hdpe technology - mol.hu l_roviden... · pdf filetotal fixed cost 31 27 27 30 31 total...
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![Page 1: HDPE Technology - mol.hu l_roviden... · PDF fileTotal fixed cost 31 27 27 30 31 Total cash cost 1529 1471 1456 1485 1477. USD/t. 80% 85% 90% 95% 100% LLDPE LLDPE HDPE HDPE HDPE](https://reader033.vdocuments.mx/reader033/viewer/2022042708/5a7875d87f8b9a1f128b4f3e/html5/thumbnails/1.jpg)
HDPE TechnologyHDPE TechnologyIncluding MDPE and LLDPEIncluding MDPE and LLDPE
20102010
ElElőőadadóó: : ÁÁddáám Csabam Csaba
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ContentContent
HDPE, MDPE and LLDPE HDPE, MDPE and LLDPE –– linear linear polyethylenespolyethylenesApplicationApplicationHistoryHistoryCatalystsCatalystsHDPE processesHDPE processesProcess controlProcess controlProcess safetyProcess safetyKey equipmentKey equipmentInvestment costInvestment costCost of productionCost of production
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The Linear Polyethylene FamilyThe Linear Polyethylene FamilyHDPE, MDPE, LLDPEHDPE, MDPE, LLDPE:: linear polyethyleneslinear polyethylenesClassification by density Classification by density –– determined by short chain branchingdetermined by short chain branching through through comonomer contentcomonomer content
PropertiesPropertiesMelt indexMelt index 0,03 0,03 -- >100 g/10 min (190 C/2,16 kg)>100 g/10 min (190 C/2,16 kg)Melting pointMelting point 120120--140 C140 CPolydispersityPolydispersity (TVK (TVK gradesgrades))
MonomodalMonomodal 66--88BimodalBimodal 1010--2020
0,915 0,926 0,940 0,970
No of SCB
LLDPEMDPE
HDPE
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ApplicationApplicationHDPE/MDPEHDPE/MDPE
LLDPELLDPE
Film77%
Extrusioncoating
6%
Injectionmoulding
5%
Other12%
Film16%
Fiber2%
Blowmoulding
36%
Injectionmoulding
20%
Pipe22%
Other4%
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Application by Application by PropertiesProperties
0,01
0,1
1
10
100
0,890 0,900 0,910 0,920 0,930 0,940 0,950 0,960 0,970
Narrow MWD
Medium MWD
Broad MWDLLDPE
INJECTIONMOULDING
LLDPEBLOWN & CASTFILM MDPE
YARNFILAMENTS HDPE
BLOW MOULDING
HDPEFILMPIPES
HDPEINJECTIONMOULDING
MFR
(g/1
0 m
inM
FR (g
/10
min
))
DensityDensity (g/cc)(g/cc)
LLDPE-MDPE-HDPEWIRE AND CABLE(Medium to broad MWD)
MDPEROTOMOULDING
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HistoryHistoryHDPE discovered in 1951 by P. Hogan and R. BanksHDPE discovered in 1951 by P. Hogan and R. BanksMid 1950s: commercial HDPE production in slurry process Mid 1950s: commercial HDPE production in slurry process (Hoechst) and solution process (Phillips Petroleum)(Hoechst) and solution process (Phillips Petroleum)1961: slurry loop reactor technology by Phillips Petroleum1961: slurry loop reactor technology by Phillips Petroleum1968: first gas phase process by Union Carbide1968: first gas phase process by Union CarbideMid 1970s: first LLDPE process by Union CarbideMid 1970s: first LLDPE process by Union CarbideVarious processes available up to 400 kt/y capacityVarious processes available up to 400 kt/y capacityGlobal consumptionGlobal consumption, 2009, 2009
HDPE/MDPEHDPE/MDPE 30 million t/y30 million t/yLLDPELLDPE 1919,2,2 mimilllion t/ylion t/y
TVK HDPE plantsTVK HDPE plants1986: Phillips slurry loop process 140 kt/y, debottlenecked to 11986: Phillips slurry loop process 140 kt/y, debottlenecked to 190 kt/y90 kt/y2004: Mitsui slurry, cascade reactor technology 200 kt/y 2004: Mitsui slurry, cascade reactor technology 200 kt/y
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CatalystsCatalystsChromiumChromium
Silica supported hexavalent CrSilica supported hexavalent CrActivation at high temperature before useActivation at high temperature before useCocatalyst not necessaryCocatalyst not necessaryMedium to broad molecular weight distributionMedium to broad molecular weight distribution
Ziegler(Ziegler(--Natta)Natta)MgClMgCl2 2 supported TiClsupported TiCl44Metal alkyl cocatalyst necessaryMetal alkyl cocatalyst necessaryNarrow molecular weight distributionNarrow molecular weight distributionPreferred for bimodal products in cascade reactor technologyPreferred for bimodal products in cascade reactor technology →→very broad MWDvery broad MWD
Metallocene (single site)Metallocene (single site)Still developingStill developingCocatalyst necessaryCocatalyst necessaryVery narrow molecular weight distributionVery narrow molecular weight distributionBimodal capability in single reactor technologyBimodal capability in single reactor technology
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Processes and ProductsProcesses and Products
Gas phaseGas phaseprocessesprocesses
