工程百世1-設(shè)計集2abstract

Process Rawmaterial Clausdesulfurization Theexhaustgashydrogenationreduction Carbondisulfideproduction Energy-saving Heatexchangernetwork Methanemembraneseparation ntlocation& Netcash Estimationofstaticbenefit TheprojectistodesignasetofdesulfurizationequipmentfortheZRCC,andalsousingtheproduceofdesulfurizationtoproductcarbondisulfide.TheequipmentusesthegasbesidessulfurelementfromtheZRCCtomeetemissionsstandardsandproducttheproduce.Thisprocessincludesrawmaterialpretreatment,Clausdesulphurization,tailgashydrogenationreductionandsulfurmethanesynthesisfoursections.Thedesignprocesscontains202,000tonsofsulfur-containingwastegas,andtherecoveryofsulfuris72,000tonsperyear,producing85,000tonsperyearofcarbondisulfide,andtheisasfollows.高純高純原1120高純含水含水260260330Fig.1.1theoverallprocessflow Thisprocesscomprehensiveutilizationtothetotalsulfur-containingwastegasfromtheZRCC,thepretreatmentofrawmaterialsgathersthegas,thenwiththeoxygenenrichedairaccordingtotheproportionintotheClaussystemofdesulfurization,exhaustintothehydrogenationprocessafterreaction,thesulfurcomponentwillbeconvertedtohydrogensulfide,thenextusingthePCenrichthehydrogensulfideinposteriorcirculation.TheproducesulfurfromtheClaussectionisvaporizedandblendedwithnaturalgasintoareactortoproducecarbondisulfide.TheprojectwillbedeepdesulfurizationthegasfromtheZRCCtoemissionstandards,thenusestheproducttoproducethecarbondisulfide.Designedtodealwithsulfur-containingwastegas202thousandtonsperyear,sulfurrecovery72thousandtonsperyear,productionofcarbondisulfide85thousandtonsperyear.RawmaterialFig.2.1theprocessflowchartofrawmaterialInthissection,thesulfur-containingwastegasispressurizedbyamulti-stage(secondary)compressorafterpassingthroughaheatexchangersothatthefeedstockreachesafeedrateof40°Cand2.5MPaintotheabsorptiontower(T0101)whichusethepropylenecarbonatetoabsorbtheH2S,toensurethatH2SfullyabsorbedintheasmuchaspossibletoremoveCO2,fortheClaussectiontofacilitate.Towerexhauststomeettherequirements,aftertheflaresystemdirectlyemptied.ThebottomisrichinH2S-containingpropylenecarbonate.Richliquidgoesthroughapressurereducingvalveandaheatexchanger,to100℃,0.4MPafeedconditions,thenintothedesorptiontower(T0102)forfractionating.TheenrientgasofH2Sfromthetopofthetower,aftercompressedintothehydrogensulfidestoragetopreparefortheuseofClaussection.ThebottomofthetowerfortheysisofthePC,containingasmallamountofwater,intothewater-containingPC.ClausdesulfurizationFig.2.2TheprocessflowchartofClausdesulfurizationBurnerInthissection,thegasfromtheH2S reactswithoxygen-enrichedinproportiontotheoxygen-enrichedburner,andonethirdoftheH2SisoxidizedtoSO2byoxygen.Then,intotheoxygen-deficientcombustionfurnaceClausreaction,andtheCOShydrolyze,thereactionequationisasfollows.2H2S+SO2==S2+2H2OCOS+H2O==CO2+Aftertwostepsoftheburnersection,theoutletgasisdivertedthroughashuntvalve,90%ofthehightemperaturegasentersthewasteheatboilerforheatexchange,afterthemulti-stage(secondary)compressorpressuresothatthegasreaches1700.11MPa,andthenintothesulfurcondensertocondense,condensedliquidsulfurintotheliquidsulfurstorage,non-condensablegasandtheresthightemperatureabout10%blend,andthetemperatureisabout300℃aftermixing,intotheClaustherebyreducingthefollow-upequipmentvolume,reduceequipmentcosts.ThefirstClausInthissection,theoutletgasoftheburnersectionisdivertedthroughtheshunt,70%ofthegasentersthefirstClaussection,andaftertheheatexchangerheatsupto330°C,entersthefirstClausreactorandcontrolsthecombustionfurnace.Theoxygen-to-airfeedrateofthesectionispreciselycontrolledbyafeedratioofH2StoSO2isThemainreactionsaretheClausreactionandthehydrolysisreactionofCOS,thereactionequationis.2H2S+SO2==S2+2H2OCOS+H20==H2S+Theoutletgasispressurizedto0.11MPabythecompressor,condensedintothesulfurcondenser,condensedliquidsulfurintotheliquidsulfurstorage,andnon-condensablegasismixedwith30%ofthehightemperaturegasoftheotheroutletofthediversionvalve.ThetemperatureisAbout200℃aftermixingandthenintothesecondClaussection.ThesecondClausTheexhaustgasfromthefirstClaussectionisheatexchangedto260°Candthenequationis:2H2S+SO2==S2+Theoutletgasispressurizedto0.11MPabyacompressorandcondensedinthesulfurcondenser,thentheliquidsulfurintotheliquidsulfurstorage,andnon-condensablegasenterstheexhaustgashydrogenationreductionsection.TheexhaustgashydrogenationreductionFig.2.3TheprocessflowchartoftheexhaustgashydrogenationreductionTailgashydrogenationInthissection,theexhaustgasfromthesecondClaussectionthroughapressurereducevalveandheatexchanger,thenintotheadiabaticflashtocondensethewater,andthenon-condensablegasthroughtheheatexchangertoexchangethetemperatureto260℃,sothatcandirectlyintothehydrogenationreactorforhydrogenation,thereactionequationis.SO2+3H2==H2S+2H2OCOS+H2O==H2S+CO2CS2+2H2O==2H2S+TheoutletgasfromthehydrogenationreactorenterstheH2SenrientsectionExhaustgasH2S