main engine (ME) or power generation engine (GE) and flow through the exhaust pipe (PE) as shown in Figure 2 through the exhaust gas inlet 210 Likewise, the inside of the reactor 200 may be introduced to flow inside the reactor 200. The exhaust gas inlet 210 may be provided at the bottom of the reactor 200 as shown in FIG. 1. However, the portion of the reactor 200 provided with the exhaust gas inlet 210 is not particularly limited, and the exhaust pipe PE connected to the exhaust gas discharge device ED is connected to exhaust exhaust from the exhaust gas discharge device ED If the gas can be introduced into the reactor 200, it can be provided in any part of the reactor 200.

The exhaust gas processed in the reactor 200 may be discharged through the exhaust gas outlet 220. For example, exhaust gas from which at least one of sulfur oxides and nitrogen oxides is removed while flowing inside the reactor 200 may be discharged through the exhaust gas outlet 220. As illustrated in FIG. 2, an exhaust gas discharge pipe PD may be connected to the exhaust gas outlet 220. The exhaust gas discharged from the exhaust gas outlet 220 flows into the turbocharger TC provided in the exhaust gas discharge pipe PD, as shown in FIG. 4 through the exhaust gas discharge pipe PD, or is illustrated in FIG. 5. As can be discharged to the outside. The exhaust gas outlet 220 may be provided on the upper portion of the reactor 200 as shown in FIG. 1. However, the portion of the reactor 200 provided with the exhaust gas outlet 220 is not particularly limited, and the exhaust gas from which at least one of sulfur oxides and nitrogen oxides is removed while flowing inside the reactor 200 may be discharged. If it is a part, it may be provided in any part of the reactor 200.

As the exhaust gas is processed in the reactor 200, for example, at least one of sulfur oxides and nitrogen oxides are removed from the exhaust gas, and the treatment by-products generated may be discharged through the treatment by-product outlet 230. The treatment by-product outlet 230 may be provided under the reactor 200 as shown in FIG. 1. However, the portion of the reactor 200 provided with the treatment by-product outlet 230 is not particularly limited, and if the treatment by-product generated as the exhaust gas is processed in the reactor 200 can be discharged, the portion of the reactor 200 It can be provided in any part. A drain pipe PL may be connected to the treatment by-product discharge port 230 as shown in FIGS. 4 and 5. In addition, the drain pipe PL may be connected to the treatment by-product collection tank TB. Accordingly, the treatment by-products discharged through the treatment by-product discharge port 230 may be stored in the treatment by-product collection tank TB through the drain pipe PL. The treatment by-products stored in the treatment by-product collection tank TB may be disposed of or disposed of by a separate device (not shown) to be recycled.

The adsorption catalyst member 300 may be provided inside the reactor 200. The adsorption catalyst member 300 may be formed with an exhaust gas passage hole (not shown) through which the exhaust gas passes. A plurality of exhaust gas through holes may be formed in the adsorption catalyst member 300. The number of exhaust gas through-holes formed in the adsorption catalyst member 300 is not particularly limited, and any number is possible, and one is possible.

The exhaust gas passage hole may be formed in the adsorption catalyst member 300 in parallel with the flow direction of the exhaust gas in the reactor 200. For example, exhaust gas passage holes may be formed in the adsorption catalyst member 300 in the height direction or the thickness direction of the adsorption catalyst member 300. However, the shape of the exhaust gas passing hole formed in the adsorption catalyst member 300 is not particularly limited, and any shape can be used as long as it is a shape through which the exhaust gas can pass.

The adsorption catalyst member 300 may have a plate shape having a predetermined thickness, as shown in FIG. 1. However, the shape of the adsorption catalyst member 300 is not particularly limited, and any shape may be used as long as the above-described exhaust gas through hole can be formed and provided in the reactor 200.

A plurality of adsorption catalyst members 300 may be provided inside the reactor 200. In this case, a plurality of adsorption catalyst members 300 may be provided inside the reactor 200 to be spaced apart from each other by a predetermined distance. For example, as shown in FIGS. 1 and 2 and 3 (a), a plurality of adsorption catalyst members 300 are spaced apart from each other at a predetermined distance from each other in the longitudinal or width direction of the reactor 200. It may be provided. In addition, as shown in (b) of FIG. 3, a plurality of adsorption catalyst members 300 may be provided inside the reactor 200 to be spaced apart from each other in a height direction of the reactor 200. However, a configuration in which a plurality of adsorption catalyst members 300 are provided inside the reactor 200 is not particularly limited, and any configuration is possible.

An adsorption catalyst (not shown) may be attached to the adsorption catalyst member 300. The adsorption catalyst may be attached to the adsorption catalyst member 300 by, for example, extrusion molding or an adhesive material. However, the configuration in which the adsorption catalyst is attached to the adsorption catalyst member 300 is not particularly limited, and any known configuration is possible.

The adsorption catalyst can adsorb sulfur oxides contained in exhaust gas and sequentially remove nitrogen oxides contained in exhaust gas. In addition, the adsorption catalyst may help nitrogen oxides contained in the exhaust gas be reduced to nitrogen by a reducing agent and removed from the exhaust gas.