SolutionSolutionprocessesprocesses
SlurrySlurryprocessesprocesses
HD
PE/
MD
PE
LLD
PE
Loop slurry only
High quality film grades
Best for blow moulding
and pipe grades
Melt index limit
with density limit
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Gas Phase ProcessGas Phase Process PolymerizationPolymerization
Gas phase process
85-110 C
20-25 bar
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Gas Phase ProcessGas Phase Process Additivation and PelletizingAdditivation and Pelletizing
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GasGas PhasePhase ProcessesProcesses CharacteristicsCharacteristics
CatalystCatalyst: : chromiumchromium, , ZieglerZiegler, (, (metallocenemetallocene))FluidizedFluidized bedbed reactorreactor
7070--110 C110 C1515--30 bar30 barLong Long residenceresidence timetime
SwingSwing technologytechnology: LLDPE : LLDPE –– HDPE HDPE capabilitycapabilitySimpleSimple processprocess designdesignLowLow investmentinvestment and and operatingoperating costcostBimodalBimodal capabilitycapability withwith twotwo reactorsreactors
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Solution ProcessSolution Process
150-250 C30-100 bar
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Solution ProcessSolution Processeses CharacteristicsCharacteristics
CatalystCatalyst: : ZieglerZiegler, (, (metallocenemetallocene))PolymerisationPolymerisation takestakes placeplace inin solutionsolution
3030--130 bar130 bar150150--300 C300 CShortShort residenceresidence timetime
BroadBroad productproduct rangerange: LLDPE : LLDPE –– HDPEHDPEBimodalBimodal capabilitycapability withwith cascadecascade reactorsreactorsHigherHigher investmentinvestment and and operatingoperating costcost
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ChevronChevronPhillips Slurry Loop ProcessPhillips Slurry Loop Process
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ChevronChevronPhillips Slurry Loop ProcessPhillips Slurry Loop Process CharacteristicsCharacteristics
CatalystCatalyst: : chromiumchromium, , ZieglerZiegler, (, (metallocenemetallocene))Chromium catalyst activationChromium catalyst activation
Fluidized bed activator Fluidized bed activator Heat treatment in air at 600Heat treatment in air at 600--870 C870 C
Reaction in loop reactorReaction in loop reactor8585--105 C; 42 bar105 C; 42 bar33--6 % ethylene concentration6 % ethylene concentrationIsobutane diluentIsobutane diluentHeat removed by coolantHeat removed by coolant inin reactor jacketreactor jacket –– very good very good surface/volume ratiosurface/volume ratio
Flash separationFlash separation10 bar; 80 C10 bar; 80 C
DegassingDegassing85 C; 0,1 bar85 C; 0,1 bar
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PhillipsPhillips ProcessProcess atat TVKTVK PolymerisationPolymerisation
CirculatingPump
Hexene-1Comonomer
Ethylene
Cat
alys
t
Hexene-1Purification
EthylenePurification
Isobutane Distillationand Purification
EthyleneCompressor
Flash GasCompressor
Flash GasFilterFlash
Tank
Dryer
Isobutaneand NitrogenRecovery Unit
Purge Column
Settling Legsand ProductTake off Valves
Loop Reactor
Powder silo
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PhillipsPhillips ProcessProcess atat TVKTVK AdditivationAdditivation
and and PelletizingPelletizing
Extruder hopper
Additiveblender
Premix feeder
Main feeder
CIM
Extruder
Dewateringscreen
Spin dryer
Classifier
Pellet watertank
Rotaryfeeder
Air blower
Pellet waterpump
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Slurry ProcessSlurry Process CSTRCSTR--
Cascade Stirred ReactorCascade Stirred Reactor
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Slurry ProcessSlurry Process –– CSRTCSRT Reactor and SurroundingReactor and Surroundingss
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Slurry ProcessSlurry Process -- CSTRCSTR Process CharacteristicsProcess Characteristics
CatalystCatalyst: : ZieglerZiegler, (, (metallocenemetallocene))Low reaction pressure and temperatureLow reaction pressure and temperature
66--88 bar, 70bar, 70--90 C90 C
Reaction heat removed byReaction heat removed byOverhead condensatorsOverhead condensatorsSlurry coolersSlurry coolersReactor jacketReactor jacket
Bimodal product capabilityBimodal product capabilityDifferent molecular weight polymer in 1st and 2nd reactorDifferent molecular weight polymer in 1st and 2nd reactorComonomer built into high molecular weight polymerComonomer built into high molecular weight polymer
Diluent and polymer separation by centrifugeDiluent and polymer separation by centrifugeDiluent cleaning for low polymer removalDiluent cleaning for low polymer removal
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Process ControlProcess ControlMelt indexMelt index
