气液分离器设计计算

CHEMICALENGINEERINGDESIGN2011215*124010。《》GB50350－2005《》SY/T0515－2007①②③、。50μm。K1K2、K3K41。。。。11.121。1、、。。1.234。。。FG=MPρL－ρVggcρVFD=π/8CDD2PUV2ρVgcUTUT=4gDPρL－ρV3CDρVUV＜UT。UV=0.75UTSaud-ers-BrownUT=KρL－ρVρ槡V81*。2007。。[e-mail]。＊＊“”2009ZX05039。2011215K=4gDp3C槡D。。K。K。K1。KK。CD1。1KK1≤P1≤15K=0.1821+0.0029P+0.0460lnP15≤P1≤40K=0.3540≤P1≤5500K=0.430－0.023lnPGPSA0≤P2≤1500K=0.35－0.01P－100/100K=0.20K'=0.6～0.8KK'=K/2、、K'=0.7～0.8KK=4gDp3C槡DCD=expYY=8.411－2.243X+0.273X2－1.865E－2X3+5.201E－4X4X=ln0．95+8ρVDPρL－ρVμV21.31NLLLLL。2NLLHLL。LLLHLL。。。。1.4DVD=4QVπU槡VDVD。DVD6inDD。1。HT=HLLL+HH+HS+HLLN+HD。1.51。LLLNLLHLL。HLL。。VH+VS=LAT－AVD+ALLL。AVD1～2ft20%。。。LUAH≥HVUT291CHEMICALENGINEERINGDESIGN2011215。。。2.11UT=KρL－ρVρ槡Vft/sUV=0.75UT1KQV=WV3600ρVft3/s2DVD=4QVπU槡Vft3～6in6in。3QL=WL60ρLft3/minVH=THQLft34VS=TsQLft32。2ftLLLin＜300psia＞300psiaLLLin≤415696156108156111066121266131666155HH=VHπ/4DV2ft1ft。6HS=VSπ/4DV2ft6in。7HLIN=12+dNHLIN=12+1/2dNdn≥4Qmπ60/ρ槡m0.5Qm=QL+QVft3/sρm=ρLλ+ρV1－λlb/ft3λ=QL/QL+QV8①②HD=0.5DVHD=36+0.5dNinHD=24+0.5dNin。96in1ft。10HTHT=+HLLL+HH+HS+HLIN+HD+HMEftHME9HME=0。2.22.2.11QV=WV3600ρVft3/sQL=WL60ρLft3/min2UV=0.75UTUT=KρL－ρVρ槡Vft/s3VH=THQLft34VS=TSQLft35L/D2D=4VH+VS0.6πL/D1/3ft0.5ftAT=πD2/40220112152HLLL=0.5D+7inDft。D≤4'HLLL=9in。63HLLL/DALLL/ATALLL。3YabcdefghiA－4.755930×10－53.9240910.174875－6.3588055.6689734.018448－4.916411－1.801705－0.145348B0.0015375626.7871013.299201－22.92393224.353518－14.844824－36.99937610.5295729.892851①Y=4.755930×10－5－0.174875X+5.668973X2－4.916411X3－0.145348X41+3.924091X－6.358805X2+4.018448X3－1.801705X4②AH/D→A/ATHv/D→Av/ATy=A/ATx=H/D③BA/At→H/DAv/AT→Hv/Dy=H/Dx=A/At7AV0.2D1ft。0.2D2ft。HV0.2D2ft1ft。HV/DAV/ATAV。8L=VH+VS/AT－AV－ALLLft9=HV/UVsUVA=QV/AVft/s10LMIN=UVAft11L＜LMINL=LMIN。LLMINHV7。L＞LMIN。LLMINHVLLMIN。7HVHV7。L/DL/D＞6.0D6。L/D＜1.5D5。12。136in。1.5＜L/D＜6.0。143ANLL=ALLL+VH/LHHLL=D－HV2.2.2、1s=PD2SE－1.2P+tcin2S=πDLft23s=PD2SE－0.2P+tcin4S=1.09D2ft25s=PD4SE－0.4P+tcin6S=1.571D2ft27s=0.885PD4SE－0.1P+tcin8S=0.842D2ft29W=490tAS+2AH12lbPpsig+15～30psi10%～15%TT＞200+25～50T＜200250t12CHEMICALENGINEERINGDESIGN2011215in。34。4×104m3/d/MPa/℃mm15300.05/0.50～20/55D3227×97002300.05/0.50～20/55D1219×21342300.05/0.50～20/55D1600×45002。4。。41《》《》。2、、、。3《》《》。Aft2ALLLft2ATft2Avft2AVDft2CDDftinDPftdNinDftinDVDftDvftEFDlbfFGlbfg32.17ft/s2Hftgc32.17lbm/ft/lbfs2HDftHHftHLftHLINHLLLftHMEftHSftHTftHvftKft/sLftLMIN/ftMPlbfPpsigpsiaQLft3/minQMft3/sft3/minQVft3/sft3/minSpsiTHminTSmintcinthintsinUAHft/sUTft/sUMft/sUVft/sUVAft/sVHft3VLLLLLLft3VSft3VTft3WlbmλμvcPρLlb/ft3ρMlb/ft3ρvlb/ft3sθminλ2522201121590%、。