The Chemical Behaviors of Nitrogen Dioxide Absorption in Sulﬁte Solution

: The simultaneous removal of nitrogen oxides (NO x ) and sulfur dioxide (SO 2 ) by absorption is considered to be one of the most promising technologies for ﬂue gas treatment, and sulﬁte is the main component of the absorption solution. To understand the chemical behaviors of the NO 2 absorption in sulﬁte solution, the absorption time dependences of concentrations of nitrogen and sulfur compositions in both gas phase and liquid phases were investigated by ﬂue gas analyzer, Ion chromatography (IC), Gas chromatography (GC), and Fourier transform infrared spectrometry (FTIR) methods using a bubbling reactor. The mass equilibrium of the N and S compositions were also studied. The results indicate that sulﬁte concentration plays a vital role in NO 2 absorption. The main absorption products are NO 3 − and NO 2 − , and NO 2 − can be converted into NO 3 − in the presence of oxygen. Besides, about 4% to 9% by-products of S compositions are formed, and 4% to 11% by-products of N compositions such as NO, N 2 , N 2 O 5 , N 2 O, and HNO 3 in the gas phase were detected in the emissions from the bubbling reactor. On the basis of N and S compositions, a possible pathway of NO 2 absorption in sulﬁte solution was proposed.


Introduction
As major poisonous air pollutants, nitrogen oxides (NO x ) and sulfur dioxide (SO 2 ) from the fossil fuel combustion are key contributors to acid deposition, photochemical smog and hazy weather, and bring out a great harm to the environment and human health [1]. NO x and SO 2 removal technologies, therefore, have been the research focus of air pollution control in recent decades. It is well known that the commonly practiced technologies of removing NO x , such as low NO x burners, selective non-catalytic reduction (SNCR), and selective catalytic reduction (SCR), have been widely developed and used. SO 2 emissions have also been effectively controlled by wet flue gas desulfurization (WFGD), circulated fluid bed flue gas desulfurization (CFB-FGD), and so on. Although the combination of the commonly practiced de-NO x and de-SO 2 processes can meet the limitations of SO 2 and NO x emissions stipulated by environmental legislation, traditional NO x and SO 2 removal technologies in a stepwise manner have some drawbacks, such as the requirement for large construction site, high capital investment, and high operation costs. Thus, the emerging technologies for the simultaneous removal of NO x and SO 2 are to be extensively developed [2,3].
The integrated oxidation-absorption process using chemical reagents for simultaneous removal of NO x and SO 2 is considered as a cost-effective and environmental friendly technology for flue gas treatment and has gained increasing interest [4]. However, nitric oxide (NO), accounting for more than 95% of NO x in typical flue gas, is almost insoluble and low active. Thus, NO has to be oxidized into soluble nitrogen dioxide (NO 2 ) at the first step. Recently, a few studies related to the NO oxidation have been reported [5][6][7][8][9][10][11][12], including gas phase catalytic oxidation, ozone oxidation, corona discharge oxidation, and liquid oxidation. After oxidation, the soluble NO 2 can be further removed with SO 2 in the subsequent absorption process [13]. Till now, the NO 2 absorption process using chemical reagents have widely been studied to develop the industrial scale process. Many absorbents such as Ca(OH) 2 , CaCO 3 , Na 2 SO 3 , (NH 4 ) 2 SO 3 , and CaSO 3 have been tested and the reaction mechanism have been probed [1,[14][15][16][17][18][19][20][21][22]. Among them, sulfite solutions have been considered as a cost-effective absorbent because of their high removal efficiency, their desulphurization byproduct characteristics, and their capacity of simultaneous removal of mercury and chlorine [23][24][25]. However, NO 2 and SO 2 absorption into sulfite absorbents involves complex chemical behaviors. Consequently, and the chemical behavior of absorption has not been widely generalized up to now. Furthermore, there are few reports on the analysis of the gas products from the NO 2 and SO 2 absorption in absorbents. Thus it is absolutely necessary to further understand the chemical behaviors of the absorption process to promote NO 2 and SO 2 removal by adsorption.
In this study, Na 2 SO 3 solution was selected as sulfite absorbent. The time-dependences of concentrations of main nitrogen and sulfur (N and S) compositions in both gas phase and liquid phase were investigated by flue gas analyzer, Ion chromatography (IC), Gas chromatography (GC) and Fourier transform infrared spectrometry (FTIR). The mass equilibrium of the N and S compositions of NO 2 absorption into absorbent through mass balance calculation were also carried out. Moreover, a possible reaction pathway of NO 2 removal was proposed.

