eatco_suez petrochemicals complex_gas to polyolefins ii

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EATeo -Suez Petrochemicals ComplexNatural Gas to Polyolefins Project (GTP)

Suez, Egypt

Final ReportVolume Two - Technical Information

For:

Egyptian Arab Trading Co. (EATCO)

Prepared by:

UOPLLC

&

Kvaerner u.s. Inc.Engineering Consultant

Together with:

Bank of America, N.A.Financial Advisor

CMAI Chemical Marketing Associates, Inc.Market Consultant

Nexant Inc.Environmental Consultant

This version of the feasibility study report excludes certain details that are provided only in the full confidential versionofthe report. REPRODUCED BY: I!.f§,

U.S. Department of CommerceNational Technical Information Service

Springfield, Virginia 22161

NOTICE

This document has been reproduced from the best copy furnished to NTISby the U.S. Trade and Development Agency. Although it is recognized thatcertain portions may be illegible, it is beingreleased in the interest ofmaking available as much information as possible.

Please direct questions about illegible pages to:

The LibraryU.S. Trade and Development AgencyTelephone: 703-875-4357

Thank you.

•

•

Feasibility Study Report - Volume 2 of2EATCO - Suez Petrochemical Complex GTP ProjectSuez, Egypt

Important Notice

The intended purpose of this report is EATCD's evaluation of thefeasibility ofinstalling a GTP Plant only and it does not constitute asolicitation, or offer or invitation to EATCD or any third party tolend or invest or otherwise participate in the GTP Plant. This reportis not intended to provide the sole basis of any credit or otherfinancial or non-financial evaluation. Any potential joint venturepartner, lender, investor or other participant to whom a copy ofthisreport is furnished should determine for itself the relevance of theinformation contained herein and its interest in participating in theGTP Plant should be based upon such investigation, as it deemsnecessary andprudent. Neither UDP LLC nor its subcontractors norany of their respective directors, employees, representatives oragents makes any warranty, representation or guarantee what soever, express or implied, in respect to the correctness, and/oraccuracy of the information, conclusions, results, opinions and/orother data contained in this report and any reliance by any party onthe information, conclusions, results, opinions and/or other data inthis report is at the sole risk ofsuch party.

PROTECTED UNDER INTERNATIONAL COPYRIGHTALL RIGHTS RESERVEDNATIONAL TECHNICAL INFORMATION SERVICEU.S. DEPARTMENT OF COMMERCE

iiJune, 2000

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This report was funded in part by Egyptian Arab Trading Company (EATCO), the Egyptian Sponsor. The opinions,fmdings, conclusions, or recommendations expressed in this document are those of the author(s) and do notnecessarily represent the official position or policies ofEATCO.

Egyptian Arab Trading Co. (EATCO), headquartered in Cairo, Egypt is a holding company for investments in theoil and gas industry in Egypt.

UOP LLC, headquartered in Des Plaines, Illinois, USA, is a leading international supplier and licensor of processtechnology, catalysts, adsorbents, process plants, and technical services to the petroleum refming, petrochemical,and gas processing industries.

•Feasibility Study Report - Volume 2 of2EATCO - Suez Petrochemical Complex GTP ProjectSuez, Egypt

Table ofContentsVolume II - Technical Information

1. Technical Summary

1.1 Overview1.2 Integration Issues1.3 Byproduct Utilization1.4 Optional Considerations

2. General

iiiJune, 2000

3. Process Descriptions

2.1 Process Design Basis2.2 General Site Infonnation2.3 Utilities2.4 Environmental Basis2.5 Units ofMeasure

• 3.13.23.33.4

Methanol ProductionOlefm ProductionPolyolefms ProductionUtilities/Offsites

•

4. Process Flow Diagrams

4.1 General4.2 Methanol4.3 MTO4.4 Polyolefins

5. Utility Flow Diagrams

5.1 Utility Block Flow Diagrams5.2 Utility Flow Diagrams5.3 Conceptual Electrical Single Line

•Feasibility Study Report - Volume 2 of2EA TCO - Suez Petrochemical Complex GTP ProjectSuez. Egypt

Table of ContentsVolume II - Technical Information

ivJune, 2000

6. Consumption Data

6.1 Material Balances6.2 Raw Materials6.3 Catalysts6.4 Chemicals6.5 Utilities

7. Equipment Information

7.1 Methanol7.2 MTO7.3 Polyolefins7.4 Utilities/Offsites

• 8. Preliminary Site Plan

Preliminary Plot Plans9.

9.1 Methanol9.2 MTO9.3 Polyolefins9.4 Utilities/Offsites

10. Buildings

11. Preliminary EPC Schedule

12. Procurement Plan

12.1 Procurement Strategy12.2 International Transportation Logistics12.3 Preliminary Host Country Logistics Plan12.4 Host Country & Middle East Suppliers12.5 Potential U.S. Suppliers

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Feasibility Study Report - Volume 2 of2EA TCO - Suez Petrochemical Complex GTP ProjectSuez, Egypt

Table of ContentsVolume II - Technical Information

13. Cost Estimates13.1 Breakdown by General Categories13.2 Explanation ofMethodology13.3 Fixed Operating Requirements

14. Environmental Considerations

14.1 Gaseous Discharges14.2 Liquid Discharges14.3 Solid Discharges14.4 Potential Major Hazards Summary

15. Technology Information

15.1 Commercial Experience Lists15.2 Performance Guarantees15.3 Technology Fees

vJune, 2000


• 1. Technical Summary

Section 1 Page 1

June, 2000

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1.11.21.31.4

OverviewIntegration IssuesByproduct UtilizationOptional Considerations

Page 2

Page 4

Page 5

Page 6

FeasibilityStudyReport - Volume2oj2EATCO - Suez Petrochemical Complex GTP ProjectSuez, Egypt

• 1.1 Overview

Section 1 Page 2

June, 2000

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This volume ofthe report studies the technical requirements for the installation ofaGas to Polyolefins plant in the Suez region ofEgypt. Engineering designinformation was prepared to detennine the process flows, raw materials, utilities,catalysts and chemicals, equipment sizing and materials, and overall siterequirements. This information was used to develop a cost estimate and detenninethe costs ofproduction for the project.

Kvaemer and UOP LLC developed the design information for the project. Kvaemeris a global engineering and construction company with extensive experience indesigning and constructing methanol and polyolefin plants. UOP is a worldwidesupplier oftechnology to the refining and petrochemical industries and possessesthe MTO (methanol to olefins) technology in conjunction with Norsk Hydro. UOPdeveloped the design information for the inside battery limits portion ofthe MTOplant. Kvaemer developed the design information ofthe integrated complex,including the methanol plant, polyolefins plant, utilities, storage and offsites, andKvaemer developed the site specific cost estimate.

Project Description

The GTP facility will be a grass-roots construction comprising an inside batterylimits (ISBL) plant supported by a utilities/offsites plant to produce 400,000 MTA(metric tons per annum) ofbagged polyolefins, 50% polyethylene and 50%polypropylene. The facility will be supplied with natural gas (for feedstock andfuel), raw water, and electric power and will generate all additional utilities required.

The ISBL complex comprises the following process units:

• Methanol Production Plant• Olefins (MTO) Production Plant• Polyethylene Production Plant• Polypropylene Production Plant

The OSBL plant comprises the following systems:

• Raw Water Treatment System• Firewater System• Potable Water System• Stripped MTO Byproduct Water Treating• Boiler Feedwater Treating• Condensate Polishing

• Deaerator and Condensate Return• Cooling Water Systems - closed loop circulation and seawater circulation• Wastewater Collection and Treating

• HPBoilers• Plant Instrwnent Air Generation and Distribution• Nitrogen Generation and Distribution• Power Generation• Flare Systems• Offsites Storage

•Feasibility Study Report - Volume 1 oflBATCO - Suez Petrochemical Complex GTP ProjectSuez, Egypt

Section 1 Page 3

June, 1000

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Site Description & Overview

The proposed site is located in the North West GulfofSuez Special EconomicZone, approximately 40 Ian south ofSuez City and 120 Ian east ofCairo City, closeto the new port at Ain El Sukhna The Gas to Polymers (GTP) facility will belocated in the southern section ofthe zone in the area designated "PetroleumSection", which comprises an area ofapproximately 11.90 Ian2

•

The proposed facility will be supplied with natural gas feedstock, raw water andelectric power at the 33 kV source level. Steam, instrument air, plant air, andnitrogen will be generated within the facility.

Cooling water for the facility will be provided via a closed loop cooling watercircuit, the circulating cooling water will be cooled by seawater. Seawater will beused directly for some cooling requirements. In addition, air coolers will also beemployed where applicable.

Infrastructure roads are provided within the facility boundary, supply roads to/fromthe facility from local highways are excluded from the scope ofthe facility.

The facility will be provided with the following buildings:

• Administration Building• WarehouselMaintenance/Stores Building• Emergency Service Building• Electrical Substation• Main Gate Guard House• Control Room/Laboratory• Unitized I/O - MCC Buildings for each process unit.

Feasibility Study Report - Volume 2 of2EA TCO - Suez Petrochemical Complex GTPProjectSuez, Egypt

• 1.2 Integration Issues

Section 1 Page 4

June, 2000

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The project is based on an integrated complex, which provides benefits oflowercapital investment and lower costs ofproduction compared to a non-integratedfacility. Among the key benefits are:

• Shared Facilities - requirements for buildings, administration, offsitesstorage, maintenance, emergency services, control rooms, and utilities arereduced.

• Uniformity ofFeeds/Products - the source of intermediate feedstocks(methanol, ethylene, propylene, hydrogen) is constant and provides a securesource ofhigh quality feeds/products without the surprises ofpurity,contaminants, and pricing that are inherent in materials purchased/shippedfrom the marketplace.

From a process design and operation perspective the integrated GTP complex offersthe following synergies:

• Water Balance - The production ofmethanol via conventional steam reformingprocesses consumes water in the reaction. An equivalent amount ofwater isreleased by the reaction ofmethanol to olefins. This offers an opportunity torecycle the water and thereby minimize the influent and efiluent amounts for thecomplex. The water treatment facilities included in the design ofthe GTPcomplex are based on this water conservation approach. In this designapproximately 75% ofthe MTO eflluent water stream is recovered as boilerfeed water after treatment. This provides about one fifth ofthe boiler feed waterused in the complex and reduces the raw water consumption to less than halfofwhat would otherwise be.

• Steam & Fuel Balance - The reactor sections ofthe methanol plant and olefinsplant operate at relatively high temperatures. Steam generation facilities areincluded as part ofthe heat recovery systems in these plants in order to conserveenergy. Steam is used in these plants for driving turbines on large compressorsand pumps, for heat input, and other process uses. Steam is also generated inboilers that utilize the byproduct fuel streams to reduce fuel importconsumption. This provides a good balance that reduces the amount offuelimported to the complex and eliminates the need to find outlets for sellingbyproducts.

Feasibility Study Report - Volume 2 of2EATCO - Suez Petrochemical Complex GTP ProjectSuez. Egypt

• 1.3 Byproduct Utilization

Hydrogen

Section 1 Page 5

June, 2000

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The methanol plant produces hydrogen as byproduct ofmethanol production. Aportion ofthe hydrogen is recovered and purified to meet the hydrogen requirementsofthe polymers plant. The remaining surplus hydrogen is blended into the fuelsystem in the complex.

Butenes

The MTO plant produces a substantial amount ofmixed butenes as a byproduct.This stream is composed ofmostly 2-butenes and I-butene and minor amounts ofisobutene and butadiene. The concentration ofbutadiene is low such that it isgenerally not economical to recover this component. The amount of I-butene isabout twenty-five percent ofthe stream composition. I-butene is a valuable productfor use as copolymer and additional facilities could be added to the complex torecover the I-butene ifnecessary. The majority ofthis stream's composition is 2butene. This component is an excellent feed for motor fuel alkylation processes.For this feasibility study, the mixed butene stream was blended into the fuel systemfor the complex. This provides the lowest value for this byproduct so it reflects aconservative utilization scheme. Other uses as mentioned herein could offer muchhigher values and increase the profit potential ofthe GTP complex.

C5+ Hydrocarbons

A much smaller yet significant byproduct ofthe MTO plant is a C5+ hydrocarbonstream. This stream could be sold for gasoline blending purposes or blended intoliquid fuel streams. For this study, the C5+ stream was used to provide a fuelsupplement to the boiler for steam production.

•Feasibility Study Report - Volume 2 of2EA TCO - Suez Petrochemical Complex GTP ProjectSuez, Egypt

1.4 Optional Considerations

Butene-l Recovery

Section I Page 6

June, 2000

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The polymer plant uses butene-l and hexene-l as a copolymer reaction material.Approximately 4,400 MTA ofbutene-l and 5,300 MTA of hexene-l will beconsumed in the polyolefins plant. It is expected that these chemicals will bepurchased as raw materials for the plant and the market study indicates that adequatesupplies will be available.

There is a significant amount ofbutene-l contained in the mixed butenes productstream from the MTO unit. Although recovery facilities were not included in theplant design for this study, it is possible to recover butene-l with additionalfacilities. There would be approximately 13,000 MTA ofbutene-l recoverablefrom this stream, which is more than enough to satisfy the consumption ofbutene-lin the polymer plant.

The facilities required to recover the butene-l are described in the confidentialversion ofthis report.

Preliminary estimates for the capital costs associated with these facilities indicatethat the economics for butene-l recovery are marginal due to the relatively smallproduction capacity. It is therefore recommended to exclude the facilities for butene1 recovery and purchase the required butene-l instead. These facilities could beadded-on in a later stage ofthe project ifthe economics improve or butene-lavailability becomes limited. A more profitable alternative for the mixed butenesstream would be to market it for alkylation feedstock for motor fuel production

KVA:RNER~

•Feasibility Study Report - Volume 2 of2EATeo - Suez Petrochemical Complex GTPProjectSuez, Egypt

Power Generation

Section 1 Page 7

June, 2000

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The GTP complex consmnes about 42 megawatts ofelectrical power per hour. Theofficial price ofelectricity from the grid is reported to be equivalent to $80 per MWh. At this price the cost ofelectricity is about $27 million per year, which is a verysignificant portion ofthe cash costs ofproduction for polyolefins. In order to reducethe operating costs ofthe complex, power generation facilities could be added to theproject. The operating cost savings based on natural gas priced at $1 per millionB.t.u. would offer a quick payback on the incremental cost ofthese facilities. Unlessa lower price for electricity can be obtained, it would be more economical to addpower generation facilities to the complex instead ofpurchasing electrical power.

Feasibility Study Report - Volume 2 of2EATCO - Suez Petrochemical Complex GTPProjectSuez, Egypt

• 2. General

Section 2 Page 1

June, 2000

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2.12.22.32.42.5

Process Design BasisGeneral Site InformationUtilitiesEnvironmental BasisUnits ofMeasure

Page 2

Page 6Page 8

Page 11

Page 13


• 2.1 Process Design Basis

Overall Scope

Section 2 Page 2

June, 2000

The scope ofthis feasibility study includes plant areas and units given below aswell as the necessary battery limit infrastructure required to support the facility.Excluded from the study and cost estimate are infrastructure items outside thefacility e.g. roads, pipelines, docks, electrical supply etc.

Area Name Unit Name

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Methanol Feedstock PurificationReformingSyngas CoolingMethanol SynthesisMethanol DistillationHydrogen Production

MTO MTO ReactionLORP

Polyethylene Raw Materials PurificationReactionResin DegassingVent RecoveryResin Additive HandlingPelletingPellet HandlingPackaging & Shipping

Polypropylene Raw Materials PurificationReactionResin DegassingVent RecoveryResin Additive HandlingPelletingPellet HandlingPackaging & Shipping

General Facilities UtilitiesOffsitesBuildingsSeawater Supply Facilities


Plant Capacity

Section 2 Page 3

June, 2000

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When furnished with adequate raw materials and utilities, the Gas to Polymersfacility will produce 400 kMTA ofpolymers, nominally 200 kMTA ofPolyethyleneand 200 kMTA ofPolypropylene.

