• <tr id="yyy80"></tr>
  • <sup id="yyy80"></sup>
  • <tfoot id="yyy80"><noscript id="yyy80"></noscript></tfoot>
  • 99热精品在线国产_美女午夜性视频免费_国产精品国产高清国产av_av欧美777_自拍偷自拍亚洲精品老妇_亚洲熟女精品中文字幕_www日本黄色视频网_国产精品野战在线观看 ?

    Simultaneous desulfurization and denitrification of sintering flue gas via composite absorbent☆

    2016-06-01 03:01:14JieWangWenqiZhong

    Jie Wang ,Wenqi Zhong ,*

    1 Key Laboratory of Energy Thermal Conversion and Control of Ministry of Education,School of Energy and Environment,Southeast University,Nanjing 210096,China

    2 Centre for Simulation and Modelling of Particulate Systems,Southeast University-Monash University Joint Research School,Suzhou 215123,China

    1.Introduction

    Among the various processes in iron and steel industry,the emission of NOXfrom the sintering process accounts for 50%of the total NOXemission.Additionally,the SO2discharging from the sintering process is about 80%.These gases are the main pollutant harmful to human and other living beings,the reduction of which is an important work of the iron and steel production enterprises[1].Along with the fact that the emission standard of NOXand SO2is more and more rigorous,the development ofnoveltechnologies for simultaneous desulfurization and denitrification of sintering flue gas will be another challenging and urgent issue following the flue gas treatment of power plant[2].At present,wet flue gas desulfurization(FGD)is a relatively mature and most widely applied technology in iron and steelindustry to controlthe SO2emission.However,It is notmuch effective For the absorption ofNOXbecause NOXfrom the sintering flue gas mainly exists in the form of NO which is poorly soluble in water[3].The common technologies for denitrification used in coalfired power plant are the selective catalytic reduction(SCR)and selective non-catalytic reduction(SNCR)methods[4-6],butneitherof them can be applied to sintering flue gas directly due to the special characteristics of sintering flue gas whose gas temperature is relative low(80-160°C),gas flow rate is too large(average 2.5 × 106m3·h-1),and the concentration of NOXis low(100-400 mg·m-3).What is more,establishment of completely new equipment and technology to remove SO2and NOXsimultaneously requires too much economic budget and thus is hardly accepted by most iron and steel industries.An alternative way is to add NO removal function to the existing FGD system to reach the goal of simultaneous absorption of SO2and NOX[7].In other words,the aim of this technique is to use proper oxidize agents to react NO into NO2which ultimately can be absorbed by water.

    Currently,commonly used oxidizing agents include ClO2[8,9],O3[10,11],KMnO4[12-15],H2O2[16-18],NaClO2[19-27],NaClO[28,29]and so on.For the wet FGD,the reaction mainly occurs in the liquid phase,so ClO2,O3etc.will not be taken into consideration.KMnO4,and H2O2could be effective for simultaneous absorption of SO2and NOXin alkaline conditions,and the removal effects improve with the increase of pH.However,the pH of actual desulfurization slurry is between 5 and 7,KMnO4,H2O2will not be primarily considered.Moreover,the reaction products of KMnO4may contaminate the FGD gypsum and causing secondary pollution.And the chemical performance of H2O2is unstable,so It is difficultto be transported for long distance and reserved for long time.In general,NaClO2is the oxidizing agents which had been researched a lot and its effect is great for simultaneous desulfurization and denitrification.For example,Sadaet al.[19-21]used NaClO2/NaOH solution as the absorbent to study the removal efficiency of NO under various operating parameters.They found that adding NaOH to NaClO2would decrease the absorption rate of NO.The removal efficiency is mainly affected by the L/G ratio and the concentration of NaClO2in the solution.Next,Chienetal.[22-24]did a series of similarex periments in a bench-scale spraying scrubber system in order to investigate the absorption kinetics of SO2and NO and the reaction mechanism was revealed.Unlike previous research,Yanget al.[25,26]performed the absorption experiments of NO by nitric acid solution of NaClO2in a packed bed scrubber and found the color of solution turned greenish yellow due to the presence of ClO2,they also used bubble column and spary chamber scrubber to absorb NO in acidic NaClO or Cl2solution and obtained the similar results.Deshwalet al.[27]revealed that NaClO2could decomposed into ClO2gas in acidic solution,which was believed to participate in denitrification and determined the removal efficiency of NO.In addition,researches on NaClO are relatively rare due to the fact that the Oxidation of NaClO is weak compared with NaClO2.Chenet al.[28,29]developed a two-stage chemical scrubbing system to removal NO,the efficiency is obvious but the process is complicated.

    According to the previous studies,NaClO2was demonstrated to be comparatively effective among all kinds of oxidizing agents in desulfurization and denitrification,but it is still difficult to be applied extensively in industry because of the high cost.In order to solve such problems,a compound absorbent containing NaClO2and NaClO was used to investigate simultaneous removal of SO2and NO in this study,and the key point of this art is to determine the amount of oxidizing agents and the optimal experimental conditions.At last,the success of engineering test proved that this novel method has advantages of both higher efficiency and lower cost compared with the NaClO2oxidation absorption method.

    2.Experimental

    The experimental device is illustrated in Fig.1 which includes four main parts:a flue gas simulation system,an absorption reactor system,a gas sampling and analyzing system and an off-gas treatment system.The flue gas simulation system mainly consists of a pure N2gas cylinder(Shangyuan Gas,purity 99.9%),a pure SO2gas cylinder(Shangyuan Gas,purity 99.9%),a pure NO gas cylinder(Shangyuan Gas,purity 99.9%),a gas buffertank and fourmass flow controllers(MFC).The absorption reactor unit mainly includes a self-designed lab-scale bubbling reactor and a digital heating and temperature control device.Besides,the reactor is made of stainless steel with a diameter D1of 320 mm and a height H1of 240 mm.There are 4 intake-tubes with a diameter D2of 14 mm and 1 exhaust tube with a diameter D3of 80 mm.The gas sampling and analyzing system contain a sample conditioner(Juchuang,JCGH-2)and a flue gas analyzer(MRU,Germany).The off-gas treatment system is a tank saturated with aqueous alkaline solution.The grade of sodium chlorite is analytical-pure(available chlorine≥80%,Aladdin IndustrialCorporation,Shanghai,China).The grade of sodium hypochlorite is technical-pure(available chlorine≥30%,Nanjing Chemical Reagent Co.,Ltd.,Nanjing,China).The grade of sodium hydroxide(≥96%)and phosphoric acid(65%-68%)is analytical-pure(BOLT Chemical Trading Co.,Ltd.,Tianjin,China).