Experimental Setup
A scheme of the experimental setup is shown in Figure 1. It consists of a reaction gas feeding unit, an absorption reactor, and a set of gas analytical instruments. A stirred bubbling device with an effective volume of 5 L (150 mm inner diameter and 300 mm in height) was used as the absorption reactor. A mechanical agitator provided continuous stirring at a speed of 105 rpm. The temperature of the reactor was maintained with the help of a thermostatic water bath. A condenser was used to cool and dehydrate the outlet flue gas and reduce the influence of H 2 O on products analysis. Appl. Sci. 2017, 7, 377 2 of 10 oxidation have been reported [5][6][7][8][9][10][11][12], including gas phase catalytic oxidation, ozone oxidation, corona discharge oxidation, and liquid oxidation. After oxidation, the soluble NO2 can be further removed with SO2 in the subsequent absorption process [13]. Till now, the NO2 absorption process using chemical reagents have widely been studied to develop the industrial scale process. Many absorbents such as Ca(OH)2, CaCO3, Na2SO3, (NH4)2SO3, and CaSO3 have been tested and the reaction mechanism have been probed [1,[14][15][16][17][18][19][20][21][22]. Among them, sulfite solutions have been considered as a cost-effective absorbent because of their high removal efficiency, their desulphurization byproduct characteristics, and their capacity of simultaneous removal of mercury and chlorine [23][24][25]. However, NO2 and SO2 absorption into sulfite absorbents involves complex chemical behaviors. Consequently, and the chemical behavior of absorption has not been widely generalized up to now. Furthermore, there are few reports on the analysis of the gas products from the NO2 and SO2 absorption in absorbents. Thus it is absolutely necessary to further understand the chemical behaviors of the absorption process to promote NO2 and SO2 removal by adsorption.
In this study, Na2SO3 solution was selected as sulfite absorbent. The time-dependences of concentrations of main nitrogen and sulfur (N and S) compositions in both gas phase and liquid phase were investigated by flue gas analyzer, Ion chromatography (IC), Gas chromatography (GC) and Fourier transform infrared spectrometry (FTIR). The mass equilibrium of the N and S compositions of NO2 absorption into absorbent through mass balance calculation were also carried out. Moreover, a possible reaction pathway of NO2 removal was proposed.

Experimental Setup
A scheme of the experimental setup is shown in Figure 1. It consists of a reaction gas feeding unit, an absorption reactor, and a set of gas analytical instruments. A stirred bubbling device with an effective volume of 5 L (150 mm inner diameter and 300 mm in height) was used as the absorption reactor. A mechanical agitator provided continuous stirring at a speed of 105 rpm. The temperature of the reactor was maintained with the help of a thermostatic water bath. A condenser was used to cool and dehydrate the outlet flue gas and reduce the influence of H2O on products analysis.