Products Requirements

Polyethylene

The polyethylene product will be packaged in Jumbo bags, ofcapacity of1 - 1.25 Te each and in palletized 25 kg bags. The packaging splitrequirement is 50% - 50% respectively.

Polypropylene

The polypropylene product will be packaged in Jumbo bags, ofcapacity of1 - 1.25 Te each and in palletized 25 kg bags. The packaging splitrequirement is 75% - 25% respectively.

Onstream Factor

The onstream factor for the facility is based upon 8000 on-stream hours per year.

Intermediate Storage

A total of24 hours of intermediate storage for each intermediate product isprovided between the Methanol and MTO plants and between the MTO andPolymer plants

Cooling System

The use ofair cooling is to be maximized where practical, the use of sea-watercooling, either directly or indirectly is to be used to minimize raw water usage.

Control System

Control ofthe facility will be via a Distributive Control System (DCS) from acentrally located control room. Each plant is to be provided with a Remote I/OBuilding (RIB) for interface to the main control system.

KVA:RNER*


Major Drives

Section 2 Page 4

June, 2000

The use of steam turbines for major drives is to be maximized in an effort toreduce electrical power consumption. This will provide for heat integrationwithin the facility by utilizing steam produced as a byproduct of the operationswithin the process plants.

Feedstocks

Natural Gas Feedstock and FuelNatural gas for use as feedstock in the methanol plant and as fuel throughout thefacility, will be provided to the facility battery limit via pipeline and will conformwith the specifcation given below.

•

ComponentMethaneEthanePropanei-Butanen-Butanei-Pentanen-PentaneC6+CO2

N2H2SMol. WtLHV (kJ/NM3

)

HHV (kJINM3)

Pressure, Barg

Temperature,oC

Mol%92.754.601.300.120.090.040.000.070.970.06

5ppmv17.49137,76041,813

34.0 (min)20.0 (min)

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Hexene-lHexene-l for use within the polymers plant will be imported to the facility andwill conform to the specification provided by the Licensor. This information canbe found in the Confidential Volume of this report.

Butene-lButene-l for use within the polymers facility will be imported to the facility andwill conform to the specification provided by the Licensor. This information canbe found in the Confidential Volume of this report.

NitrogenNitrogen for use in the polymers plant will be generated within the facility andwill conform to the specification provided by the Licensor. This information canbe found in the Confidential Volume ofthis report.


Section 2 Page 5

June, 2000

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Intermediate Products

MethanolCrude methanol will be produced in the methanol plant for use in the MID plant,and will conform to the specification provided by the Licensor. This informationcan be found in the Confidential Volume ofthis report.

HydrogenHydrogen will be produced in the methanol plant for use in the polymers plantand will conform to the specification provided by the Licensor. This informationcan be found in the Confidential Volume ofthis report.

PropylenePolymer grade propylene will be produced in the MID plant for use within thepolymers plant, and will conform to the specification provided by the Licensor.This information can be found in the Confidential Volume ofthis report.

EthyleneEthylene will be produced in the MID plant for use within the polymers plant,and will conform to the specification provided by the Licensor. This informationcan be found in the Confidential Volume ofthis report.


• 2.2 General Site Information

Site Location

Section 2 Page 6

June, 2000

The proposed site is located in the North West Gulfof Suez Special EconomicZone, approximately 40 KIn south of Suez City and 120 KIn east of Cairo City.The Gas to Polymers (GTP) facility will be located in the northern section ofthezone in the area designated "Petroleum Section", which comprises ofan area ofapproximately 11.90 Km2

•

Ambient Conditions

The following ambient conditions have been assumed for the feasibility study:

Ave Daily Maximum Dry Bulb Temperature (Aug) 36°CAve Daily Minimum Dry Bulb Temperature (Jan) 8°C

Maximum Wet Bulb Temperature 28°CMaximum Ambient (Air) Temperature 45°CMinimum Ambient (Air) Temperature 5°C

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Normal Atmospheric PressureMaximum Atmospheric PressureMinimum Atmospheric Pressure

Rainfall

Maximum rainfall in 1 hour:Maximum rainfall in 1 day

Seismic Activity

Uniform Building Code ZoneFactor, I

1.013 BarA1.045 BarA0.970 BarA

10mm55mm

2B1

•Feasibility Study Report - Volume 2 of2EATeO - Suez Petrochemical Complex GTPProjectSuez, Egypt

Civil Information

Section 2 Page 7

June, 2000

Site Elevation:Site Condition:

Ground Conditions

CoastalClear, level and free from obstructions (aboveand below ground), subject to sandstorms

Facility to be designed for the following wind loading conditions in accordancewith ASCE 7-95

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Ground Load Bearing CapacityGround Water Level (below ground level)Ground Water Type

Cathodic Protection Requirement

Wind Loading

Maximum Basic Wind SpeedExposureImportance Factor, IPrevailing wind direction

66te/m280m

2500 - 4000 IDS

For Buried Steel

160km/hC

1.0From Northwest

K.VA:RNER~


2.3 Utilities

Fresh Water Supply

Section 2 Page 8

June, 2000

Treated Fresh Water suitable for use in the production ofHP Steam and as potablewater will be supplied to the facility battery limit at the following conditions:

ConductivitySuspended SolidsTotal Dissolved SolidsHardnesspH RangeTurbidityHeavy MetalsSupply TemperatureSupply Pressure

IlS/cmmg/lmg/lmg/l

NTUmg/l°CBarg

750 (max)<1

500 (max)60-1206.5 - 8.55 (max)

<0.1Ambient

6.9

•Sea water

Sea water temperature 30°C (Max) 18°C (Min) to be taken directly from sea,maximum return temperature is 40°C. The quality of the Seawater will be asfollows:

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pHConductivity @ 25°CTDSTSSTotal HardnessTemporary HardnessPermanent HardnessHardness due to Calcium ionsHardness due to Magnesium ionsChloride content as chloride ionsSulfate ionsCarbonateBicarbonateSilicaIronSodium ionsCalcium ionsPotassium ionsOrganic matter

mS/cmppmppmppm (CaC03)

ppm (CaC03)

ppm (CaC03)

ppmppmppmppmppm (CaC03)

ppm (CaC03)

ppm (Si0:Jppmppmppmppmppm

8.25520048200

83083501400695019756375

261203580

40110

50.5

15227790540288

KVA:RNER*

•Feasibility Study Report - Volume 2 0/2EATCO - Suez Petrochemical Complex GTPProjectSuez, Egypt

Electric Power

Section 2 Page 9

June, 2000

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Electric Power will be made available to the substation within the facility batterylimit at the following conditions:

Voltage, kV 33FrequencY,Hz 50Phase 3

Utilization Voltages

Electric Power will be utilized as follows within the facility:

Motor Power Above 151 to 1 to Below 1 Lighting &-Ranges,kW 1000 1000 150 Instruments

Voltage, V 11000 3300 400 115/230 115/230Frequency, Hz 50 50 50 50 50Phase 3 3 3 1 1

Applicable standards International Electrotechnical Commission (lEC) andrelevant documents issued by the European Committee for ElectrotechnicalStandardization (CENELEC).

K.VRERNER~

Feasibility Study Report - Volume2of2 Section 2 Page 10EA TCO - Suez Petrochemical Complex GTP ProjectSuez, Egypt June, 2000

• Utility Conditions (at Battery limits of each process unit)

Pressure TemperatureMin. Norm. Max. Min. Norm. Max.-- --Barg Barg Barg °C °C °C- -

HHP Steam(l) 100.00 105.00 107.00 450 480 480HP Steam 39.65 41.37 43.10 251 254 256MPI Steam(2) 27.00 27.80 28.50 323MP2 Steam 10.00 10.30 11.00 184 186 200LP Steam 3.30 3.45 3.80 145 148 165LLP Steam 1.00 1.05 1.10 121Condensate Return 0.69 2.07 2.76 10 110 125Cooling Water 3.10 3.45 4.14 10 33 33Supply (3)(4)

Cooling Water 0.34 1.03 1.38 43 43Return (3)(4)

Sea Water Supply 5.50 6.20 6.90 18 30 30Sea Water Return 4.10 4.80 5.50 40 40Potable Water 3.45 4.14 5.17 10 20 37

• Demineralized 4.40 5.17 5.86 27 40WaterPlant Air 5.52 6.90 7.58 -10 30 40Instrument Air 5.52 6.90 7.58 -10 30 40Nitrogen 6.20 6.90 8.27 -10 30 40Flare (7) (7) (7) -10 30 40

Notes:

•

(1)

(2)

(3)

(4)

(5)

(6)

(7)

Used solely within the methanol plantUsed solely within the methanol plantWater pressure drop for exchanger design is 0.34 to 0.69 BarDesign ofcooling water exchangers will be based on supply and returntemperatures of 33°C and 43°C respectivelyCooling Water cooled via Sea-water exchangersPotable Water quality to be in accordance with US Federal RegulationsTo be determined during detailed engineering phase

kVA:RNER*


• 2.4 Environmental Basis

Gaseous Emissions

Section 2 Page 11

June, 2000

Hydrocarbon emissions occur during abnormal operation, e.g. from relief valvesand from emergency venting. These emissions are routed to the flare.

The following emission limits have been assumed for the study:

SPM*

Emission Limits@Plant Stacks

PermissibleLimits @ Grade

Unitsmg/Nm3 300

6

2500

5

10

10

100

3.5

•* Suspended Particulate Matter.

Liquid Wastes

It is assumed that aqueous liquid discharges from the complex will need to meetthe following limits:

Aqueous Discharge Limits

BODmgILCODmgIL

Suspended Solids mgIL

Solid Wastes

308080

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The polymer granules and pellets, separated from the storm water in the polymerinterceptor, may be saleable. Any polyethylene granules, pellets or additive spillswill be contained, removed as soon as possible and either recycled or transportedto an offsite facility for disposal by others. Other solid waste e.g. spent catalystswill be transported to an offsite facility for disposal by others.

Noise

Not to exceed 90 Decibels in normally accessible locations.

KV)ERNER~

•Feasibility Study Report - Volume 2 of2EATCO - Suez Petrochemical Complex GTP ProjectSuez. Egypt

Radiation

Section 2 Page 12

June, 2000

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Max Flare Radiation at accessible locations 1.6 kW1m2 (Solar not included)

Insulation

Insulation for personnel protection to be provided where the process operatingtemperature exceeds 65°C.


2.5 Units ofMeasure

Section 2 Page 13

June, 2000

The units ofmeasure detailed below are to be applied to this project:

Length Metres mMillimetre rom

Area Square metres m2

Volume Cubic metres m3

Volumetric Flow Cubic metres per second m3/sCubic metres per hour m3/h

Normalm3 Normal metre cubed (@ DoC & 1.013 BarA) Nm3

Velocity Meters per second mlsMass kilogram kgMolecular kglkmol kglkmolWeightPressure Bar Bar (lOS N/m2

)

millibar mbarMolecular mass Kilogram mole KmolDensity Kilogram per cubic metre kg/m3

• Mass flow Kilogram per second kg/sKilogram per hour kg/h

Force Newton NStress Kilo Newton per square metre kN/m2

Viscosity Centipoise cPEnthalpy Kilo Joules per kilogram kJ/kgHeat Capacity Kilo Joules per kilogram per °c kJ/kgOCLatent heat Kilo Joules per kilogram kJ/kgThermal Kilo Watts per metre per °c kW/moCConductivityCurrent Amp AVoltage Volt VNoise Decibel dB(A)Line size Inch InEnergy or Power Mega watt, MW,

Kilo watt kWWatt W

Temperature Degrees Celsius °c

•KVA:RNER~


• 3. Process Description

Section 3 Page 1

June,lOOO

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3.13.23.33.4

Methanol ProductionOlefin ProductionPolyolefins ProductionUtilities/Offsites

Page 2

Page 3Page 4

Page 5


• 3.1 Methanol Production

General

Section 3 Page-2

June, 2000

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The process route consists ofthe following five main steps to produce methanol:

• Feedstock Desulfurization and Saturation• Synthesis Gas Production and Heat Recovery• Synthesis Gas Compression• Methanol Synthesis

• Distillation

Natural gas feedstock is desulfurized, saturated with steam in the saturator, preheated, pre-reformed and then mixed with remainder ofprocess steam to achieve thedesired steam to carbon ratio. The mixed feed is further heated and then introducedinto the Reformer.

The steam/natural gas feedstock mixture reacts in the reformer and produces synthesisgas. A considerable amount ofwaste heat is available from the synthesis gas, which isutilized by raising steam, preheating boiler feed water and preheating demineralizedwater. Waste heat from the reformer flue gas is recovered by preheating feedstock,raising and superheating steam and preheating combustion air.

Cooled synthesis gas is compressed and mixed with circulating gas in the methanolsynthesis loop. After synthesis and heat exchange, crude methanol is condensed andseparated. A continuous loop purge is maintained to keep the inerts at a level suitablefor satisfactory methanol production. The purge gas is used as reformer fuel, as ahydrogen source for desulfurization and as a hydrogen source for the PSA Unit tosupply the hydrogen requirements for the PPIPE Plants.

Light end gases are separated from the crude methanol in the Topping Column toobtain the crude methanol product. The crude methanol product is then cooled andsent to Storage.

CONFIDENTIAL


• 3.2 Olefin Production

Section 3 Page 3

June, 2000

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The UOPIHYDO MTO Process consists ofthe following main processing steps:

• Methanol Feed Vaporization

• Reactor & Regenerator• Product Cooling & Water Removal

• Compression• Oxygenate Recovery

• Impurity Removal• Fractionation & Purification

The methanol feed is preheated primarily by heat exchange with the reactoreffluent product streams. A portion of the methanol feed is first routed throughthe oxygenate recovery section before recombining with the rest ofthe methanolfeed. The combined methanol feed is vaporized by further heat exchange prior toentering the MTO Reactor.

The reactor is a fluidized catalytic type. It consists of a feed distributor, afluidized bed ofcatalyst, and vapor/catalyst disengagement devices. A smallamount ofcoke is accumulated on the catalyst as a byproduct of the MTOreactions. Therefore, the catalyst is continuously regenerated by combusting thecoke with air in the regenerator to maintain catalyst activity. The regeneratorsimilarly includes a fluidized bed ofcatalyst and vapor/disengagement devices.The regenerator flue gas is cooled to recover heat and then catalyst fines areremoved prior to venting to the atmospheric flue gas stack.

The reactor effluent stream is partially cooled by heat exchange, transferring heatto the methanol feed. The effluent is further cooled and byproduct water iscondensed and stripped to remove hydrocarbons. After water removal, theeffluent product is compressed and treated to recover small amounts ofoxygenates that are returned to the reactor for more complete conversion to lightolefins.

Following the oxygenate recovery section, the effluent is caustic scrubbed toremove carbon dioxide and then dried to remove moisture. The effluent is furtherprocessed in the fractionation and purification section to separate the key productsfrom the byproduct components. Trace impurities are removed in this sectionusing conventional technologies for diolefm saturation and ,?xygenate removal.The ethylene and propylene are produced as polymer grade products and sent tointermediate storage.


• 3.3 Polyolefins Production

Polypropylene Unit

Section 3 Page 4

June, 2000

•

•

The plant will be based on the well proven UNIPOL Polypropylene process licensedby VCC. The technology comprises ofthe fluidised bed and catalyst technologies ofVCC. The plant is designed to produce 200,000 tpa ofPolypropylene and the plantdesign includes for the manufacture of homopolymer, random copolymer andimpact copolymer resins.

Polyethylene Unit

The unit will be based on the UNIPOL PE process which is simple to operate andproduces low and high density Polyethylene economically in a safe manner. Theplant is designed to produce 200,000 tpa of Polyethylene (LLDPE and HDPE)including high strength copolymers, which incolpOrate Hexene and Butene as thecopolymers.