    Fig.1.Schematic diagram of experimental system.

    During the experiment,the flow rates of N2,SO2and NO were controlled through the mass flow meters and mixed into desired concentrations in a buffer tank firstly.10 L aqueous solution with a required amountof NaClO2/NaClO in the reactorwas heated and then kept in desired temperatures by a digital heating and temperature control device.Thereafter,the simulated gas continuously flowed through the reactor with a flow rate and was absorbed by the solution.After reaction,the simulated flue gas was sampled by a sample conditioner and analyzed through a flue gas analyzer so that the concentration of NO and SO2would be monitored in real time.Meanwhile,the testdata was recorded in every 2 min,so the removalefficiency ofNOand SO2can be calculated through Eqs.(1)to(2).

    In addition,the initial pH of absorption solution in the bubbling reactor could be adjusted by adding acid or alkaline solution(H3PO4and NaOH)and detected by the LEICI pH meter.Continuous stirring was provided by a mechanical agitator.The operating conditions are shown in Table 1.Finally,the simulated flue gas before being released into atmosphere would be post-processed by the off-gas treatment system.

    Table 1Operating conditions

    3.Results and Discussion

    3.1.Effect of the concentration of NaClO2(ms)and NaClO(mp)

    Fig.2.Effect of the concentration ofNaClO2/NaClOon the removalefficiencies(T R=25°C,pH=6,V g=30 L·h-1,C N=350 mg·m-3,C S=1000 mg·m-3).

    Fig.2 depicts the variation in NO and SO2removal efficiencies with the concentration of absorbent,it can be seen that the removal efficiency of NO increases at first and then slow down withmsand the SO2removal efficiency almost remains constant.Whenmsincreases from1 to 3 mmol·L-1,the removalefficiency ofNOis sharply improved by 11%.Whilemschanges from 4 to 6 mmol·L-1,the removalefficiency increases by 4%only.Ifmsis constant,the removal efficiency of NO inmp=3 mmol·L-1is higher thanmp=0 mmol·L-1.It means that adding NaClOto NaClO2aqueous solution hasobvious promotion on denitrification but the effect would be weakened if excess quantities of NaClO were used.

    Moreover,considering that the oxidation properties of the solution may be different under different molar ratios of NaClO2/NaClO(M)which iscalculated by using Eq.(3),experiments were carried out in different molar ratios of NaClO2/NaClO to check the oxidization of the solution.Due to the fact that the removal efficiency of SO2is less affected by the concentration of oxidizing agent,we focus on the removal efficiency of NO here.

    As shown in Fig.3,the removal efficiency of NO shows an upward trend with the increase ofM.WhenMis above 1.3,the removal efficiency of NO begins to be stable.These results indicate that NaClO2plays an important role in the process of oxidative absorption,slight change of its concentration can lead to significant increase of the removal efficiency of NO.From the aspect of economy that the price of NaClO2is much higher than NaClO,the cost of oxidizing agent can be reduced by decreasing NaClO2concentration while increasing NaClO concentration.In this study,based on the efficiency and the cost consideration,the optimalMwas chosen as 1.3.

    Fig.3.Effect of the molar ratio of NaClO2/NaClO on the removal efficiencies(T R=25°C,pH=6,V g=30 L·h-1,C N=350 mg·m-3,C S=1000 mg·m-3).

    3.2.Effect of solution temperature(TR)

    For the gas-liquid two phase chemical reaction,the temperature plays dual role.On one hand,the increase of temperature is beneficial to ion diffusion in solution which accelerates the rate of reaction and promotes the removal of SO2and NO.On the other hand,the increase of temperature lowers the solubility ofSO2and NOin solution which increases the mass transfer resistance between gas and liquid and restrains the oxidation and absorption of SO2and NO.Therefore,the rise of temperature has effects of promoting and inhibiting on the experiment.Theoretically,the reaction exists optimal reaction temperature.As shown in Fig.4,whenTRis between 30 °C and 50 °C,the removal efficiency of NO increases with the increase ofTR,which indicates that the positive effect of temperature is greater than its inhibition on the reaction.When the temperature is above 50°C,the removal efficiency ofNO remains almost unchanged with furtherincreasingTR,which indicates that the promotion and inhibition of temperature on the reaction are in an equilibrium state.In the actual projects,the reaction temperature is between 50 and 70 °C,so the optimalTRwas selected as 55 °C.

    Fig.4.Effect of solution temperature on the removal efficiencies(pH=6,V g=30 L·h-1,m s=4 mmol·L-1,m p=3 mmol·L-1,C N=350 mg·m-3,C S=1000 mg·m-3).

    3.3.Effect of initial solution pH

    Previous study shows that the removal efficiencies of NO and SO2were greatly affected by the initial solution pH[27],because the variation of pH would influence the oxidative absorption characteristics of solution and lead to the change of the removal efficiencies of SO2and NO.As shown in Fig.5,the removal efficiency of SO2is slightly affected and the removal efficiency of NO decreases with increasing the initial solution pH.The main reasons are as follows:SO2is easily soluble in water to produceand H+.When the solution pH increases,the equilibrium reaction takes place in the positive direction which promotes the absorption of SO2.Furthermore,when the solution pH decreases,ClO2and Cl2are generated by the aqueous solution of NaClO2/NaClO in acidic condition,and both of the gases are beneficial to increase the removal efficiencies of NO and SO2.Therefore,the solution pH has slight effect on desulfurization,but its decrease can dramatically improve the removal efficiency of NO.Moreover,NO is insoluble in water which means that the absorption ofNOcan only rely on oxidizing agent.Therefore,the removal of efficiency of NO drops continuously when pH of the solution increases.Above analysis indicates that the lower the initial pH of the solution is,the higher removal efficiency of NO will be obtained.By considering that strong acid condition could cause severe corrosion on the experimental equipment,optimal solution pH was usually taken as 6.

    Fig.5.Effect of initial solution pH on the removal efficiencies(T R=25 °C,V g=30 L·h-1,m s=4 mmol·L-1,m p=3 mmol·L-1,C N=350 mg·m-3,C S=1000 mg·m-3).

    3.4.Effect of gas flow rate(Vg)

    For a specific experiment device,Vgdetermines the staying time of gas in water,influences the gas-liquid mass transfer process,and changes the removal efficiencies of NO and SO2,so it is necessary to takeVginto consideration.From Fig.6,it can be seen that the removal efficiency of SO2decreased slightly but NO drops almost linearly asVgincreases.The high removal efficiency of SO2is due to the SO2dissolved in water.While NO is not soluble in water,it must be oxidized firstly by composite absorbent,and then absorbed by water.WhenVgis large,the time of NO touching oxidizing agent will be reduced,consequently,there is notenough time for NOto be oxidized and absorbed thoroughly.The results indicate thatVgis lower,the removal efficiency of NO is higher.Considering aboutVgis constant in actual projects,we just discuss the effect of it,and the optimalVgwill not be given.

