DEVICE AND METHOD FOR CLEANING EXHAUST GAS FROM A SHIP

Description

[Technical Field]

[0001] The present specification relates to a ship exhaust gas cleaning apparatus and method, and more particularly, to proposing a method for sequentially removing sulfur dioxide (SO 2 ) and nitrogen oxides (NO x ) through a process composed of two steps, in the removal of sulfur dioxide (SO 2 ) and nitrogen oxides (NO x ) which are contained in ship exhaust gas, and provides a ship exhaust gas cleaning apparatus and method for maximizing the conversion efficiency of sulfur dioxide (SO 2 ) into ammonium bisulfate (NH 4 HSO 4 ), thereby being capable of preventing, during the following process of removing nitrogen oxide (NO x ), sulfur dioxide (SO 2 ) remaining in ship exhaust gas from lowering nitrogen oxide (NO x ) removal efficiency.[Background Art]

[0002] Exhaust gas of a ship engine using a fuel oil with high sulfur content includes carbon dioxide (CO 2 ), carbon monoxide (CO), sulfur dioxide (SO 2 ), nitrogen oxide (NO x ), water vapor (H 2 O), oxygen (O 2 ), nitrogen (N 2 ), and the like. Among these exhaust materials, especially SO 2 and NO x becomes more strictly regulated not to be emitted to the outside of the ship by the International Maritime Organization (IMO). For example, since 2016, regulations have been strengthened to reduce NO x emissions from ships sailing in emmission control area (ECA) such as the coast of the United States to 20% or less of the previously permitted emissions. In particular, in the case of SO 2 emission, which is expected to tighten regulations from 2020, when sailing in global water for all ships, exhaust gas should be purified and discharged to be less than the amount of SO 2 emitted when using a fuel oil containing 0.5% or less of sulfur, and when sailing in ECA, exhaust gas should be purified and discharged to be less than the amount of SO 2 emitted when using a fuel oil containing 0.1% or less of sulfur.

[0003] Therefore, in particular, it is a very urgent issue to establish the best plan to respond to the SO 2 regulation scheduled from 2020. As a method proposed or developed so far to solve such an issue in the shipping industry, first, there is a method using a low-sulfur fuel oil, as proposed by the IMO. However, if this method is adopted, there is an economic disadvantage that a huge price is added as much as the price difference between a low-sulfur fuel oil and a high-sulfur fuel oil.

[0004] Second, there is a method of installing and utilizing a scrubber that dissolves SO 2 contained in the engine exhaust gas with a large amount of water to convert SO 2 into low-concentration sulfurous acid or sulfuric acid and then releasing the same into seawater, or converting into sodium or calcium salt and storing the same and then disposing the same. However, in this method, there is a serious additional economic burden, such as the need for special steel of expensive materials and the need to install a very large-scale scrubber. Also, there are technical difficulties that the stability of the technology is not perfect yet.

[0005] Third, SO 2 contained in the ship exhaust gas may be removed using activated carbon. This method is for adsorbing SO 2 to the surface and pores of the activated carbon, but there is a problem in that the adsorption property is lowered at a temperature of 200°C or higher due to the nature of the activated carbon. Also, the activated carbon must be continuously supplied, which is poor in economic feasibility.

[0006] Meanwhile, as described above, the ship exhaust gas contains nitrogen oxide (NO x ) in addition to SO 2 , and nitrogen oxide (NO x ) is usually removed through a SCR (Selective Catalytic Reduction) device. The SCR device uses urea or ammonia (NH 3 ) as a reducing agent and reduces nitrogen oxide (NO x ) to N 2 by accelerating the reduction reaction through a SCR catalyst. In operating the SCR device, if an exhaust gas containing both SO 2 and nitrogen oxide (NO x ) is supplied to the SCR device, ammonium bisulfate (NH 4 HSO 4 ) is generated, and the generated ammonium bisulfate (NH 4 HSO 4 ) is formed in the pores of the SCR catalyst. Ammonium bisulfate (NH 4 HSO 4 ) formed in the pores of the SCR catalyst remains as a liquid up to about 320°C, which weakens the performance of the SCR catalyst.

[0007] EP2955345 discloses a ship exhaust gas cleaning apparatus according to the preamble of appended claim 1.[Disclosure] [Technical Problem]

[0008] This disclosure is designed to solve the problem as described above, and the present disclosure is directed to proposing a method for sequentially removing sulfur dioxide (SO 2 ) and nitrogen oxides (NO x ) through a process composed of two steps, in the removal of sulfur dioxide (SO 2 ) and nitrogen oxides (NO x ) which are contained in ship exhaust gas, and provides a ship exhaust gas cleaning apparatus and method for maximizing the conversion efficiency of sulfur dioxide (SO 2 ) into ammonium bisulfate (NH 4 HSO 4 ), thereby being capable of preventing, during the following process of removing nitrogen oxide (NO x ), sulfur dioxide (SO 2 ) remaining in ship exhaust gas from lowering nitrogen oxide (NO x ) removal efficiency.

[0009] In addition, the present disclosure is directed to providing a ship exhaust gas cleaning apparatus and method capable of improving wet scrubbing efficiency for sulfur (S) components by maximizing the production rate of ammonium bisulfate (NH 4 HSO 4 ), which is a reaction by-product of ammonia (NH 3 ) and sulfur dioxide (SO 2 ).[Technical Solution]

[0010] A ship exhaust gas cleaning apparatus according to an embodiment of the present disclosure to accomplish the above object comprises a sulfur dioxide removal device configured to provide a space for inducing the reaction among ammonia (NH 3 ), steam (H 2 O), oxygen (O 2 ) and sulfur dioxide (SO 2 ) and convert sulfur dioxide (SO 2 ) contained in a ship exhaust gas into ammonium bisulfate (NH 4 HSO 4 ); a wet scrubber configured to remove the ammonium bisulfate (NH 4 HSO 4 ) generated by the sulfur dioxide removal device by dissolving the ammonium bisulfate (NH 4 HSO 4 ) in a feed water; and it is characterized by comprising a SCR device configured to reduce nitrogen oxide (NO x ) contained in the ship exhaust gas to nitrogen (N 2 ) for the ship exhaust gas discharged from the sulfur dioxide removal device.

[0011] In the sulfur dioxide removal device, an ammonium bisulfate (NH 4 HSO 4 ) production reaction may be activated, and a nitrogen reduction reaction by the reaction of nitrogen oxide (NO x ) and ammonia (NH 3 ) may be suppressed.

[0012] The temperature inside the sulfur dioxide removal device or the temperature of the ship exhaust gas introduced into the sulfur dioxide removal device may be 150-300°C, more preferably 180-250°C.

[0013] Ammonia (NH 3 ) may be put into the sulfur dioxide removal device in an amount of 1-2 times compared to the molar equivalent of the sulfur dioxide (SO 2 ) contained in the ship exhaust gas, more preferably in an amount of 1.1-1.6 times compared to the molar equivalent of the sulfur dioxide (SO 2 ).

[0014] An ammonium bisulfate synthesis catalyst may be charged into the sulfur dioxide removal device, and the ammonium bisulfate synthesis catalyst may serve to promote the production of ammonium bisulfate (NH 4 HSO 4 ).