The adsorption catalyst may include an adsorbent and a catalyst. For example, the adsorption catalyst may be a powder form in which the adsorbent and the catalyst are mixed. In addition, the adsorption catalyst in powder form may be attached to the adsorption catalyst member 300 by extrusion molding or an adhesive material. In addition, after the catalyst in powder form is first attached to the adsorption catalyst member 300 by extrusion molding or an adhesive material, the powder type adsorbent may be attached to the adsorption catalyst member 300 by adhesive material or extrusion molding. However, the shape of the adsorption catalyst and the structure attached to the adsorption catalyst member 300 are not particularly limited, and any shape and configuration may be used as long as it is a shape and configuration including an adsorbent and a catalyst.

The adsorbent may allow sulfur oxides contained in the exhaust gas to be adsorbed and nitrogen oxides to be sequentially removed. For example, the sulfur oxides contained in the exhaust gas can be removed from the exhaust gas by being adsorbed to the adsorbent by a chemical reaction to become a desulfurization by-product. In addition, nitrogen oxides may be removed from the exhaust gas by chemically reacting the desulfurization by-product with the nitrogen oxide contained in the exhaust gas to become a denitrification by-product.

The adsorbent may include at least one of iron oxide (Fe ₂ O ₃ ), copper oxide (CuO), and cerium oxide (CeO). As described above, as described above, the sulfur oxides contained in the exhaust gas are adsorbed to become desulfurization byproducts, and the desulfurization byproduct reacts with nitrogen oxides contained in the exhaust gas to become denitrification byproducts, thereby removing sulfur oxides and nitrogen oxides from the exhaust gas. In addition to the role to be possible, it can also serve as a co-catalyst to increase the activity of the catalyst contained in the adsorption catalyst.

When the adsorbent is, for example, iron oxide (Fe ₂ O ₃ ), the sulfur oxides contained in the exhaust gas may be removed from the exhaust gas by being adsorbed to the adsorbent as a chemical reaction equation 1 below to become a desulfurization by-product.

[Chemical Reaction Formula 1]

2Fe ₂ O ₃ + 4SO ₂ + O ₂ = 4FeSO ₄

In addition, in this case, nitrogen oxides contained in the exhaust gas may be removed from the exhaust gas by reacting with the desulfurization by-product as shown in Chemical Reaction Formula 2 below to become a denitrification by-product.

[Chemical Reaction Formula 2]

FeSO ₄ + NO = Fe (NO) SO ₄

Meanwhile, the adsorbent may be regenerated by the regenerant supplied inside the reactor 200 by the regenerant supply unit 500 to be described later. As described later, the regenerant may be an aqueous alkali solution, such as sodium hydroxide (NaOH). In addition, when the regenerant, which is an aqueous alkali solution, is supplied into the reactor 200 by the regenerant supply unit 500, the regenerant is chemically reacted with nitrogen oxides, sulfur oxides, desulfurization by-products and denitrification by-products contained in the exhaust gas, and adsorbents. Precursors can be made. For example, when the adsorbent is iron oxide (Fe ₂ O ₃ ), the regenerant is chemically reacted with nitrogen oxides, sulfur oxides, desulfurization by-products and denitrification by-products contained in the exhaust gas, and iron hydroxide (Fe (OH) ₃ ) as an adsorbent precursor Can generate In addition, iron hydroxide (Fe (OH) ₃ ), which is an adsorbent precursor, may be thermally decomposed by heat of exhaust gas inside the reactor 200 and regenerated as iron oxide (Fe ₂ O ₃ ), which is an adsorbent. In this way, since the adsorbent is regenerated by the regenerant, it is not necessary to additionally supply the adsorbent.

As described later, before the exhaust gas flows into the reactor 200, a reducing agent precursor such as ammonia (NH ₃ ) or a reducing agent precursor such as urea water may be mixed into the exhaust gas by the reducing agent supply unit 400. have. In addition, nitrogen oxides contained in the exhaust gas in the reactor 200 may be reduced to nitrogen by a reducing agent and removed from the exhaust gas as shown in Chemical Reaction Formula 3 below.

[Chemical Reaction Formula 3]

4NO + 4NH ₃ + O ₂ = 4N ₂ + 6H ₂ O

In this case, the above-described catalyst included in the adsorption catalyst may help nitrogen oxides contained in the exhaust gas be reduced to nitrogen by a reducing agent and removed from the exhaust gas. Therefore, the nitrogen oxides contained in the exhaust gas can be reduced to nitrogen by a reducing agent and a catalyst and removed from the exhaust gas.

The nitrogen oxides contained in the exhaust gas in the reactor 200 may be removed from the exhaust gas by reacting with the desulfurization by-products to become a denitrification by-product, or reduced to nitrogen by a reducing agent and a catalyst to be removed from the exhaust gas. .