    Fig.6.Effect of gas flow rate on the removal efficiencies(T R=25°C,pH=6,m s=4 mmol·L-1,m p=3 mmol·L-1,C N=350 mg·m-3,C S=1000 mg·m-3).

    3.5.Effect of the inlet concentration of SO2(CS)and NO(CN)

    In the practical engineering process,the content of nitrogen and sulfuris differentin various types ofcoal,which willchangeCSandCNfrom the sintering flue gas and affectthe concentration driving force between gas and liquid phases.Therefore,the removal efficiencies of SO2and NO will also change.As shown in Fig.7,the removal efficiency of SO2remains 100%and the removal efficiency of NO presents a slight upward trend with the increase ofCS.The phenomenon may be attributed to the hydrolysis of SO2,resulting in decreasing the solution pH and improving the oxidation of the absorbent.As seen from Fig.8,the removal efficiency of SO2remains stable and the removal efficiency of NO increases slightly with increasingCN.The reason might be that the increase ofCNmakes the pressure of NO in the gas phase rise and accelerates the gas-liquid mass transfer,which leads to the increase of removal efficiency of NO.

    3.6.Parallel tests

    Fig.7.Effect of SO2 concentration on the removal efficiencies(T R=25°C,pH=6,V g=30 L·h-1,m s=4 mmol·L-1,m p=3 mmol·L-1,C N=350 mg·m-3).

    Fig.8.Effect of NO concentration on the removal efficiencies(T R=25°C,pH=6,V g=30 L·h-1,m s=4 mmol·L-1,m p=3 mmol·L-1,C S=1000 mg·m-3).

    In order to check the stability and accuracy of experiment,parallel tests were carried out under the optimal conditions in whichms=4 mmol·L-1,mp=3 mmol·L-1,TR=55 °C,the initial solution pH=6,Vg=30 L·h-1,andCS=1000 mg·m-3,CN=350 mg·m-3.From Table 2,it can be seen that the average removal efficiencies of SO2and NO are 99.5%and 90.8%,respectively,and the standard deviation of removal efficiencies are 0.5 and 0.795,respectively.It indicates that the reproducibility of experiment date is good,and the performance of experiment apparatus is stable.

    Table 2Results of parallel experiments

    4.Reaction Mechanism

    For revealing the reaction mechanism and the process of simultaneous removal of SO2and NO by the aqueous solution of NaClO2/NaClO,products of desulfurization and denitrificationwere qualitatively and quantitatively analyzed.As we know,the possible existence of ionand some intermediate products ClO2or Cl2[7].Based on the chemical properties of different ions,Cl-,were tested by the hydronium chromatography method and,ClO2,were detected by the electric potential titrimetric method.

    4.1.Interaction mechanism of NaClO2/NaClO

    By monitoring the color and smell of absorption solution and analyzing the reaction products,we can find that the oxidizability of NaClO2/NaClO may be different under various initial solution pH.As shown in Fig.9.Samples 1 and 2 are the aqueous solution containing NaClO2and NaClO,respectively.Sample 3 is the aqueous solution of NaClO2/NaClO whose pH is 9.8 without adding acid or alkaline solution to adjust,the solution is almost colorless and a little pungent odor could be smelled.Sample 4 is the solution whose initial pH is adjusted to 6 on the basis of Sample 3,the color of it turns yellowish green,pungent odor becomes more intense.The phenomenon is attributed to products from the reaction of NaClO2/NaClO in acidic condition.From a survey of previous literatures[30-32],we can speculate that the products may be ClO2and Cl2which have positive effect on desulfurization and denitrification.In order to further understand the interaction mechanism of NaClO2/NaClO,ions concentration of a single absorbents and its mixture were determined.The results are shown in Table 3.

    Fig.9.The color contrast of absorbents in different experiments process.

    Table 3The changes of ions concentration in absorbing liquid(mg·L-1)

    The possible reactions between ClO2and Cl2in alkaline solution are listed as follows:

    So the existence of ClO2and Cl2can be con firmed by checking the variation ofand Cl-concentration.Comparing Samples 1 to 3,we can find that Samples 1 and 2 both contain Cl-,but ClO3-only exists in Sample 1.It can be considered that the properties of single oxidant had changed under acid condition,the reaction equations are presumed as follows[32,33]:

    The concentration ofand Cl-in Sample 3 is higher than in Samples 1 and 2,indicating that ClO2and Cl2are produced.In addition,by comparing Samples 3 and 4,we can find that the concentration ofand ClO-decreases,while the concentration ofand Cl-increases,stating that a lower pH of the solution makes it more favorable for the generation of ClO2.According to the analysis of the reaction products and the reaction mechanism presumed above,the overall reaction equation of NaClO2/NaClO acid solution can be considered as follow:

    4.2.Reaction mechanism of simultaneous desulfurization and denitrification

    In order to explore reaction mechanism of simultaneous absorption of NO and SO2,experiments were carried out under the optimal conditions and the reaction products were detected.The results of products analysis are listed in Table 4.

    Table 4Products analysis of simultaneous desulfurization and denitrification using NaClO2/NaClO complex absorbent(mg·L-1)

    Sample 5 is the initial solution containing NaClO2/NaClO which is not involved in the reaction of simultaneous removal of NO and SO2,Sample 6 is NaClO2/NaClO aqueous solution which has been in reaction for 10 min,and Sample 7 is the solution whose oxidizability has been in failure for 5 min.As shown in Table 4,both the concentration ofanddecreases,and meanwhile Cl-,,andare produced continuously by comparing Sample 5 and 6.It indicates that composite absorbent can oxidize SO2and NO to the highest state in acidic condition.After the failure ofoxidizing agent,the concentration of Cl-andis stillrising whileconcentration begins to decline,sois speculated as an intermediate product.

    According to the previous analysis of interaction mechanism of NaClO2/NaClO,it was found that there exists a small quantity of ClO2and Cl2in the complex absorbent solution,and there might be a part ofClO2and Cl2from the liquid phase to the gas phase because their partial pressures in gas phase are smaller than the gas-liquid equilibrium partial pressures.Considering that SO2is soluble in water,the absorption of SO2mainly happens in the liquid phase.However,NO is poorly soluble in water,and the mass transfer resistance from liquid phase to gas phase is large,so the oxidation of NO mainly through touching with ClO2and Cl2in the interface between gas and liquid phases,then the reaction products can be absorption in the liquid phase,so the absorption of NO might happen in the gas and liquid phases at the same time.