KV)ERNER-

Feasibility Study Report - Voiume2of2£ATCO - Suez Petrochemical Complex GTP ProjectSuez, Egypt

• 3.4 Utilities & Offsites

General

Section 3 Page 5

June, 2000

•

•

Water treating and usage is the largest portion of the utilities and offsites. The watertreating and handling consists ofthe following basic systems:

• Raw Water/Firewater

• Potable Water• Stripped MTO Byproduct Water• Boiler Feedwater Treating

• Condensate Polishing• Deaerator and Condensate Return• Cooling Water Systems• Wastewater Collection and Treating

These systems interact with each other to provide the water needs to the processplants and the utilities systems.

The other utility systems are:

• HP Steam Boilers• Plant and Instrument Air• Nitrogen Generator• Power Generation• Flare Systems• Offsites Storage

These systems supply the necessary utilities and offsites storage to operate the processplants and the utility systems.


Raw Water/Firewater

Section 3 Page 6

June, 2000

•

•

The raw water supply to the site is assumed to be drinking water quality that ischlorinated, free ofsuspended solids, and about 600 ppm TDS max.

The raw water will be stored in a large storage tank that will reserve a four (4) hoursupply of firewater plus a one day supply of raw water for normal plant operationabove the portion reserved for fIrewater

Firewater pressure is maintained in the system with a jockey pump. Electric anddiesel powered fIrewater pumps will start on low fIrewater system pressure. ThefIrewater supply is backed up with an emergency bypass to utilize seawater suppliedby the Diesel Firewater Backup Pump.

Potable Water

The potable water treating system consists of a storage tank and a chlorinator that willbe used to maintain a safe level of chlorine. To maintain the potable water at anacceptable temperature during hot weather an underground distribution system will beused with a continuous recirculation loop and a potable water cooler. This systemwill provide safe water for safety showers and eyewash stations without thepossibility ofhot water burns.

Stripped MTO Byproduct Water

A fIxed fIlm or fluidized bed biological system is used to remove the organics fromstripped MTO byproduct water. This process does not produce any waste disposalproblems and will recover over 91% ofthe water. The biological solids produced andassociated water will go to drying beds where the water will be removed without anyenvironmental problems. The dried solids will be non-hazardous solids that can berecycled for use in agriculture.

The effluent from the biological system will be fIltered through a back-washable fIlterwhere the backwash stream will be recycled to the inlet of the biological treatmentsystem. The remaining organics will be removed using an organic trap, whichcontains a strong base anion resin operated in the chloride form that is regeneratedusing salt. The wastewater from regeneration of the organic trap will be discharged tothe sea without additional treatment. The water from the organic trap will be fed to aReverse Osmosis unit that will remove most of the sodium carbonate and other ions.Product water from the reverse osmosis unit will then be combined with treated rawwater for boiler feedwater treating.

KVJERNER~

•Feasibility Study Report - Volume 2 of2EATCO - Suez Petrochemical Complex GTPProjectSuez, Egypt

Boiler Feedwater Treating

Section 3 Page 7

June, 2000

•

•

The raw plant makeup water will be dechlorinated with chemicals and sent to a WaterSoftener. The soft water from the Water Softener will be treated in a ReverseOsmosis Treatment Package to remove most of the inorganic salts. The treated waterwill be combined with the treated MTO wastewater for further treating.

The pretreated plant water and treated MTO byproduct water will be further treated inan additional RO polishing package followed by a Mixed Bed Polisher.

Condensate Polishing

Process condensate from the Methanol Plant is steam stripped in a decarbonator.Condensate from the steam turbine surface condensers is mixed with thedecarbonated condensate, cooled, then sent to the condensate polishers.

Product water from the mixed bed polishers make up the demineralized water supplyand are stored in the Boiler Feed Water Tank. The boiler feedwater tank is designedto hold 8 hours of boiler feed water or an equivalent of20 hours oftreated raw water.

Deaerator and Condensate Return

The Deaerator is supplied with condensate from the condensate flash drum and thebalance is made up from preheated water the Boiler Feed Water Tank. Thecondensate is then stripped of any entrained or dissolved air and non-condensableswith 1 barg steam to remove the oxygen and non-condensables from the boilerfeedwater. The deaerated boiler feedwater is fed to the various boilers by two sets ofboiler feedwater pumps.

HP Steam Boilers

Two HP Steam boilers are provided that will produce up to 200,000 kg/hr of steamfor start-up and abnonnal operation when the methanol unit is operating at 66% rateand the methanol plant is in start-up mode. The boilers will also provide steam tosupplement the steam produced by the methanol refonner and provide a use for thewaste gaseous and liquid fuel produced. The excess steam produced from waste fuelwill be used to generate power with a condensing turbine. Both boilers will operatecontinuously sharing the steam load.

HP steam produced in the MTO unit is superheated in these boilers to the HP steamheader superheat level in addition to their capability to generate 200,000 kg/hr ofsuperheated steam.


Cooling Water Systems

Sea-water Cooling

Section 3 Page 8

June, 2000

•

•

Seawater flows into a Seawater Suction Structure at the seashore through trashscreens that are designed to keep fish and trash out of the seawater pump intakes.The seawater pumps will supply seawater to the plant for cooling processesdirectly and also for removing heat from the freshwater closed loop system.

An Electrolytic Chlorinator is provided to generate sodium hypochlorite from aseawater slipstream to control the growth of sea life that will foul and plug thecooling system. After the seawater removes process heat from direct and indirectcooling duties it will be discharged back into the sea

Closed Loop Cooling Water

A closed loop fresh water cooling system will provide a circulating coolingmedium to remove heat from the process coolers. The cooling water will becirculated via the cooling water pumps, heat will be removed from the closed loopcircuit by seawater in plate and frame exchangers.

Plant & Instrument Air System

Plant and instrument air is being compressed with two centrifugal compressors and aspare where it is cooled and sent to a Plant Air Receiver prior to being distributed asplant air and sent to the air dryers to become instrument air

Nitrogen Generator

The requirement for large quantities of high purity nitrogen in the Polyolefms plantrequires the use of a cryogenic nitrogen plant (air separation plant) for the productionof the plant nitrogen.

Power Generation

The facility produces a small amount of electric power from the excess supply ofbyproduct streams that are used to raise HP steam that is condensed via a steamturbine generator/condenser set.

Flare Systems

The flare system consists of two separate systems. One for all cryogenic andcontinuous reliefs, the other for emergency releases.


Wastewater Collection and Treating

Section 3 Page 9

June, 2000

•

•

Wastewater is collected in process area sumps on a fIrst flush principle from thepaved process areas where organic contamination may occur. The sources ofwastewater are from wash down water, maintenance steam outs, process drainage,and rainfall, which will run off to a wastewater collection sump. The collectedwastewater is pumped to a dissolved air flotation unit to remove any free oil down toa few parts per million. The remaining oil-free wastewater will flow to theFacultative Pond.

Sanitary sewage will be collected in a lift station and pumped to the Sanitary SewageTreatment Package where it will be treated. The Sanitary Sewage Treatment Plantwill discharge into the Facultative Pond to supply nutrients to the pond and furthertreat the sanitary sewage effluent. The Facultative Pond will discharge to the stormwater drainage ditch, which flows to the sea.

Offsites Storage

The intermediate storage tanks between the process plants supply a 24 hour surge ofproduct and or raw material. The co-monomer tanks provide a 14 day supply due toshipping requirements. The Debutanizer bottoms tank is sized for two days ofdebutanizer bottoms to accommodate start-ups and shutdowns when the bottomsproduction is greater than fuel usage.


• 4. Process Flow Diagrams

Section 4 Page 1

June, 2000

•

•

4.14.24.34.4

GeneralMethanolMTOPolyolefins

Page 2

Page 3

Page 4

Page 5


4.1 General

Section 4 Page 2

June, 2000

•

•

This section contains the process flow schematics for the inside batterylimits (lSBL) portion of the facility. More detailed process flow diagramsare included in the confidential version ofthe feasibility study.


•

•

•

4.2 Methanol

Section 4 Page 3

June, 2000

II

• •Synthesis Gas GenerationII II II

•

FlueGas

SynthesisGas

.... Air

Compression

Em

USc..~

Reformer

Heat Recovery

Steam DrumtFuel

Water

•Steam

KVA:RNER™

Desulfurizer Saturator Prereformer

HotWater~

Natural Gas

III

• •Methanol SynthesisHI II III

•

Purge

Circulator

Synthesis Gas

Heat RecoverySaturator

Water

KVA:RNERTM

Crude Methanol

Converter

•

z:E::J..Jo()

C)z-Q.Q.o~

_0CJ C:::s eu-c-C0I- CDa.:E--.

oc

CD eu-c-C:::sI- CDo:E

c:o--wi-'.

CO----wi-' 1/1

CJ)--o.

•

•


•

•

•

4.3 MTO

Section 4 Page 4

June, 2000

KYA:RNER~

• • •MTO Reactor Section

UOP/HYDRO MTO Process

TO/FROMRECOVERY

SECTION

Water

OlefinProduct

TORECOVERYSECTION

HEATRECOVERY

& FEEDPREHEAT

Air

HEATRECOVERY~

CrudeMethanol" •

Flue.,Gas _ IHEAT ~

RECOVERY

Regenerator Reactor WaterRemoval

uop

• • •MTO Recovery Section

UOP Light Olefins Recovery Process (LORP)i I

• C2=

, C3=

SP

.. allITTER--oJ

I ~C2

y C4

i .. ETHYLENERECOVERY I I C1-

, P C5+

oEBUT.. .IANIZER

oEME

ACETYLENE ~I~REMOVAL 1"'71 ~

IZER C

3

S.1 OXYGENATE I '-.lr

po........~ REMOVAL 711TTER

t I C3

, al COMPRESSION

DEPRo

,. al PANIZER

t >-

~ET

I alHANIZER

CAUSTICSCRUBBING

OXYGENATERECOVERY

COMPRESSION

Olefin ProductFROM

REACTOR SECTION

FROM/TOREACTOR SECTION

1- =-:' I

uop


•

•

•

4.4 Polyolefins

Section 4 Page 5

June, 2000

KVA:RNER~

•

Cooler

ProductDischarge

Cooler

ProductDischarge

--'1 I I i ~I 1--.

• •UNIPOL™ PP Process - Reaction• •• Blovver Blovver

Catalyst--.

Propylene t 1 I IttCo-Monomer ~Hydrogen

KV~RNERStage 1: Homopolymer/Random Copolymer Stage 2: Impact Copolymer

II!I

11II

• •PP Purging, Pelleting &Dispatch• • •

•

......

Palletizing

Blending

r7---l ~2s.B--i-)~::I. --P-;od~':-:L.J ... - DispatchBagging

"7

Additives

Purging

Pelletizing

KVA:RNER™

• •Univation PE Process - Reaction

•Blower

Cooler

ProductDischarge

-.

•

Catalyst-.

••

KV~RNERTM

EthyleneCo-MonomerHydrogen

EIJ

•+~ .cCo) Co)

::s~

I "C a:sOC-

I '- f/)n. .-I C

I

..c:()

C)c

......,.-N

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en"C

n.

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.-n. "C

N.-«

~

s....Q)

::J

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~

a..n.

•.....

WI

• 0... II!III

Feasibility Study Report - Volume 2 of2E4TCO - Suez Petrochemical Complex GTP ProjectSuez, Egypt

• 5. Utility Flow Diagrams

Section 5 Page 1

June, 2000

•

•

5.15.25.3

Utility Block Flow DiagramsUtility Flow DiagramsConceptual Electrical Single Line

Page 2

Page 3

Page 4

KVA:RNER~


5.1 Utility Block Flow Diagrams

Drawing List

Drawing No. Rev. No. Description

Section 5 Page 2

June, 2000

•

•

UB-IUB-2UB-3UB-4UB-5UB-6UB-7UB-8UB-9

UB-IOUB-IIUB-12UB-13UB-14UB-15

ooooooooooooooo

Steam & Condensate Overall Mass BalanceOverall Site Water Mass BalanceHHPSteamHP SteamMPI SteamMP2 SteamLP SteamLLP SteamCooling WaterSeawaterInstrument AirPlant AirNitrogenFuelElectric Power

OVERALL SITE WATER MASS BALANCE

REV,118-1

Kvaerner ProcessSUEZ PETROCHEMICAL COMPLEX

GTP FEASIBll.lIY S rUDY

CONTRACfNo

H1990720

10647

Units ~ kg/h

659337442

2500

122233

~,I Heal~ rp'reheal''""'~'.. ~ ".,.,.Condensate MW

E-102RADIANT SHIELD

BOilER

E-!Q~

Sl!=AMSUPERHE,A.TER

!=...:JQIBE.fORMEO §!\.~

BOILER

~!j)~

HHPc!illll-J~Iiff~

W~I~RJ:!!=A1fB

E..:19!i!:DEMINERALIZEDWATER HEATER

6Til 1;-1.9)

JO-PQ.LSYNGAS TURBINE

CONDENSER

E·U701GENERATORCONDENSER

y.:10:~

HHP STEAM DRUM

'{:§Q1BOfLER

SLOWDOWN

Y_:J,J.§QlCONDENSATEFLASH DRUM

X:W50QDEAERATOR

,1';-601PHOSPHATEDOSING SET

x-usosHYDRAZtNEDOSING SET

x·u~p

MORPHOLINEOOSINGSET

REV

o

HP STEAM FROM MTOBOLER

~

LP STEAM HEADER

DRAWINGtlo

UB·2

Kvaerner Process

STEAM AND CONDENSATE OVERALLMASS BALANCE

HP STEAM FROM PACKBOILERS

i • I cu:o;-

CONTRACT No·

H19907.20

SUEZ PETROCHEMICAL COMPLEX

I- ~~ ~EA~I~~ITY~~Ur.:y . _

Flow, kglhPressure, barg

Temperature, °c0-D--

Legend

I I

@TQ.MEOH

F-oil

, , ,

E:..lllQ1N.ftGENERATOR

CONDENSATE PUMP

e~G--'---------

e:JJ~3te'S

CONDENSATE FlAS~i

DRUM PUMP

3,187

!"·U.5Q2&~Q

MP BOILERfEEOWATER PUMP

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E-l09

~:U_5Q1~~

HP BOILERFEEDWATER PUMP

~

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750B

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E:!,J;>Q2:tV81~

42.8 BARG BFW TODESUPERHEATERS

19.Y.:l0~

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I I ~, 107 BARG BFW TODESUPERHEATER

Gsr-lJ!()!STEAM TURBINE

GENERATOR

DMWFROMP·U513 NB

~

tKOMBOILERBLOWDOWNDRUMS

~

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BFWTOBOtLERS

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<==:J----

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~~

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M

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• ,Ir .. • .. ~Ir

C) ... ..I~ ... Z 0C)

z :s a.0 z:s ~ c:(

~ a. 0 ... :J:a. ..I :t ljj0 a. w~ a. a. :t

Kvaerner ProcessNOTES: SUEZ PETROCHEMICAL COMPLEX GTP FEASIBILITY STUDY

(1) FIGURES REPRESENT NORMAL FLOW UTILITY BLOCK FLOW DIAGRAM(2) UNITS OF FLOW: MT/H

HHPSTEAM

CONTRACT No: -1~RAW1NG No: I REV.

H1990720 UB-3 0

• • •U) ww (!)It:j:

~~:Jj: ~gj C.

All. All.

10 CIC! U!cO ... ...''It N N...

",.01)

10M 0en 0CD 0.- ",. .. "Ir ",. .".

(!)l- I- ...I

Z Z 0a z c. zj j It: 0 <C

~ c. 0 l- XC. ...I :E I-0 C. W w<C c. c. :Ec.

Kvaerner ProcessNOTES:

SUEZ PETROCHEMICAL COMPLEX GTP FEASIBILITY STUDY


HPSTEAM

CONTRACT No: I~RAWING No: I REV.

H1990720 UB-4 0

• • •U)wi=:ii=:J

~C')

00C')

o I 0C') 1i..t.. NC')

C) ...

I Iz ... ..I

C)Z Z D.

0

~ ~z

~n:: e «

D. D. 00 ..I ::E ::E:

« D. w ...D. D. W

D. ::E


(1) FIGURES REPRESENT NORMAL FLOW

(2) UNITS OF FLOW: MT/H


UTILITY BLOCK FLOW DIAGRAM

MP1 STEAM

CONTRACT No:

H1990720 IDRAWING No:

UB-5I R~V.