The catalyst included in the adsorption catalyst may include at least one of vanadium (V), tungsten (W), and titanium oxide (TiO ₂ ). In terms of improving the efficiency of removing nitrogen oxides, the catalyst preferably includes both vanadium (V) and tungsten (W) and titanium oxide (TiO ₂ ), wherein vanadium (V) is 0.1 to 0.1 based on the total weight of the catalyst. 5% by weight, tungsten (W) is 0.1 to 10% by weight, titanium oxide (TiO ₂ ) may be included from 85 to 99.8% by weight. The content of each component of the catalyst represents the maximum nitrogen oxide removal rate within the above range, and when vanadium (V) and tungsten (W) are present together, the reduction reaction of nitrogen oxide is further activated.

In particular, in the catalyst, if the content of vanadium (V) is less than 0.1% by weight, there is a fear that the activity of the nitrogen oxide reduction reaction will not appear. On the other hand, when the content of vanadium (V) exceeds 5% by weight, excess vanadium (V) forms SO ₃ by oxidizing SO ₂ in the exhaust gas, and the catalyst is poisoned due to the SO ₃ to reduce the rate of nitrogen oxide reduction. This can fall. On the other hand, when the content of tungsten (W) exceeds 10% by weight, considering the aspect of improving the removal rate of nitrogen oxides compared to cost, it is not preferable.

For example, the catalyst is made of vanadium (V), tungsten (W), and titanium oxide (TiO ₂ ) of 5% by weight, 9% by weight, and 86% by weight, respectively, and vanadium (V) in titanium oxide (TiO ₂ ) as a support. And tungsten (W) may be attached or inserted. However, the composition and form of the catalyst are not particularly limited, and any composition and form may be used as long as it is at least one of vanadium (V), tungsten (W), and titanium oxide (TiO ₂ ).

In the adsorption catalyst, the mixing ratio of the adsorbent and catalyst is preferably 1: 0.1 to 1:10. When the mixing ratio of the adsorbent and the catalyst is out of the above range, the content of the adsorbent or the catalyst is too small, so that sulfur oxide or nitrogen oxide may not be sufficiently removed from the exhaust gas.

In addition, the adsorption catalyst may be used to remove sulfur oxides and nitrogen oxides at a temperature of 200 ° C to 500 ° C, preferably 250 ° C to 500 ° C, which is consistent with the catalytic activity temperature range of the nitrogen oxide reduction reaction. Therefore, when the temperature is outside the above range, the adsorption reaction of sulfur oxides is not significantly affected, but the reduction activity of nitrogen oxides is shown to be less than 50%, and the nitrogen oxide reduction rate is rapidly reduced, which is not preferable.

6 is a graph showing whether the adsorption catalyst contained in the adsorption catalyst affects the reduction rate of nitrogen oxides to nitrogen when the adsorption catalyst is made by mixing the adsorbent and the catalyst as in the present invention.

As shown, when only an adsorbent that is iron oxide (Fe ₂ O ₃ ) is used, when only a catalyst composed of vanadium (V), tungsten (W), and titanium oxide (TiO ₂ ) is used, and the adsorption catalyst according to the present invention is used. Divided into use cases. In the case of using the adsorption catalyst according to the present invention, the mixing ratios of the catalyst and the adsorbent were divided into 1: 0.1, 1: 0.3, 1: 1, 1: 3, and 1: 6, respectively. Then, the reduction rate of nitrogen oxides to nitrogen by the same amount of a reducing agent was measured for exhaust gas without sulfur oxides and only nitrogen oxides.

As can be seen from the graph of FIG. 6, when only an adsorbent that is iron oxide (Fe ₂ O ₃ ) was used, the reduction rate of nitrogen oxide was relatively low regardless of the temperature of the exhaust gas. And, when the temperature of the exhaust gas was lower than 200 ° C, the reduction rate of nitrogen oxide was lower when the adsorption catalyst according to the present invention was used than when only the catalyst was used. However, when the temperature of the exhaust gas is 200 ° C or more and less than 400 ° C, which is within the operating range of the exhaust gas treatment apparatus 100 according to the present invention, the reduction rate of nitrogen oxides uses only the catalyst and the adsorption catalyst according to the present invention When used, it could be confirmed that there was no significant difference. Rather, in the temperature range of 200 ° C to 300 ° C, the nitrogen oxide reduction rate when using the adsorption catalyst according to the present invention was higher than the nitrogen oxide reduction rate when only the catalyst was used.

Accordingly, it can be seen that even if the adsorption catalyst according to the present invention in which the adsorbent and the catalyst are mixed is used, the nitrogen oxide contained in the exhaust gas can be reduced to nitrogen by the oxidant and the catalyst regardless of the adsorbent.

Table 1 below shows that the adsorption catalyst according to the present invention was tested to find out its ability to adsorb sulfur oxides.

Experiments were conducted on exhaust gas containing only sulfur oxides, and as shown in Table 1 below, it was based on the amount of sulfur oxides adsorbed when only the copper oxide (CuO) adsorbent was used. In addition, when only a catalyst composed of vanadium (V), tungsten (W), and titanium oxide (TiO ₂ ) is used, only an adsorbent that is iron oxide (Fe ₂ O ₃ ) is used, and the mixing ratio of the adsorbent and the catalyst is 1: It was divided into the case of using the adsorption catalyst according to the present invention for one person. In addition, in each case, compared to the case where only an adsorbent that is copper oxide (CuO) was used, the increased amount of adsorbed sulfur oxides was expressed as%.