    On the basis of analysis above and the results of previous research[31-33],the possible reaction equations of simultaneous desulfurization and denitrification by NaClO2/NaClO acid solution are listed as follows:

    In conclusion,the process of simultaneous removal of SO2and NO using NaClO2/NaClO aqueous solution is relatively complex,the overall reaction equations can be summarized as follows:

    5.Engineering Experiments

    In order to verify the availability of above experimental results and provide a solid technical support on the large-scale industrial application in the future,engineering experiments were carried out in a 2×220 m2sintering flue gas desulfurization tower at Nanjing Iron&Steel Co.The system of the wet FGD is shown in Fig.10.The experimental conditions are as follow:the flow rate of inlet gas ranges from 1.36× 106to 2.51× 106m3·h-1,the inlet gas temperature increases from 125.1 to 166.63°C,the desulfurization slurry temperature in absorber is between 50 to 70°C,the SO2concentration of inlet gas changes from 517.24 to 1128.06 mg·m-3,the NOXconcentration of inlet gas ranges from 249.75 to 340.05 mg·m-3and the molar ratio of NaClO2/NaClO is about 1.3.The variation of NO and SO2mass flux was monitored through the Pollution Source On-line Monitoring system of Nanjing City,then the removal efficiencies of NOXand SO2can be evaluated by Eqs.(26)to(27),respectively.

    As shown in Figs.11 and 12,during the experimental period,QSdecreases from 9.8 to 6.9 kg·min-1,the removal efficiency of NOXincreases around 20%compared with ordinary times and the removal efficiency of SO2remains stable above 94%.The results meet national environmental standards and demonstrate the capability of the technology for simultaneous desulfurization and denitration.However,it can be seen in Fig.12 that the increase of NOXremoval efficiency is limited.It is speculated that when NO was oxidized to NO2which cannot be absorbed completely,because the treated flue gas with a little reddish brown color(the original flue gas color is white)and the color is similar to NO2during engineering experiment.

    In terms of the present running situation of Nanjing Iron&Steel Co,the annual costs of the composite absorbent is about 5.43 million,the fee for pollutant discharge can be saved about 1.19 million a year.If the reagents are purchased in large quantities,the price could be reduced by 30%-40%.Compared with other simultaneous desulfurization and denitrification technologies,using NaClO2/NaClO as the absorbent has certain advantages in the aspect of environmental protection and economy.

    6.Conclusions

    A composite absorbentcontaining NaClO2and NaClO was used to simultaneous desulfurization and denitrification from flue gas.The effects of various operating parameters on the experiment were considered and the reaction products were analyzed.According to the results of discussion,following conclusions can be made:

    1.Under the optimal experimental conditions,the removal efficiencies of SO2and NO reach 99.5%and 90.8%,respectively.These results indicate that the oxidizing agent,which is made of NaClO2and NaClO,has good promotion prospects in simultaneous removal of NO and SO2.

    2.The removal efficiency of SO2is slightly affected by different operating parameters in the experiment and holds steady above 98%.

    3.In acidic condition,high removal efficiencies of SO2and NO owe to the fact that ClO2and Cl2are produced by the reaction between NaClO2and NaClO.

    4.The initial solution pH and the gas flow rate are the main factors affecting simultaneous desulfurization and denitrification.

    Nomenclature

    CNinitial NO inlet concentration,mg·m-3

    CNO,inthe inlet concentration of NO,mg·m-3

    CNO,outthe outlet concentration of NO,mg·m-3

    CSinitial SO2inlet concentration,mg·m-3

    CSO2,inthe inlet concentration of SO2,mg·m-3

    CSO2,outthe outlet concentration of SO2,mg·m-3

    Mthe molar ratio of NaClO2/NaClO

    mpNaClO concentration,mmol·L-1

    msNaClO2concentration,mmol·L-1

    QNOX,inthe inlet mass flux of NOX,kg·min-1

    QNOX,outthe outlet mass flux of NOX,kg·min-1

    QSO2,inthe inlet mass flux of SO2,kg·min-1

    QSO2,outthe outlet mass flux of SO2,kg·min-1

    TRsolution temperature,°C

    Vggas flow rate,L·h-1

    η the removal efficiency

    ηNremoval efficiency of NO

    ηSremoval efficiency of SO2

    Fig.10.The system of wet FGD:(a)Appearance of bubbling gas absorbing tower;(b)the technological progress of sintering flue gas desulfurization.

    Fig.11.The mass flux change of NO X/SO2 during experimental period.

    Fig.12.The change of removal efficiencies during experimental period.

    [1]Y.Li,W.Q.Zhong,J.Ju,Experiment on simultaneous absorption of NO and SO2from sintering flue gas by oxidizing agents of KMnO4/NaClO,Int.J.Chem.React.Eng.12(1)(2014)1-9.

    [2]D.G.Streets,S.T.Waldhoff,Present and future emissions of air pollutants in China:SO2,NOXand CO,Atmos.Environ.34(3)(2000)363-374.

    [3]F.J.Gutierrez Ortiz,F.Vidal,P.Ollero,L.Salvador,V.Cortes,Pilot-plant technical assessment of wet flue gas desulfurization using limestone,Ind.Eng.Chem.Res.45(4)(2006)1466-1477.

    [4]G.Qi,R.T.Yang,R.Chang,MnOX-CeO2mixed oxides prepared by co-precipitation for selective catalytic reduction of NO with NH3at low temperatures,Appl.Catal.B Environ.51(2)(2004)93-106.

    [5]M.T.Javed,N.Irfan,B.M.Gibbs,Control of combustion-generated nitrogen oxides by selective non-catalytic reduction,J.Environ.Manag.83(3)(2007)251-289.

    [6]S.W.Bae,S.A.Roh,S.D.Kim,NO removal by reducing agents and additives in the selective non-catalytic reduction(SNCR)process,Chemosphere65(1)(2006)170-175.

    [7]Y.Zhao,T.Guo,Z.Chen,Y.Du,Simultaneous removal of SO2and NO using M/NaClO2complex absorbent,Chem.Eng.J.160(1)(2010)42-47.

    [8]D.S.Jin,B.R.Deshwal,Y.S.Park,H.K.Lee,Simultaneous removal of SO2and NO by wet scrubbing using aqueous chlorine dioxide solution,J.Hazard.Mater.135(1-3)(2006)412-417.

