中國工程熱物理學 燃燒學術會 編號，*，，，石月（山東理工大學交通與車輛，山東淄博 ,E- 摘要為了研究運行參數對甲烷氧化過程的影響，利用自行搭建的雙反應室煤礦乏風預熱催化氧化增大；隨濃度的增加，甲烷的反應速率加快；溫度對甲烷的氧化反應有較大影響，溫度升高ExperimentalStudyonVentilationAirMethaneCatalyticOxidationReactorwithTwo-reactionSunJuanjuan,LiuYongqi,SunPeng,ZhengBin,Shi(SchoolofTransportationandVehicleEngineering,ShUniversityofTechnology,Zibo ( ,E- :Tostudytheeffectofoperationparametersonmethaneoxidationprocess,experimentalstudywasdownontheventilationairmethanepreheatingcatalyticoxidationdevicewithtwo-reactionchamber,andtheheatlossofeachcatalyticceramiclayerwascalculated.Theresultsshowthattheheatlossofoxidationbedgrowwiththetemperaturerisingandthechangeofthelastcatalyticceramiclayerwasobviously.Withtheincreaseofspacevelocity,themajorzoneofmethaneoxidationmovetotheendofoxidationbedandtheeffectivereactionlengthextendgradually.Themethanereactionsspeedupwiththeincreaseofintakemethaneconcentration.Theinletgastemperaturehasagreatinfluenceonmethaneoxidation,asthetemperaturerise,theeffectivereactionlengthshortendramatically.:ventilationairmethane,preheatingcatalyticoxidation,oxidationbed,methaneoxidationprogress向機構，操作復雜，對可靠性要求較高，使得其在工業上的推廣受到限制[3-5]山東理工大學自主研發的雙反應室煤礦乏風預熱催化氧化裝置[7-8]，將兩個反應器12000（標況，其系統組成主要包括供氣系統、預熱系統、加熱啟動系統、反應室和數據采乏風分別從不同的進入反應后在同一個出口排出催化氧化床由3層負d0.7g/100m的立方體；系統為自行設計的C控柜，實現對進氣流量、進氣甲烷體積分數和溫度與。進氣流量采用孔板流量計進量，測量范圍250~2500Nm3/h；進氣甲烷濃度測量RBRJ2KN0~4%0.001%；溫度測量采K42所示，1處，溫度取為截面各測點的平均值。乏煙

(a)(b)1Fig.1VAMpreheatingcatalyticoxidationreactorwithtwo-reaction反應室一

123 432

50100100

1001001002Fig.2ExperimentalarrangementoftestedsectionsandsectionaltemperatureQ散i=qvcp1iT1icp2iT2i

式中，Qii（i=1~3）層陶瓷的散熱量，kJ/h；ρ1.22kg/m3；qvcp1i、cp2i分別為第i層陶瓷、出口截面空氣定壓比熱容，kJ/(kg?K)，按三次多項式pc0.39109T30.85106T20.365103Tp

1%Q放i=Q散iqvcp2iT2icp1iT1i式中，Qii（i=1~3）層催化陶瓷中甲烷的氧化放熱量，kJ/h

VQ放i

式中，Vii層催化陶瓷的甲烷氧化量，m3/h；q35900kJ/m3（SV（T0，1所示。

1Table1Specificoperationconditionsofevery運行參 工 3800h-1、5400h-1、7100h-1、8100h- 3（a40kW6000h-1、甲烷濃度0.8%。圖中可以看出，兩種狀態下，兩個反應室軸向溫度分布規律均相同，且1%

0

x

0

x（a）預熱完 （b）自維持狀3Fig.3Axialtemperatureoftworeactionchambersafterpreheatingandinself-heating40070045%，一、二層陶瓷的散熱6%，第二層陶瓷的散熱量要明顯小于其他兩層。從氧化床的結構可iiiiQQ

4Fig.4Theheatlossofcatalyticceramicmonolithchangewith，如圖LLccx

5Fig.5FittedcurvesofCH4concentration圖6為氧化床溫度530℃、甲烷濃度0.8%時，氧化床軸向溫度、甲烷濃度及160℃，甲烷濃度迅速下降，x>100mm區域內變化較小，說明甲烷的催化氧催化陶瓷的氧化已經幾近完全，300mm處的溫度略有下降，說明第三層催化陶瓷的散8100h-1200mm，甲烷氧化率略有下降。3800h-3800h-5400h-7100h-8100h-0Tc 0Tc 0 00

0

SV/h-（c）6Fig.6Theeffectsofspacevelocityontheaxialtemperature,CH4concentrationandeffectivelengthofoxidationbed圖7為氧化床溫度520℃、空速4630h-1時，氧化床軸向溫度、甲烷濃度及有氧化床的逐漸增大，且升溫區間主要集中在氧化床前端100mm距離內，甲烷濃度0.6%0.8%20mm。