As can be seen from Table 1, when only the catalyst was used, no sulfur oxides contained in the exhaust gas were adsorbed. In addition, in the case of using only the adsorbent, the use of iron oxide (Fe ₂ O ₃ ) as the adsorbent was three times greater than the use of copper oxide (CuO) as the adsorbent. In addition, when the adsorption catalyst according to the present invention was used, the amount of adsorbed sulfur oxides was smaller than when using only the adsorbent which is iron oxide (Fe ₂ O ₃ ), but the amount of adsorbed sulfur oxides was higher than when only the adsorbent that was copper oxide (CuO) was used. It was twice as many.

Accordingly, it can be seen that even when the adsorption catalyst according to the present invention in which the adsorbent and the catalyst are mixed is used, the sulfur oxides contained in the exhaust gas can be adsorbed by the adsorbent regardless of the catalyst.

matter
The rate of increase in the amount of adsorption of sulfur oxides based on the amount of adsorption of CuO adsorbent (%)

V (5), W (9) / TiO ₂ (catalyst)
0
Fe ₂ O ₃ (adsorbent)
300
V (5), W (9) / TiO ₂ + Fe ₂ O ₃ (1: 1)
(Adsorption catalyst)
200

FIG. 7 shows the measurement of the nitrogen oxide to nitrogen reduction rate by the same amount of the reducing agent and the adsorption catalyst according to the present invention when nitrogen oxide is present in the exhaust gas and when both nitrogen oxide and sulfur oxide are present. It is a graph to show. The adsorption catalyst used in the experiment is a mixture of adsorbent and catalyst in a 1: 1 ratio. As shown, even if sulfur oxides are included in the exhaust gas, it can be seen that the reduction rate of nitrogen oxides to nitrogen by the reducing agent and the adsorption catalyst according to the present invention does not change.

Based on the above points, the adsorption catalyst according to the present invention adsorbs the sulfur oxides contained in the exhaust gas and helps the nitrogen oxides to be reduced by the reducing agent to remove the sulfur oxides and nitrogen oxides from the exhaust gas. You can see.

The reducing agent supply unit 400 may mix a reducing agent precursor that becomes a reducing agent or a reducing agent in the exhaust gas before the exhaust gas flows into the reactor 200. The reducing agent mixed in the exhaust gas by the reducing agent supply unit 400 may be, for example, ammonia (NH ₃ ). However, the reducing agent is not particularly limited, and is known as long as it can be mixed with the exhaust gas and the nitrogen oxide contained in the exhaust gas is reduced to nitrogen and removed from the exhaust gas with the aid of the catalyst of the adsorption catalyst in the reactor 200. Anything is possible. The Hanwonje precursor mixed with the exhaust gas by the reducing agent supply unit 400 may be, for example, urea water. Urea water can be ammonia (NH ₃ ) when mixed in the exhaust gas. However, the reducing agent precursor is not particularly limited, and any known material may be used as long as it is mixed with exhaust gas and can be a reducing agent such as ammonia (NH ₃ ).

The amount of nitrogen oxides contained in the exhaust gas inside the reactor 200 can be removed by the catalyst of the reducing agent and the adsorbing catalyst, so that the reducing agent or reducing agent precursor is mixed with the exhaust gas by the reducing agent supply unit 400. Can be. In this case, some of the nitrogen oxides contained in the exhaust gas may be removed by the catalyst of the reducing agent and the adsorption catalyst, and at least some of the remaining nitrogen oxides may be removed by the adsorbent of the adsorption catalyst. That is, as described above, some of the nitrogen oxides contained in the exhaust gas may be removed from the exhaust gas by the reduction of nitrogen oxides to nitrogen by the catalyst of the reducing agent and the adsorption catalyst. In addition, at least a part of the remaining nitrogen oxides contained in the exhaust gas, the sulfur oxides contained in the exhaust gas are adsorbed by a chemical reaction to the adsorbent to become desulfurization by-products, and the desulfurization by-product reacts with nitrogen oxides contained in the exhaust gas to denitrify by-products. By this, it can be removed from the exhaust gas.

Accordingly, since a relatively small amount of the reducing agent or the reducing agent precursor can be used, the amount of the reducing agent or reducing agent precursor mixed in the exhaust gas and the size of the reducing agent supply unit 400, for example, the size of the reducing agent storage tank 410 to be described later. It can be made small.

The reducing agent supply unit 400 may include a reducing agent storage tank 410 and a reducing agent supply pipe 420 as illustrated in FIGS. 2 to 5.

In the reducing agent storage tank 410, a reducing agent such as ammonia (NH ₃ ) or a reducing agent precursor such as urea water may be stored. One side of the reducing agent supply pipe 420 is connected to the reactor 200, for example, the exhaust gas inlet 210 of the reactor 200 and connected to the exhaust pipe PE through which the exhaust gas flows, and the other side is the reducing agent storage tank 410 Can be connected to. In addition, one side of the reducing agent supply pipe 420 may be connected to the exhaust gas inlet 210 of the reactor 200. The reducing agent supply pipe 420 may be provided with an on-off valve VL. Accordingly, when the on / off valve VL of the reducing agent supply pipe 420 is opened, as shown in FIG. 2, the reducing agent or reducing agent precursor stored in the reducing agent storage tank 410, through the reducing agent supply pipe 420, the reactor 200 It is supplied to the exhaust gas before entering the, it can be mixed with the exhaust gas. The reducing agent or reducing agent precursor may be vaporized by a vaporizer (VP) as shown in FIGS. 4 and 5 before being mixed with the exhaust gas before entering the reactor 200.