    [9]H.K.Lee,B.R.Deshwal,K.S.Yoo,Simultaneous removal of SO2and NO by sodium chlorite solution in Wetted-Wall column,Korean J.Chem.Eng.22(2)(2005)208-213.

    [10]Y.S.Mok,H.J.Lee,Removal of sulfur dioxide and nitrogen oxides by using ozone injection and absorption reduction technique,Fuel Process.Technol.87(7)(2006)591-597.

    [11]Z.Wang,J.Zhou,Y.Zhu,Simultaneous removal of NOX,SO2and Hg in nitrogen flow in a narrow reactor by ozone injection:experimental results,Fuel Process.Technol.88(8)(2007)817-823.

    [12]H.Chu,T.W.Chien,S.Y.Li,Simultaneous absorption of SO2and NO from flue gas with KMnO4/NaOH solutions,Sci.Total Environ.275(1-3)(2001)127-135.

    [13]H.Chu,S.Y.Li,T.W.Chien,The absorption kinetics of NO from flue gas in a stirred tank reactor with KMnO4/NaOH solutions,J.Environ.Sci.Health A33(5)(1998)801-827.

    [14]C.Brogren,H.T.Karlsson,I.Bjerle,Absorption of NO in an alkaline solution of KMnO4,Chem.Eng.Technol.20(6)(1997)396-402.

    [15]Z.Wei,H.Niu,Y.Ji,Simultaneous removal of SO2and NOXby microwave with potassium permanganate over zeolite,Fuel Process.Technol.90(2)(2009)324-329.

    [16]D.Thomas,S.Colle,J.Vanderschuren,Kinetics of SO2absorption into fairly concentrated sulphuric acid solutions containing hydrogen peroxide,Chem.Eng.Process.42(6)(2003)487-494.

    [17]S.Colle,J.Vanderschuren,D.Thomas,Pilot-scale validation of the kinetics of SO2absorption into sulphuric acid solutions containing hydrogen peroxide,Chem.Eng.Process.43(11)(2004)1397-1402.

    [18]S.Colle,J.Vanderschuren,D.Thomas,Simulation of SO2absorption into sulfuric acid solutions containing hydrogen peroxide in the fast and moderately fast kinetic regimes,Chem.Eng.Process.60(22)(2005)6472-6479.

    [19]E.Sada,H.Kumazawa,I.Kudo,T.Kondo,Absorption of NO in aqueous mixed solutions of NaClO2 of and NaOH,Chem.Eng.Sci.33(3)(1978)315-318.

    [20]E.Sada,H.Kumazawa,Y.Yamanaka,I.Kudo,T.Kondo,And nitric oxide in aqueous mixed solutions of sodium chlorite and sodium hydroxide,J.Chem.Eng.Jpn11(4)(1978)276-282.

    [21]E.Sada,H.Kumazawa,M.A.Butt,Single and simultaneous absorptions of lean SO2and NO2into aqueous slurries of Ca(OH)2or Mg(OH)2particles,J.Chem.Eng.Jpn12(2)(1979)111-117.

    [22]T.W.Chien,H.Chu,H.T.Hsueh,Kinetic study on absorption of SO2and NOXwith acidic NaClO2solutions using the spraying column,J.Environ.Eng.129(11)(2003)967-974.

    [23]H.Chu,T.W.Chien,B.W.Twu,The absorption kinetics of NO in NaClO2/NaOH solutions,J.Hazard.Mater.84(2-3)(2001)241-252.

    [24]T.W.Chien,H.Chu,Removal of SO2and NO from flue gas by wet scrubbing using an aqueous NaClO2solution,J.Hazard.Mater.80(1-3)(2000)43-57.

    [25]C.Yang,H.Shaw,H.Perlmutter,Absorption of NO promoted by strong oxidizing agents:1.Inorganic oxychlorites in nitric acid,Chem.Eng.Commun.143(1)(1996)23-38.

    [26]C.Yang,H.Shaw,Aqueous absorption of nitric oxide induced by sodium chlorite oxidation in the presence of sulfur dioxide,Environ.Prog.17(2)(1998)80-85.

    [27]B.R.Deshwal,S.H.Lee,J.H.Jung,B.H.Shon,H.K.Lee,Study on the removal of NOxfrom simulated flue gas using acidic NaClO2solution,J.Environ.Sci.20(1)(2008)33-38.

    [28]L.Chen,C.Hsu,C.Yang,Oxidation and absorption of nitric oxide in a packed tower with sodium hypochlorite aqueous solutions,Environ.Prog.24(3)(2005)279-288.

    [29]L.Chen,J.W.Lin,C.L.Yang,Absorption of NO2in a packed tower with Na2SO3aqueous solution,Environ.Prog.21(4)(2002)225-230.

    [30]B.R.Deshwal,H.Jo,H.Lee,Reaction kinetics of decomposition of acidic sodium chlorite,Can.J.Chem.Eng.82(3)(2004)619-623.

    [31]T.W.Chien,H.Chu,H.T.Hsueh,Spray scrubbing of the nitrogen oxides into NaClO2solution under acidic conditions,J.Environ.Sci.Health A36(4)(2001)403-414.

    [32]B.Kormanyos,I.Nagypal,G.Peintler,A.Horvath,Effect of chloride ion on the kinetics and mechanism of the reaction between chlorite ion and hypochlorous acid,Inorg.Chem.47(17)(2008)7914-7920.

    [33]T.Lehtimaa,V.Tarvo,G.Mortha,S.Kuitunen,T.Vuorinen,Reactions and kinetics of Cl(III)decomposition,Ind.Eng.Chem.Res.47(15)(2008)5284-5290.