• • •C/)wi=:Ji=;:)

or:'l""C')

,r

0or:'l""C')

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~ 0z Z 0. ZC>~ ~ 0: 0 «

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• • •enwj::::::ij:::::J

.4~

It) ~cO ....C'? C'?

",A~ A~ A~

C'?

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.... ~ N 00 "Ii 0 .... It).... .... .... "" ....

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~ 0Z Z 0. ZC> :s :s 0:: 0 «~ 0. 0 l- X0.

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==0.



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H1990720 UB-7 0

• • •tnW~::i~:::J

A~

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; cDC')

-"

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't-"

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LLP STEAM

CONTRACT No: I~RAWlNG No: I REV.

H1990720 UB·8 0

• • •>..I

(i)0C)o. wWzo. - ...-~ ... -..10 -000: ..I II.

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~

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r-.N~

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C) ... ... ..IZ ac; z Z 0. Z

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(1) FIGURES REPRESENT NORMAL FLOW UTILITY BLOCK FLOW DIAGRAM(2) UNITS OF FLOW: M3/H

COOLING WATER


H1990720 UB-9 0

•0::w>~.J=:8:~~tn

• •mtnWW-lI--tndu.I-u.::JO

('II(")....

.~

.. CQ'C""

"':.CQ'C""

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~~

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:50..0..0..

Q

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...

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.. c?

-+

e:E

...

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~iii:E

~en,.:

NOTES:

(1) FIGURES REPRESENT NORMAL FLOW

(2) UNITS OF FLOW: M3/H

Kvaerner ProcessSUEZ PETROCHEMICAL COMPLEX GTP FEASIBILITY STUDY

UTILITY BLOCK FLOW DIAGRAM

SEAWATER

,CONTRACT No:

H1990720 lDRAWlNG No:

UB·10I R~V.

• • •1-)- mz .... wWD. j:::ED.::J::J :JO::m j:1-0:: ::Jtn_~<C

.j~

N ~....

0 00 10 0 0en ~ l!!.~ """~r ~

N ~ 10 Ii) ;nC') CD CO ~ 10en 10 N 10 CO ~

""" N""" ~, """ N 10.... ....

""" """• -. ...... ~, .. ~,

C)I- ....

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(1) FIGURES REPRESENT NORMAL FLOW UTILITY BLOCK FLOW DIAGRAM(2) [ I REPRESENTS PEAK FLOW

INSTRUMENT AIR(3) UNITS OF FLOW: NM3/HR


H1990720 UB-11 0

• • •~> tn

Wc( -' i=... 0- :::iz 0-

:S~ i=:::»

0-

~~Q .... 0'co ~ Q~

.... Q Q.... en II) coen ....,,. ....

....Q co ....co l") Q Q~ N Q .... Q lO'~ l") .... ~ Q co....

~ ~r l!1 CIQ en...... " .. .. .. "C) ... -'~ ... Z 0Z 0- ZC) :3 :3 0::: 0 c(

~ 0- 0 I- ::c0- -' :l!1 ...0 0- W Wc( 0- 0- :E0-




PLANT AIR(3) UNITS OF FLOW: NM3/HR


H1990720 UB·12 0

• • •z> en

ww-' EC)a.0a. -'o:::~ i=!:en ~z

A~

~1~ 0'C") co 0C") t-. 0 0C") .... 'It ~.... 'It

~

0...0 co ...

0 0 co ...0 0 C") C") 0en en \I) \I) 0 'It....

C") " f2 0 0'It ...... + ....

" • • ."

C)l- I- -'

Z 0(; z z a. z

:3 :3 0::: 0 «~ a. 0 I- :l:a. ::!0 w -' \ija.« a. a. ::!a.




NITROGEN(3) UNITS OF FLOW; NM3/HR

CONTRACT No: WRAWlNGNO: I REV.

H1990720 UB-13 0

•NATURAL GAS

IMPORT

(NORMAllYNil)

(OMW)

UTILITIESIOFFSITES

•MTO liquid Fuel

MTO Fuel Gas(44.00 MW)

(39.08MW) .. (2.70 MW)

•1------------"\, II I

I' MTO/LORP IPLANT I

I II IL. .. .__J

1 ~

Methanol Fuel Gas

484.4MW t

METHANOLPLANT

MTO Fuel Gas

(86.32 MW)

...

~ 0al 1S 5> 1S8 ::I

" ::I 0al

~e

~ " ~Qi ~ex: Q. e

al al Q. Zl: CD l: 0 al .~

CDal co>. ..... III C') l: 10 0

«i .r:~

III ci l: cO.r: W 0-W .....

~ ~~ e ~

E Q. .Q

0al

ot: 0

MTO Fuel Gas ~

128.10 MW

Kvaerner ProcessSUEZ PETROCHEMICAL COMPLEX

GTP FEASIBILITY STUDY

UTILITY BLOCK FLOW DIAGRAMFUEL

CONTRACT No:H199072 I

DRAWING No:UB·14 rEV. 0

•

•

•

>- [;00 a:::::>l-I/) -~:::i :iEiii ~(/) Ci5

(/) L5 ~..... CI) u.

C 0::'ONVH~31111 a..

~~ (,) I-

0 C) ~1l'ta.'a. .. ~ 0 0

a.. ...J a. 0..J U. Za.. U C).. :E ~ ii: ZlI)

CI) 0 () I- ~;;;;0 0C ..J ...J()

.E...2.... C3 co wCI) ...J

~ ~w

DNUHDn ~ !2 w... J: :::iIS3~IS:l:lO

... O~IIII s=: 0 I-IS31~nl~n 801l"t~ ~ :::>

I-wa.. 0N ZoW tiN:::> ~~I/)... lzm... 0 .....

oJ:

89L'~ ..dHO'

NOUW3N3D ...H3MOd

....OOt'S

z

~0

~NYld3d E0z00C)z

A'ddnS H3MOd... ~~ w

S~O'~1l'a..0..J

.... ~~ ~NYld dd a::

0Sa.O'O~ z

I-ZWI/)wa::a..w

~a::I/)w

~a::.. :::>DNIDV>lOVd Ui C) Z

w u:: :::>

b ~ ~

z ::.~


5.2 Utility Flow Diagrams

Drawing List

Drawing No. Rev. No. Description

Section 5 Page 3

June, 2000

•

U-OIU-02U-03U-04U-05U-06U-07U-OSU-09U-lOU-IIU-I2U-13U-I4U-I5

ooooooooooooooo

Raw Water & Firewater SystemRaw Water Treating SystemMTO Byproduct Water Treating System (1 of2)MTO Byproduct Water Treating System (2 of2)Boiler Feedwater Treating SystemDeaeratorPackage BoilerCooling Water SystemPlant & Instrument Air SystemNitrogen & Electric GeneratorFlare SystemsPlant & Sanitary Wastewater TreatingCrude Methanol & Hexene StorageEthylene & Propylene StorageButene-I & Debutanizer Bottoms Storage

•

These drawings are included in the confidential version of the feasibilitystudy.

KYJERNER-

•

•

•

Feasibility Study Report - Volume 2 of2BATCO - Suez Petrochemical Complex GTP ProjectSuez, Egypt