Experimental Methods
All experiments were performed at atmospheric pressure and the temperature of 325 ± 5 K. The simulated flue gas, which was supposed to be outlet flue gas after NO oxidation, was simulated by mixing proper amount of NO2, O2, SO2, and Ar from compressed gas cylinders. The basic simulated flue gas compositions were 260 ppm NO2, 300 ppm SO2, 6% O2 and Ar. The gas flow rate

Experimental Methods
All experiments were performed at atmospheric pressure and the temperature of 325 ± 5 K. The simulated flue gas, which was supposed to be outlet flue gas after NO oxidation, was simulated by mixing proper amount of NO 2 , O 2 , SO 2 , and Ar from compressed gas cylinders. The basic simulated flue gas compositions were 260 ppm NO 2 , 300 ppm SO 2 , 6% O 2 and Ar. The gas flow rate was adjusted by mass flow controller (MFC), and the four gas streams with a total flow rate of 4 L min −1 were completely mixed in a mixing chamber before being fed into the absorption reactor. The volume of Na 2 SO 3 solution (0.02 M) stored in the stirred bubbling device was 2 L. pH of absorption solution was maintained at 6-7 by adding 1 M HCl or 1 M NaOH solution. The liquid samples at different times for IC analysis were attained from the sampling port. Qualitative analysis of liquid phase (NH 4 + , NO 3 − , NO 2 − , and SO 4 2− ) was carried out by ion chromatography (IC, Metrohm 792, Herisau, Switzerland). The concentrations of NO 2 , NO, SO 2 , and O 2 in the tail gas were monitored by a flue gas analyzer (Testo350-pro, Schwarzwald, Germany). Sulfite ions (SO 3 2− ) in the liquid phase were measured by an iodometric titration method. N 2 formed in the absorption reaction was monitored using gas chromatography (GC, Agilent 7890, Santa Clara, CA, USA) with a Thermal conductivity detector (TCD, Agilent, Santa Clara, CA, USA), and 5 A molecular sieve chromatographic column (Agilent, Santa Clara, CA, USA), and the temperature of column oven and detector were 40 and 180 • C, respectively. Other N compositions of outlet gas were analyzed by Fourier transform infrared spectrometry (FTIR, Nicolet 6700, Waltham, MA, USA) equipped with a high-sensitivity mercury cadmium telluride detectors (MCT, Nicolet, Waltham, MA, USA) cooled by liquid nitrogen. The outlet gas stream passed through a 2.5 L gas cell, which had optical path length of 10 m, accordingly averaged spectra after 32 scans at 4 cm −1 resolution were collected in the 3000-650 cm −1 ranges. In the current system, inlet NO 2 , SO 2 concentrations, and initial sulfite concentration were previously set, without other sources of nitrogen and sulfur compositions. The molar quantity of N and S compositions in a closed loop system from absorption reaction could be calculated by graphical integration during a fixed period, and the theoretical values in this loop-locked system were expressed as follows: where TN t and TS t are the total molar quantity of N and S compositions absorbed into reaction system during t absorption time (mol). C 0 and C t are inlet and outlet concentrations of NO 2 or SO 2 (ppm), respectively. Q is the total flow rate of the flue gas (L min −1 ). V m is the molar volume of NO 2 or SO 2 in 325 K (L mol −1 ), and t is the absorption time (min). Meanwhile, 0.04 in Equation (2) is the original molar quantity of SO 3 2− in stirred bubbling device (mol).

