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HDPE TechnologyHDPE TechnologyIncluding MDPE and LLDPEIncluding MDPE and LLDPE

20112011

22

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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33

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 S CB

LLDPEMD PE

HD PE

44

ApplicationApplicationHDPE/MDPEHDPE/MDPE

LLDPELLDPE

Film77%

Extrusioncoating

6%

Injectionmoulding

5%

Other12%

Film16%

Fiber2%

Blowmoulding

36%

Injectionmoulding

20%

Pipe22%

Other4%

3

55

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

66

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 very broad MWDbroad 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

SlurrySlurryprocessesprocesses

SolutionSolutionprocessesprocesses

Gas phaseGas phaseprocessesprocesses

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

5

99

Gas Phase ProcessGas Phase ProcessPolymerizationPolymerization

Gas phase process

85-110 C

20-25 bar

1010

Gas Phase ProcessGas Phase ProcessAdditivation and PelletizingAdditivation and Pelletizing

6

1111

GasGas PhasePhase ProcessesProcessesCharacteristicsCharacteristicsCatalystCatalyst: : 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

1212

Solution ProcessSolution Process

150-250 C30-100 bar

7

1313

Solution ProcessesSolution ProcessesCharacteristicsCharacteristics

Catalyst: Ziegler, (Catalyst: Ziegler, (metallocenemetallocene))Polymerization takes place in solutionPolymerization takes place in solution

3030--130 bar130 bar150150--300 C300 CShort residence timeShort residence time

Broad product range: LLDPE Broad product range: LLDPE –– HDPEHDPEBimodal capability with cascade reactorsBimodal capability with cascade reactorsHigher investment and operating costHigher investment and operating cost

1414

ChevronChevronPhillips Slurry Loop ProcessPhillips Slurry Loop Process

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1515

ChevronChevronPhillips Slurry Loop ProcessPhillips Slurry Loop ProcessCharacteristicsCharacteristics

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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Phillips Process at TVKPhillips Process at TVKPolymeriPolymerizzationation

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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1717

Phillips Process at TVKPhillips Process at TVKAdditivationAdditivation and Pelletizingand Pelletizing

Extruder hopper

Additiveblender

Premix feeder

Main feeder

CIM

Extruder

Dewateringscreen

Spin dryer

Classifier

Pellet watertank

Rotaryfeeder

Air blower

Pellet waterpump

1818

Slurry ProcessSlurry ProcessCSTRCSTR-- Cascade Stirred ReactorCascade Stirred Reactor

10

1919

Slurry ProcessSlurry Process –– CSRTCSRTReactor and SurroundingReactor and Surroundingss

2020

Slurry ProcessSlurry Process -- CSTRCSTRProcess 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[H22]/[Et]]/[Et]↑↑ MI MI ↑↑

Chromium catalyst: T, Chromium catalyst: T, [Et], [H[Et], [H22]]T T ↑↑ MI MI ↑↑[Et][Et]↑↑ MI MI ↓↓[H[H22]]↑↑ MI MI ↑↑

DensityDensity[comonomer] [comonomer] ↑↑ D D ↓↓

Molecular weight distributionMolecular weight distributionCatalyst 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 system, down valves release to closed system, connected toconnected toFlare to burn blown hydrocarbonFlare to burn blown hydrocarbon

Double mechanical seal on pumps in liquefied gas serviceDouble mechanical seal on pumps in liquefied gas serviceGas 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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2525

Loop Reactor Circulating Loop Reactor Circulating PPumpump

2626

Decanter CentrifugeDecanter Centrifuge

14

2727

CMP Extrusion Line ArrangementCMP Extrusion Line Arrangement

2828

CMP ElementsCMP Elements

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2929

Mixing in CMPMixing in CMP

3030

InvestmentInvestment CostCostBasisBasis: WE 2010 Q1: WE 2010 Q1

LLDPE HDPE HDPEProcess Gas phase Gas phase SlurryCapacity 325 300 300Investment, million EURISBL 98 94 88OSBL 49 47 44Other project costs 53 50 48Total investment 200 191 180

Specific investment cost, EUR/t 615 637 600

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3131

CostCost of of ProductionProductionBasisBasis: WE 2010 Q1: WE 2010 Q1

LLDPE HDPE HDPEGas phase Gas phase Slurry

Ethylene 851,8 927,8 927,8Comonomer 96,2Catalysts&chemicals 19,9 19,9 17,9Total raw materials 967,9 947,7 945,7

Power 28,9 26,9 29Other utilities 7 8,4 13,5Steam creditTotal utilities 35,9 35,3 42,5

Direct fix costs 17,1 15,8 18,2Allocated fix costs 13,7 14,7 14,2Total fixed costs 30,8 30,5 32,4

Total cash costs 1034,6 1013,5 1020,6

EUR/t

40%

50%

60%

70%

80%

90%

100%

325 kt 300 kt 300 kt

Gas phase Gas phase Slurry

LLDPE HDPE HDPE

Total raw materials Total utilities Total f ixed costs

3232

Spring Rotary SealRing

Stationary SealRing

Rotary SealPacking

Stationary SealPacking

Appendix: Typical Mechanical Seal

Product

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3333

Appendix: Appendix: Blow MouldingBlow Moulding

3434

Appendix: Pipe Appendix: Pipe ExtrusionExtrusion