5.3 Conceptual Electrical Single Line

Section 5 Page 4

June, 2000

33 KV SOuRCE POWER A 33 KV SOURCE POWER B

MAINBREAKER

Ir,(AINBREAKER

TIE BREAKER

PRII.lARYBREAKER

PRIIoCARYBREAKER

33 KV~5l,4VA~

3.3 KV

PRII.4ARYBREAKER

PRIl,4ARYBREAKER

PRIMARYBRHKER

33 KV

5MVA~

~3.3 KV

7.5 MVA 12.5 IrNA 17.5 MV" I 2.5 "'VA I 7.5 MVA 12.5 ,",VA 17.5 MVA33KV 33K¥ 33KV 33K¥ 33KV 33KV 33KV

~~~~~~~~

~~~~~~~~380 V 3.3 KV 380 V 3.3 K¥ 380 V 3.3 KV 380 V 3.3 KV

TIE BREAKER 3.3 KV SWGR CILORP/t.lTO A.REA MAIN SUB FOR

LORP/IolTO AREA 3.3 KV BUS A 3.3 KV BUS B LORP/MTD AREA

I MVA d""'CY""'-'-"-""""""""':"~~~'~"'-"-" .._._._.__.._ 1~ l,IOTORS I ~ UDTORS

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PRII.4ARYBREAKER

33 KV SWGRFOR UTILITIES/QFFSITES

PRIIr,lAAYBREAKER

UTILI TIES/OFFSITESAREA 33 KV 8US A

TIE8REAKER UT I LIT IES/QFFS I TES

AREA 33 KV BUS B

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PRII.IARYBREAKER

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2.51.4VA 17.5 I.4VA I 2.5 IoCVA 17.5 t.lVA33KV 33KV 33KV 33KV

~~~~

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PRIMARYSWITCH

FROU33 KV SOURCE

MOTORS

OFF PLOT AREA33 KV 8US B

1.40TORS

OFF PLOT AREA33 KV BUS A

FROI,433 KV SOURCE

33 K V TIE BREAKER 33 K¥

~ ~

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33 K V

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3.3 KV

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33 KV 8US 8

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PRIl,4ARYSWITCH

33 K V~5I.lVA

~3.3 KV

"-"-"-"-"-"-'-'3:3"-KV-"SWGA-"-"-"-"-"-"-"_.._..PRIMARY FOR I.le:THANOL AREA PRIMARYBREAKER BREAKER

METHANOL AREA METHANOL AREA3.3 KV BUS B TIE BREAKER 3.3 KV BUS B

L~·'··'··B··_··_·~&=:..·..····Q..·······:~ MOTORS ~ 1.40TORS

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• 6. Consumption Data

Section 6 Page 1

June, 2000

•

•

6.16.26.36.46.5

Material BalancesRaw MaterialsCatalystsChemicalsUtilities

Page 2

Page 3

Page 4

Page 5

Page 6


• 6.1 Material Balances

Section 6 Page 2

June, 2000

•

•

The infonnation included within this section is the expected nonnal plantoperating consumption data. For purposes of the economic modelevaluation, allowances will need to be added to the values herein due toLicensor guarantee requirements.

KVA:RNER~

• • •----------------------,

NATURAL GASFEEDSTOCK + FUEL

2.79 MMNm3/Day(104.1 MMSCFD)

[~E:~~i~O~l CRUDE METHANOl,.

[MTOJl..ORP]

PLANT_._.._----

ETHYLENE -. I;~~-T---Il -----l

. POLYETHYLENE~600 MTD

f-t.

POLYOLEFINSPLANT

IIIIIII

NATURAL GAS (FUEL).Normally Nil

600MTD ....-)POLYPROPYLEN~ ...[~~~~;]

t PROPYLENE,I •

.

~

[~Egf~~~]

---.RAW WATER

1861 m1Day

ELECTRIC POWER.42MW

•~ ~~:l 0en ....~ E~ 18c( II)

~ ~en

z ~~ >- W >-:l co ~ coIii Q ~ ",Q~ EwE~co I-COWCO en oI- II) <:( Ol

~ :B ~is coen..Ir • Kvaerner Process

Notes:Normal Condition is at O°CMTD = Metric Tons per DayMM Nm3/Day = Million Normal Cubic Meter per DayContinuous Operation= 8000 hrs per YearElectric Power Consumption is nett value, assumes internal generation from excess fuel

SUEZ PETROCHEMICAL COMPLEXGTP FEASIBILITY STUDY

OVERALL FLOW DIAGRAM

CONTRACT No: TORAWING No:H1990720 IOFD.1

rEV. 0


• 6.2 Raw Materials

Section 6 Page 3

June, 2000

The raw materials consumed by the facility are summarized below. Detailsofthe specifications ofthe raw materials can be found in section 2.1.

Raw Material

Natural Gas

Copolymer Production

Quantity

2.79104.1

Units

The copolymer reaction materials consumed by the facility are summarizedbelow. Details of the specifications of the feed materials can be found in section2.1.

(1) During the annual plant operation, this amount ofnatural gas will be replacedwith the quantities ofcopolymer reaction materials shown.•

•

Copolymer Reaction Materials

Natural Gas(1)Butene-1 & Hexene-1

Quantity

(22.55)9,701

Units

MMNm3/YrTe/Yr


• 6.3 Catalysts

Section 6 Page 4

June, 2000

•

•

The individual catalyst quantities and costs information for the facility are regarded asConfidential by the Licensors. The costs for the catalysts for the GTP facility areincluded in the cost estimate


• 6.4 Chemicals

Section 6 Page 5

June, 2000

•

•

The expected consumption of chemicals in the facility are summarizedbelow:

Chemical Purpose MonthlyUsageMT

Phosphate To prevent scale and deposition oninternal surfaces ofthe boilers 10.8

Sodium Hydroxide(l) To neutralize traces ofacid in themethanol and olefin products and inwater treatment (ionic exchange) 195.0

Sulfuric Acid(2) In water treatment (ionic exchange) 14.2Chlorine (Gas) To disinfect and control algae

growth in raw and potable water 0.13Sodium Chloride Water softner 134.0Calcium Hypochlorite(3) Effluent disinfectant 0.1Hydrazine(4) Oxygen scavenger in boiler water

preparation 1.8Mixed Amines Corrosion control in boiler water

preparation 1.1Sodium Sulfite To protect water treatment resin 0.15

(l)Quantity expressed as 50% caustic.(2)Quantity expressed as 98% acid.(3)porm ofdry chlorine.(4)Or equal.

In addition, machinery lube oils, per manufacturers' recommendations, anddiesel fuel, for emergency use operation and for the standby operation(estimated at four (4) hours per week per item), for the generator, emergencyfirewater pump and backup seawater pump will be required.

Feasibility Study Report - Volume 2 of2EA TeO - Suez Petrochemical Complex GTP ProjectSuez, Egypt

• 6.5 Utilities

Section 6 Page 6

June, 2000

•

•

The following table swnmarizes the utility conswnption for the facility.


Utilities Summary

• •Section 6 Page 7

June, 2000

Utility Units ISBL Utilities! Utilities! Total("+" Produced Plants Offsites Offsites Complex& "_" Consumed) Net Consumed Supplied NetHHP Steam (lJ MT/h 3.9 -3.9 0.0 0.0HP Steam (1) MT/h -51.7 -48.5 100.2 0.0MPI Steam (1) MT/h 38.3 -38.3 0.0 0.0MP2 Steam (I) MT/h -31.1 0.0 31.1 0.0LP Steam (1) MT/h -7.5 -31.0 38.5 0.0LLP Steam (1) MT/h -8.2 -36.0 44.2 0.0Steam Condensate (1) MT/h 152.3 -152.3 0.0 0.0Turbine Condensate (I) MT/h 107.3 -140.2 32.9 0.0Cooling Water(2) m3/h -15,556 -427 15,983 0.0Potable Water (1) m3/h -2.1 -0.4 2.5 0.0Demin. Water (1) m3/h 0.0 -327.5 327.5 0.0Boiler Feed Water (1) m3/h -398.1 -107.2 505.3 0.0Seawater (3) m3/h -11,616 -16,116 27,732 0.0RawlPlant Water (4) m3/h -7.5 -70.0 0.0 -77.5Instrument Air (1) Nm3/h -4,502 -400 4,902 0.0Plant Air (1) Nm3/h -6,660 -500 7,160 0.0Nitrogen (1) Nm3/h -12,938 -400 13,338 0.0Natural Gas! Fuel Gas (5) MW -85.8 -85.8 0.0 0.0Electric Power (4)(6) kW -23,917 -23,408 5,300 -42,025Notes:(I) Streams are internally generated within the GTP Facility.(2) Closed loop circuit within the GTP Facility.(3) Seawater supply/return via pipelines from/to sea.(4) Import to GTP Facility(5) Net make-up of fuel to the GTP Facility is nil. Energy is provided by byproduct fuels generated within the GTP Facility.(6) A small amount of electric power (approximately 5300kw) will be generated by the GTP Facility.(1) All flows are those expected at normal operating conditions.

uop KVJERNER-


• 7. Equipment Information

Section 7 Page 1

June, 2000

•

•

7.17.27.37.4

MethanolMTOPolyolefinsUtilities/Offsites

Page 2

Page 7

Page 17

Page 20


•

•

•

7.1 Methanol

Single Line Equipment List

Section 7 Page 2

June, 2000

KVA:RNER*

•

•

;(vaerner Process uop PROJECT: GTP FEASIBILITY STUDY PROJ.#: H1990720

CLIENT: SUEZ PETROCHEMICAL COMPLEX

ONE LINE EQUIPMENT LIST LOCATION: SUEZ, EGYPT

METHANOL PLANT AREA: METHANOL

REV: 0 BY: MK DATE: 8/9/99

Item No. Description No. Remarks Rev.

COLUMNS

C-101 Saturator 1

C-401 Topping Column 1

C-601 Decarbonator 1

COMPRESSORS

K-201 Syngas Compressor 1

K-301 Circulator 1

FANS

K-101 F.D. Fan 1

K-102 1.0. Fan 1

FILTERS

F-101 AlB F.D. Fan Filters/Silencers 2

F-301A1B Crude Methanol Filter 2

HEAT EXCHANGERS

E-101 HDS Heat Exchanger 1

E-102 Radiant Shield Boiler 1

E-103 Steam Superheater 1

E-104 Reformer Feed Preheater 1

E-105 N.G. Feed Preheater 1

E-106 Combustion Air Preheater 1

E-107 Reformed Gas Boiler 1

E-108 H.P. BFW Heater 1

E-109 Demineralized Water Heater 1

E-110 Syngas Air Cooler 1

E-111 Prereformer Feed Preheater 1

E-112 Syngas Trim Cooler 1

Section 7 Page 3

•

•

•

Kvaerner Process uop PROJECT: GTP FEASIBILITY STUDY PROJ.#: H1990720


ONE LINE EQUIPMENT LIST LOCATION: SUEZ,EGYPT




HEAT EXCHANGERS (Conrd)

E-201 Interstage Cooler 1

E-301 Warm Shell Loop Interchanger 1

E·302 Saturator Water Heater 1

E-303 Loop Start-Up Heater 1

E-304 Cold Shell Loop Interchanger 1

E-305 Crude Methanol Condenser 1

E-306 Crude Methanol Trim Cooler 1

E-401 Topping Column Steam Reboiler 1

E-402 Topping Column Bottoms Cooler 1

E-403 Topping Column Reflux Condo 1

E-404 Topping Column Vent Condenser 1

E-601 Syngas Turbine Condenser 1

E-603 Stripped Condensate Cooler 1

E-604 Polishing Cooler 1

MISCELLANEOUS ITEMS

H-101 Reformer 1

H-102 Flue Gas Stack 1

J-301 Fuel Gas Eductor 1

PACKAGES

X-301 PSA Unit 1

X-601 Phosphate Dosing Set 1

X-602 Caustic Dosing Set 1

Section 7 Page 4

•

•

•







PUMPS

P-101 AlB Saturator Circulation Pump 2

P-102 AlB Process Condensate Pump 2

P-402A1B Topping Column Reflux Pump 2

P-403A1B Topping Column Bottoms Pump 2

P-601 AlB Syngas Turbine Condo Pump 2

P-603AIB Stripped Condensate Pump 2

REACTORS

R-101 Pre-Reformer 1

R-301 Methanol Converter 1

TURBINES

KST-101 F.D. Fan Turbine 1

KST-102 I.D. Fan Turbine 1

KST-201 Syngas Compressor Turbine 1

KST-301 Circulator Turbine 1

MiscellaneousTurbine 1

VESSELS

V-101 Natural Gas K.O. Drum 1

V-102 Hydrodesulfurization Vessel 1

V-104 109 Barg Steam Drum 1

V-105 Reformed Gas Separator #1 1

V-106 Reformed Gas Separator #2 1

V-201 1st Interstage Separator 1

Section 7 Page 5

•

•

•






Item No. I Description No. Remarks Rev.

VESSELS (Cont'd)

V-301 Methanol Separator 1

V-302 Letdown Vessel 1

V-303 Loop Start-Up Heater Condensate Drum 1

V-401 Topping Column Reflux Drum 1

V-402IToppmg Column Reboiler Condensate

1Drum

V..s01 Boiler Blowdown Drum 1

Section 7 Page 6

•

•

•


7.2 MTO


Section 7Page 7

June, 2000

•

•

•

Kvaerner Process PROJECT: GTP FEASIBILITY STUDY PROJ.#: H1990720

uop CLIENT: SUEZ PETROCHEMICAL COMPLEX


MTOPLANT AREA: MTOPLANT



BLOWERS

1065-C1 Main Air Blower 1

HEAT EXCHANGERS

1065-E1 Flue Gas Cooler 1

1065-E2 Catalyst Cooler 1

1065-E3 Reactor Product Desuperheater 1

1065-E4 Feed Superheater 1

1065-E5 Quench Tower Bottom Pumparound 1

1065-E6luuencn lower lOP t'umparouna I nm

1ICooler

1065-E7 Feed-Waste Water 1

1065-E8 Feed Vaporizer 1

1065-E9 Feed Stripper Reboiler 1

1065-E1 0 Waste Water Cooler 1

1065-E11 Waste Water Stripper Reboiler 1

1065-EA1 Quench Tower Top Pumparound Cooler 1

1

EXPANSION JOINTS 1

1065-EJ1 Regenerated Catalyst 1

1065-EJ2 Spent Catalyst 1

1065-EJ3A Recirculating Catalyst 1

1065-EJ3B RecircUlating Catalyst 1

1065-EJ4 Flue Gas (before cooler) 1

1065-EJ5 Flue Gas (after cooler) 1

FIRED HEATERS

1065-H1 Direct Fired Air Heater 1

1065-H3 Startup Heater 1

Section 7 Page 8

•

•

•




MTO PLANT AREA: MTOPLANT



FILTERS

1065-ME1 Main Air Blower Suction 1

1065-ME7 WasteWater 1

1065-ME8A Methanol Feed 1

1065-MEBB Methanol Feed 1

MISCELLANEOUS

1065-ME2 Main Air Blower Vent Silencer 1

1065-ME3 Main Air Blower Special Check Valve 1

1065-ME4 Flue Gas Stack 1

1065-ME5 Flue Gas Orifice Plates 1

1065-ME1 0 Reactor Feed Special Check Valve 1

1065-ME11 Catalyst Hoppers Ejector 1

1065-ME12 Reactor Stripper Steam Separator 1

1065-ME13 Steam Superheater Vent Silencer 1

DUST COLLECTORS

1065-ME6 Electrostatic Precipitator 1

DESUPERHEATERS

1065-ME9 Reactor Feed 1

PUMPS

1065-P2A Boiler Feed Water Circulation 1

1065-P2B Boiler Feed Water Circulation 1

1065-P2C Boiler Feed Water Circulation 1

1065-P2D Boiler Feed Water Circulation 1

1065-P4A Quench Tower Top Pumparound 1

1065-P4B Quench Tower Top Pumparound 1

1065-P5 Startup 1

1065-P6A Quench Tower Bottom Pumparound 1

Section 7 Page 9

•

•

•




MTO PLANT AREA: MTO PLANT



PUMPS (CONT'D)

1065-P6B Quench Tower Bottom Pumparound 1

1065-P7A Caustic Injection 1

1065-P7B Caustic Injection 1

1065-P8A Quench Tower Middle Pumparound 1

1065-P8B Quench Tower Middle Pumparound 1

1065-P9A Feed Stripper Bottoms 1

1065-P9B Feed Stripper Bottoms 1

1065-P1OA Feed Flash Drum 1

1065-P10B Feed Flash Drum 1

1065-P11A Waste Water Stripper Bottoms 1

1065-P11B Waste Water Stripper Bottoms 1

1065-P12A Sump 1

1065-P12B Sump 1

1065-P13A Slop 1

1065-P13B Slop 1

REACTOR

1065-R1 Reactor 1

1065-R2 Regenerator 1

1065-R3 Spent Catalyst Stripper 1

SLIDE VALVES

1065-SV1 Regenerated Catalyst 1

1065-5V2 Spent Catalyst 1

1065-SV3A Recirculating Catalyst 1

1065-SV3B Recirculating Catalyst 1

1065-SV4 Flue Gas 1

Section 7 Page 10

•

•

•




MTOPLANT AREA: MTOPLANT



CYCLONES

MTO Reactor 11

MTO Regenerator 2

TANKS

1065-TK1 Slop

VESSEL

1065-V1 Fresh Catalyst Storage Hopper 1

1065-V2 Equilibrium Catalyst Storage Hopper 1

1065-V3 Continuous Blowdown Drum 1

1065-V4 Intermittent Blowdown Drum 1

1065-V5 Steam Disengaging Drum 1

1065-V6 Feed Stripper 1

1065-V7 Feed Flash Drum 1

1065-V8 Quench Tower 1

1065-V9 Blow Pot 1

1065-V1 0 Waste Water Stripper 1

1065-V11 Caustic Injection Pot 1

1065-V12 Fuel Gas Knockout Drum 1

1065-V13 Sump Tank 1

Section 7 Page 11

•

•

•




LORP PLANT AREA: LORP PLANT



COMPRESSORS

1066-C1 MTO Product 1

1066-C2 Propylene 1

FILTERS

1066-ME1A MTO Product 1

1066-ME1B MTO Product 1

1066-ME2A Acetylene Saturation 1

1066-ME2B Acetylene Saturation 1

HEAT EXCHANGERS

1066-E1 Interstage Cooler No 1 1



1066-E4 DME Stripper Reboiler 1

1066-E5 DME Stripper Bottoms Cooler 1

1066-E6 Wash Water Exchanger 1

1066-E7 Wash Water Cooler 1

1066-E8 Methanol Absorber Effluent Cooler 1

1066-E9 Drier Feed Chiller 1

1066-E1 0 Regenerant Heater 1

1066-E11 Regenerant Cooler 1

1066-E12 Deethanizer Feed Chiller 1

1066-E13 Deethanizer Condenser 1

1066-E14 Deethanizer Reboiler 1

1066-E15 Acetylene Saturation Feed-Effluent 1

1066-E16 Acetylene Saturation Feed Heater 1

1066-E17 Makeup Gas Cooler 1

1066-E18 Net Gas Exchanger 1

1066-E19 Ethane Product Exchanger 1

1066-E20 Demethanizer Feed Chiller 1

1066-E21 Demethanizer Condenser 1

1066-E22 Demethanizer Reboiler 1

Section 7 Page 12

•

•

•

Kvaerner Process PROJECT: GTP FEASIBILITY STUDY PROJ.#: H1990720uop CLIENT: SUEZ PETROCHEMICAL COMPLEX





HEAT EXCHANGERS (CONTD)

1066-E23 Ethane/Ethylene Splitter Condenser 1

1066-E24 Ethane/Ethylene Splitter Reboiler 1

1066-E25 Depropanizer Condenser 1

1066-E26 Depropanizer Reboiler 1

1066-E27 Debutanizer Feed-Effluent 1

1066-E28 Debutanizer Condenser 1

1066-E29 Debutanizer Reboiler 1

1066-E30 Debutanizer Bottoms Cooler 1

1066-E31 Propane/Propylene Splitter Condenser 1

1066-E32 Propane/Propylene Splitter Reboiler 1

1066-E33 Propane Vaporizer 1

1066-E34 Propylene Condenser 1

1066-E35 Surface Condenser No 1 1

1066-E36 Surface Condenser No 2 1

87D-E1 Regenerant Steam Superheater 1

87D-E2 Regenerant Electric Superheater 1

87D-E3 Regenerant Cooler 1

MISCELLANEOUS

1066-ME3 MTO Product Driers Ejector 1

1066-ME4 Acetylene Saturation Ejector 1

1066-ME5 C2 and C3 Splitters Ejector 1

1066-ME6 Propylene Compressor Ejector 1

PACKAGES

1066-ME7 Ethylene Recovery PSA Unit 1

1

PUMPS

1066-P1A Interstage Condensate 1

1066-P1B Interstage Condensate 1

1066-P2A Surface Condenser Condensate No 1 1

Section 7 Page 13

•

•

•



LORP PLANT AREA: LORPPLANT



PUMPS (CONT'D) 1

1066-P2B Surface Condenser Condensate No 1 1

1066-P3A Surface Condenser Condensate No 2

1066-P3B Surface Condenser Condensate No 2 1

1066-P4A DME Stripper Charge 1

1066-P4B DME Stripper Charge 1

1066-P5A Methanol Booster 1

1066-P5B Methanol Booster 1

1066-P6A First Stage Caustic Circulation 1

1066-P6B First Stage Caustic Circulation 1

1066-P7 Second Stage Caustic Circulation 1

1066-P8A Water Circulation 1

1066-P8B Water Circulation 1

1066-P9A Caustic Injection 1

1066-P9B Caustic Injection 1

1066-P10A Water Injection 1

1066-P10B Water Injection 1

1066-P14A Deethanizer Bottoms 1

1066-P14B Deethanizer Bottoms 1

1066-P15A Ethane/Ethylene Splitter Overhead 1

1066-P15B Ethane/Ethylene Splitter Overhead 1

1066-P16A Depropanizer Overhead 1

1066-P16B Depropanizer Overhead 1

1066-P17A Debutanizer Overhead 1

1066-P17B Debutanizer Overhead 1

1066-P18A Propane/Propylene Splitter Overhead 1

1066-P18B Propane/Propylene Splitter Overhead 1

1066-P19A Propylene Compressor Suction Drum 1

1066-P19B Propylene Compressor Suction Drum 1

REACTORS

1066-R1 Acetylene Saturation 1

Section 7 Page 14