[0015] The ammonium bisulfate synthesis catalyst may be any one of an oxidation catalyst, a mixture of oxidation catalyst and solid acid, and a solid acid support of oxidation catalyst, or a mixture thereof. The oxidation catalyst may be any one of MnO 2 , V 2 O 5 , Ni, Pd, and Pt, or a mixture thereof, and the solid acid may be any one selected from the group consisting of basalt, granite, limestone, sandstone, shale, metamorphic rock, kaolinite, attapulgite, bentonite, montmorillonite, zeolite, zinc oxide (ZnO), aluminum oxide (Al 2 O 3 ), titanium oxide (TiO 2 ), cesium oxide (CeO 2 ), vanadium oxide (V 2 O 5 ), silicon oxide (SiO 2 ), chromium oxide (Cr 2 O 3 ), calcium sulfate (CaSO 4 ), manganese sulfate (MnSO 4 ), nickel sulfate (NiSO 4 ), copper sulfate (CuSO 4 ), cobalt sulfate (CoSO 4 ), cadmium sulfate (CdSO 4 ), magnesium sulfate (MgSO 4 ), iron sulfate II (FeSO 4 ), aluminum sulfate (Al 2 (SO 4 ) 3 ), calcium nitrate (Ca(NO 3 ) 2 ), zinc nitrate (Zn(NO 3 ) 2 ), iron nitrate III (Fe(NO 3 ) 3 ), aluminum phosphate (AlPO 4 ), iron phosphate III (FePO 4 ), chromium phosphate (CrPO 4 ), copper phosphate (Cu 3 (PO 4 ) 2 ), zinc phosphate (Zn 3 (PO 4 ) 4 ), magnesium phosphate (Mg 3 (PO 4 ) 2 ), aluminum chloride (AlCl 3 ), titanium chloride (TiCl 4 ), calcium chloride (CaCl 2 ), calcium fluoride (CaF 2 ), barium fluoride (BaF 2 ) and calcium carbonate (CaCO 3 ), or a mixture thereof.

[0016] A substance to be dissolved by the wet scrubber may be ammonium bisulfate (NH 4 HSO 4 ), and the feed water put into the wet scrubber may be in an amount of 100-2,000 times compared to the mass of ammonium bisulfate (NH 4 HSO 4 ), and more preferably, the feed water put into the wet scrubber may be in an amount of 300-1,000 times compared to the mass of ammonium bisulfate (NH 4 HSO 4 ).

[0017] Ammonia (NH 3 ) may be put into the SCR device as a reducing agent, and the ammonia (NH 3 ) may be put into the sulfur dioxide removal device in an amount of 0.7-1.5 times compared to the molar equivalent of nitrogen oxide (NO x ) contained in the ship exhaust gas.

[0018] A ship exhaust gas cleaning method according to an embodiment of the present disclosure is characterized in comprising: a sulfur dioxide removing step of converting sulfur dioxide (SO 2 ) contained in a ship exhaust gas into ammonium bisulfate (NH 4 HSO 4 ) by the reaction among sulfur dioxide (SO 2 ), steam (H 2 O), oxygen (O 2 ) and ammonia (NH 3 ); and an ammonium bisulfate removing step of removing the ammonium bisulfate (NH 4 HSO 4 ) by dissolving the ammonium bisulfate (NH 4 HSO 4 ) in a feed water; wherein a nitrogen oxide removing step is performed between the sulfur dioxide removing step and the ammonium bisulfate removing step, and the nitrogen oxide removing step further includes a nitrogen oxide removing step of removing the nitrogen oxide (NO x ) contained in the ship exhaust gas by reducing the nitrogen oxide (NO x ) to nitrogen (N 2 ).

[0019] In the sulfur dioxide removing step, a condition of controlling the temperature of the ship exhaust gas to 150-300°C, a condition of putting ammonia (NH 3 ) in an amount of 1-2 times compared to the molar equivalent of the sulfur dioxide (SO 2 ) contained in the ship exhaust gas, and a condition of charging an ammonium bisulfate synthesis catalyst may be applied selectively or in combination to maximize ammonium bisulfate (NH 4 HSO 4 ) synthesis efficiency.

[0020] In the ammonium bisulfate removing step, the feed water may be put in an amount of 100-2,000 times compared to the mass of ammonium bisulfate (NH 4 HSO 4 ) to dissolve the ammonium bisulfate (NH 4 HSO 4 ).

[0021] The nitrogen oxide removing step may be carried out by a SCR device, and a condition of controlling the temperature of the ship exhaust gas or the temperature of the inside of the SCR device to 200-450°C and a condition of putting ammonia (NH 3 ) in an amount of 0.7-1.5 times compared to the molar equivalent of nitrogen oxide (NO x ) contained in the ship exhaust gas may be applied selectively or in combination.

[0022] In addition, in the sulfur dioxide removing step, ammonia (NH 3 ) in an amount of 1-2 times compared to the molar equivalent of sulfur dioxide (SO 2 ) contained in the ship exhaust gas and ammonia (NH 3 ) in an amount of 0.7-1.5 times compared to the molar equivalent of nitrogen oxide (NO x ) contained in the ship exhaust gas may be put into a sulfur dioxide removal device.[Advantageous Effects]

[0023] The ship exhaust gas cleaning apparatus and method according to one aspect of the present disclosure has the following effects.

[0024] In removing sulfur dioxide (SO 2 ) contained in the ship exhaust gas, ammonium bisulfate (NH 4 HSO 4 ) is generated by inducing a reaction among sulfur dioxide (SO 2 ), steam(H 2 O), oxygen(O 2 ) and ammonia (NH 3 ), and ammonium bisulfate (NH 4 HSO 4 ) is removed through a wet scrubbing process, thereby completely removing sulfur dioxide (SO 2 ) in the ship exhaust gas. In addition, compared to the conventional wet scrubbing process using sulfur dioxide (SO 2 ) as a material to be dissolved, the amount of feed water used may be reduced to 1 / 10 or less.

[0025] In addition, when a following SCR process is combined, as sulfur dioxide (SO 2 ) is completely removed by the sulfur dioxide removing process described above, it is fundamentally blocked that ammonium bisulfate (NH 4 HSO 4 ) is generated inside the pores and on the surface of the SCR catalyst, thereby preventing the SCR efficiency from being deteriorated due to ammonium bisulfate (NH 4 HSO 4 ) in a liquid phase.[Description of Drawings]

[0026] FIG. 1 is a diagram showing a ship exhaust gas cleaning apparatus according to the first embodiment of the present disclosure. FIG. 2 is a diagram showing a ship exhaust gas cleaning apparatus according to the second embodiment of the present disclosure. FIG. 3 is a flowchart for illustrating a ship exhaust gas cleaning method according to the first embodiment of the present disclosure. FIG. 4 is a flowchart for illustrating a ship exhaust gas cleaning method according to the second embodiment of the present disclosure. FIG. 5 is a diagram showing an experiment device to which Experimental Examples 1 to 5 are applied. [Best Mode]

[0027] An embodiment of the present disclosure proposes a technology that may effectively remove sulfur dioxide (SO 2 ) contained in a ship exhaust gas. In addition, an embodiment of the present disclosure proposes a technology capable of removing not only sulfur dioxide (SO 2 ) but also nitrogen oxide (NO x ) by combining a nitrogen oxide removing process.