The regenerant supply unit 500 may supply the regenerator capable of regenerating the adsorbent contained in the adsorption catalyst attached to the adsorption catalyst member 300 to the reactor 200. The regeneration agent supplied from the regeneration agent supply unit 500 may be, for example, an alkali aqueous solution such as an aqueous sodium hydroxide (NaOH) solution.

As described above, inside the reactor 200, when the sulfur oxides contained in the exhaust gas are adsorbed by a chemical reaction to the adsorbents contained in the adsorption catalyst, desulfurization by-products are generated as reaction by-products. In addition, when desulfurization by-products are chemically reacted with nitrogen oxides contained in exhaust gas, denitrification by-products are generated as reaction by-products. As such, desulfurization by-products and denitrification by-products are generated in the process of treating the exhaust gas, and the exhaust gas may include desulfurization by-products and denitrification by-products in addition to sulfur oxides and nitrogen oxides. When an alkaline aqueous solution such as sodium hydroxide (NaOH) aqueous solution is supplied to the exhaust gas inside the reactor 200 as a regenerant, the regenerant reacts chemically with sulfur oxides, nitrogen oxides, desulfurization by-products, and denitrification by-products contained in the exhaust gas. Precursors can be made. In addition, the adsorbent precursor may be thermally decomposed by the heat of the exhaust gas and regenerated with the adsorbent. In this way, since the adsorbent is regenerated by the regenerant, it is not necessary to additionally supply the adsorbent.

For example, when the adsorbent is iron oxide (Fe ₂ O ₃ ), when an alkaline aqueous solution such as an aqueous sodium hydroxide (NaOH) solution is supplied into the reactor 200 as a regenerant, an aqueous alkaline solution such as an aqueous sodium hydroxide (NaOH) aqueous solution is used. Iron hydroxide (Fe (OH) ₃ ) may be formed as an adsorbent precursor by chemically reacting with sulfur oxides, nitrogen oxides, desulfurization by-products, and denitrification by-products contained in the exhaust gas. In addition, the adsorbent precursor, which is iron hydroxide (Fe (OH) ₃ ), is thermally decomposed by the heat of the exhaust gas and can be regenerated into the adsorbent, iron oxide (Fe ₂ O ₃ ).

As described above, in order for the adsorbent precursor to be thermally decomposed by the heat of the exhaust gas and regenerated with the adsorbent, the temperature of the exhaust gas inside the reactor 200 may be 200 ° C or higher. When the temperature of the exhaust gas inside the reactor 200 is less than 200 ° C, the adsorbent precursor is not thermally decomposed by the heat of the exhaust gas. In this case, the temperature of the exhaust gas inside the reactor 200 may be 200 ° C or more and less than 500 ° C so that thermal decomposition of the adsorbent precursor and reduction of the nitrogen oxide by the catalyst with the reducing agent and the adsorbent are possible. When the temperature of the exhaust gas inside the reactor 200 is 500 ° C. or higher, thermal decomposition of the adsorbent precursor is performed, but the reduction of nitrogen oxides to nitrogen by the catalyst of the reducing agent and the adsorbing catalyst is not achieved.

The regeneration agent supplied from the regeneration agent supply unit 500 is not limited to the above-described sodium hydroxide (NaOH), and any aqueous solution such as an aqueous potassium hydroxide (KOH) solution may be used as long as it is an aqueous alkali solution.

On the other hand, when the reactant reacts first with the sulfur oxides contained in the exhaust gas, the adsorbent contained in the adsorbent catalyst cannot be regenerated as described above. In order to prevent this, the regenerant supply unit 500 may supply the regenerant inside the reactor 200 after the exhaust gas flows into the reactor 200. Accordingly, a regenerant can be supplied to a portion inside the reactor 200 after the sulfur oxides contained in the exhaust gas have been removed from the exhaust gas to a certain extent.

1, 2, and 3, the regenerant supply unit 500 supplies regenerant to a portion inside the reactor 200 that is a predetermined distance away from the exhaust gas inlet 210 in the exhaust gas flow direction. Can be. For example, as shown in FIGS. 1 and 2 and 3 (a), a plurality of adsorption catalyst members 300 are spaced apart from each other at a predetermined distance from each other in the longitudinal or width direction of the reactor 200. It may be provided. In this case, as shown in FIGS. 1 and 2, in the regenerant supply unit 500, a portion inside the reactor 200 at the exhaust gas outlet 220 side, for example, a regenerant at the top inside the reactor 200 Can supply. In addition, as shown in (a) of FIG. 3, the regenerant supply unit 500 may supply the regenerant to the upper portion of the interior of the reactor 200. In addition, as shown in Figure 3 (b), a plurality of adsorption catalyst members 300 may be provided inside the reactor 200 to be spaced apart from each other in a height direction of the reactor 200. In this case, the part inside the reactor 200 equipped with the adsorption catalyst member 300 provided at the bottom does not supply a regenerant, and the adsorption catalyst member above the adsorption catalyst member 300 provided at the bottom ( The regenerant may be supplied to a portion inside the reactor 200 provided with 300).