•

•

•







TURBINES

1066-T1 MTO Product Compressor 1

1066-T2 Propylene Refrigerant Compressor 1

VESSELS

1066-V1 First Stage Suction Drum 1

1066-V2 Second Stage Suction Drum 1

1066-V3 Third Stage Suction Drum 1

1066-V5 DME Stripper Charge Drum 1

1066-V6 DME Stripper 1

1066-V7 Water Wash Column 1

1066-V8 DME Absorber 1

1066-V9 Methanol Absorber 1

1066-V10 Methanol Absorber Knockout Pot 1

1066-V11 Caustic Scrubber 1

1066-V12 Caustic Scrubber Knockout Pot 1

1066-V13 Caustic Injection Tank 1

1066-V14 Water Injection Tank 1

1066-V15A MTO Product Drier 1

1066-V15B MTO Product Drier 1

1066-V16 Regenerant Knockout Pot 1

1066-V17 Guard Drier 1

1066-V18 Deethanizer 1

1066-V19 Deethanizer Receiver 1

1066-V20 Demethanizer 1

1066-V21 Ethane/Ethylene Splitter 1

1066-V22 Ethane/Ethylene Splitter Receiver 1

1066-V23 Depropanizer 1

1066-V24 Depropanizer Receiver 1

1066-V25 Debutanizer 1

1066-V26 Debutanizer Receiver 1

Section 7 Page 15

•

•

•






Item No. I Description No. Remarks Rev.

VESSELS (CONTD)

1066-V27 Propane/Propylene Splitter 1

1066-V28 Propane/Propylene Splitter Receiver 1

1066-V29 Propylene Compressor Suction Drum No 1 1




1066-V33 Propylene Surge Drum 1

87o-V1A Oxygenate Absorber 1

87o-V1B Oxygenate Absorber 1

87o-V1C Oxygenate Absorber 1

Section 7 Page 16

•

•

•

Feasibility Study Report - Volume 2 of2EA TCO - Suez Petrochemical Complex GTPProjectSuez, Egypt

7.3 Polyolefins

Overview Equipment List

Section 7 Page 17

June, 2000

KVA:RNER~

Feasibility Study Report - Volume 2 of2 Section 7 Page 18EATCO - Suez Petrochemical Complex GTP ProjectSuez, Egypt June, 2000

• Polyethylene

System Equipment

Ethylene Purification System Guard BedsComonomer Purification System Degassing Equipment

Guard BedsNitrogen Purification System Guard BedsHydrogen Purification System Guard BedsReaction System Reactor

Cycle Gas BlowerCycle Gas CoolerCatalyst FeederProduct Discharge

Resin Degassing Product Purge SystemRotary FeederScreener

Vent Recovery CondensersSeparatorsCompressor

• Resin Additive Handling HoppersBlenderFeedersTank

Pelleting Continuous MixerMelt PumpPelleterPelleter Cycle Water SystemPellet DryerConveying System

Packaging System BaggingIPalletizing Packages

•

Feasibility Study Report - Volume 2 of2 Section 7 Page 19EATCO - Suez Petrochemical Complex GTP ProjectSuez, Egypt June, 2000

• Polypropylene

System Equipment

Propylene Purification System Degassing EquipmentGuard Beds

Reaction System No. I ReactorCycle Gas BlowerCycle Gas CoolerCatalyst FeederProduct Discharge

Reaction System No.2 ReactorCycle Gas BlowerCycle Gas CoolerResin Transfer SystemProduct Discharge

Resin Degassing Product Purge SystemRotary Feeder

Vent Recovery CondensersRecovery Column

•Compressor

Resin Additive Handling HopperBlenderFeederTank

Pelleting Continuous MixerMelt PumpPelleterPelleter Cycle Water SystemPellet DryerPellet Screener

Packaging System Bagging/Palletizing Packages

•

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•

•

Feasibility Study Report - Volume 2 of2BATCO - Suez Petrochemical Complex GTPProjectSuez, Egypt

7.4 Utilities/Offsites


Section 7 Page 20

June, 2000

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UTILITIES/OFFSITES AREA: UTIL1TIES/OFFSITES

REV: PO BY: HLB DATE: 10/5/99


AGITATORS

Raw Water Treatment System

Y-U101 Sodium Sulfite Agitator 1 Part of Package X-U105

HP Boiler/Deaerator

Y-U500 Phosphate Tank Agitator 1 Part of Package X-U504

Y-U505 Morpholine Tank Agitator 1 Part of Package X-U505

Y-U506 Hydrazine Tank Agitator 1 Part of Package X-U506

BLOWERS

Condensate Treatment

K-U501 AlB Regeneration Blower 2 Part of Package X-U507

Plant & Sanitary Wastewater Treatment

K-U800AlB Aeration Blower 2 Part of Package X-U800

Flare Systems

K-U900 Cryogenic Flare Air Blower 1 Part of Package X-U901

TURBINES

BFW Treatment System

PST-U501 HP Boiler Feed Water Pump Turbine 1

Electrical Generator

GST-U701 Power Generating Steam Turbine 1

COMPRESSORS

Instrument Air/Plant Air Compressor

K-U701 AlB/C Air Compressor 3 Part of Package X-U701

Section 7 Page 21

•

•

•


ONE LINE' EQUIPMENT LIST LOCATION: SUEZ, EGYPT

UTILITIES/OFFSITES AREA: UTILITIES/OFFSITES



FILTERS

Raw Water Treating

Y-U106A1B Raw Water Filter 2

Seawater Cooling

Y-U200AlB Seawater Strainer 2

MTO Byproduct Water Treating

Y-U400AlB Organic Trap Filter 2

Instrument AirlPlant Air Compressor

Y-U701 AlBIC Inlet Air Filter 3 Part of Package X-U700

Y-U702 AlBIC Dryer Pre-filter 3 Part of Package X-U701

Y-U703 AlBIC Dryer After-filter 3 Part of Package X-U701

HEAT EXCHANGERS

Seawater Cooling System

E-U200 A-G Seawater I Fresh Water Exchanger 7

Potable Water System

E-U300 Potable Water Cooler 1

Electric Generator

E-U701 Power Generating Surface Condenser 1

Instrument AirlPlant Air Compressor

E-U702 AlBIC Intercooler 3 Part of Package X-U700

E-U703 AlBIC Aftercooler with KO pot 3 Part of Package X-U700

Section 7 Page 22

•

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MISCELLANEOUS


ME-U102 Raw Water Chlorinator 1 Part of Package X-U101

ME-U103 Raw Water Chlorinator Eductor 1 Part of Package X-U101

ME-U107 AlB Water Softener 2 Part of Package X-U112

ME-U108 Salt Dissolving Sump 1

ME-U110AlB Reverse Osmosis Membranes 2 Part of Package X-U109

ME-U115AlB Mixed Bed Polisher 2 Part of Package X-U114

ME-U117 RO Polisher Membranes 1 Part of Package X-U116

Seawater Cooling

ME-U200AlB Seawater Suction Screen 2


ME-U305 Potable Water Chlorinator 1 Part of Package X-U304

ME-U306 Potable Water Chlorinator Eductor 1 Part of Package X-U304

ME-U401 AlB Organic Trap 2 Part of Package X-U409

ME-U402A1B Pressurized Bubble Contactor 2 Part of Package X-U400

ME-U403 Thickener 1

ME-U404A1B Fluidized Bed Reactor 2 Part of Package X-U400

ME-U406A1B Reverse Osmosis Membranes 2 Part of Package X-U405

ME-U407 Oxygen PSA Unit 1 Part of Package X-U400

ME-U408 Drying Beds 1

Condensate Treatment System

ME-U510AlB Condensate Polisher 2 Part of Package X-U507

HP Boiler I Deaerator

ME-U500 Deaerator 1

ME-U501 107 Barg Steam Desuperheater 1

ME-U503A1B HP Boiler 2 Part of Package X-U502

Section 7 Page 23

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MISCELLANEOUS (CONrD)

HP Boiler I Deaerator (Cont'd)

ME-U508 42.8 Barg Steam Desuperheater 1

ME-U509 27.8 Barg Steam Desuperheater 1

Cryogenic Nitrogen System

ME-U601 Nitrogen Generator 1 Part of Package X-U600

Instrument Air Dryer System

ME-U704 AlBIC Air Dryers 3 Part of Package X-U701


ME-U801 Dry Chlorine Feeder 1 Part of Package X-U800

ME-U802 Sewage Treatment Plant 1 Part of Package X-U800

ME-U803 Dissolved Air Flotation Unit 1 Part of Package X-U804

ME-U805 Waste Water Facultative Pond 1

Sumps

ME-U813 Process Sump- Methanol Unit 1

ME-U814 Process Sump- MTO Unit 1

ME-U815 Process Sump- PEIPP Unit 1

ME-U816 Process Sump- Utilities Area 1

ME-U817 Process Sump- Storage Area 1

Flare Systems

ME-U902 Main Flare Stack 1 Part of Package X-U900

ME-U903 Main Flare Ignition System 1 Part of Package X-U900

ME-U904 Cryogenic Flare Stack 1 Part of Package X-U901

ME-U905 Cryogenic Flare Ignition System 1 Part of Package X-U901

Section 7 Page 24

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PACKAGES


X-U101 Raw Water Chlorination Package - Includes Items ME-U102 & ME-U103

X-U105 Sodium Sulfite Addition Package 1 Includes Items V-U101, Y-U101 & P-U101 AlB

X-U109 Reverse Osmosis Treatment Package - Includes Items ME-U110 AlB & P-U106 AlB

X-U112 Water Softener Package - Includes Items ME-U107 AlB & P-U107 AlB

X-U114 Mixed Bed Package - Includes Items ME-U115 AlB & P-U113 AlB

X-U116 RO Polishing Package - Includes Items ME-U117 & P-U118 AlBIC

Cooling Water System

X-U201 Electrolitic Chlorinator Package 1


X-U304 Potable Water Chlorination Package - Includes Items ME-U305 & ME-U306.

MTO Water Treating System

X-U400 Biological Treatment Package - Includes Items ME-U402 AlB , ME-U404 AlB,

ME-U407, P-U403 AlB & P-U404 AlBIC.

X-U405 MTO Reverse Osmosis Package Includes Items ME-U406 AlB & P-U405 AlB.

X-U409 Organic Trap Package - Includes Items ME-U401 AlB

HP Boiler System

X-U502 HP Boiler Package Includes items ME-U503 AlB.

X-U504 Phosphate Package - Includes items V-U502, Y-U500 & P-U504 AlB.

Section 7 Page 25

•

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UTILITIESIOFFSITES AREA: UTIL1TIES/OFFSITES



PACKAGES (CONTO)

Oeaerator System

X-U505 Morpholine Dosing Package Includes items V-U505, Y-U505 & P-U505 NB.

X-U506 Hydrazine Dosing Package Includes items V-U506, Y-U506 & P-U506 NB.

Condensate Treatment System

X-U507 Condensate Polisher Package - Includes Items ME-U510 NB , K-U501 NB &

P-U512NB.

Nitrogen Generation System

X-U60D Cryogenic Nitrogen Package - Includes Item ME-U601.

Instrument Air 1Plant Air Compressor

X-U7DD Air Package - Includes Items K-U701 NB/C, Y-U701 NB/C,

ME-U704 NB/C, E-U702 NB/C & E-U703 NB/C.

Instrument Air Dryer System

X-U701 Air Dryer Package - Includes Items ME-U704 NB/C, Y-U702 NB/C &

Y-U7D3 NB/C.

Plant & Sanitary Wastewater Treating

X-U80D Sanitary Sewage Treatment Package Includes Items ME-U801, ME-U802 & K-U8DD NB.

X-U804 Dissolved Air Flotation Package Includes Items ME-U803, P-U800 NB & P-U801 NB.

Flare Systems

X-U9DD Main Flare Package - Includes Items ME-U9D2 & ME-U903.

X-U901 Cryogenic Flare Package Includes Items ME-U904, ME-U905 & K-U900.-

Section 7 Page 26

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PUMPS


P-U101 NB Sodium Sulfite Pump 2 Part of Package X-U105

P-U102NB Plant Water Supply Pump 2

P-U106NB/C Reverse Osmosis Feed Pump 3 Part of Package X-U109

P-U107 NB Regeneration Pump 2 Part of Package X-U112

P-U113NB Acid Regeneration Pump 2 Part of Package X-U114

P-U118NB/C Treated Water RO Feed Pump 3 Part of Package X-U116

Firewater System

P-U103NB Diesel Firewater Pump 2

P-U104 Electric Firewater Pump 1

P-U105NB Firewater Jockey Pumps 2

P-U108NB Firewater Diesel Fuel Pump 2


P-U201 NB/C Seawater Supply Pump 3

P-U203NB Seawater Diesel Fuel Pump 2

P-U204NB/C Fresh Cooling Water Pump 3


P-U300NB Potable Water Pump 2


P-U401 NB Organic Trap Feed Pump 2

P-U407 NB Mixed Bed Polisher Feed Pump 2

P-U403NB Fludization Pump 2 Part of Package X-U400

P-U404NB/C Recycle Pump 3 Part of Package X-U400

P-U405NB/C Reverse Osmosis Feed Pump 3 Part of Package X-U405

Section 7 Page 27

•

•

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PUMPS (CONT'D)

BFW Treating System

P-U510 Neutralization Mixing & Transfer Pump 1

P-U512AlB Caustic Regeneration Pump 2 Part of Package X-U507

P-U513AlB BFW Transfer Pump 2

HP BoilerlDeaerator

P-U501 AlB HHP Boiler Feedwater Pump 2

P-U502 AlBIC HP Boiler Feedwater Pump 3

P-U503A1B Condensate Flash Drum Pump 2

P-U504 AlB/C Phosphate Pump 3 Part of Package X-U504

P-U505A1B Morpholine Pump 2 Part of Package X-U505

P-U506A1B Hydrazine Pump 2 Part of Package X-US06

Storage Area

P-U600AlB Debutanizer Bottoms Fuel Pump 2

P-U601 AlB Methanol Feed Pump 2

P-U602A1B Hexene Comonomer Charge Pump 2

P-U603A1B Ethylene Feed Pump 2

P-U604A1B Propylene Charge Pump 2

P-U605A1B Butane Comonomer Charge Pump 2

Electric Generator

PU701 AlB GST Condensate Return Pump 2


P-U800AlB Slops Removal Pump 2 Part of Package X-U804

P-U801 AlB Recirculation/Aeration Pump 2 Part of Package X-U804

Sumps

P-U802A1B Methanol Area Sump Pump 2

P-U803A1B MTO Process Area Sump Pump 2

P-U804A1B PEIPP Process Area Sump Pump 2

Section 7 Page 28

•

•

•







PUMPS (CONrD)

Sumps (Cont'd)

P-U805A1B Utilities Area Sump Pump 2

P-U806A1B Storage Area Sump Pump 2

Flare System

P-U900 Main K.O. Drum Transfer Pump 1

VESSELS


V-U101 Sodium Sulfite Tank 1 Part of Package X-U105

Firewater System

V-U103 Plant Water & Firewater Storage Tank 1

V-U104 Firewater Diesel Fuel Storage Tank 1


V-U200 Fresh Cooling Water Drum 1

V-U201 Seawater Diesel Fuel Tank 1


V-U300 Potable Water Storage Tank 1


V-U401 Clearwell 1

V-U403 Mixed Bed Polisher Surge Tank 1

BFW Treating System

V-U501 Condensate Flash Drum 1

V-U51 0 Acid Storage Tank 1

V-U511 Caustic Storage Tank 1

V-U512 Neutralization Tank 1

V-U513 Boiler Feed Water Tank 1

Section 7 Page 29

•

•

•







VESSELS (CONrD)

HP Boiler I Deaerator

V-U500 HP Boiler Blowdown Drum 1

V-U502 Phosphate Tank 1 Part of Package X-U504

V-U505 Morpholine Tank 1 Part of Package X-U505

V-U506 Hydrazine Tank 1 Part of Package X-U506

Nitrogen Generation System

V-U600 Nitrogen Surge Drum 1

Instrument/Plant Air System

V-U700 Instrument Air Receiver 1

V-U701 Plant Air Receiver 1

Flare Systems

V-U900 Main Flare K.O. Drum 1

V-U901 Cryogenic Flare K.O. Drum 1

Storage Tanks

TK-101 Crude Methanol Storage Tank 1

TK-102 AlBIC Ethylene Storage Tank 3

TK-103 AlBIC Propylene Storage Tank 3

TK-104 Butene-1 Storage Sphere 1

TK-105 Hexene Storage Tank 1

TK-106 Debutanizer Bottoms Storage Tank 1

Section 7 Page 30


•

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8. Preliminary Site Plan

Section 8 Page 1

June, 2000

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• 9. Preliminary Plot Plans

Section 9 Page 1

June, 2000

•

•

Preliminary plot plans are included only in the confidential version of the feasibility studyreport.


• 10. Buildings

Section 10 Page 1

June, 2000

•

•

The following buildings have been included in the scope of the Suez PetrochemicalComplex Gas to Polymers facility:

Administration Building

A single story building, approx. 40m wide x 60m long x 5m high, to provide officespace for the facility administration staff.

Main Gate Guard House

A single story building, approx. 5m wide x 10m long x 3m high, to provide guardhousing at the main gate.

Stores Warehouse/Maintenance Building

A single story building, approx. 60m wide x 75m long x 5m high, to provide storagespace for spare parts and to provide a maintenance shop area for minor repairs.

Firehouse/Clinic Building

A single story building, approx. 20m wide x 30m long x 5m high, to provide aparking area for emergency vehicles and a treatment area for minor first aid cases.

Electrical Substation Building

A single story building, approx. 25m wide x 25m long x 705m high, to house thefacility electrical switchgear. The electrical power transformers will be located in anoutdoors area immediately adjacent to the building.

Control Room/Laboratory

A single story control room/laboratory, approx. 30m wide x 50m long x 5m high, toprovide facilities for the plant operations staff. , The building also includes alaboratory for the testing offeedstocks and products for the facility.

Remote I/O Buildings(RIB's)

A total of four RIB's have been included within the facility scope. One RIB will belocated in each of the three process plants, the remaining RIB will be located in theOffsite/Utility area These purpose built buildings will serve as DCS I/Omarshalling points as well as housing the electrical motor control center for the unit.

•

•

•

Feasibility Study Report - Volume 2 of2BATCO - Suez Petrochemical Complex GTP ProjectSuez, Egypt

11. Preliminary EPC Schedule

Section 11 Page 1

June, 2000

KV~RNER~

•

PruJeci Sta'" OIJANOO

p,.jc" Flnbh JOJUN04

Dat. Date GUANO.

Run Date 17JULOO

C Prknavera S)'Item-. Inc.

Earlj'Bar

ProlreuOar

tAn

•

SUZ PETROCHEMICAL COMPLEX, EGYPTGTP FEASffiILITY STUDY

PRELmnNARYPROJECTSCHEDULE

Sbedlorl KVAERNERE&CDate Rnltlon o.ccbd ~ppron.


•

•

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12. Procurement Plan

12.1 Procurement Strategy12.2 International Transportation Logistics12.3 Preliminary Host Country Logistics Plan12.4 Host Country & Middle East Suppliers12.5 Potential U.S. Suppliers

Section 12 Page 1

June, 2000

Page 2

Page 4

Page 6

Page 7

Page 10


12.1 Procurement Strategy

Section 12 Page 2

June, 2000

•

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One of the keys to success for a project is the planning and control ofmaterials from their inception in engineering through to site installation. Aprime procurement motivation is 'Buy Early' to insure that vendor datadoes not drive the design schedule, and materials availability does notdrive the construction schedule.

The approach to procurement services for the Suez Petrochemical Complexwill be to purchase equipment and materials on a worldwide basis inaccordance with project specifications, complete with Supplier Certificates,schedule and in compliance with the project Approved Manufacturer's Listdeveloped for the project.

During the initial phase of the project a procurement strategy will bedeveloped to address the following critical areas:

• Construction Contracts Strategy plan, this will set the framework for thevarious inquiry/contract packages and drive the design engineering andprocurement effort to meeting the key dates in the overall projectschedule.

• Identification of long lead equipment and critical vendor data to insurethat the lead times are incorporated into the project schedule.

• Identification of supplier representative support requirements toconstruction and/or commissioning/start-up.

• Analyze logistics to identify the optimum methods and routes oftransportation.

During the course ofthe project, the following procurement activities will beundertaken:

• Solicit quotations, make appropriate recommendations, negotiate withthe successful vendor, award and issue purchase orders for equipmentand/or materials to be purchased.

• Purchase at optimum cost consistent with quality and performancerequired.

• Implement procedures for the purchasing of construction contingencyspare parts at the time of placement of the purchase order to reduce thecapital cost ofthe facility.


Section 12 Page 3

June, 2000

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• Process all purchase orders through to final invoice.

• Utilize pro-active expediting via both in-house and in-plant presence toensure timely delivery ofvendor data and materials.

• Monitor manufacture or fabrication and provide early warning ofpossible delays to insure that pro-active corrective action can be taken.

• Ensure that Vendor's documentation is received in accordance with thePurchase Order requirements to meet the project program.

• Develop an inspection plan to determine the level of inspection for allequipment and materials. For critical items, pre-inspection meetingswill be conducted at the manufacturer's facility. The purpose of suchmeetings will be to review the project specifications, inspection criteria,the manufacturer's quality program and to establish the requiredinspection hold points.


12.2 International Transportation Logistics

Introduction

Section 12 Page 4

June, 2000

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The project will utilize the services ofa worldwide Freight Forwarder to insurethat all equipment and materials will be transported to the appropriate port ofexportation and/or marshalling area(s). The Contractor working in conjunctionwith the Freight Forwarder will interface with a Host Country Freight Forwarderto insure all required documentation has been prepared to expedite customsclearance and subsequent delivery ofequipment and materials to the project site.

Shipping Plans

As soon as weights, sizes, countries of origin, destinations and delivery dates areidentified, the requirements will be reviewed against possible transportationroutes and a Shipping Plan will be drawn up. Size and weight limitations,transportation, time span and any problem areas will be determined to identifyequipment for which rigging and spreader beams may be required for handlingand transportation.

Packing Instructions

Packing Instructions will be prepared and issued as part ofthe purchase order toensure that the equipment and materials are suitably protected during lifting,transport and storage.

Transportation Procedures

The Contractor will be responsible for the coordination ofall inland, air and oceantransportation. In order to control the shipment ofmaterials and/or equipment, theContractor will purchase all materials and equipment 'Ex Works' (i.e. Loaded) atthe manufacturer's facilities. This approach will allow for maximum control,resulting in schedules being maintained and cost savings for the project.

Freight Forwarding Management

The use of a Freight Forwarder will provide a single point contact for theshipment ofmaterials and equipment. The Freight Forwarder will coordinate withthe Contractor for all movements from the manufacturer's and/or suppliersfacilities to a marshaling area at the port ofexport. The progress ofeach shipmentwill be monitored to ensure timely and safe delivery to the project site.

The Freight Forwarder will utilize regular liner service and where applicable,Charter/Part Charter to deliver equipment and materials to Egypt in accordancewith the project schedule. The preferred port ofcall for carriers will be the port ofAin EL Sokhna, due to its proximity to the project site.

•Feasibility Study Report - Volume 2 of2EATCO ~ Suez Petrochemical Complex GTPProjectSuez, Egypt

Section 12 Page 5

June, 2000

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Marshaling Plans

All equipment and materials will be delivered to a Marshaling area at the port(s)ofexport to facilitate export boxing/crating and preservation as required. Onceexport crating is completed all goods will then be consolidated. It is proposed tomaximize the use ofcontainerization and/or flat racks where possible in the eventequipment and materials will be shipped on liner service.

KVA:RNER"'


12.3 Preliminary Host Country Logistics Plan

Host Country Freight Forwarder

Section 12 Page 6

June, 2000

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The Contractor and the Freight Forwarder will coordinate with a Host CountryFreight Forwarder to ensure the timely customs clearance ofequipment andmaterials and to ensure that any duties/tax arrangements that the Client hasnegotiated with the local authorities are adhered to.

In-Country Transport

The Host Country Freight Forwarder will be responsible to coordinatewith an in-country transport carrier for the transportation ofequipment andmaterials from the port ofentry to the project site.

Route Survey

The Host Country Freight Forwarder will be responsible for the productionof a route survey from the portes) of entry. The purpose of the survey willbe to identify all potential hazards, e.g. bridges, power lines etc. on theroutes from the port(s) of entry to the project site. The survey will need tobe carried out as soon as shipping weights/sizes have been identified toinsure that all required changes are carried out in a timely manner.

Materials Receipt

Materials receipt is the responsibility ofthe Contractor and all boxes/packingcases etc. will be opened and examined on site, in accordance with the appropriateProject Procedure prior to being entered into the system as received.

Preservation and Storage

All materials and equipment will be stored in accordance with theappropriate Project Procedure or the Vendor's recommendations. Recordswill be maintained of all preservation requirements and any periodicactions that are needed during the storage phase will be logged andmonitored to ensure that they are carried out.


12.4 Host Country & Middle East Suppliers

Section 12 Page 7

June, 2000

The following provides an indication of potential Egyptian and MiddleEastern suppliers for the Suez Petrochemical Complex GTP Facility.

•

•

Electrical Equipment

Heat Exchangers

Merlin Gerin Dre Branch3 Nahda StreetNasrcity1st ZoneCairoEgypt

Saudi ElectricsBalbalaCorner ofBaladya & Binzagar StreetJeddah

Schneider Electric LtdPO Box 43103Abu DhabiUAE

Group ScheiderIndustrial City No.2PO Box 42472Riyadh 11541Kingdom of Saudi Arabia

FerrometalcoIsmai1ia Desert RoadHeliopolisCairoEgypt

Belleli Saudi Heavy Industries LtdPO Box 10138Jubai1 Industrial City 31961Kingdom of Saudi Arabia

Balcke-Durr Abu DhaiPO Box 8865Abu Dhabi

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Instrumentation

Pipe Fabrication

Steel

Valves

Section 12 Page 8

June, 2000

Dresser AI Rushaid Valve & Instr.PO Box 10145Jubail Industrial City 31961Kingdom of Saudi Arabia

ABB Arescon ECBuilding 175, Road 4304, Area 343Mina Sulman Industrial EstatePO Box 2774Manama

FerrometalcoIsmailia Desert RoadHeliopolisCairoEgypt

Saudi Iron & Steel CompanyMadinat AI- JubailAl - Sinaiyah 31961Kingdom of Saudi Arabia

FerrometalcoIsmailia Desert RoadHeliopolisCairo·Egypt

Keystone Saudi Inc.PO Box 1017Damman 31431Kingdom of Saudi Arabia

KVJERNER~

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Vessels

Section 12 Page 9

June, 2000

FerrometalcoIsmailia Desert RoadHeliopolisCairoEgypt

Belleli Saudi Heavy Industries LtdPO Box 10138Jubail Industrial City 31961Kingdom of Saudi Arabia

Deutsche Babcock Services CompanyPO Box 8865MussafahAbu Dhabi


12.5 Potential U.S. Suppliers

Section 12 Page 10

June, 2000

The following summarizes the potential U.S. suppliers ofmajor equipmentitems for the Suez Petrochemical Complex GTP Facility.

General Major Equipment Items

•

•

Columns

Heat Exchangers

PMSC-IRBY Steel14472 Creosote RoadGulfport, MS 39501

Tel.: 601-863-7733Fax: 601-863-7861

Tex-Fab Inc.P.O. Box 40508Houston, TX 77240

Tel.: 281-373-0855Fax: 281-373-0855

General Welding Works Inc.6800 Old Katy RoadHouston, TX 77024

Tel.: 713-869-6401Fax: 713-869-5405

Southern Heat Exchanger6100 Old Montgomery Hwy.Tuscaloosa, AL 35405

Tel.: 205-345-5335Fax: 205-345-0009

Steeltek Inc.602 W. 41 st StreetTulsa, OK 74107

Tel.: 918-446-4001Fax: 918-446-8317

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Pumps

Storage Tanks

Section 12 Page 11

June, 2000

Ingersoll Dresser Pump6840 Wynnwood LaneHouston, TX 77008

Tel.: 713-803-4400Fax: 713-803-4499

Flowserve Rotating Equipment Division4214 Bluebonnet DriveStafford, TX 77477

Tel.: 281-240-4120Fax: 281-240-5182

Pitt-Des Moines Inc.10200 Grogan's Mill Road, Ste. 300The Woodlands, TX 77380

Tel.: 281-774-2200Fax: 281-774-2201

Chicago Bridge & Iron8900 Fairbank N. HoustonHouston, TX 77064

Tel.: 713-896-2989Fax: 713-466-1259

KYA:RNERW

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Feasibility Study Report - Volume 2 of2BATCD - Suez Petrochemical Complex GTP ProjectSuez, Egypt

Vessels

Control Valves

Section 12 Page 12

June, 2000

Tex-Fab Inc.P.O. Box 40508Houston, TX 77240

TeL: 281-373-0855Fax: 281-373-5317

General Welding Works Inc.6800 Old Katy RoadHouston, TX 77024

TeL: 713-869-6401Fax: 713-869-5405

Freeport Welding & Fabricating Inc.211 East 8th

Freeport, TX 77541

TeL: 800-560-0121Fax: 409-233-0349

Fisher Controls4230 Greenbriar Dr.Stafford, TX 77477

TeL: 281-240-2000Fax: 281-274-6419

ValtekInc.1243 Nations Ford RoadCharlotte, NC 28217

TeL: 704-588-3040Fax: 704-588-3104

KVA:RNER*

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Feasibility Study Report - Volume 2 of2EATCO - Suez Petrochemical Complex GTP ProjectSuez. Egypt

Transmitters

Control Systems

Honeywell Inc USA8440 Westglen DriveHouston, TX 77063

Tel.: 713-780-6500Fax: 713-780-6684

Fisher-Rosemount9110-F Perimeter Woods DriveCharlotte, NC 28216

Tel.: 704-598-5660Fax: 704-598-5681

Honeywell Inc USA8440 Westglen DriveHouston, TX 77063

Tel.: 713-780-6500Fax: 713-780-6684

Fisher-Rosemount Systems Inc4230 GreenbriarStafford, TX 77477

Tel.: 281-274-1850Fax: 281-274-1839

Moore Products Inc520 Clanton Road, Ste. B-1Charlotte, NC 28217

Tel.: 704-523-7355Fax: 704-525-3432

Bently Nevada Corporation7651 Airport Blvd.Houston, TX 77061

Tel.: 713-640-1111Fax: 713-640-1180

Section 12 Page 13

June, 2000

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Electrical Controls

uop

General Electric Company37 Villa Road, #412Greenville, SC 29615

Tel.: 803-241-3001Fax: 803-241-3005

ABB121 Woody Creek RoadGreer, SC 29650

Tel.: 803-244-9635Fax: 803-244-9634

Westinghouse25 Woods Lake Road, Ste. 314Greenville, SC 29607

Tel.: 803-233-8270Fax: 803-298-5692

Allen Bradley835 Hillcrest DriveCharleston, WV 25311

Tel.: 304-348-5211Fax: 304-348-4922

Section 12 Page 14

June, 2000


Methanol Plant Specific Equipment Items

Section 12 Page 15

June, 2000

•

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This information is included only in the confidential version of thefeasibility study report.

MTO Specific Equipment Items

This information is included only m the confidential verSIOn of thefeasibility study report.

Polyolefins Specific Equipment Items

This information is included only in the confidential verSIOn of thefeasibility study report.

OffsitefUtility Specific Equipment Items

This information is included only in the confidential verSIon of thefeasibility study report.

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Feasibility Study Report - Volume 2 of2£4TCO - Suez Petrochemical Complex GTP ProjectSuez, Egypt

13. Cost Estimates

13.1 Breakdown by General Categories13.2 Explanation ofMethodology13.3 Fixed Operating Requirement

Section 13 Page 1

June, 2000

Page 2

Page 13

Page 14


13.1 Breakdown by General Categories

Introduction

Section 13 Page 2

June, 2000

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The total estimated installed cost for the Suez Petrochemical Complex Gas toPolymers (GTP) Facility is broken down into the following major parts:

• Methanol Plant

• MTOPlant• Polyolefins Plant• Utilities/Offsites

• Other Costs

The EPC cost estimate summary is presented at the end of this section. The scope,basis, accuracy and breakdown details ofthe estimate are discussed below.

Scope of the Estimate

The GTP facility will be a grass-roots construction comprising an ISBL plantsupported by a utilities/offsites plant to produce 400 kMTA of bagged polyolefms,50% polyethylene and 50% polypropylene. The facility will be supplied withnatural gas (for feedstock and fuel), raw water, and electric power and willgenerate all additional utilities required.

The ISBL Plant comprises the following production units:

• Methanol production plant• Olefins production plant• Polyethylene production plant• Polypropylene production plant

The OSBL plant comprises the following systems:

• Raw Water Treatment System• Firewater System• Potable Water System• Stripped MTO Byproduct Water Treating

• Boiler Feedwater Treating• Condensate Polishing

• Deaerator and Condensate Return

• Cooling Water Systems - Closed Loop circulation and Sea-watercirculation, including seawater intake supply and return piping

• Wastewater Collection and Treating

• HP Boilers• Plant and Instrument Air Generation and Distribution

• Nitrogen Generation and Distribution

• Power Generation

• Flare Systems• Offsites Storage


Section 13 Page 3

June, 2000

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Site Description Overview

The proposed site is located in the North West Gulf of Suez Special EconomicZone, approximately 40 Km south of Suez City and 120 Km east of Cario City,close to the New Port at Ain El Sukhna. The Gas to Polymers (GTP) facility willbe located in the southern section of the zone in the area designated "PetroleumSection", which comprises of an area ofapproximately 11.90 Km2

•

The proposed facility will be supplied with natural gas feedstock, raw water andelectric power at the 33KV source level. Steam, instrument air, plant air andnitrogen will be generated within the facility.

Cooling water for the facility will be provided via a closed loop cooling watercircuit, the circulating cooling water will be cooled by seawater. Seawater will beused directly for some cooling requirements. In addition, air coolers will also beemployed where applicable.

Infrastructure roads are provided within the facility boundary, supply roads to/fromthe facility from the local highways are excluded from the scope ofthe facility.

The facility will be provided with the following buildings:

• Administration Building• Warehouse/Maintenance/Stores Building

• Emergency Services Building

• Electrical Substation

• Main Gate Guard House• Control RoomlLaboratory• Unitized I/O - MCC Buildings for each process unit


Estimate Basis

Section 13 Page 4

June, 2000

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The basis for the EPC cost estimate is given in Section 2 ofthis report, inaddition, the estimate is based on the following information:

• Project Description• Preliminary Plot Plans• Process Flow Diagrams

• Utility Flow Diagrams• Equipment Lists, with preliminary sizes and materials

• Licensor Information

Estimate Accuracy

The EPC cost estimate was developed utilizing the ICARUS (T") 2000 costestimating system and in-house criteria and methods to achieve an estimate that isreasonably considered to be within an accuracy of±15%.

Estimate Breakdown

The EPC cost estimate as presented at the end of this section, is broken down asfollows:

Materials

The direct cost portion of the EPC cost estimate includes equipment andmaterials as defmed below:

• Equipment

Process, Utility and Offsites equipment, as shown on the EquipmentLists contained in Section 7 of this Volume. This includes theinstalled spares as shown in the Equipment Lists.