[0028] It is difficult to simultaneously remove sulfur dioxide (SO 2 ) and nitrogen oxide (NO x ) contained in the ship exhaust gas through one process. Therefore, the sulfur dioxide (SO 2 ) removing process and the nitrogen oxide (NO x ) removing process are separately performed, and the sulfur dioxide (SO 2 ) removing process and the nitrogen oxide (NO x ) removing process are linked.

[0029] In carrying out the sulfur dioxide (SO 2 ) removing process in conjunction with the nitrogen oxide (NO x ) removing process, it should be minimized that a gas to be treated in each process is remained in the ship exhaust gas after each process is carried out, and it should be suppressed that the treatment efficiency of a following removing process is deteriorated.

[0030] As mentioned in the 'Background Art' section above, if the nitrogen oxide (NO x ) reduction process is performed by a SCR device in a state where sulfur dioxide (SO 2 ) remains in the exhaust gas, ammonium bisulfate (NH 4 HSO 4 ) is generated to block pores of the SCR catalyst, which may deteriorate the nitrogen oxide (NO x ) removal efficiency. In addition, even in the method of removing sulfur dioxide (SO 2 ) using activated carbon, if sulfur dioxide (SO 2 ) and nitrogen oxide (NO x ) are supplied together, the adsorption properties of activated carbon may be deteriorated due to adsorption of ammonium bisulfate (NH 4 HSO 4 ).

[0031] An embodiment of the present disclosure proposes a technology for removing sulfur dioxide (SO 2 ) through the reaction among ammonia (NH 3 ), steam(H 2 O), oxygen(O 2 ) and sulfur dioxide (SO 2 ). In addition, an embodiment of the present disclosure induces the production of ammonium bisulfate (NH 4 HSO 4 ) through the reaction among ammonia (NH 3 ), steam(H 2 O), oxygen(O 2 ) and sulfur dioxide (SO 2 ) and maximizes the synthesis efficiency of ammonium bisulfate (NH 4 HSO 4 ).

[0032] As mentioned in the 'Background Art' section above, ammonia (NH 3 ) is generally used as a reducing agent in the nitrogen oxide (NO x ) removing process. In an embodiment of the present disclosure, ammonia (NH 3 ) is applied to the sulfur dioxide (SO 2 ) removing process.

[0033] The reason for applying ammonia (NH 3 ) to the sulfur dioxide (SO 2 ) removing process in an embodiment of the present disclosure is to induce the production of ammonium bisulfate (NH 4 HSO 4 ) along with the removal of sulfur dioxide (SO 2 ) through the reaction among ammonia (NH 3 ), steam(H 2 O), oxygen(O 2 ) and sulfur dioxide (SO 2 ). In addition, it is to maximize the synthesis efficiency of ammonium bisulfate (NH 4 HSO 4 ) and to minimize the sulfur dioxide (SO 2 ) remaining in the ship exhaust gas by removing ammonium bisulfate (NH 4 HSO 4 ) component by means of wet scrubbing. As the residual sulfur dioxide (SO 2 ) component in the ship exhaust gas is minimized, it is possible to prevent the nitrogen oxide (NO x ) removal process efficiency from deteriorating due to the sulfur dioxide (SO 2 ) component.

[0034] Along with this, an embodiment of the present disclosure proposes a technology capable of improving the wet scrubbing efficiency for sulfur (S) components compared to the prior art. In the conventional wet scrubbing process for desulfurization, the wet scrubbing process is carried out for sulfur dioxide (SO 2 ), but in an embodiment of the present disclosure, the wet scrubbing process is performed not for sulfur dioxide (SO 2 ) but for ammonium bisulfate (NH 4 HSO 4 ). Ammonium bisulfate (NH 4 HSO 4 ) has higher solubility than sulfur dioxide (SO 2 ), so the wet scrubbing process may be performed using a relatively small amount of water (or seawater).

[0035] Hereinafter, a ship exhaust gas cleaning apparatus and method according to the first and second embodiments of the present disclosure will be described in detail with reference to the drawings. The first embodiment relates to purifying sulfur dioxide (SO 2 ) contained in the ship exhaust gas, and the second embodiment relates to sequentially purifying sulfur dioxide (SO 2 ) and nitrogen oxide (NO x ) contained in the ship exhaust gas.

[0036] Referring to FIG. 1, the ship exhaust gas cleaning apparatus according to the first embodiment of the present disclosure includes a sulfur dioxide removal device 110 and a wet scrubber 120.

[0037] The sulfur dioxide (SO 2 ) contained in the ship exhaust gas is purified while passing through the sulfur dioxide removal device 110 and the wet scrubber 120 sequentially. The sulfur dioxide (SO 2 ) contained in the ship exhaust gas is converted into ammonium bisulfate (NH 4 HSO 4 ) by the sulfur dioxide removal device 110, and the wet scrubber 120 removes the ammonium bisulfate (NH 4 HSO 4 ) produced by the sulfur dioxide removal device 110 by dissolving the ammonium bisulfate (NH 4 HSO 4 ).

[0038] The sulfur dioxide removal device 110 provides a space to induce the reaction among ammonia (NH 3 ), steam(H 2 O), oxygen(O 2 ) and sulfur dioxide (SO 2 ). The ship exhaust gas is introduced into the sulfur dioxide removal device 110 from a ship engine, and ammonia (NH 3 ) is supplied to the sulfur dioxide removal device 110 through a separate ammonia supply device 140.

[0039] The sulfur dioxide (SO 2 ) contained in the ship exhaust gas reacts with ammonia (NH 3 ), steam(H 2 O) and oxygen(O 2 ) and ammonium bisulfate (NH 4 HSO 4 ) is produced by the reaction of sulfur dioxide (SO 2 ) and ammonia (NH 3 ). The reaction of sulfur dioxide (SO 2 ) and ammonia (NH 3 ) and the production of ammonium bisulfate (NH 4 HSO 4 ) by the reaction of sulfur dioxide (SO 2 ) and ammonia (NH 3 ) are explained through the reaction of Equations 1 and 2 below. In the reaction of Equations 1 and 2, the reaction of SO 2 and O 2 is promoted at a low temperature of 300°C or below, and finally ammonium bisulfate (NH 4 HSO 4 ) is produced by the reaction of SO 3 , H 2 O and NH 3 .         (Equation 1)     2SO 2 + O 2 → 2SO 3         (Equation 2)     SO 3 + H 2 O + NH 3 --+ NH 4 HSO 4         (Equation 3)     2NO + O 2 → 2NO 2         (Equation 4)     NO + NO 2 + NH 3 → 2N 2 + 3H 2 O

[0040] Meanwhile, in the sulfur dioxide removal device 110, in addition to the ammonium bisulfate (NH 4 HSO 4 ) production reaction (see Equations 1 to 3), the reaction of nitrogen oxide (NO x ) contained in the ship exhaust gas and NH 3 may occur by adding NH 3 (see Equations 3 and 4). That is, in the sulfur dioxide removal device 110, the ammonium bisulfate (NH 4 HSO 4 ) production reaction by Equations 1 and 2 and the reaction of nitrogen oxide (NO x ) and NH 3 by Equation 4 may be performed together.