Quantitative Analysis of N and S Compositions in Gaseous and Liquid Phases
In order to analyze the distribution of N and S compositions in closed loop reaction system, the dependence of outlet NO 2 and SO 2 concentrations with the absorption time were investigated, and the results are shown in Figure 2. Due to the high sulfite concentration, both NO 2 and SO 2 were not detected in the outlet flue gas during the initial absorption period of about 200 min, which suggests that nearly all of NO 2 and SO 2 are absorbed. The outlet NO 2 and SO 2 concentrations rapidly increase from 210 min to 230 min and are almost unchanged after 230 min. It is clear that the absorption equilibrium is established after a certain absorption time. These results also show that that the reaction between NO 2 and sulfite may be mainly controlled by diffusion in the initial reaction period, which is due to the sulfite concentration makes reaction rate is much faster than the diffusion rate [22,26]. Figure 2 also shows that NO, as one of the absorption products, has similar time dependence to NO 2 and SO 2 concentrations. It was found that hardly any NO was detected during initial absorption period of about 200 min. NO concentration gradually increases from about 210 min to 230 min and almost keeps unchanged after 230 min. This can be explained as follows: in the initial absorption period, NO 2 can oxidize sulfite solutions directly (R1). However, with the depletion of sulfite solutions, Appl. Sci. 2017, 7, 377 4 of 10 NO 2 absorption in H 2 O (R2) occurs, and HNO 2 may be formed. Generally, HNO 2 is unstable in its liquid phase and can decompose into NO as R3 [22,27].
absorption period, NO2 can oxidize sulfite solutions directly (R1). However, with the depletion of sulfite solutions, NO2 absorption in H2O (R2) occurs, and HNO2 may be formed. Generally, HNO2 is unstable in its liquid phase and can decompose into NO as R3 [22,27]. NO3 − , NO2 − , SO3 2− , and SO4 2− , which are main reactants or products of liquid phase, are synchronously analyzed by IC at the absorption times of 30 min, 60 min, 210 min, 220 min, 230 min and 300 min to better understand the chemical behaviors of NO2 and SO2 absorption in sulfite solution. As shown in Figure 3, NO3 − , NO2 − , and SO4 2− concentrations in absorption solution increase as the absorption proceeds. Compared with NO2 − , more NO3 − was formed at the same absorption time, which can be ascribed to the oxidation of NO2 − and the decomposition of unstable HNO2 [22,28]. After the absorption time of about 300 min, NO2 − concentration is almost unchanged although NO3 − ions still increase, which is attributed to the fact that nitrite ions are further oxidized into nitrate ions. Figure 3 also shows that the sulfite concentration gradually decreases as the absorption proceeds and are almost unavailable after 220 min, which results in a sharp decrease of NO2 absorption performance. It indicates that sulfite concentration is closely related with the performance of the removal of NO2, which agrees well with the findings shown in Figure 2. The sulfite is consumed because of its reaction with NO2 or O2. For NO2 absorption in sulfite solution, the sulfate is formed through the reaction between NO2 or O2 and sulfite (R1) [29].  increase as the absorption proceeds. Compared with NO 2 − , more NO 3 − was formed at the same absorption time, which can be ascribed to the oxidation of NO 2 − and the decomposition of unstable HNO 2 [22,28]. After the absorption time of about 300 min, NO 2 − concentration is almost unchanged although NO 3 − ions still increase, which is attributed to the fact that nitrite ions are further oxidized into nitrate ions. Figure 3 also shows that the sulfite concentration gradually decreases as the absorption proceeds and are almost unavailable after 220 min, which results in a sharp decrease of NO 2 absorption performance. It indicates that sulfite concentration is closely related with the performance of the removal of NO 2 , which agrees well with the findings shown in Figure 2. The sulfite is consumed because of its reaction with NO 2 or O 2 . For NO 2 absorption in sulfite solution, the sulfate is formed through the reaction between NO 2 or O 2 and sulfite (R1) [29].

Equilibrium Analysis of Nand S Compositions
Figures 4 and 5 present the N and S equilibrium of NO2 and SO2 absorption in sulfite solution, respectively. It can be seen from Figure 4 that the sum of NO3 − and NO2 − ions in the absorption solution is lower than the calculated TNt for almost all the reaction times, which suggests that other N compositions of about 4% to 11%, are formed in the absorption process. Some researchers have confirmed the existence of other N compositions. Siddiqi et al. [30] studied the effect of nitrogen dioxide on the absorption of sulfur dioxide in wet flue gas cleaning processes and pointed out that nitrogen-sulfur compounds could be formed and further decomposed into gaseous products in the co-existence condition of NO2 and SO2 absorption process. Yan, et al. [31] also reported that the reaction of sulfite with NO could produce N2. However, few quantitative researches about gas phase products have been previously reported. In addition, Figure 4 also shows that the amount of other N compositions is almost kept constant before 210 min, and then decreases as the absorption proceeds, which means that sulfite plays a dominant role in the formation of other N compositions. These results are consistent with the dependence of NO2 removal ( Figure 2) and SO3 2− amount ( Figure 3) with the reaction time.  Similarly, the calculated TSt is also more than the sum of detected SO3 2− and SO4 2− , as shown in Figure 5. Other S compositions besides SO3 2− and SO4 2− account for about 4% to 9% in the reaction system. Besides the above-mentioned nitrogen-sulfur compounds, Chen et al. [32] and Zhuang et al. [32,33] thought that the sulfite radicals could be formed by the reaction between NO2 and sulfite, the sulfite radicals could undergo either recombination or reaction with oxygen. By comparing Figure 4 with Figure 5, it can be seen that the amount of other S compositions is much lower than that of other