3。3kt/a4046704370.83991.63542.33165.65106.84760.73、。3.2.2670kt/a2040kt/a、。4。41774kt/a1370kt/a+670kt/akg/h4205044630kg/h3962455430kg/h－4653－4296m3/h598538kW24882224MW64.7940.33MJ/h533008.79504105.03①②《》MJ/h。4670kt/a。3.2.348333020。1/3。1400kt/a670kt/a。4190%、、。C9A、。2C9A、C7A、。1．P.CN01131953.42001－10－22．2011－06－14檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪檪22HLLLHLLLLLNLLMV1GB50350－2005S．2005．2SvrcekW．Y．andMonneryW．D．．DesignTwo-PhaseSep-aratorsWithintheRightLimitsJChemicalEngineeringPro-gress1993October53－60．3．1M．199335－37．4DEP31．22．05．11－Gen．Gas/LiquidSeparators-TypeSe-lectionandDesignRules．DesignandEngineeringPracticeUsedbyCompaniesoftheRoyalDutch/ShellGroup．19969－10．5SY/T0515－2007S．2008．2011－02－07522011215ABSTRACTSOFCHEMICALENGINEERINGDESIGNABSTRACTSProbeonFeedstockRouteofMethanolProductionfromNaturalGasandCoalZhouFang，etal(ChinaChengdaEngineeringCo．，Ltd．，Chengdu610041)Introducetheprocessprincipleofthehydrogenandcarbonbeingcomplementaryinco-productionofmethanolfromnaturalgasandcoal，comparetheprocessflows，rawmaterialconsumptions，coalgasshiftrates，CO2emissions，powerconsumptions，investmentsandeconomiesamongthemethanolproductionfromnaturalgasorcoalandtheco-production，andpointoutthattheco-productionfromnaturalgasandcoalcanbecomplementaryforhydrogenandcarbon，andminimizethecoalgasshiftrate．Theco-productionfromnaturalgasandcoalhascertainadvantageovertheotherprocessesinboththerawmaterialandpowerconsumption，CO2emissionandtheinvestmentandeconomics，andisabetterfeedstockrouteformethanolproduction．Keywordsco-productionfromnaturalgasandcoalmethanolprocesscomparisonTypeSelectionofTrayforCO2AbsorptionTowerinLowTemperatureMethanolPurificationProcessZhangXin，etal(LanzhouBranchofBeijingAerospaceWanYuanCoalChemicalEngineeringTechnologyCo．，Ltd．，Lanzhou730050)DeterminethetypeoftowertrayinvarioussectionoftheCO2absorptiontowerbyusingthethermodynamicmodelandthegeneralprocessingsimulationsoftwaretosimulatetheCO2absorptiontowerdividedintothreesections．KeywordslowtemperaturemethanolpurificationprocessCO2absorptiontowerBDHMVGConsiderationofFlareSystemDesigninLarge-scalePetrochemicalComplexWuDengzhong(ChinaHuanqiuContracting＆EngineeringCorporation，Beijing100029)Flaresystemdesignisanimportantpartofthepetrochemicalcomplex，whichhasabearingonthesafe，long-timestableoperationforthecomplex．Thisarticlediscussesthedesignconsiderations，theparameterstobedeterminedandtheproblemstobepaidattentionfromthedesignreality．Keywordspetrochemicalindustryflaredesignmainpointfl