[0041] As such, in the sulfur dioxide removal device 110, the ammonium bisulfate (NH 4 HSO 4 ) production reaction and the nitrogen reduction reaction by the reaction of nitrogen oxide (NO x ) and NH 3 may occur simultaneously, and in an embodiment of the present disclosure, the ammonium bisulfate (NH 4 HSO 4 ) production reaction is activated and the reaction between nitrogen oxide (NO x ) and NH 3 is suppressed. The reason is that, if the reaction between nitrogen oxide (NO x ) and NH 3 is performed, the nitrogen oxide (NO x ) contained in the ship exhaust gas may be partially removed, but the sulfur dioxide (SO 2 ) removal efficiency is deteriorated as the ammonium bisulfate (NH 4 HSO 4 ) production reaction is relatively inactivated. In addition, in an embodiment of the present disclosure, a method of maximizing the production of ammonium bisulfate (NH 4 HSO 4 ) through the reaction of ammonia (NH 3 ) and sulfur dioxide (SO 2 ) and removing the generated ammonium bisulfate (NH 4 HSO 4 ) through a following wet scrubbing process is applied. However, if the ammonium bisulfate (NH 4 HSO 4 ) production reaction is relatively inactive, it is difficult to completely remove the sulfur (S) component of the ship exhaust gas.

[0042] By controlling the reaction temperature, it is possible to maximize the ammonium bisulfate (NH 4 HSO 4 ) production reaction (see Equations 1 and 2) and to minimize the nitrogen reduction reaction (see Equations 3 and 4) by the reaction of nitrogen oxide (NO x ) and NH 3 . In other words, it is possible to maximize the ammonium bisulfate (NH 4 HSO 4 ) production reaction and minimize the nitrogen reduction reaction by the reaction of nitrogen oxide (NO x ) and NH 3 by controlling the temperature in the sulfur dioxide removal device 110 or the temperature of the ship exhaust gas. This is because the ammonium bisulfate (NH 4 HSO 4 ) production reaction (see Equations 1 to 3) is carried out at a relatively low temperature and the nitrogen reduction reaction (see Equations 3 and 4) by the reaction of nitrogen oxide (NO x ) and NH 3 is carried at a relatively high temperature.

[0043] The ammonium bisulfate (NH 4 HSO 4 ) production reaction occurs predominantly at 150-300°C, and if the temperature in the sulfur dioxide removal device 110 or the temperature of the ship exhaust gas exceeds 300°C, the nitrogen reduction reaction occurs by the reaction of nitrogen oxide (NO x ) and NH 3 . In consideration of this, the temperature in the sulfur dioxide removal device 110 or the temperature of the ship exhaust gas is preferably adjusted to 150-300°C, more preferably 180-250°C. If the temperature in the sulfur dioxide removal device 110 or the temperature of the ship exhaust gas is lower than 180°C, the generated ammonium bisulfate (NH 4 HSO 4 ) may be liquefied, and if the temperature in the sulfur dioxide removal device 110 or the temperature of the ship exhaust gas exceeds 250°C, the ammonium bisulfate (NH 4 HSO 4 ) synthesis efficiency may be rapidly deteriorated. Considering that the temperature of the exhaust gas discharged through a turbo charger of the ship engine is about 220°C, the ammonium bisulfate (NH 4 HSO 4 ) production reaction may be maximized without additional temperature control after the ship exhaust gas is introduced into the sulfur dioxide removal device 110.

[0044] Meanwhile, in order to increase the ammonium bisulfate (NH 4 HSO 4 ) synthesis efficiency, it is required to control the amount of put ammonia (NH 3 ) together with the temperature control as described above. Specifically, it is required to put ammonia (NH 3 ) in an amount of 1-2 times compared to the molar equivalent of sulfur dioxide (SO 2 ) contained in the ship exhaust gas. As a more preferable condition, it is required to put ammonia (NH 3 ) in an amount of 1.1-1.6 times compared to the molar equivalent of sulfur dioxide (SO 2 ) contained in the ship exhaust gas. Here, if the amount of ammonia (NH 3 ) is less than 1.1 times compared to the molar equivalent of sulfur dioxide (SO 2 ), the ammonium bisulfate (NH 4 HSO 4 ) synthesis efficiency is deteriorated, and if the amount of ammonia (NH 3 ) is greater than 1.6 times compared to the molar equivalent of sulfur dioxide (SO 2 ), ammonia (NH 3 ) is more likely to be lost.

[0045] As another method to increase the ammonium bisulfate (NH 4 HSO 4 ) synthesis efficiency, an ammonium bisulfate synthesis catalyst may be used. The ammonium bisulfate synthesis catalyst serves to promote the production of ammonium bisulfate (NH 4 HSO 4 ), and may be optionally charged into the sulfur dioxide removal device 110.

[0046] The ammonium bisulfate synthesis catalyst may employ any one of an oxidation catalyst, a mixture of oxidation catalyst and solid acid, and a solid acid support of oxidation catalyst, or a mixture thereof. The oxidation catalyst may be any one of MnO 2 , V 2 O 5 , Ni, Pd, and Pt, or a mixture thereof. In addition, the solid acid may be any one selected from the group consisting of basalt, granite, limestone, sandstone, shale, metamorphic rock, kaolinite, attapulgite, bentonite, montmorillonite, zeolite, zinc oxide (ZnO), aluminum oxide (Al 2 O 3 ), titanium oxide (TiO 2 ), cesium oxide (CeO 2 ), vanadium oxide (V 2 O 5 ), silicon oxide (SiO 2 ), chromium oxide (Cr2O 3 ), calcium sulfate (CaSO 4 ), manganese sulfate (MnSO 4 ), nickel sulfate (NiSO 4 ), copper sulfate (CuSO 4 ), cobalt sulfate (CoSO 4 ), cadmium sulfate (CdSO 4 ), magnesium sulfate (MgSO 4 ), iron sulfate II (FeSO 4 ), aluminum sulfate (Al 2 (SO 4 ) 3 ), calcium nitrate (Ca(NO 3 ) 2 ), zinc nitrate (Zn(NO 3 ) 2 ), iron nitrate III (Fe(NO 3 ) 3 ), aluminum phosphate (AlPO 4 ), iron phosphate III (FePO 4 ), chromium phosphate (CrPO 4 ), copper phosphate (Cu 3 (PO 4 ) 2 ), zinc phosphate (Zn 3 (PO 4 ) 4 ), magnesium phosphate (Mg 3 (PO 4 ) 2 ), aluminum chloride (AlCl 3 ), titanium chloride (TiCl 4 ), calcium chloride (CaCl 2 ), calcium fluoride (CaF 2 ), barium fluoride (BaF 2 ) and calcium carbonate (CaCO 3 ), or a mixture thereof.

[0047] Heretofore, the sulfur dioxide removal device 110 and its operating conditions have been described. Next, the wet scrubber 120 will be described. The wet scrubber 120 is a device that applies a wet scrubbing process to the ship exhaust gas treated by the sulfur dioxide removal device 110.

