Zinc Oxide Desulfurization Adsorbent, Catalyst

Zinc Oxide Desulfurization Adsorbent, Catalyst
ZincOxideDesulfurizationAdsorbentHL-305iswidelyapplicabletofeedstockpurificationprocessesinproduction
ofhydrogen,ammonia,alcoholsandorganicchemicals.Itcanremovehydrogensulfidefromvariousfeedgases
(oils)toaslowaslessthan0.1ppm.
Mainreactionofthedesulfurizationprocessisasfollows:
H2S+ZnS=ZnS+H2O
TheadsorbentalsoiscapableofconvertingandabsorbingsimpleorganicsulfursuchasCOSandCS2
AdsorbentT305ishighlyadaptable.Itcanworkinsevereconditionswithhighsulfurabsorptioncapacity,high
activity,highstrength,goodsustainabilityforactivityandsulfurabsorptioncapacity,andgoodtolerancetohigh
steamtogasratio.Itcanobtainsatisfactoryoperationresultsbothathigher(about400°C)andlower(about200°c)
temperature.
CompositionandPhysicalProperties
Appearance
whiteorlight-grayextrusions
Particlesize,mm
Φ4mmx4-10mm
Bulkdensity,kg/l
1.1-1.3
lossOnIgnition,%
max2
Zincoxidecontent,%
min95
QualityStandard
lossonabrasion,%
max6
Breakthroughsulfurcapacity,%
min20(220°C)
min30(350°C)
NormalOperationCondition
Feedstock:lightoil,residuecrackinggas,naturalgas,synthesisgas,coalgasandshiftedgas,withrecommendedhydrogensulfideconcentrationoflessthan250ppm.
Pressure,MPa
ambientto4
Temperature,°C
200~400
Steam/feedgas
1~1.5ordrygas
Spacevelocity,h-1
1000~3000(gas)
1~6(liquid)
Sulfurinprocessedstream,ppm
<0.1
Poisons
Oxygen:oxygencontentinfeedgas(oil)shouldnotexceed0.5%.Excessiveoxygenmaylowerbreakthroughsulfur
capacityoftheadsorbent.
Chlorine:Chlorinepresenceinanystatewillaffectdesulfurizationresult.
Loading
Loadingdepth:recommendedloadingdepth/reactordiameterratiois3,soastoensureenoughresidencetimeofthegasesinthebed.Configurationoftworeactorsinseriescanimproveutilizationefficiencyoftheadsorbent.
Loadingprocedure:
(1)Cleanthereactorbeforeloading;
(2)Screentheadsorbenttoremovedust;
(3)Loadalayerofrefractoryspheresatbothtopandbottomoftheadsorbentbed.Therefractoryisseparatedfromtheadsorbentbystainlessnetswithmeshsizesmallerthantheadsorbent;
(4)Usespecialtooltoensureevenlydistributionoftheadsorbentbothinthecenterandaroundtheinnerwall;
(5)Inspectuniformityofthebedduringloading.Wheninner-reactoroperationisneeded,Awoodplateshouldbeputontheadsorbentfortheoperatortostandupon.
(6)Astainlessnetanda50mmlayerofrefractoryspheresshouldbeinstalledatthetopoftheadsorbentbedsoas
toprevententrainmentoftheadsorbentandensureevendistributionofthegasstream.
Start-up
(1)Replacethesystembynitrogenorotherinertgasesuntiloxygenconcentrationinthegasislessthan0.5%;
(2)Preheatthefeedstreamwithnitrogen,purgegasorsynthesisgasunderambientorelevatedpressure;
(3)Heatingspeed:30-50°C/hfromroomtemperatureto120°C,120°Cfor2h,50°C/hover120°Cuntilrequiredtemperatureisattained.Keepatthetemperaturefor4h.
(4)Elevatethepressureat0.5MPa/10minduringthethermostaticstepsuntiltheoperationpressureisattained.
(5)Afterpre-heatingandpressureelevation,thesystemshouldbeoperatedathalfloadtoregulatetemperature,
pressureandflowrate.Thenraisetheloadsteadilywhenoperationbecomesstabletillfull-scaleoperation.
(6)Ifpressureelevationisdonepriortopre-heating,carefulcontrolisneededinaccordancetotheprocedureabove.
Rapidtemperaturerisemaycausestressandresultinpulverizationoftheadsorbent.