Equilibrium Analysis of Nand S Compositions
Figures 4 and 5 present the N and S equilibrium of NO2 and SO2 absorption in sulfite solution, respectively. It can be seen from Figure 4 that the sum of NO3 − and NO2 − ions in the absorption solution is lower than the calculated TNt for almost all the reaction times, which suggests that other N compositions of about 4% to 11%, are formed in the absorption process. Some researchers have confirmed the existence of other N compositions. Siddiqi et al. [30] studied the effect of nitrogen dioxide on the absorption of sulfur dioxide in wet flue gas cleaning processes and pointed out that nitrogen-sulfur compounds could be formed and further decomposed into gaseous products in the co-existence condition of NO2 and SO2 absorption process. Yan, et al. [31] also reported that the reaction of sulfite with NO could produce N2. However, few quantitative researches about gas phase products have been previously reported. In addition, Figure 4 also shows that the amount of other N compositions is almost kept constant before 210 min, and then decreases as the absorption proceeds, which means that sulfite plays a dominant role in the formation of other N compositions. These results are consistent with the dependence of NO2 removal ( Figure 2) and SO3 2− amount ( Figure 3) with the reaction time.  Similarly, the calculated TSt is also more than the sum of detected SO3 2− and SO4 2− , as shown in Figure 5. Other S compositions besides SO3 2− and SO4 2− account for about 4% to 9% in the reaction system. Besides the above-mentioned nitrogen-sulfur compounds, Chen et al. [32] and Zhuang et al. [32,33] thought that the sulfite radicals could be formed by the reaction between NO2 and sulfite, the sulfite radicals could undergo either recombination or reaction with oxygen. By comparing Figure 4 with Figure 5, it can be seen that the amount of other S compositions is much lower than that of other Similarly, the calculated TS t is also more than the sum of detected SO 3 2− and SO 4 2− , as shown in Figure 5. Other S compositions besides SO 3 2− and SO 4 2− account for about 4% to 9% in the reaction system. Besides the above-mentioned nitrogen-sulfur compounds, Chen et al. [32] and Zhuang et al. [32,33] thought that the sulfite radicals could be formed by the reaction between NO 2 and Appl. Sci. 2017, 7, 377 6 of 10 sulfite, the sulfite radicals could undergo either recombination or reaction with oxygen. By comparing Figure 4 with Figure 5, it can be seen that the amount of other S compositions is much lower than that of other N compositions, which suggests that not all other S compositions participate in the formation of other N compositions.