[0048] The sulfur dioxide (SO 2 ) contained in the ship exhaust gas is converted to ammonium bisulfate (NH 4 HSO 4 ) by the sulfur dioxide removal device 110, and the wet scrubber 120 plays a role of removing the ammonium bisulfate (NH 4 HSO 4 ) by dissolving the ammonium bisulfate (NH 4 HSO 4 ) contained in the ship exhaust gas in a feed water and discharging the same. As the feed water, water or seawater may be used, and the feed water in which ammonium bisulfate (NH 4 HSO 4 ) is dissolved, namely a dissolved water, may be moved to a dissolved water storage tank provided at one side of the ship or discharged to the sea.

[0049] In the wet scrubber 120 according to an embodiment of the present disclosure, a substance to be dissolved is ammonium bisulfate (NH 4 HSO 4 ). Whereas a substance to be dissolved in the wet scrubber 120 for desulfurization of the ship exhaust gas is generally sulfur dioxide (SO 2 ), the present disclosure is characterized in that a substance to be dissolved in the wet scrubber 120 according to an embodiment of the present disclosure is not sulfur dioxide (SO 2 ) but ammonium bisulfate (NH 4 HSO 4 ). As the substance to be dissolved in the wet scrubber 120 is ammonium bisulfate (NH 4 HSO 4 ), the amount of feed water required for the wet scrubber 120 may be significantly reduced. This is due to the difference in solubility between sulfur dioxide (SO 2 ) and ammonium bisulfate (NH 4 HSO 4 ). Based on water, the solubility of sulfur dioxide (SO 2 ) is about 10.5 g / 100 g, whereas the solubility of ammonium bisulfate (NH 4 HSO 4 ) is about 115 g / 100 g, which is about 10 times different. In addition, while sulfur dioxide (SO 2 ) requires water at a relatively low temperature to increase solubility, ammonium bisulfate (NH 4 HSO 4 ) has a property of increasing solubility in water as the temperature increases. Therefore, when performing the wet scrubbing process for ammonium bisulfate (NH 4 HSO 4 ), the wet scrubbing process may be performed using a feed water in an amount of 1 / 10 or less compared to the sulfur dioxide (SO 2 ) wet scrubbing process, so the amount of used feed water may be drastically reduced. Considering that ammonium bisulfate (NH 4 HSO 4 ) in a gas state needs to be dissolved, it is preferable that water or seawater put into the wet scrubber 120 is in an amount of 100-2,000 times, preferably 300-1,000 times, compared to the mass of ammonium bisulfate (NH 4 HSO 4 ).

[0050] Heretofore, the ship exhaust gas cleaning apparatus according to the first embodiment of the present disclosure has been described. As described above, the first embodiment of the present disclosure is a technology for purifying sulfur dioxide (SO 2 ) contained in the ship exhaust gas. The second embodiment of the present disclosure relates to a technology for purifying not only sulfur dioxide (SO 2 ) but also nitrogen oxide (NO 2 ).

[0051] The ship exhaust gas cleaning apparatus according to the second embodiment of the present disclosure further includes a SCR device 130 in addition to the components of the first embodiment in order to purify not only sulfur dioxide (SO 2 ) but also nitrogen oxide (NO 2 ), as shown in FIG. 2. In the second embodiment of the present disclosure, the configuration and functions of the sulfur dioxide removal device 110 and the wet scrubber 120 are the same as in the first embodiment.

[0052] The SCR device 130 is a device that reduces and removes nitrogen oxide (NO x ) contained in the ship exhaust gas for the ship exhaust gas discharged from the sulfur dioxide removal device 110. Specifically, if the reducing agent is added to the SCR device 130 in a state where the ship exhaust gas is supplied to the SCR device 130 equipped with the SCR catalyst, nitrogen oxide (NO x ) reacts with the reducing agent and is reduced to nitrogen (N 2 ). The SCR catalyst promotes the reaction of nitrogen oxide (NO x ) and the reducing agent.

[0053] As the reducing agent, ammonia (NH 3 ) may be used, and it is preferable that ammonia (NH 3 ) is put in an amount of 0.7-1.5 times compared to the molar equivalent of nitrogen oxide (NO x ) contained in the ship exhaust gas. As a more preferable condition, it is required to putting ammonia (NH 3 ) into the SCR device 130 in an amount of 0.9-1.2 times compared to the molar equivalent of nitrogen oxide (NO x ) contained in the ship exhaust gas. Here, if the amount of ammonia (NH 3 ) is less than 0.9 times compared to the molar equivalent of nitrogen oxide (NO x ), the nitrogen oxide (NO x ) removal rate may be drastically reduced, and if the amount of ammonia (NH 3 ) is greater than 1.2 times compared to the molar equivalent of nitrogen oxide (NO x ), ammonia (NH 3 ) is more likely to be lost.

[0054] The ammonia (NH 3 ) used as a reducing agent for the SCR reaction may be directly supplied to the SCR device 130 or may be supplied to the sulfur dioxide removal device 110. Referring to the first embodiment, it is specified that ammonia (NH 3 ) in an amount of 1-2 times compared to the molar equivalent of sulfur dioxide (SO 2 ) contained in the ship exhaust gas is put into the sulfur dioxide removal device 110. However, if the SCR device 130 is added as in the second embodiment, ammonia (NH 3 ) in an amount of 0.7-1.5 times compared to the molar equivalent of nitrogen oxide (NO x ) contained in the ship exhaust gas may be additionally put into the sulfur dioxide removal device 130. That is, if the sulfur dioxide removal device 110 and the SCR device 130 are provided as in the second embodiment, ammonia (NH 3 ) in an amount of 1-2 times compared to the molar equivalent of sulfur dioxide (SO 2 ) and ammonia (NH 3 ) in an amount of 0.7-1.5 times compared to the molar equivalent of nitrogen oxide (NO x ) contained in the ship exhaust gas may be put into the sulfur dioxide removal device 110. In another embodiment, it is also possible that ammonia (NH 3 ) in an amount of 1-2 times compared to the molar equivalent of sulfur dioxide (SO 2 ) is put into the sulfur dioxide removal device 110, and ammonia (NH 3 ) in an amount of 0.7-1.5 times compared to the molar equivalent of nitrogen oxide (NO x ) contained in the ship exhaust gas is put into the SCR device 130.

[0055] For the SCR reaction (selective catalytic reduction reaction) in the SCR device 130, it is necessary to adjust the temperature of the ship exhaust gas to 200-450°C. More preferably, it is necessary to adjust the temperature of the ship exhaust gas introduced into the SCR device 130 to 300-400°C. If the temperature of the ship exhaust gas is lower than 300°C, there is a possibility that the SCR reaction efficiency may decrease, and if the temperature of the ship exhaust gas exceeds 400°C, there is a disadvantage that the energy cost is increased.

[0056] Meanwhile, in the 'Background Art' section above, it is mentioned that if the ship exhaust gas is supplied to the SCR device in a state where both sulfur dioxide (SO 2 ) and nitrogen oxide (NO x ) are contained therein, ammonium bisulfate (NH 4 HSO 4 ) is produced, and the produced ammonium bisulfate (NH 4 HSO 4 ) is adsorbed to the pores of the SCR catalyst. The phenomenon that ammonium bisulfate (NH 4 HSO 4 ) is adsorbed to the pores of the SCR catalyst to block the pores is caused by the formation of ammonium bisulfate (NH 4 HSO 4 ) inside the SCR device.