entThehydrogenationreactoroutletgasispressurizedbyamulti-stage(secondary)compressorafterheatexchangebyaheatexchanger,followedbyanadiabaticflash.AfterthedehydrationofthegasintotheH2Sabsorptiontower(T0401)toabsorb,afterthePCabsorbedtheexhaust,aftertheflaresystemtomeetthedischargestandards,canbedirectlyemptying.Absorbentsolutionthroughthepressurereducevalve,heatexchangerheattransferto52℃,0.12MPafeedconditions,thenintothedesorptiontower(T0402)forfractionating.ThetopoftheH2SgasispressurizedbythecompressorandpassedintotheH2S.BottomwithasmallamountofwaterPCsolution,intothewater-containingPCstorage.PCdehydrationMaterialsfromthewater-containingPCstorage,throughtheheatexchangerheattransferto50℃,intothedehydratedtower(T0403)fordehydration.Thebottomofthehigh-purityPCsendintothehigh-purityPCstorageforrecycling.ThegasfromtopofthetowercontainsasmallamountofPC,emptiedbytheflaresystem.CarbondisulfideproductionFig.2.4TheprocessflowchartofthecarbondisulfideproductionInthissection,thesulfurfromtheliquidsulfurstorage,throughtheheatexchangertovaporizeintotheflash.ThesulfurforminthehightemperatureisS2asthesameascontrolthefeedtemperatureatabout700℃.Naturalgasispressurizedto1.5MPabythecompressor,intotheheatexchangerheatto200℃.ThegaseoussulfurismixedwithnaturalgasintotheCS2reactorforreaction.Topreventmethanefromcoking,thenaturalgasiscontrolledfromthecenterofthereactiontube,andthegaseoussulfurisfedfromtheedgeofthereactiontubeandthereactiontemperatureiscontrolledat650°C.Reactoroutletgasthroughtheheatexchanger,thenintothesulfurcondenser,recyclingtheliquidsulfurintothesulfurstorageNon-condensablegasispressurizedbythecompressorpressure,andthenthroughtheheatexchangerintothecondensercondensation,thematerialreached14.4℃(bubblepointtemperature),2.5MPafeedconditions.thenintothedesorptiontower(T0301)forfractionating.Thebottomproductsofthehigh-purityCS2thenintothecarbondisulfideproductstorage.ThetopofthetowerforthehighconcentrationisH2Sgas,thencompressorpressureintotheH2S ,topreparefortheuseofClausEnergy-savingHeatexchangernetworkFig.3.1OptimizationofthedesignbeforetheThisprojectinvolvedinmanyUtilities.InordertomakefulluseofEnergy,thisprojectbyusingtheAspenEnergyyzersoftware,accordingtothepinchandthresholddesignmethod,combinedwiththeactualsituationofthefactoryequipmentarrangement,inmeetingthedesigngoalutilitycostminimumandequipmentcostminimum,undertheconditionofthevariousprocessflowsandheatofthematchingbetweentheutility,designedakindofoptimummatchingschemeofcoldandhotflowstocks.MoredetailswillbeshownintheAspenprocesssimulationsourcefilesandPIDdrawings.Theheatexchangernetworknumberis29,accordingtotheminimumprincipleofheatexchangerunits,removedanumberofheatexchangers,suchasheatexchangerenergyisverysmall,evencloseto0kJ/h,whichtheheatexchangersarenotreasonablesothatcanberemoved.Fig.3.2TheheatexchangernetworkafterThenumberofheatexchangersrequiredfortheoptimizedheatexchangernetworkis16,include6heatexchangers,afterthatthestructureismorestreamlined,andtheenergyconsumptioncanbesavedby34.36%.Table3.1UtilityThecoldThehotTheamountofbeforeTheamountofafterSavingMethanemembraneseparationTable3-2PermeationrateofgasmoleculesinasymmetriccompositemembranesofPolyimide((30℃)SerialPermeationrate123456Weusedthesoftwaretosimulatethemembraneseparationprocess,andthedetailsinformationasfollows.Theprogramclc;clear%逆流接觸的模型_membraneseparatorna(1)=516.3832;nb(1)=ni(1)=271874; forR=na(N)/na(1)%甲烷的分離比TheRR_2hydrogen_1hydrogen=458.0187xishouji_1=5.8043e+05xishouji=8.4569e+03Theresultsof showthatwhentheeffectiveareais3900m2,thepolyimidefilmcanachieveseparationeffect.ntlocation&ThisfactorywillbelocatedinZRCC.Consideringthetopographyandgeologicalstructureofthentandthenatureandcharacteristicsoftheproductandthetechnologicalprocessoftheproject,thelayoutof