    91久久精品国产一区二区成人| 日韩一本色道免费dvd| 99国产综合亚洲精品| 亚洲精品视频女| 婷婷色综合大香蕉| 亚洲精品视频女| 少妇高潮的动态图| 一级毛片黄色毛片免费观看视频| 国产成人精品一,二区| 日日啪夜夜爽| 性色av一级| 国产视频内射| 超碰97精品在线观看| 91精品国产九色| 国产乱人偷精品视频| 97在线人人人人妻| 欧美一级a爱片免费观看看| 黄色欧美视频在线观看| 午夜福利在线观看免费完整高清在| 26uuu在线亚洲综合色| 成人18禁高潮啪啪吃奶动态图 | 乱码一卡2卡4卡精品| 久久精品国产亚洲av涩爱| 国产女主播在线喷水免费视频网站| 国产极品粉嫩免费观看在线 | 精品人妻一区二区三区麻豆| 人体艺术视频欧美日本| 久久久久久伊人网av| 亚洲,一卡二卡三卡| a级毛色黄片| 午夜免费男女啪啪视频观看| 日韩人妻高清精品专区| 黑人猛操日本美女一级片| 99久国产av精品国产电影| 亚洲精品乱码久久久v下载方式| 国产在线视频一区二区| 国产一区二区在线观看日韩| 美女福利国产在线| 亚洲国产精品国产精品| 大香蕉久久网| 少妇人妻 视频| 日本av手机在线免费观看| 秋霞在线观看毛片| 少妇的逼水好多| 亚洲av日韩在线播放| 精品国产一区二区久久| 国语对白做爰xxxⅹ性视频网站| 久久久久久久国产电影| 国产毛片在线视频| 婷婷色综合大香蕉| 国模一区二区三区四区视频| 久久久久久久久久久丰满| 黄色配什么色好看| 亚洲美女视频黄频| 精品国产国语对白av| 18禁观看日本| 99视频精品全部免费 在线| 免费播放大片免费观看视频在线观看| 18禁在线无遮挡免费观看视频| 精品99又大又爽又粗少妇毛片| 不卡视频在线观看欧美| 又大又黄又爽视频免费| 99九九在线精品视频| 蜜桃久久精品国产亚洲av| 99re6热这里在线精品视频| 日韩人妻高清精品专区| 久久人人爽av亚洲精品天堂| 精品卡一卡二卡四卡免费| av播播在线观看一区| 亚洲精品av麻豆狂野| 欧美性感艳星| 青春草亚洲视频在线观看| 久久精品久久精品一区二区三区| 国语对白做爰xxxⅹ性视频网站| 狂野欧美白嫩少妇大欣赏| 狠狠精品人妻久久久久久综合| 国产高清三级在线| 中国美白少妇内射xxxbb| 国产成人精品福利久久| 免费观看av网站的网址| 日本与韩国留学比较| 久久久久久伊人网av| 久久影院123| 亚洲国产最新在线播放| 狂野欧美白嫩少妇大欣赏| 国产成人精品一,二区| 日本黄大片高清| 色吧在线观看| 国产精品久久久久久精品电影小说| 国产色婷婷99| 人成视频在线观看免费观看| 免费大片18禁| 亚洲av综合色区一区| 亚洲在久久综合| 中文欧美无线码| 亚洲情色 制服丝袜| 一级黄片播放器| 色5月婷婷丁香| 国产精品偷伦视频观看了| 青青草视频在线视频观看| 亚洲精品中文字幕在线视频| 人人妻人人澡人人爽人人夜夜| www.色视频.com| 亚洲精品国产av成人精品| 免费黄频网站在线观看国产| 男女边摸边吃奶| 丰满乱子伦码专区| 国产一级毛片在线| 亚洲经典国产精华液单| 一级片'在线观看视频| 国产精品熟女久久久久浪| 日本欧美视频一区| 久久99精品国语久久久| 嫩草影院入口| 波野结衣二区三区在线| 亚洲怡红院男人天堂| 久久午夜福利片| 18禁观看日本| 韩国高清视频一区二区三区| 婷婷色综合大香蕉| 亚洲国产av影院在线观看| 久久久亚洲精品成人影院| av在线观看视频网站免费| 最黄视频免费看| 国产欧美另类精品又又久久亚洲欧美| 91久久精品国产一区二区成人| 性色av一级| 亚洲国产毛片av蜜桃av| .国产精品久久| 99热国产这里只有精品6| 观看美女的网站| 免费看av在线观看网站| 国产毛片在线视频| 人人妻人人爽人人添夜夜欢视频| 久久久久久久久久久免费av| 日韩av不卡免费在线播放| 一本色道久久久久久精品综合| 国模一区二区三区四区视频| 蜜桃久久精品国产亚洲av| av在线老鸭窝| 国产成人精品在线电影| 我的老师免费观看完整版| 久久国产精品大桥未久av| 精品久久久久久久久亚洲| 女人精品久久久久毛片| 亚洲av成人精品一二三区| 七月丁香在线播放| 成人影院久久| 亚洲婷婷狠狠爱综合网| 久久久久精品久久久久真实原创| 亚洲内射少妇av| 男男h啪啪无遮挡| 欧美精品亚洲一区二区| 午夜激情av网站| 丝袜在线中文字幕| 中文字幕免费在线视频6| 十八禁高潮呻吟视频| 国产精品不卡视频一区二区| 91aial.com中文字幕在线观看| 国产av国产精品国产| 91成人精品电影| 纵有疾风起免费观看全集完整版| 久久97久久精品| 亚洲精品一区蜜桃| 91久久精品电影网| 黑人猛操日本美女一级片| 婷婷成人精品国产| 满18在线观看网站| 久久99热这里只频精品6学生| 老熟女久久久| 男女啪啪激烈高潮av片| 国产精品久久久久久av不卡| 97在线人人人人妻| 精品酒店卫生间| 精品国产一区二区三区久久久樱花| 色94色欧美一区二区| av福利片在线| 亚洲综合色网址| 国模一区二区三区四区视频| 老熟女久久久| 亚洲人成77777在线视频| 亚洲欧洲国产日韩| 亚洲色图综合在线观看| 99热这里只有精品一区| 一个人看视频在线观看www免费| 欧美xxⅹ黑人| 亚洲精品,欧美精品| 熟女电影av网| 日本黄色日本黄色录像| 欧美xxⅹ黑人| 亚洲国产精品专区欧美| av播播在线观看一区| 青春草视频在线免费观看| 国产一区有黄有色的免费视频| 麻豆乱淫一区二区| 久久久久久人妻| 一区二区日韩欧美中文字幕 | 亚洲精品日本国产第一区| 国产日韩欧美亚洲二区| 免费高清在线观看日韩| 看非洲黑人一级黄片| 亚洲综合色惰| 精品久久久噜噜| 老熟女久久久| 丁香六月天网| 岛国毛片在线播放| 少妇高潮的动态图| 国产av码专区亚洲av| 