As shown in FIG. 2, the regeneration agent supply unit 500 may include a regeneration agent storage tank 510, a regeneration agent supply pipe 520, and a regeneration agent injection nozzle 530. The regenerant storage tank 510 may store a regenerant that is an aqueous alkali solution, such as an aqueous sodium hydroxide (NaOH) solution. One side of the regeneration agent supply pipe 520 may be connected to the regeneration agent storage tank 510. The other side of the regenerant supply pipe 520 may penetrate the one surface of the reactor 200 and be provided inside the reactor 200. For example, as shown in FIGS. 2 and 3 (a), the other side of the regenerant supply pipe 520 may penetrate the upper surface of the reactor 200 and be provided inside the reactor 200. In addition, the other side of the regenerant supply pipe 520 is branched into a plurality as shown in FIG. 3 (b), and then penetrates through one surface of the reactor 200, respectively, on each of the plurality of adsorption catalyst members 300. It may be provided in the interior of the reactor 200. The regenerant supply pipe 520 may be provided with an on-off valve (VL). Accordingly, when the on-off valve VL of the regenerant supply pipe 520 is opened, the regenerant stored in the regenerant storage tank 510 may flow the regenerant supply pipe 520. The regenerator injection nozzle 530 may be provided in a portion of the regenerator supply pipe 520 provided inside the reactor 200. The regeneration agent flowing through the regeneration agent supply pipe 520 may be injected into the reactor 200 by the regeneration agent injection nozzle 530. The regenerant may be vaporized by a vaporizer (VP) as shown in FIGS. 4 and 5 while flowing the regenerant supply pipe 520 before being supplied into the reactor 200.

On the other hand, the mixing of the reducing agent or the reducing agent precursor to the exhaust gas by the reducing agent supply unit 400 and the supply of the regenerant into the reactor 200 by the regenerant supply unit 500 are made together, if necessary. It can be done individually or individually.

When it is necessary to remove both sulfur oxides and nitrogen oxides from the exhaust gas, mixing of a reducing agent or a reducing agent precursor to the exhaust gas and supply of a regenerant into the reactor 200 may be performed together. In addition, when it is necessary to remove only sulfur oxides from the exhaust gas, since mixing of a reducing agent or a reducing agent precursor to the exhaust gas for removing nitrogen oxides is not required, only supply of the regenerant into the reactor 200 is performed. It can be done. In addition, when it is necessary to remove only nitrogen oxides from the exhaust gas, since the regeneration of the adsorption catalyst adsorbent is not required for the removal of sulfur oxides, it is not necessary to supply the regenerant into the reactor 200, so the exhaust gas Only a mixture of a reducing agent or a reducing agent precursor may be made. In addition, when regeneration of the adsorption catalyst, that is, regeneration of the adsorption catalyst is required, only supply of the regeneration agent into the reactor 200 may be made.

The exhaust gas treatment apparatus 100 according to the present invention may be provided, for example, on a ship. In this case, the exhaust gas treatment apparatus 100 may be provided before the turbocharger TC as illustrated in the upper portion of FIG. 4 or may be provided after the turbocharger TC as illustrated in the upper portion of FIG. 5. Can be.

When a ship passes through an area that is also an emission control area (ECA) and also a sulfur emission control area (SECA), it is necessary to remove both sulfur oxides and nitrogen oxides from exhaust gas. Therefore, in this case, mixing of the reducing agent or the reducing agent precursor to the exhaust gas by the reducing agent supply unit 400 and the supply of the regenerant into the reactor 200 by the regeneration agent supply unit 500 can be made together. have.

In addition, when a ship passes through an area that is not an emission control area (ECA) but a sulfur emission control area (SECA) or uses fuel that does not satisfy the sulfur content standards, exhaust gas You may remove only sulfur oxide from. Therefore, in this case, it is not necessary to mix the reducing agent or the reducing agent precursor to the exhaust gas by the reducing agent supply unit 400 for removing nitrogen oxides. Then, in order to regenerate the adsorbent of the adsorbent catalyst attached to the adsorbent catalyst member 300, only the supply of the regenerant into the reactor 200 by the regenerant supply unit 500 can be made.

Further, although the ship is an emission control area (ECA), but passes through an area other than the sulfur emission control area (SECA), only nitrogen oxide may be removed from the exhaust gas. Therefore, in this case, since it is not necessary to regenerate the adsorbent of the adsorbent catalyst attached to the adsorbent catalyst member 300, only the mixing of the reducing agent or the reducing agent precursor to the exhaust gas by the reducing agent supply unit 400 can be achieved.