Ziegler catalystZiegler catalyst[H[H
22
]/[Et]]/[Et]↑↑
MI MI ↑↑Chromium catalyst: T, Chromium catalyst: T, [Et], [H[Et], [H22]]
T T ↑↑
MI MI ↑↑[Et][Et]↑↑
MI MI ↓↓
[H[H
22
]]↑↑
MI MI ↑↑DensityDensity
[comonomer] [comonomer] ↑↑
D D ↓↓Molecular weight distributionMolecular weight distribution
Catalyst typeCatalyst typeReactors operated at different parametersReactors operated at different parameters
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Process SafetyProcess SafetyRisk of high volume liquid hydrocarbonRisk of high volume liquid hydrocarbonInterlock systemInterlock system
Emergency kill to prevent reaction runawayEmergency kill to prevent reaction runaway –– except for CSRTexcept for CSRTAction valves automatically operated by predefined process Action valves automatically operated by predefined process parameters to separate/blowparameters to separate/blow--down equipmentdown equipment
Closed blowClosed blow--down systemdown systemPressure safety valves, blowPressure safety valves, blow--down valves release to closed down valves release to closed system, connected tosystem, connected toFlare to burn blown hydrocarbonFlare to burn blown hydrocarbon
Double mechanical seal on pumps in liquefied gas Double mechanical seal on pumps in liquefied gas serviceserviceGas detectorsGas detectorsFire fighting systemFire fighting system
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Key EquipmentKey Equipment
ReactorsReactorsLoopLoop with axial circulating pumpwith axial circulating pumpGas phaseGas phase
Decanter centrifuge Decanter centrifuge –– in CSin CSTRTR onlyonlyExtrusion lineExtrusion line
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ReactorsReactorsLoop reactorsLoop reactors
Long jacketed pipe Long jacketed pipe –– straight vertical sections straight vertical sections interconnected by elbows at top and bottominterconnected by elbows at top and bottomBuilt in axial pump to circulate slurryBuilt in axial pump to circulate slurryGood surface to volume ratio Good surface to volume ratio –– easy reaction heat easy reaction heat removalremoval
Gas phase reactorsGas phase reactorsVertical pressure vessel with increased top section to Vertical pressure vessel with increased top section to reduce polymer carry overreduce polymer carry overLong residence timeLong residence timeReaction heat removed by external heat exchanger in Reaction heat removed by external heat exchanger in recycle gas streamrecycle gas streamDifficult reaction controlDifficult reaction control
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Loop Reactor Circulating Loop Reactor Circulating PPumpump
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Decanter CentrifugeDecanter Centrifuge
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CMP Extrusion Line ArrangementCMP Extrusion Line Arrangement
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CMP ElementsCMP Elements
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Mixing in CMPMixing in CMP
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InvestmentInvestment CostCost BasisBasis: USGC 2008Q1; 400 : USGC 2008Q1; 400 ktkt
Technology Solution Gas phase Gas phase Slurry loop Slurry CSTRProduct LLDPE LLDPE HDPE HDPE HDPE
ISBL 126,4 93,8 94,7 114,1 126,8OSBL 115,3 102,6 102,7 113,7 116,4Other project cost 131,3 116,5 114,2 123,9 127,3Total investment 373 312,9 311,6 351,7 370,5
Specific investment, USD/t 933 782 779 879 926
million USD
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CostCost of of ProductionProduction BasisBasis: USGC 2008Q1; 400 : USGC 2008Q1; 400 ktkt
Technology Solution Gas phase Gas phase Slurry loop Slurry CSTRProduct LLDPE LLDPE HDPE HDPE HDPE
Ethylene 1223 1222 1326 1324 1334Comonomer 176 159 25 24 25Catalysts&Chemicals 47 14 27 42 22Additives 13 15 18 18 18Total raw materials 1459 1410 1396 1408 1399
Power 15 22 25 30 26Steam 16 2 2 6 13Other utilities 8 10 6 11 8Total utilities 39 34 33 47 47
Variable cost 1498 1444 1429 1455 1446
Direct cash cost 14 12 12 14 14Allocated cash cost 17 15 15 16 17Total fixed cost 31 27 27 30 31
Total cash cost 1529 1471 1456 1485 1477
USD/t
80%
85%
90%
95%
100%
LLDPE LLDPE HDPE HDPE HDPE
Solution Gas phase Gas phase Slurry loop Slurry CSTR
Total f ixed cost
Total utilities
Total raw materials
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Spring Rotary SealRing
Stationary SealRing
Rotary SealPacking
Stationary SealPacking
Appendix: Typical Mechanical Seal
Product
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Appendix: Appendix: Blow MouldingBlow Moulding
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Appendix: Pipe Appendix: Pipe ExtrusionExtrusion