欧美bdsm另类| 免费久久久久久久精品成人欧美视频 | 免费观看无遮挡的男女| 欧美日韩av久久| 国产日韩欧美在线精品| 免费高清在线观看日韩| 国产一区二区在线观看日韩| 成人漫画全彩无遮挡| 少妇人妻精品综合一区二区| 少妇的逼水好多| 一级,二级,三级黄色视频| 日本猛色少妇xxxxx猛交久久| 国产精品久久久久久久久免| 欧美精品人与动牲交sv欧美| 少妇猛男粗大的猛烈进出视频| 精品视频人人做人人爽| 亚洲综合色惰| 亚洲av不卡在线观看| 丝袜脚勾引网站| 一区二区日韩欧美中文字幕 | 一本—道久久a久久精品蜜桃钙片| 日韩一区二区三区影片| 夜夜看夜夜爽夜夜摸| 国产精品女同一区二区软件| 国产色婷婷99| 欧美bdsm另类| 天堂俺去俺来也www色官网| 免费av不卡在线播放| 搡老乐熟女国产| 国产日韩欧美亚洲二区| 国产一区二区在线观看日韩| 久久久久国产精品人妻一区二区| 天天影视国产精品| 欧美成人午夜免费资源| 女人精品久久久久毛片| 午夜久久久在线观看| 夜夜骑夜夜射夜夜干| 狠狠精品人妻久久久久久综合| 人体艺术视频欧美日本| 久久综合国产亚洲精品| 秋霞伦理黄片| 我的女老师完整版在线观看| 自线自在国产av| 久久久午夜欧美精品| 国产在视频线精品| 国产免费现黄频在线看| 9色porny在线观看| 国产淫语在线视频| 99久久中文字幕三级久久日本| 国产成人aa在线观看| 色网站视频免费| 在线观看美女被高潮喷水网站| 久久国产精品男人的天堂亚洲 | 精品午夜福利在线看| 欧美日韩亚洲高清精品| 大香蕉久久成人网| 国产精品99久久99久久久不卡 | 我要看黄色一级片免费的| 国产探花极品一区二区| 国产视频首页在线观看| videos熟女内射| 免费观看a级毛片全部| 99久国产av精品国产电影| 九草在线视频观看| 青春草亚洲视频在线观看| 久久久久久久亚洲中文字幕| 免费播放大片免费观看视频在线观看| 美女视频免费永久观看网站| 日本与韩国留学比较| 在线 av 中文字幕| 亚洲第一区二区三区不卡| 一二三四中文在线观看免费高清| 国产伦理片在线播放av一区| 国产精品人妻久久久影院| 成年av动漫网址| 久久久午夜欧美精品| 99久国产av精品国产电影| 成人亚洲精品一区在线观看| 国产亚洲午夜精品一区二区久久| 夜夜爽夜夜爽视频| 我的女老师完整版在线观看| 国产精品久久久久久精品古装| 亚洲av日韩在线播放| 一二三四中文在线观看免费高清| 考比视频在线观看| 日韩av免费高清视频| 涩涩av久久男人的天堂| 九九久久精品国产亚洲av麻豆| 啦啦啦啦在线视频资源| 视频在线观看一区二区三区| av女优亚洲男人天堂| 美女脱内裤让男人舔精品视频| 下体分泌物呈黄色| 国产成人aa在线观看| 欧美少妇被猛烈插入视频| 日韩免费高清中文字幕av| 国产色爽女视频免费观看| 看十八女毛片水多多多| 黑人巨大精品欧美一区二区蜜桃 | 丝袜美足系列| 亚洲精品国产av蜜桃| 国产白丝娇喘喷水9色精品| 99热网站在线观看| 成年人午夜在线观看视频| 尾随美女入室| 亚洲美女黄色视频免费看| 99久久综合免费| 国产免费又黄又爽又色| 亚洲精品视频女| 日日爽夜夜爽网站| 乱码一卡2卡4卡精品| 国产av码专区亚洲av| 中文精品一卡2卡3卡4更新| 狂野欧美激情性bbbbbb| 岛国毛片在线播放| 亚州av有码| 51国产日韩欧美| 日韩,欧美,国产一区二区三区| 日韩av免费高清视频| 亚洲av在线观看美女高潮| 高清黄色对白视频在线免费看| 国产亚洲最大av| 欧美成人精品欧美一级黄| 99视频精品全部免费 在线| 又粗又硬又长又爽又黄的视频| 国产老妇伦熟女老妇高清| 久久久久久久久久久丰满| 老熟女久久久| 91在线精品国自产拍蜜月| 天堂俺去俺来也www色官网| 少妇精品久久久久久久| 精品人妻熟女毛片av久久网站| 一级,二级,三级黄色视频| 大码成人一级视频| av电影中文网址| 国产成人精品一,二区| 性高湖久久久久久久久免费观看| 欧美日韩精品成人综合77777| 日韩成人av中文字幕在线观看| 欧美日韩av久久| 国产成人精品一,二区| 天天躁夜夜躁狠狠久久av| av国产精品久久久久影院| 国产成人精品一,二区| 汤姆久久久久久久影院中文字幕| 毛片一级片免费看久久久久| 国产一区有黄有色的免费视频| 欧美亚洲 丝袜 人妻 在线| 热re99久久国产66热| 秋霞伦理黄片| 免费播放大片免费观看视频在线观看| 大香蕉97超碰在线| 夜夜爽夜夜爽视频| 日韩精品有码人妻一区| 精品久久久久久电影网| 精品国产国语对白av| 日本欧美视频一区| 超色免费av| 一区二区三区乱码不卡18| 赤兔流量卡办理| 日韩中字成人| 国内精品宾馆在线| 久久久久久久久久成人| 精品国产乱码久久久久久小说| 高清欧美精品videossex| 亚洲人成网站在线观看播放| 精品久久久久久久久亚洲| av女优亚洲男人天堂| 大香蕉久久网| 九色成人免费人妻av| 亚洲av综合色区一区| 永久网站在线| 日本爱情动作片www.