000000000c0c00 0 0 0 0 0c（c）圖7甲烷濃度對氧化床軸向溫度、甲烷濃度和有效反應長度的影Fig.7TheeffectsofintakeCH4concentrationontheaxialtemperature,CH4concentrationandeffectivelengthofoxidationbed氧化床溫度的影速率逐漸加快，溫度由422℃升高至537℃時，第二層催化陶瓷的由30℃減小422260mm537105mm

0000c0c0000 TT0（c）圖8氧化床溫度對氧化床軸向溫度、甲烷濃度和有效反應長度的影Fig.8Theeffectsofintaketemperatureontheaxialtemperature,CH4concentrationandeffectivelengthofoxidationbed3結1%400700℃45%；3800h-197mm7000h-1后，有效反應長度變化加8100h-1200隨甲烷濃度的增大，氧化床增大，甲烷濃度0.8%時的比0.6%700.6%0.8%時，有20mm；隨氧化床溫度的升高氧化床升溫速率加快溫度由422℃升高至537時，第二層催化陶瓷的由30℃減小到3℃，甲烷的氧化反應變化明顯，主要氧260mm105mmShiSu,JennyAgnew.Catalyticcombustionofcoalmineventilationairmethane[J].Fuel,2006,K.Baris.Assessingventilationairmethane(VAM)mitigationandutilizationopportunities:AcasestudyatKozluMine,Turkey[J].EnergyforSustainableDevelopment,2013,17:13-23GosiewskiK,MatrosYS,WarmuzinskiK,etal.Homogeneousvscatalyticcombustionofmethane-airmixturesinreverse-?owreactors[J].ChemicalEngineeringScience,2008,63:5010-,,等.煤礦乏風的蓄熱逆流氧化[J].煤炭學報,2009,34(11):1475-ZhengBin,LiuYongqi,etal.Oxidationofcoalmineventilationairmethaneinthermalreverse-flowreactor[J].JournalofCoalSociety,2009,34(11):1475-1478D.Gao,S.Wang,C.Zhang,etal.MethanecombustionoverPd/Al2O3catalyst:EffectofChlorineandWateroncatalyticactivity[J].JournalofCatalysis,2008,29(12):1221-,劉瑞祥,王延遐,高振強,.煤礦乏風預熱催化氧化器[P].中國專利: U,2012-01-18LiuYongqi,LiuRuixiang,WangYanxia,GaoZhenqiang,ZhengBin.APreheatingCatalyticOxidationReactorforCoalMineVentilationAirMethane[P].Patent:CN U,2012-01-18,劉瑞祥,王延遐,,高振強.多反應室煤礦乏風預熱催化氧化器[P].中國專利: A,2011-10-LiuYongqi,LiuRuixiang,WangYanxia,ZhengBin,GaoZhenqiang.APreheatingCatalyticOxidationReactorforCoalMineVentilationAirMethanewithMultipleReactionChambers[P]. A,2011-10-,劉瑞祥,王延遐,,高振強.帶有燃燒器啟動的煤礦乏風預熱催化氧化器[P].中國專利: A,2011-10-26LiuYongqi,LiuRuixiang,WangYanxia,ZhengBin,GaoZhenqiang.APreheatingCatalyticOxidationReactorforCoalMineVentilationAirMethanewithBurnerStartup[P].Patent:CN ,,劉瑞祥,等.煤礦乏風預熱催化氧化裝置的起動性能[J].煤炭學報,2014,39(6):1084-ZhengBin,LiuYongqi,LiuRuixiang,etal.Startingcharacteristicsofventilationairmethanepreheatingcatalyticoxidationreactor[J].Journalof CoalSociety,2014,39(6):1084-1088孫金宇,,,等.煤礦乏風預熱催化氧化裝置的阻力特性實驗[J].中國煤炭,40(6):106-SunJinyv,LiuYongqi,ZhengBin,etal. characteristictestofcoalmineventilationairpreheatingcatalyticoxidationdevice[J].ChineCoal,2014,40(6):106-109毛明明,,,等.預熱催化氧化床溫度分布均勻性的研究[J].煤炭學報,40(1):109-MaoMingming,LiuYongqi,ZhengBin,etal.InvestigationofTemperaureDistributionUniformityinaPreheatingCatalyticOxidationBed[J].Journalof CoalSociety,2015,40(1):109-114杜德娟,,等.預熱催化氧化器的變參數模擬計算[J].山東理工大學學報(自然科學版2013,27(3):1-DuDejuan,LiuYon