[0057] As in an embodiment of the present disclosure, if sulfur dioxide (SO 2 ) is converted to ammonium bisulfate (NH 4 HSO 4 ) gas by the sulfur dioxide removal device 110, since the ammonium bisulfate (NH 4 HSO 4 ) gas is larger than the pore size of the SCR catalyst, the ammonium bisulfate (NH 4 HSO 4 ) gas passes through the SCR device 130 without being adsorbed to the pores of the SCR catalyst.

[0058] Therefore, the ship exhaust gas discharged from the SCR device 130 comes into a state where nitrogen oxide (NO x ) is removed and ammonium bisulfate (NH 4 HSO 4 ) gas is contained, and the ship exhaust gas discharged from the SCR device 130, namely the ship exhaust gas containing the ammonium bisulfate (NH 4 HSO 4 ) gas, is supplied to the wet scrubber 120.

[0059] The wet scrubber 120 serves to remove ammonium bisulfate (NH 4 HSO 4 ) by dissolving the ammonium bisulfate (NH 4 HSO 4 ) contained in the ship exhaust gas in the feed water and discharging the same as in the first embodiment described above. In addition, as in the first embodiment, in removing ammonium bisulfate (NH 4 HSO 4 ), the amount of feed water used may be reduced to 1 / 10 or less compared to the wet scrubber 120 for sulfur dioxide, and the amount of feed water put into the wet scrubber 120 is 100-2,000 times compared to the mass of ammonium bisulfate (NH 4 HSO 4 ).

[0060] Heretofore, the ship exhaust gas cleaning apparatus and its operation according to the first embodiment and the second embodiment of the present disclosure have been described. In the above description, the operations of the ship exhaust gas cleaning apparatus according to the first embodiment and the second embodiment of the present disclosure correspond to the ship exhaust gas cleaning method according to the first embodiment and the second embodiment of the present disclosure, respectively.

[0061] The ship exhaust gas cleaning method according to the first embodiment of the present disclosure is to sequentially perform a sulfur dioxide removing process (S301) and an ammonium bisulfate removing process (S302) as shown in FIG. 3. The sulfur dioxide removing process is carried out by the sulfur dioxide removal device 110, and the ammonium bisulfate removing process is carried out by the wet scrubber 120.

[0062] During the sulfur dioxide removing process, it is necessary to maximize the ammonium bisulfate (NH 4 HSO 4 ) synthesis efficiency. For this, a condition of controlling the temperature of the ship exhaust gas to 150-300°C, a condition of putting ammonia (NH 3 ) in an amount of 1-2 times compared to the molar equivalent of the sulfur dioxide (SO 2 ) contained in the ship exhaust gas, and a condition of charging an ammonium bisulfate synthesis catalyst to the sulfur dioxide removal device 110 may be applied selectively or in combination.

[0063] In addition, in removing ammonium bisulfate (NH 4 HSO 4 ) through the wet scrubber 120, the amount of feed water used may be reduced to 1 / 10 or less compared to the wet scrubber 120 for sulfur dioxide, and the amount of feed water put into the wet scrubber 120 is 100-2,000 times compared to the mass of ammonium bisulfate (NH 4 HSO 4 ).

[0064] The ship exhaust gas cleaning method according to the second embodiment of the present disclosure is to sequentially perform a sulfur dioxide removing process (S401), a nitrogen oxide removing process (S402), and an ammonium bisulfate removing process (S403) as shown in FIG. 4. The sulfur dioxide removing process is carried out by the sulfur dioxide removal device 110, the nitrogen oxide removing process is carried out by the SCR device 130, and the ammonium bisulfate removing process is carried out by the wet scrubber 120.

[0065] During the sulfur dioxide removing process, it is necessary to maximize the ammonium bisulfate (NH 4 HSO 4 ) synthesis efficiency. For this, a condition of controlling the temperature of the ship exhaust gas to 150-300°C, a condition of putting ammonia (NH 3 ) in an amount of 1-2 times compared to the molar equivalent of the sulfur dioxide (SO 2 ) contained in the ship exhaust gas, and a condition of putting an ammonium bisulfate synthesis catalyst may be applied selectively or in combination.

[0066] During the nitrogen oxide removing process using the SCR device 130, the nitrogen oxide (NO x ) contained in the ship exhaust gas may be effectively removed by applying a condition of controlling the temperature of the ship exhaust gas to 200-450°C and a condition of putting ammonia (NH 3 ) in an amount of 0.7-1.5 times compared to the molar equivalent of nitrogen oxide (NO x ) contained in the ship exhaust gas selectively or in combination. Here, the condition of putting ammonia (NH 3 ) in an amount of 0.7-1.5 times compared to the molar equivalent of nitrogen oxide (NO x ) contained in the ship exhaust gas may also be applied to the sulfur dioxide removing process. That is, during the sulfur dioxide removing process, ammonia (NH 3 ) in an amount of 1-2 times compared to the molar equivalent of sulfur dioxide (SO 2 ) and ammonia (NH 3 ) in an amount of 0.7-1.5 times compared to the molar equivalent of nitrogen oxide (NO x ) contained in the ship exhaust gas may be put into the sulfur dioxide removal device 110.

[0067] In addition, in removing ammonium bisulfate (NH 4 HSO 4 ) through the wet scrubber 120, the amount of feed water used may be reduced to 1 / 10 or less compared to the wet scrubber 120 for sulfur dioxide, and the amount of feed water put into the wet scrubber 120 is 100-2,000 times compared to the mass of ammonium bisulfate (NH 4 HSO 4 ).[Mode for Invention]

[0068] Heretofore, the ship exhaust gas cleaning apparatus and method according to the first embodiment and the second embodiment of the present disclosure have been described. Hereinafter, the embodiments of the present disclosure will be described in more detail with reference to experimental examples.<Experimental Example 1: SO 2 removal efficiency according to the change of temperature>

[0069] An experimental device as shown in FIG. 5 was prepared. Under the experimental device of FIG. 5, by adjusting a flow regulator 6, N 2 was supplied from a N 2 (100%) cylinder 1 at a rate of 97mL / min, a NO / SO 2 / N 2 mixed gas was supplied from a NO (8%) / SO 2 (5%) / N 2 (87%) mixed gas cylinder 2 at a rate of 1 mL / min rate, and an O 2 / N 2 mixed gas was supplied from an O 2 (3%) / N 2 (97%) mixed gas cylinder 3 at a rate of 1 mL / min rate, respectively, and passed through preheaters 7 to be heated to 250°C and then transferred to a first gas mixer 8. At the same time, a distilled water was supplied from a distilled water tank 4 to a flow controller at a rate of 0.3 g / hour, and was heated to 250°C by a preheater 7 and also put into the first gas mixer 8. The mixed gas composed of SO 2 , NO, O 2 and water vapor was transferred to a second gas mixer, and was mixed again with NH 3 at 250°C that was preheated and supplied from a NH 3 (NH 3 -8%, N 2 -92%) cylinder 5 through the flow regulator 6 at a rate of 1 mL / min. The final mixed gas passed through a reactor inlet sample port 9 and was adjusted to a final reaction temperature at a cooler 11 and a reactor furnace 13 (with an inner diameter of 5 cm, an outer diameter of 13 cm, and a length of 42 cm), and was discharged to the outside through a reactor 12 (with an inner diameter of 8 mm, an outer diameter of 10 mm, and a length of 48 cm), a reactor outlet sample port 10 and a gas bubbler 16. Reference numeral 14 in FIG. 5, not described, denotes 0.5 g of alumina in which 0.5 wt% of platinum is supported as an ammonium bisulfate synthesis catalyst, and reference numeral 15 denotes a catalyst support asbestos.