在线观看| 日本欧美视频一区| 欧美日韩精品成人综合77777| 国产片特级美女逼逼视频| 久久99一区二区三区| 热99国产精品久久久久久7| 免费观看av网站的网址| 曰老女人黄片| 国产极品天堂在线| 婷婷成人精品国产| freevideosex欧美| 一级,二级,三级黄色视频| 欧美日韩av久久| 久久久久精品性色| 国产又色又爽无遮挡免| 街头女战士在线观看网站| 久久 成人 亚洲| 亚洲三级黄色毛片| 久久久午夜欧美精品| 美女内射精品一级片tv| 尾随美女入室| 多毛熟女@视频| 久久国产亚洲av麻豆专区| 老熟女久久久| 免费播放大片免费观看视频在线观看| 国产成人freesex在线| 少妇人妻久久综合中文| 亚洲精品日本国产第一区| 国产白丝娇喘喷水9色精品| 久久午夜综合久久蜜桃| 少妇精品久久久久久久| 啦啦啦在线观看免费高清www| 自线自在国产av| 日本与韩国留学比较| 亚洲国产精品成人久久小说| 九九在线视频观看精品| 卡戴珊不雅视频在线播放| 看免费成人av毛片| 久久久久人妻精品一区果冻| 精品人妻在线不人妻| av免费在线看不卡| 免费黄网站久久成人精品| 男的添女的下面高潮视频| 王馨瑶露胸无遮挡在线观看| 岛国毛片在线播放| 青青草视频在线视频观看| 日本91视频免费播放| 99热国产这里只有精品6| 久久精品夜色国产| 美女大奶头黄色视频| 最后的刺客免费高清国语| 成人免费观看视频高清| 国国产精品蜜臀av免费| 熟女av电影| 午夜久久久在线观看| 丝袜喷水一区| 一区二区av电影网| 久久精品国产亚洲av天美| 国产一区二区三区av在线| 97精品久久久久久久久久精品| 亚洲国产精品一区二区三区在线| 嫩草影院入口| 欧美老熟妇乱子伦牲交| 国产亚洲最大av| 日韩欧美一区视频在线观看| 午夜久久久在线观看| 成年女人在线观看亚洲视频| 啦啦啦在线观看免费高清www| 久久久国产欧美日韩av| 亚洲综合色惰| 中文字幕精品免费在线观看视频 | 99re6热这里在线精品视频| 赤兔流量卡办理| 在线观看一区二区三区激情| 亚洲第一av免费看| 精品人妻熟女毛片av久久网站| 制服丝袜香蕉在线| 精品久久久久久久久亚洲| 免费av中文字幕在线| 国产精品一二三区在线看| 全区人妻精品视频| 一区二区三区免费毛片| 久久久国产精品麻豆| 91在线精品国自产拍蜜月| 高清视频免费观看一区二区| 亚洲欧洲精品一区二区精品久久久 | 制服诱惑二区| 99久国产av精品国产电影| 熟女电影av网| 免费观看的影片在线观看| 亚洲精华国产精华液的使用体验| 丰满乱子伦码专区| 日韩精品免费视频一区二区三区 | 久久久亚洲精品成人影院| 国产精品嫩草影院av在线观看| 22中文网久久字幕| 黄色视频在线播放观看不卡| 男的添女的下面高潮视频| 丝袜脚勾引网站| 免费观看av网站的网址| 亚洲高清免费不卡视频| 久久女婷五月综合色啪小说| 美女内射精品一级片tv| 欧美日韩综合久久久久久| 国产亚洲最大av| 青春草视频在线免费观看| 午夜久久久在线观看| 国产不卡av网站在线观看| 男女高潮啪啪啪动态图| 日韩欧美一区视频在线观看| 国产片内射在线| 国产成人午夜福利电影在线观看| 搡老乐熟女国产| 亚洲无线观看免费| 美女xxoo啪啪120秒动态图| 欧美激情 高清一区二区三区| 一级毛片电影观看| 少妇的逼水好多| 男女高潮啪啪啪动态图| 尾随美女入室| 久久精品久久精品一区二区三区| 欧美老熟妇乱子伦牲交| av免费在线看不卡| 在线观看人妻少妇| 一级片'在线观看视频| 日韩视频在线欧美| 精品久久久久久久久av| 精品99又大又爽又粗少妇毛片| 精品一区二区免费观看| 天天影视国产精品| 亚洲内射少妇av| 国产又色又爽无遮挡免| 亚洲欧洲日产国产| 高清视频免费观看一区二区| 精品国产露脸久久av麻豆| 久久午夜福利片| 亚洲av日韩在线播放| 久久99热6这里只有精品| 搡女人真爽免费视频火全软件| 免费人成在线观看视频色| 免费大片18禁| 美女脱内裤让男人舔精品视频| 熟女人妻精品中文字幕| 欧美日韩精品成人综合77777| 在线观看人妻少妇| 9色porny在线观看| 日本免费在线观看一区| 国产日韩欧美视频二区| 国产伦精品一区二区三区视频9| 大又大粗又爽又黄少妇毛片口| 免费大片18禁| 永久网站在线| 欧美丝袜亚洲另类| 亚洲av.av天堂| 另类亚洲欧美激情| 亚洲成人手机| 精品人妻偷拍中文字幕| 亚洲精品国产av蜜桃| 国产成人精品婷婷| 岛国毛片在线播放| 日韩 亚洲 欧美在线| 久久久久精品久久久久真实原创| 午夜免费观看性视频| 午夜福利视频精品| 母亲3免费完整高清在线观看 | 观看美女的网站| 夜夜看夜夜爽夜夜摸| a级毛色黄片| 日韩大片免费观看网站| 中国美白少妇内射xxxbb| av国产久精品久网站免费入址| 亚洲欧洲日产国产| 久久精品国产亚洲av涩爱| 美女cb高潮喷水在线观看| av播播在线观看一区| 老女人水多毛片| 在线观看国产h片| 免费av不卡在线播放| 亚洲精品第二区| 极品人妻少妇av视频| 国产精品国产av在线观看| 丝袜美足系列| 亚洲一区二区三区欧美精品| 亚洲精品乱码久久久v下载方式| 国产精品免费大片| 亚洲中文av在线| 少妇 在线观看| 99热网站在线观看| 国产精品国产av在线观看| 能在线免费看毛片的网站| 亚洲精品,欧美精品| 午夜福利视频在线观看免费| 成人漫画全彩无遮挡| 99视频精品全部免费 在线| 国产精品国产三级国产专区5o| 美女国产视频在线观看| 高清视频免费观看一区二区| 亚洲精品日本国产第一区| 最新中文字幕久久久久| 另类亚洲欧美激情| 午夜91福利影院| 亚洲av中文av极速乱| 久久精品国产鲁丝片午夜精品| 国产片内射在线| 国产精品久久久久久久电影| 在线观看www视频免费| 一本—道久久a久久精品蜜桃钙片| 亚洲在久久综合| 亚洲精品日本国产第一区| 人人妻人人澡人人看| 国产又色又爽无遮挡免| 我要看黄色一级片免费的| 3wmmmm亚洲av在线观看| 亚洲三级黄色毛片| 久久国产亚洲av麻豆专区| 91久久精品电影网| 嘟嘟电影网在线观看| 亚洲内射少妇av| 成人亚洲欧美一区二区av| 国产视频内射| av又黄又爽大尺度在线免费看| 欧美激情国产日韩精品一区| 亚洲国产色片| 草草在线视频免费看| 欧美老熟妇乱子伦牲交| 老司机影院成人| 日韩精品有码人妻一区| kizo精华| 久久久久网色| 国产精品秋霞免费鲁丝片| 熟女av电影| 亚洲国产精品成人久久小说| 日本vs欧美在线观看视频| 不卡视频在线观看欧美| 国产精品一区www在线观看|