锅炉废气流化床污泥干化塔的热力计算与分析

*钱炜楼波510640120～190℃。12、3。、、。。DOI10.7617/j.issn.1000－8942.2013.04.020THETHERMODYNAMICCALCULATIONANDANALYSISOFCIRCULATINGFLUIDIZEDSLUDGEDRYINGTOWERUSINGWASTEGASFROMBOILERSQianWeiLouBoGuangdongKeyLaboratoryofCleanEnergyTechnologySchoolofElectricPowerSouthChinaUniversityofTechnologyGuangzhou510640ChinaAbstractTodrysewagesludgebyusingtheexhaustfumeoftheboiler120～190℃canreducemoisturecontentofsludgeforachievingsubsequentlyreasonableuse．Thedryingofsludgecanbeanalyzedinthreeaspects1Tostudyrelationshipsbetweenthedriedsludgeandquantityofsludgetreatment．2Tostudyrelationshipsbetweeninletgastemperatureorinletgasflowrateandquantityofsludgetreatment．3Tostudyinfluencedfactorofrelativehumidityofoutletgas．Theresultsshowthatquantityofsludgetreatmentcanbeimprovedifincreasingtheinletgastemperatureorgasflowrateoroutletwatercontentofsludge．Themoisturecontenthasahigherinfluenceonquantityofsludgetreatmentunderconditionsofhigherinletgastemperatureorgasflowrate．Whentheoutletmoisturecontentofsludgeishigherimprovingoutletgastemperaturecanimprovequantityofsludgetreatmentobviously．Wheninletgasflowrateishigherthequantityofsludgetreatmentcanbeincreasedobviouslyifimprovingtheinletgastemperature．Therelativehumidityofoutletgasisrelatedtoinletgastemperature．Therelativehumidityofthedriedgasisfarfromsaturatedstate．Therelativehumidityofoutletgashasmorespacetoincreasewithinthistemperaturerange．Keywordssewagesludgeboilerfluegascirculatingfluidizeddryingtowerheatcalculation*12C72081667。01。、。2、3、4。5。、。。6720138314、。、、。。。175%11578.6kJ/kg40%4000kJ/kg。130t/h120～190℃22162.48kJ/kg1。1Table1Ingredientofanthraciteblindcoalandfluegas%ωCarωHarωOarωNarωSarωAarωMarωCO2ωH2OωN2ωO2ωSO259.1620.80.80.526.310.4618.143.1571.047.050.084SA。7.87kg/s8.985m3/kg1.419kg/m3360t/h。21。95%40℃。5%。1Fig．1Flowchartofsewagewatersludge’drying33.1干化塔热平衡分析105℃。80℃。2。2Table2Parameterofmaterialandfluegasa/%75b/%0～70T1/℃25T2/℃80T3/℃120～190T4/℃105Q1=Q21Q1=M1h2－h1+M2Cp1T4－T1+M3Cp1T2－T1+M4Cp2T2－T12Q2=kM5Cp3T3－Cp4T43Q1、kJQ2kJM1kg/sM2kg/sM3kg/sM4kg/sM5kg/sh1h2kJ/kgk0.95Cp1=0.84kJ/kg·℃Cp2=4.1868kJ/kg·℃Cp3Cp4kJ/kg·℃G1G2G3M25%。3.2干燥后污泥含水率与污泥处理量关系360t/h7720138314T3b4G1=3421.0854T3－107.4100－b/194766－2559.7b42。20%～70%0%～40%40%。、6。30%～40%160℃1%0.127t。2。2Fig．2Relationcurveofmoisturecontentofoutletsludgeandquantityofsludgetreatment3.3入口烟温与污泥处理量关系360t/hb3。4。3。0%1℃0.1906t70%1℃0.575t。。3Fig．3Relationcurveofinletfluegas’temperatureandquantityofsludgetreatment3.4入口烟气流量与污泥处理量关系40%5G1=0.000603M51.085T3－107.38654。4。120℃1t0.01378t190℃1t0.0596t。。4Fig．4Relationcurveofinletfluegas’flowrateandquantityofsludgetreatment3.5干燥后烟气相对湿度影响因素872013831429.88g/mol7d=0.603pv/p6Φ=pv/p7Φ=1/1+1/G11.71－40.67/100－b/M5+0.0548360t/h。5、70%50%0%。5120℃6.4%190℃10.6%。5Fig．5Relationcurveofinletfluegas’temperatureandrelativehumidityofoutletgas41。2。3、、。440%120～190℃1℃0.058%。1．M．20051-26．2．J200228116-19．3NezihKamilSalihogluVedatPinarliGuraySalihoglu．SolardryinginsludgemanagementinTurkeyJ．RenewableEnergy200732101661-1675．4JohnBeckleySujitBanerjee．OperationalissueswithimpulsedryingsludgeJ．WaterScienceandTechnology19994011/12163-168．5．J．20051119[e-mail]2012－11－029720138314