[0070] The concentrations of SO 2 and NO x in the mixed and reaction gases were collected and measured at both the sample ports installed at the inlet and outlet of the reactor, and the results are summarized in Table 1 below. In Table 1 below, the concentration of each gas in the mixed gas except for water vapor is SO 2 500 ppm, NO 800 ppm, NH 3 800 ppm and O 2 3%, and the amount of water vapor in the total gas is 6%. This composition is similar to the composition of an engine exhaust gas using a fuel oil containing 3.5% sulfur. [Table 1]<Change of SO 2 and NO x concentrations according to reaction temperature (unit: ppm)>concentration measuring point270°C230°C190°C150°CSO 2 NO x SO 2 NO x SO 2 NO x SO 2 NO x mixed gas500800500800500800500800reactor inlet503811501808505798502795reactor outlet32145312661562683213732

[0071] Referring to Table 1, it may be found that the SO 2 removal rate decreases as the temperature increases at 230°C or higher and as the temperature decreases at 190°C or lower. This is because as the temperature increases above 230°C, the ammonium bisulfate (NH 4 HSO 4 ) production reaction rate decreases, and the reaction between NO x and NH 3 is rather activated and because at the temperature of 190°C or lower, as the temperature decreases, the rate of all reactions also decreases significantly.<Experimental Example 2: SO 2 removal rate change according to NH 3 input concentration change>

[0072] The experiment was carried out in the same manner as in Experimental Example 1, the concentration of NH 3 in the raw material mixed gas was changed from 500 ppm to 1,100 ppm, and the reaction temperature was fixed at 220°C during the experiment. The results are summarized in Table 2. [Table 2]<Change of SO 2 removal rate according to NH 3 input concentration change>gas typeNH 3 concentration (ppm) in raw material5007009001100SO 2 29515750NO x 706685576471NH 3 202242185273

[0073] Referring to Table 2, it may be found that at the reaction temperature of 220°C, if the concentration of NH 3 is maintained at 900 ppm (1.8 times of the SO 2 concentration) or higher, SO 2 is converted to 100% ammonium bisulfate (NH 4 HSO 4 ) gas and removed.<Experimental Example 3: Change of SO 2 removal rate when an ammonium bisulfate synthesis catalyst is used>

[0074] The experiment was carried out in a state where 0.5 g of alumina in which 0.5 wt % of platinum was supported was charged into the reactor, and was compared with the case without catalyst charging. The concentration of NH 3 was changed from 600 ppm to 900 ppm, and other experimental conditions were applied in the same way as in Experimental Example 2. The experimental results are shown in Table 3 below. [Table 3]<Change of SO 2 concentration when using ammonium bisulfate synthesis catalyst>reaction method and concentration (ppm)input NH 3 concentration (ppm)600700800900non-catalyst reaction SO 2 concentration215157855catalyst reaction SO 2 concentration22000

[0075] Referring to Table 3, it may be found that the SO 2 removal rate is improved when the experiment is performed in a state where the catalyst is charged into the reactor.<Experimental Example 4: Ammonium bisulfate removal rate according to water usage>

[0076] One aspect of the present disclosure is directed to inputting and reacting NH 3 to be converted into ammonium bisulfate (NH 4 HSO 4 ) in order to remove SO 2 from the exhaust gas, and then dissolving it in water or seawater to be finally discharged and discharged in seawater. Therefore, it is very important to determine the amount of water for complete dissolution of ammonium bisulfate (NH 4 HSO 4 ).

[0077] In Experimental Example 4, 0.5 g of alumina in which 0.5 wt% of platinum was supported was charged into the reactor, and reaction temperature was fixed at 220°C, and the experiment was conducted in the same way as in Experimental Example 1. After the experiment, the exhaust gas was allowed to pass through the water of the bubbler 16 filled with water, just before being discharged. The amount of water contained in the bubbler was adjusted, and the amount of ammonium bisulfate (NH 4 HSO 4 ) dissolved in water was measured after the exhaust gas was passed for 10 hours. The results are summarized in Table 4. [Table 4]<Ammonium bisulfate dissolution rate according to water usage>amount of water in the bubbler (g)153050100150weight of NH 4 HSO 4 after drying (g)0.1010.1460.1540.1540.154NH 4 HSO 4 dissolution rate (%)65.694.8100100100

[0078] Referring to Table 4, it may be found that the entire ammonium bisulfate in the exhaust gas is dissolved in water and removed when the amount of water inside the bubbler is about 300 times or greater than the amount of ammonium bisulfate (NH 4 HSO 4 ) in the exhaust gas.<Experimental Example 5: NO x removal rate by SCR device>

[0079] A NO x SCR commercial catalyst (V 2 O 5 / TiO 2 / WO 3 ) was charged into the reactor and the experiment was conducted in the same manner as in Experimental Example 1. For reference, the temperatures of the preheaters were all fixed at 210°C, and the temperature of the reactor in which the catalyst was charged was increased to 350°C, during the experiment. The concentrations of SO 2 , NO x and NH 3 were measured at the reactor outlet while changing the concentration of NH 3 in the raw material mixed gas from 1,200 ppm to 2,000 ppm, and the results are summarized in Table 5. [Table 5]< NO x removal effect according to NH 3 input amount>exhaust gasNH 3 input amount (ppm) and NH 3 / NO x ratio1200 ppm1400 ppm1600 ppm1800 ppm2000 ppm0.8751.1251.3751.6251.875NO x 212861453SO 2 00000NH 3 88151287492695

[0080] Referring to Table 5, when the SO 2 concentration is 500 ppm and the NO x concentration is 800 ppm in the raw material mixed gas, if the total amount of NH 3 input is 1,400 ppm or more, after passing the NO x SCR commercial catalyst, the SO 2 concentration becomes 0 ppm and the NO x concentration becomes 50 ppm, so it may be found that SO 2 removal rate becomes 100% and the NO x removal rate becomes 95% or more.[Reference Signs]

[0081] 110:sulfur dioxide removal device120:wet scrubber130:SCR device140:ammonia supply device

Claims

1. A ship exhaust gas cleaning apparatus, comprising: a sulfur dioxide removal device 110 configured to provide a space for inducing the reaction among ammonia (NH3) and sulfur dioxide (SO2) in the presence of steam (H2O) and oxygen (O2) and convert sulfur dioxide (SO2) contained in a ship exhaust gas into ammonium bisulfate (NH4HSO4) by the reaction of sulfur dioxide (SO2) and ammonia (NH3); a wet scrubber 120 configured to remove the ammonium bisulfate (NH4HSO4) generated by the sulfur dioxide removal device 110 by dissolving the ammonium bisulfate (NH4HSO4) in a feed water, characterized in that it further comprises an SCR device 130 configured to reduce nitrogen oxide (NOx) contained in the ship exhaust gas to nitrogen (N2) for the ship exhaust gas discharged from the sulfur dioxide removal device 110.