Qualitative Analysis of N Compositions
Besides NO2, NO, NO2 − , and NO3 − , the nitrous products such as N2O, N2O3, N2O5, and N2, can form during the NO2 absorption into sulfite solution [10,30]. IC, GC, and FTIR were used to detect these products in this study. Figures 6 and 7 present the GC and FTIR spectra of the gaseous products, respectively.
It can be seen from Figure 6 that the gaseous N2 is formed mainly in the initial absorption period, declines as the absorption proceeds, and finally disappears after 230 min. N2 formation can be explained by the following reactions [31], The sulfite plays an important role in N2 formation according to Reactions (4) and (5). Thus N2 concentration decrease is due to the fact that sulfite concentration in reaction system gradually declines and finally disappears. Although N2 concentration cannot contribute to the equilibrium analysis of nitrogen, the observed declining tendency of N2 peaks with the absorption time indicates that N2 is one of other nitrogen compositions. Based on the FTIR analysis, the effect of absorption time on the gaseous N-product distribution can be seen, as shown in Figure 7. Six distinct absorbance peaks are observed at 2930 cm −1 , 2287 cm −1 , 1720 cm −1 , 1600 cm −1 , 1326 cm −1 , and 887 cm −1 , and the bands are assigned to NO2, N2O, N2O5, NO2,

Qualitative Analysis of N Compositions
Besides NO 2 , NO, NO 2 − , and NO 3 − , the nitrous products such as N 2 O, N 2 O 3 , N 2 O 5 , and N 2 , can form during the NO 2 absorption into sulfite solution [10,30]. IC, GC, and FTIR were used to detect these products in this study. Figures 6 and 7 present the GC and FTIR spectra of the gaseous products, respectively. It can be seen from Figure 6 that the gaseous N 2 is formed mainly in the initial absorption period, declines as the absorption proceeds, and finally disappears after 230 min. N 2 formation can be explained by the following reactions [31], The sulfite plays an important role in N 2 formation according to Reactions (4) and (5). Thus N 2 concentration decrease is due to the fact that sulfite concentration in reaction system gradually declines and finally disappears. Although N 2 concentration cannot contribute to the equilibrium analysis of nitrogen, the observed declining tendency of N 2 peaks with the absorption time indicates that N 2 is one of other nitrogen compositions.