In addition, sulfuric acid is used when high sulfur content is used as fuel, even if the ship passes through both the Emission Control Area (ECA) and the Sulfur Emission Control Area (SECA). It is necessary to respond to cargo emission regulations. In this case, since mixing of a reducing agent or a reducing agent precursor to the exhaust gas by the reducing agent supply unit 400 for removing nitrogen oxides is not required, for regeneration of the adsorbing agent of the adsorbing catalyst for removing sulfur oxides, a regenerant Only supply of regenerant into the reactor 200 by the supply unit 500 can be made.

Exhaust gas treatment method

One embodiment of the method for treating exhaust gas according to the present invention may include a mixing step (S100), an inflow step (S200), a processing step (S300), and a regeneration step (S400).

In the mixing step (S100), a reducing agent precursor to be a reducing agent or a reducing agent may be mixed with the exhaust gas. For example, as described above, before the exhaust gas flows into the reactor 200, a reducing agent precursor such as ammonia (NH ₃ ) or a reducing agent precursor, such as urea water, is reduced by the reducing agent supply unit 400. The exhaust pipe PE connected to the discharge device ED may be mixed with the exhaust gas flowing.

On the other hand, in the mixing step (S100), in the treatment step (S300), only a portion of the nitrogen oxides contained in the exhaust gas can be removed by the catalyst of the reducing agent and the adsorption catalyst, so that the reducing agent or reducing agent precursor is mixed in the exhaust gas can do.

In this case, some of the nitrogen oxides contained in the exhaust gas are removed by the catalyst of the reducing agent and the adsorption catalyst in the processing step (S300), and at least some of the remaining nitrogen oxides are removed by the adsorbent of the adsorption catalyst in the processing step (S300). Can be. That is, as described above, some of the nitrogen oxides contained in the exhaust gas may be removed from the exhaust gas by the reduction of nitrogen oxides to nitrogen by the catalyst of the reducing agent and the adsorption catalyst. In addition, at least a part of the remaining nitrogen oxides contained in the exhaust gas, the sulfur oxides contained in the exhaust gas are adsorbed by a chemical reaction to the adsorbent to become desulfurization byproducts, and the desulfurization byproduct reacts with the nitrogen oxides contained in the exhaust gas to denitrify byproducts. By this, it can be removed from the exhaust gas.

Accordingly, since a relatively small amount of the reducing agent or the reducing agent precursor can be used, the amount of the reducing agent or reducing agent precursor mixed in the exhaust gas and the size of the reducing agent supply unit 400, for example, the size of the reducing agent storage tank 410, etc. can be reduced. You can ...

In the inflow step (S200), the exhaust gas in which the reducing agent or the reducing agent precursor is mixed may be introduced into the reactor 200 in the mixing step (S100) as described above. For example, through the exhaust gas inlet 210 connected to the exhaust pipe PE, an exhaust gas in which a reducing agent or a reducing agent precursor is mixed may be introduced into the reactor 200.

In the treatment step (S300), nitrogen oxides contained in the exhaust gas may be removed by a reducing agent and an adsorbing catalyst inside the reactor 200. For example, nitrogen oxides contained in the exhaust gas may be nitrogen with the aid of a catalyst of an adsorption catalyst attached to the adsorption catalyst member 300 provided inside the reactor 200 with a reducing agent such as ammonia (NH ₃ ) mixed with the exhaust gas. The nitrogen oxides contained in the exhaust gas can be removed from the exhaust gas by reducing to.

In addition, in the treatment step (S300), the sulfur oxides contained in the exhaust gas may be adsorbed and the nitrogen oxides contained in the exhaust gas may be sequentially removed by the adsorption catalyst inside the reactor 200. For example, the sulfur oxides contained in the exhaust gas are adsorbed by the chemical reaction to the adsorbent of the adsorption catalyst attached to the adsorption catalyst member 300 provided inside the reactor 200 to be desulfurized by-products to remove sulfur oxides from the exhaust gas. Can be. Then, the desulfurization by-product reacts with the nitrogen oxide contained in the exhaust gas to become a denitrification by-product, so that the nitrogen oxide can be removed from the exhaust gas.

In the regeneration step (S400), an adsorbent may be regenerated by supplying a regenerant inside the reactor 200, that is, an adsorbent. For example, in the regeneration step (S400), an aqueous alkali solution such as sodium hydroxide (NaOH) may be supplied to the reactor 200 by the regeneration agent supply unit 500.

Then, the regeneration step (S400) may include a precursor generation step (S410) and a pyrolysis step (S420).

In the precursor generation step (S410), the regenerant supplied to the reactor 200, nitrogen oxides, sulfur oxides, and desulfurization by-products produced in the above-described treatment step (S300) and denitrification by-products are chemically reacted, For example, an adsorbent precursor such as iron hydroxide (Fe (OH) ₃ ) can be made.

In the thermal decomposition step (S420), the adsorbent precursor such as iron hydroxide (Fe (OH) ₃ ) produced in the precursor generation step (S410) is thermally decomposed with the heat of the exhaust gas, and can be regenerated with an adsorbent such as iron oxide (Fe ₂ O ₃ ). have. To this end, the temperature of the exhaust gas inside the reactor 200 may be 200 ° C or higher to allow thermal decomposition of the adsorbent precursor. In this case, the temperature of the exhaust gas inside the reactor 200 may be 200 ° C or more and less than 500 ° C so that thermal decomposition of the adsorbent precursor and reduction of nitrogen oxides with a reducing agent and a catalyst are possible.