2. The ship exhaust gas cleaning apparatus according to claim 1, wherein in the sulfur dioxide removal device 110, an ammonium bisulfate (NH4HSO4) production reaction is activated, and a nitrogen reduction reaction by the reaction of nitrogen oxide (NOx) and ammonia (NH3) is suppressed.

3. The ship exhaust gas cleaning apparatus according to claim 1, wherein the temperature inside the sulfur dioxide removal device 110 or the temperature of the ship exhaust gas introduced into the sulfur dioxide removal device 110 is 150-300°C.

4. The ship exhaust gas cleaning apparatus according to claim 1, wherein ammonia (NH3) is put into the sulfur dioxide removal device 110 in an amount of 1-2 times compared to the molar equivalent of the sulfur dioxide (SO2) contained in the ship exhaust gas.

5. The ship exhaust gas cleaning apparatus according to claim 1, wherein an ammonium bisulfate synthesis catalyst is charged into the sulfur dioxide removal device 110, and the ammonium bisulfate synthesis catalyst serves to promote the production of ammonium bisulfate (NH4HSO4).

6. The ship exhaust gas cleaning apparatus according to claim 5, wherein the ammonium bisulfate synthesis catalyst is any one of an oxidation catalyst, a mixture of oxidation catalyst and solid acid, and a solid acid support of oxidation catalyst, or a mixture thereof.

7. The ship exhaust gas cleaning apparatus according to claim 6, wherein the oxidation catalyst is any one of MnO2, V2O5, Ni, Pd, and Pt, or a mixture thereof, and wherein the solid acid is any one selected from the group consisting of basalt, granite, limestone, sandstone, shale, metamorphic rock, kaolinite, attapulgite, bentonite, montmorillonite, zeolite, zinc oxide (ZnO), aluminum oxide (Al2O3), titanium oxide (TiO2), cesium oxide (CeO2), vanadium oxide (V2O5), silicon oxide (SiO2), chromium oxide (Cr2O3), calcium sulfate (CaSO4), manganese sulfate (MnSO4), nickel sulfate (NiSO4), copper sulfate (CuSO4), cobalt sulfate (CoSO4), cadmium sulfate (CdSO4), magnesium sulfate (MgSO4), iron sulfate II (FeSO4), aluminum sulfate (Al2(SO4)3), calcium nitrate (Ca(NO3)2), zinc nitrate (Zn(NO3)2), iron nitrate III (Fe(NO3)3), aluminum phosphate (AlPO4), iron phosphate III (FePO4), chromium phosphate (CrPO4), copper phosphate (Cu3(PO4)2), zinc phosphate (Zn3(PO4)4), magnesium phosphate (Mg3(PO4)2), aluminum chloride (AlCl3), titanium chloride (TiCl4), calcium chloride (CaCl2), calcium fluoride (CaF2), barium fluoride (BaF2) and calcium carbonate (CaCO3), or a mixture thereof.

8. The ship exhaust gas cleaning apparatus according to claim 1, wherein a substance to be dissolved by the wet scrubber 120 is ammonium bisulfate (NH4HSO4), and the feed water put into the wet scrubber 120 is in an amount of 100-2,000 times compared to the mass of ammonium bisulfate (NH4HSO4).

9. The ship exhaust gas cleaning apparatus according to claim 1, wherein ammonia (NH3) is put into the SCR device 130 as a reducing agent, and the ammonia (NH3) is put in an amount of 0.7-1.5 times compared to the molar equivalent of nitrogen oxide (NOx) contained in the ship exhaust gas.

10. The ship exhaust gas cleaning apparatus according to claim 1, wherein ammonia (NH3) in an amount of 1-2 times compared to the molar equivalent of sulfur dioxide (SO2) contained in the ship exhaust gas and ammonia (NH3) in an amount of 0.7-1.5 times compared to the molar equivalent of nitrogen oxide (NOx) contained in the ship exhaust gas are put into the sulfur dioxide removal device 110.

11. A ship exhaust gas cleaning method, comprising: a sulfur dioxide removing step of converting sulfur dioxide (SO2) contained in a ship exhaust gas into ammonium bisulfate (NH4HSO4) by the reaction among sulfur dioxide (SO2) and ammonia (NH3) in the presence of steam (H2O) and oxygen (O2); and an ammonium bisulfate removing step of removing the ammonium bisulfate (NH4HSO4) generated by the reaction of sulfur dioxide (SO2) and ammonia (NH3) by dissolving the ammonium bisulfate (NH4HSO4) in a feed water, wherein a nitrogen oxide removing step is performed between the sulfur dioxide removing step and the ammonium bisulfate removing step, and wherein the nitrogen oxide removing step further includes a nitrogen oxide removing step of removing the nitrogen oxide (NOx) contained in the ship exhaust gas by reducing the nitrogen oxide (NOx) to nitrogen (N2).

12. The ship exhaust gas cleaning method according to claim 11, wherein in the sulfur dioxide removing step, an ammonium bisulfate (NH4HSO4) production reaction is activated, and a nitrogen reduction reaction by the reaction of nitrogen oxide (NOx) and ammonia (NH3) is suppressed.

13. The ship exhaust gas cleaning method according to claim 11, wherein in the sulfur dioxide removing step, a condition of controlling the temperature of the ship exhaust gas to 150-300°C, a condition of putting ammonia (NH3) in an amount of 1-2 times compared to the molar equivalent of the sulfur dioxide (SO2) contained in the ship exhaust gas, and a condition of charging an ammonium bisulfate synthesis catalyst are applied selectively or in combination to maximize ammonium bisulfate (NH4HSO4) synthesis efficiency.

14. The ship exhaust gas cleaning method according to claim 11, wherein in the ammonium bisulfate removing step, the feed water is put in an amount of 100-2,000 times compared to the mass of ammonium bisulfate (NH4HSO4) to dissolve the ammonium bisulfate (NH4HSO4).

15. The ship exhaust gas cleaning method according to claim 11, wherein the nitrogen oxide removing step is carried out by a SCR device 130, and wherein a condition of controlling the temperature of the ship exhaust gas or the temperature of the inside of the SCR device 130 to 200-450°C and a condition of putting ammonia (NH3) in an amount of 0.7-1.5 times compared to the molar equivalent of nitrogen oxide (NOx) contained in the ship exhaust gas are applied selectively or in combination.

16. The ship exhaust gas cleaning method according to claim 11, wherein in the sulfur dioxide removing step, ammonia (NH3) in an amount of 1-2 times compared to the molar equivalent of sulfur dioxide (SO2) contained in the ship exhaust gas and ammonia (NH3) in an amount of 0.7-1.5 times compared to the molar equivalent of nitrogen oxide (NOx) contained in the ship exhaust gas are put into a sulfur dioxide removal device 110.