Qualitative Analysis of N Compositions
Besides NO2, NO, NO2 − , and NO3 − , the nitrous products such as N2O, N2O3, N2O5, and N2, can form during the NO2 absorption into sulfite solution [10,30]. IC, GC, and FTIR were used to detect these products in this study. Figures 6 and 7 present the GC and FTIR spectra of the gaseous products, respectively.
It can be seen from Figure 6 that the gaseous N2 is formed mainly in the initial absorption period, declines as the absorption proceeds, and finally disappears after 230 min. N2 formation can be explained by the following reactions [31], The sulfite plays an important role in N2 formation according to Reactions (4) and (5). Thus N2 concentration decrease is due to the fact that sulfite concentration in reaction system gradually declines and finally disappears. Although N2 concentration cannot contribute to the equilibrium analysis of nitrogen, the observed declining tendency of N2 peaks with the absorption time indicates that N2 is one of other nitrogen compositions. Based on the FTIR analysis, the effect of absorption time on the gaseous N-product distribution can be seen, as shown in Figure 7. Six distinct absorbance peaks are observed at 2930 cm −1 , 2287 cm −1 , 1720 cm −1 , 1600 cm −1 , 1326 cm −1 , and 887 cm −1 , and the bands are assigned to NO2, N2O, N2O5, NO2, Based on the FTIR analysis, the effect of absorption time on the gaseous N-product distribution can be seen, as shown in Figure 7. Six distinct absorbance peaks are observed at 2930 cm −1 , 2287 cm −1 , 1720 cm −1 , 1600 cm −1 , 1326 cm −1 , and 887 cm −1 , and the bands are assigned to NO 2 , N 2 O, N 2 O 5 , NO 2 , HNO 3 , and HNO 3 , respectively [34]. In the initial absorption period, the intensities of bands at 2287 cm −1 , 1720 cm −1 , 1326 cm −1 , and 887 cm −1 almost keep unchanged, which shows that N 2 O, N 2 O 5 , and HNO 3 as gaseous products are continuously generated from the absorption reactions. Then the amounts of N 2 O, N 2 O 5 , and HNO 3 rapidly decrease after the absorption time of about 210 min and finally disappear after about 230 min, which indicates that the absorption equilibrium is established, and no sufficient sulfite is used to react with NO 2 to produce gaseous N 2 O, N 2 O 5 , and HNO 3 . These results are consistent with the equilibrium analysis of sulfur compositions (see Figure 5). In fact, not all sulfite would be converted to sulfate ions, nitrogen-sulfur compounds, and sulfite radical may exist in reaction system. In addition, the occurrence of N 2 O 5 is due to the reaction between NO 2 and O 2 in gas phase, or the decomposition of nitrogen-sulfur compounds. Furthermore, the gaseous HNO 3 is not only attributed to the fact that HNO 3 in absorption liquid enters gas phase, but also that gas phase reaction happens, which can be described by the following Reaction (6): Figure 7 also shows that the peak at 1600 cm −1 , assigned to NO 2 , gradually increases and the peak at 1900 cm −1 , assigned to NO, gradually decreases after the absorption time of about 210 min. The results are also in accordance with those of gas phase composition analysis by flue gas analyzer (Testo350-pro, Germany), as shown in Figure 2.
Appl. Sci. 2017, 7, 377 7 of 10 HNO3, and HNO3, respectively [34]. In the initial absorption period, the intensities of bands at 2287 cm −1 , 1720 cm −1 , 1326 cm −1 , and 887 cm −1 almost keep unchanged, which shows that N2O, N2O5, and HNO3 as gaseous products are continuously generated from the absorption reactions. Then the amounts of N2O, N2O5, and HNO3 rapidly decrease after the absorption time of about 210 min and finally disappear after about 230 min, which indicates that the absorption equilibrium is established, and no sufficient sulfite is used to react with NO2 to produce gaseous N2O, N2O5, and HNO3. These results are consistent with the equilibrium analysis of sulfur compositions (see Figure 5). In fact, not all sulfite would be converted to sulfate ions, nitrogen-sulfur compounds, and sulfite radical may exist in reaction system. In addition, the occurrence of N2O5 is due to the reaction between NO2 and O2 in gas phase, or the decomposition of nitrogen-sulfur compounds. Furthermore, the gaseous HNO3 is not only attributed to the fact that HNO3 in absorption liquid enters gas phase, but also that gas phase reaction happens, which can be described by the following Reaction (6): Figure 7 also shows that the peak at 1600 cm −1 , assigned to NO2, gradually increases and the peak at 1900 cm −1 , assigned to NO, gradually decreases after the absorption time of about 210 min. The results are also in accordance with those of gas phase composition analysis by flue gas analyzer (Testo350-pro, Germany), as shown in Figure 2.  Figure 8 shows the distribution of nitrogen products for NO2 absorption into sulfite solution, based on mass balance for a typical inlet gas with 260 ppm NO2, as the sole N source. Because NO2 is hardly detected in the outlet flue gas of the reactor before 60 min, NO2 absorbed into the liquid phase is 2.56 mmol during initial absorption time of 60 min. NO3 − and NO2 − concentrations in the absorption solution, based on IC results, are 1.511 and 0.766 mmol, respectively. Because both NH3 and NH4 + have not been found by FTIR and IC, the other N compositions is calculated as 0.283 mmol according to mass balance, account for 11% of the total N compositions, and the calculated values of other N compositions content are in good agreement with the experimental values.  Figure 8 shows the distribution of nitrogen products for NO 2 absorption into sulfite solution, based on mass balance for a typical inlet gas with 260 ppm NO 2 , as the sole N source. Because NO 2 is hardly detected in the outlet flue gas of the reactor before 60 min, NO 2 absorbed into the liquid phase is 2.56 mmol during initial absorption time of 60 min. NO