When using the exhaust gas treatment apparatus according to the present invention as described above, it is possible to simultaneously remove sulfur oxides and nitrogen oxides from the exhaust gas with one exhaust gas treatment apparatus, and reduce the exhaust gas to the exhaust gas before it enters the reactor. After the reducing agent precursor that becomes the reducing agent is mixed, and exhaust gas is introduced into the reactor, a regenerant can be supplied inside the reactor.

The exhaust gas treatment device described above is not limited to the configuration of the above-described embodiment, the embodiments may be configured by selectively combining all or part of each embodiment so that various modifications can be made. have.

100: exhaust gas treatment device 200: reactor
210: exhaust gas inlet 220: exhaust gas outlet
230: treatment by-product outlet 300: adsorption catalyst member
400: reducing agent supply unit 410: reducing agent storage tank
420: reducing agent supply pipe 500: regenerant supply unit
510: Regenerator storage tank 520: Regenerator supply pipe
530: Regenerator injection nozzle ED: Exhaust gas emission device
ME: Main engine GE: Power generation engine
PE: exhaust pipe PD: exhaust pipe
TC: Turbocharger VL: Open / close valve
PL: Drain pipe TB: Treatment by-product collection tank
VP: Vaporizer

Claims (15)

A reactor through which exhaust gas flows;
A reducing agent supply unit for mixing a reducing agent or a reducing agent precursor that becomes the reducing agent in the exhaust gas before the exhaust gas enters the reactor; And
A regenerant supply unit for supplying a regenerant into the reactor after the exhaust gas flows into the reactor;
Exhaust gas treatment device comprising a. According to claim 1, The reactor is provided with an exhaust gas inlet to allow exhaust gas to flow, and in the regenerant supply unit, the regenerant is disposed in a portion of the reactor spaced a predetermined distance away from the exhaust gas inlet in the exhaust gas flow direction. Exhaust gas treatment device for supplying. According to claim 2, The reactor is provided with an exhaust gas outlet through which the treated exhaust gas is discharged, and the regenerant supply unit processes exhaust gas to supply the regenerant to a portion inside the reactor at the exhaust gas outlet side. Device. According to claim 1, Adsorption catalyst member provided in the reactor; Exhaust gas processing apparatus further comprising. The nitrogen oxide contained in the exhaust gas is removed by the reducing agent and the adsorption catalyst attached to the adsorption catalyst member, and the sulfur oxide contained in the exhaust gas is adsorbed by the adsorption catalyst to the exhaust gas. Exhaust gas treatment apparatus in which the nitrogen oxide contained is sequentially removed. The adsorbent of claim 5, wherein the adsorption catalyst is adsorbed so that the sulfur oxides contained in the exhaust gas and nitrogen oxides are sequentially removed, and the nitrogen oxides contained in the exhaust gas are reduced to nitrogen by the reducing agent from the exhaust gas. Exhaust gas treatment device comprising a catalyst that helps to be removed. The exhaust gas treatment apparatus according to claim 6, wherein the adsorbent catalyst is a powder form in which the adsorbent and the catalyst are mixed, and is attached to the adsorbent catalyst member by extrusion molding or an adhesive material. The exhaust according to claim 6, wherein the catalyst in powder form is first attached to the adsorption catalyst member by extrusion molding or adhesive material, and then the powder type adsorbent is attached to the adsorption catalyst member by adhesive material or extrusion molding. Gas treatment device. The method of claim 6, wherein the sulfur oxides contained in the exhaust gas is removed from the exhaust gas by being adsorbed to the adsorbent by chemical reaction to become a desulfurization by-product,
The nitrogen oxide contained in the exhaust gas is an exhaust gas treatment apparatus that is removed from the exhaust gas by chemically reacting with the desulfurization byproduct to become a denitrification byproduct. The method of claim 9, wherein the regenerant is chemically reacted with the nitrogen oxides, sulfur oxides, desulfurization by-products, and denitrification by-products contained in the exhaust gas to make an adsorbent precursor, and the adsorbent precursor is thermally decomposed by the heat of the exhaust gas to the adsorbent. Regenerative exhaust gas treatment system. The exhaust gas treatment apparatus according to claim 10, wherein the regenerant is an aqueous alkali solution. The exhaust gas treatment apparatus according to claim 10, wherein the temperature of the exhaust gas inside the reactor is 200 ° C or more and less than 500 ° C so that thermal decomposition of the adsorbent precursor and reduction of nitrogen oxide by the reducing agent and the catalyst are possible. The exhaust gas treatment apparatus of claim 9, wherein the adsorbent includes at least one of iron oxide (Fe ₂ O ₃ ), copper oxide (CuO), and cerium oxide (CeO). The exhaust gas treatment apparatus of claim 10, wherein the adsorbent is iron oxide (Fe ₂ O ₃ ) and the adsorbent precursor is iron hydroxide (Fe (OH) ₃ ). The apparatus of claim 6, wherein the catalyst comprises at least one of vanadium (V), tungsten (W), and titanium oxide (TiO ₂ ).

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