NO2 Absorption Pathway
According to the above-mentioned analyses, a possible NO2 absorption pathway can be proposed, as depicted in Figure 9.
The main reactants in the gas phase include NO2, SO2, and O2. The sole N source in the inlet flue gas is NO2. When NO2 laden gas contacts with sulfite solution, the transfer of the NO2 into absorption solution occurs, meanwhile, reactions take place in the liquid phase, and the main products of NO2 absorption in flue gas are NO3 − and NO2 − , especially NO3 − in absorption solution dramatically increases due to the absorption of NO2 and the oxidation of NO2 − . HNO3 is considered to involve gas and liquid states existing in reaction system, and the gaseous HNO3 in outlet flue gas is from both HNO3 escape in absorption solution and the reaction between NO2 and H2O in the gas phase. HNO2 may be produced by NO2 − combining with H + , and HNO2 is unstable in liquid phase and easily decomposes, which leads to HNO3 formation and NO release. As NO increasing, a homogeneous reaction of NO and NO2 results in an increase of the N2O3 to a smaller extent, the NO or N2O3 can react with SO3 2− to form hydroxylamine-disulfonate (HADS), which is a precursor of numerous N-S compounds. In addition, the existence of SO2 in the gas phase is in favor of the sulfite and bisulfate formation, and HNO2 can also react with HSO3 − to form HADS. The intermediate products of N-S compounds finally decompose to N2O5, N2O, and N2 in gas phase.

NO 2 Absorption Pathway
According to the above-mentioned analyses, a possible NO 2 absorption pathway can be proposed, as depicted in Figure 9.
The main reactants in the gas phase include NO 2 , SO 2 , and O 2 . The sole N source in the inlet flue gas is NO 2 . When NO 2 laden gas contacts with sulfite solution, the transfer of the NO 2 into absorption solution occurs, meanwhile, reactions take place in the liquid phase, and the main products of NO 2 absorption in flue gas are NO 3 − and NO 2 − , especially NO 3 − in absorption solution dramatically increases due to the absorption of NO 2 and the oxidation of NO 2 − . HNO 3 is considered to involve gas and liquid states existing in reaction system, and the gaseous HNO 3 in outlet flue gas is from both HNO 3 escape in absorption solution and the reaction between NO 2 and H 2 O in the gas phase. HNO 2 may be produced by NO 2 − combining with H + , and HNO 2 is unstable in liquid phase and easily decomposes, which leads to HNO 3 formation and NO release. As NO increasing, a homogeneous reaction of NO and NO 2 results in an increase of the N 2 O 3 to a smaller extent, the NO or N 2 O 3 can react with SO 3 2− to form hydroxylamine-disulfonate (HADS), which is a precursor of numerous N-S compounds. In addition, the existence of SO 2 in the gas phase is in favor of the sulfite and bisulfate formation, and HNO 2 can also react with

NO2 Absorption Pathway
According to the above-mentioned analyses, a possible NO2 absorption pathway can be proposed, as depicted in Figure 9.
The main reactants in the gas phase include NO2, SO2, and O2. The sole N source in the inlet flue gas is NO2. When NO2 laden gas contacts with sulfite solution, the transfer of the NO2 into absorption solution occurs, meanwhile, reactions take place in the liquid phase, and the main products of NO2 absorption in flue gas are NO3 − and NO2 − , especially NO3 − in absorption solution dramatically increases due to the absorption of NO2 and the oxidation of NO2 − . HNO3 is considered to involve gas and liquid states existing in reaction system, and the gaseous HNO3 in outlet flue gas is from both HNO3 escape in absorption solution and the reaction between NO2 and H2O in the gas phase. HNO2 may be produced by NO2 − combining with H + , and HNO2 is unstable in liquid phase and easily decomposes, which leads to HNO3 formation and NO release. As NO increasing, a homogeneous reaction of NO and NO2 results in an increase of the N2O3 to a smaller extent, the NO or N2O3 can react with SO3 2− to form hydroxylamine-disulfonate (HADS), which is a precursor of numerous N-S compounds. In addition, the existence of SO2 in the gas phase is in favor of the sulfite and bisulfate formation, and HNO2 can also react with HSO3 − to form HADS. The intermediate products of N-S compounds finally decompose to N2O5, N2O, and N2 in gas phase.