• Piping

Including all pipe, fittings, flanges, piping valves and specials for allabove and below ground piping associated with the process, utilityand offsite areas ofthe facility.


• Electrical

Section 13 Page 5

June, 2000

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Including all electrical commodities, e.g. cable, conduit, cable tray,transformation equipment and switchgear etc. associated with theprocess, utility and offsite areas of the facility.

• Instrumentation

Including all tagged instrumentation including control systemassociated with the process, utility and offsite areas of the facilityas well as all required bulk materials e.g. hook-up materials,wiring, supports etc .

• Allowances

Allowances have been included in this portion of the EPC costestimate for the following items:

• Laboratory Equipment• Commissioning Spares• Delivery/Packing Costs FOB

Subcontracts

The costs for the following subcontracts for the erection of the facility havebeen included in the EPC cost estimate:

• Civils & Site Development

Includes all civil materials and labor costs associated with sitepreparation, drainage, in-plant roads, foundations and buildings, asidentified above, associated with the project.

• Steelwork

Includes all structural steel materials and labor associated with theprocess, utility and offsite areas of the facility including processstructures, pipe-racks and buildings.


• Painting

Section 13 Page 6

June, 2000

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Includes both paint materials and labor for the painting ofequipment and piping associated with the process, utility andoffsite areas of the facility.

• Insulation

Includes all insulation materials and labor for insulation ofequipment and piping associated with the process, utility andoffsite areas of the facility.

• Equipment Erection

Includes all labor and equipment (including cranes up to 25tonnes capacity) for the installation of all Equipment associatedwith the plant.

• Pipework Erection

Includes all labor for fabrication and erection of all above andbelow ground piping associated with the plant.

• Electrical Erection

Includes all labor associated with the erection of all electricalequipment and materials for the plant.

• Instrumentation Erection

Includes all labor required to erect instrument tagged items andbulk materials for the plant.

KV~RNER~

•Feasibility Study Report - Volume 2 0/2EA TCO - Suez Petrochemical Complex GTP ProjectSuez, Egypt

Other Direct Costs

Section 13 Page 7

June, 2000

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Additional direct costs have been included in the EPC cost estimate as follows:

• Temporary Facilities

This allowance includes the costs associated with setting up and runningtemporary field facilities required for both a Client and anEngineeringIManagement contractor at site. The allowance includes forOffices etc., a central warehouse, including all required racking and fittingsetc., as well as computing and communications systems and furniture etc.

• Plant/Field Costs

This allowance includes all general plant and site/road vehicles required bythe EngineeringlManagement contractor e.g. Fork-lift trucks for thewarehouse, vehicles for supervisory personnel etc., Heavy liftequipment/contracts and any special construction equipment that may benecessary for the erection/construction of the process, utility and offsiteareas ofthe facility.

• Artisan Assistance

An allowance has been included for Artisan labor to assist theEngineeringlManagement contractor during both the construction phase ofthe project and during testing and pre-commissioning.

• Shipping

This is an estimate of the freight costs from marshaling ports around theworld to the project site.

• Vendors Staff

This is an estimate of the cost of vendor specialists to supervise theinstallation and start-up ofequipment.

KVA:RNER*


Project ManagementlEngineeringlConstrnction Management

Section 13 Page 8

June, 2000

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This is an estimate of the cost associated with detail engineering, procurement andproject, construction and commissioning management and/or supervisory servicesto design, purchase, install and pre-commission the equipment and materials asdefined in this Volume.

Additional Costs

The costs for the following additional items have been included in the EPC costestimate:

• Profit/Contingency

A contingency allowance and Contractor Profit/Fee has been included in theEPC cost estimate based on a percentage of the Projects Total Engineering,Procurement and Construction estimate.

• Consultants

Consultant costs have been included in the EPC cost estimate.

Estimate Clarifications

The following clarifications to the cost estimate are provided:

• Schedule

The estimates are based on the overall schedule given in Section 9 of thisVolume.

• Soils Data

A soils survey was not provided for the feasibility study.

• Seawater Supply and Return

For the purpose of the feasibility study, the distance from the sea waterintake/return to the plant fence line has been assumed as 7km. It has alsobeen assumed that the seawater intake/return will occur at the sea-shore.


• Maintenance and Equipment Operating Tools

Section 13 Page 9

June, 2000

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It has been assumed that a third party "Core Maintenance" capabilityincluding craftsmen, supervision, equipment and small tools will be utilizedby the Owner to maintain the facility.

• Operating Procedures

The estimate includes for the preparation of operating procedures for theplant. Detailed operating procedures and training will be by the Owner.

Estimate Allowances

Allowances have been provided in the direct cost portion of the EPC cost estimateas shown below. They are termed "allowances" due to the uncertain state of theirspecification.

• Fire Fighting, Safety and Medical Equipment and Supplies - This wouldallow for small items used by individual personnel. Large or mobileequipment is assumed available.

• Vehicles - Trucks, rail cars, site vehicles,. and other mobile equipment thatenter and leave plant property, except as shown in the Equipment Lists.


Estimate Exclusions

Section 13 Page 10

June, 2000

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The following items are excluded from the EPC cost estimate as presented:

• Owner's N Development, Pre-Operations, Project Management,Commissioning/Start-up and Operations Costs, which include management,operations and support labor, including wages and benefits, recruitingexpenses and operator training.

• Working Capital, to cover the costs of raw materials, chemicals, catalysts,operating supplies, e.g. fuel, pallets, containers etc.

• License Fees and Initial Catalyst Charge

• Import Duties/Sales Taxes

• Currency Fluctuation

• Bank & Legal Fees

• Pre-completion Interest

• ECA Insurance Costs

• Owner's Contingency

• Permit Costs and Fees

• Owner Required Testing and Surveys

• Land Purchase Costs

• Capital/Running Spares

• Insurance

• Escalation

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Feasibility Study Report - Volume 2 of2EATCD - Suez Petrochemical Complex GTP ProjectSuez, Egypt

Equipment Cost Summary

Description Total ISBL OSBL TotalUSD,OOO USD,OOO USD,OOO

ColumnslTowers incl. Internals 54,557 1,153 55,710

Pressure Vessels 10,674 8,158 18,832

Storage Tanks 117 2,788 2,905

BinslHoppers & Fabricated Plate 5,012 5,012

FilterslDust Collectors/Screens 2,243 34 2,277

Stacks 387 387

Shell & Tube Heat Exchangers 32,617 679 33,296

Double Pipe Exchangers 284 284

Air Coolers 6,139 6,139

Other Heat Exchangers 9,636 908 10,544

Flares 751 566 1,317

Furnace Heaters 22,633 22,633

Compressors incl. Drivers 37,299 6,711 44,010

Fans and Blowers incl. Drivers 1,053 1,053

Pumps incl. Drivers 4,684 6,004 10,688

Steam Turbines 2,265 3,342 5,607

Packaged Equipment 20,426 11,219 31,645

CraneslHoists/Elevators etc. 796 79 875

Miscellaneous 5,691 3,848 9,539

Total Equipment 217,264 45,489 262,753

uop

Section 13 Page 11

June, 2000

KVA:RNER*


EPC Cost Estimate Summary

Costs reflect 1st Quarter 2000 levels, Suez, Egypt Location

Inside Battery Limits Plants:

Methanol Plant

MTOPlant

Polypropylene/Polyethylene Plants

Total Inside Battery Limits Plants

Outside Battery Limits Plants

Section 13 Page 12

June, 2000

USD 188,350,000

USD 164,200,000

USD 136,900,000

usn 489,450,000

USD 214,750,000

Total Estimated Erected Cost usn 704,200,000

• Escalation USD Excluded

SubTotal usn 704,200,000

Consultants USD Included

Contractor's Profit/Contingency USD Included

Total Lump Sum EPC Cost usn 799,100,000

•


13.2 Explanation ofMethodology

Section 13 Page 13

June, 2000

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The methodology by which this estimate was developed included fixing ofequipment prices via both vendor communications and in-house informationgathered from recent similar projects. The equipment information was input intothe ICARUS 2000 cost estimating system, bulk material information was adjustedas applicable based on Licensor information (where available), preliminary plotplan(s) and in-house experience for each of the particular production plants aswell as the Utilities and Off-sites etc.

To develop the overall cost estimate, individual unit cost estimates were preparedusing the ICARUS 2000 estimating software. These individual ICARUS unitestimates were then consolidated within ICARUS to achieve a total "Direct FieldCost". To these ICARUS generated figures has been added (outside the ICARUSsystem) productivity adjustments, commissioning and Capital/Running spares,freight, escalation, applicable owner costs and other project-related costs to developthe overall project cost estimate.

The cost estimate was initially developed on a US Gulf Coast basis using anestimated average subcontractor construction labor rate. The average rate includedwages, benefits, tools and consumables, construction equipment, management andsupervision, and other normal construction indirect costs including subcontractorrisk and profit. The US Gulf Coast estimate was then modified to an Egyptianbasis using both in-house and locally obtained data to reflect local Egyptian laborproductivity and costs.


13.3 Fixed Operating Requirements

Staffing Requirements

Section 13 Page 14

June, 2000

•

The following tables summarizes an estimate of the staffing requirements for thefacility.

Shift Personnel

The basis for the numbers ofpersonnel for shift related activities is four (4) shiftsi.e. three working shifts and one shift offper day.

Operations StaffUnit Control Plant Lab. Truck Total--

Supervisors Room Operators Staff Operators--Operators

Methanol PlantMTOPlantPE UnitPPUnitPolymerPackagingUtilities PlantOSBL Plant

Total per Shift 5 5 18 6 9 43

Maintenance StaffSupervisor Instrument Electrical Analyzer Mechanical Laborers Total

Total per Shift 1 2 1 1 2 2 9

Security Staff

•

ITotal per Shift

Total Shift Staff

ITotal Shift Staffper Shift

ITotal Shift Staff (Total of Four Shifts)

2

54

216


Day Staff

Section 13 Page 15

June, 2000

The following summarizes the numbers ofnon-shift personnel associated with theoperation of the facility.

Operations ManagementTotal

Operations ManagerMaintenance ManagerlIE EngineerChief chemistPlant Engineer

Total

Maintenance Sta:f:t<l)

12

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Supervisor Instrument Electrical Analyzer Mechanical Laborers Total

MethanolMTOPE UnitPPUnitPackagingUtilities/SupportWorkshop

Total 6 5 4 15 13 43

(1) The maintenance staff is for nonnal day-to-day operations support. Duringplant turnarounds and for major maintenance work, it is assumed that a thirdparty contractor will supplement the plant maintenance staff.

Laboratory StaffTotal

MethanolMTOPE UnitPPUnitPackagingUtilities

•

Total

Total Day Staff

ITotal Day Staff 62

7


Administrative Personnel

Section 13 Page 16

June, 2000

The following is an estimate ofthe administrations personnel required for thefacility.

TotalWorks ManagerAccountantAccounting ClerksSecretarialReceptionistWarehouse ClerkEMT

Total

Other Costs

10

•The following summarizes the infonnation that is to fonn the basis of the economicmodel:

Stock Information

• An allowance of3 weeks offinal product is recommended.

• An allowance of2 months stock ofpolymer catalyst/additives and MTOcatalyst is recommended.

• An allowance of 2 days of final product is recommended as work inprogress material.

Replacement Material

The following monetary sums for periodic replacement of catalysts andadsorbents are to be included in the economic model.

•

ItemCatalyst/AdsorbentCatalyst/AdsorbentCatalyst/AdsorbentCatalyst!Adsorbent

Amount

$4,030,000

Replacement PeriodEvery 2 YearsEvery 3 YearsEvery 5 Years

Every 10 YearsAnnual Average


Maintenance Costs

Section 13 Page 17

June, 2000

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An allowance for the average annual maintenance costs for the facility areincluded in the cost estimate, this allowance includes both maintenance labor,material costs and miscellaneous fixed costs, including insurance premiums.

The cost for the periodic reformer tube replacement in the methanol plant hasbeen included in this allowance.


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14. Environmental Considerations

14.1 Gaseous Discharges14.2 Liquid Discharges14.3 Solid Discharges14.4 Potential Major Hazards Summary

Section 14 Page 1

June, 2000

Pagel

Page 4

Page 5

Page 6


14.1 Gaseous Discharges

The gaseous discharges from the facility are categorized as follows:

Section 14 Page 2

June, 2000

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Stack EmissionsContinuous vent to atmosphere of the gases produced in the combustionoffuels.

Vent EmissionsContinuous vent to atmosphere of steam purges containing traceamounts ofdissolved gases.

Flare EmissionsEmergency and/or upset venting of process gases to the atmosphere viacombustion at the flare tip.

Stack Emissions

During normal operation, stack gases will be emitted to the atmosphere fromthe following sources:

Methanol Reformer StackMTO Reactor StackPackage Boiler Stacks

The estimated flowrates and composition data are presented ill theconfidential volume ofthe feasibility report.

Vent Emissions

During normal operation, the following vent streams will be emitted to theatmosphere:

Decarbonator VentThe decarbonator vent stream will contain small amounts of dissolvedhydrogen, carbon dioxide and methane.

Deaerator VentThe deaerator vent will contain trace amounts of dissolved oxygen andcarbon dioxide.

Intermittent Boiler BlowdownFlash steam from the boiler blowdown will be periodically vented to theatmosphere, flow-rates will be dependent upon boiler vendorrecommendations.

•Feasibility Study Report - Volume 2 of2EA TCO - Suez Petrochemical Complex GTPProjectSuez, Egypt

Section 14 Page 3

June, 2000

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Flare Emissions

Two flare systems are provided for the facility. One will provide for thehandling of all cryogenic service vents. The other flare will handle all otherflare discharges.

The flare systems are provided for emergency and/or upset conditions.During normal operation venting to the flare is not anticipated. Preliminaryflare loads for each ofthe plant areas are provided in the confidential volumeofthe feasibility report.


14.2 Liquid Discharges

General

Section 14 Page 4

June, 2000

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The liquid discharges from the process plants will be fIrst treated within thefacility prior to fInal discharge from the facility.

The source locations for this discharge from the facility are as follows:

Organic Trap (MTO Waste Treatment)Reverse Osmosis Unit (MTO Waste Treatment)Water Polisher (MTO Waste Treatment)Water Polisher (Boiler Feedwater Treatment)Water Softner (Raw Water Treatment)Reverse Osmosis Unit (Raw Water Treatment)

These streams will be combined and will be discharged to the sea via theseawater return line.

An additional water stream that combines the stonn water drainage systemoutfall and the Faculative Pond outfall will be sent to the sea via a trench(provided by others).

Other Liquid Waste Streams

An oil removal system has been included in the plant design. Thisprocess, will remove oil from water streams that could possibly becontaminated with oil in process equipment, e.g. compressor trains. Thisoil will need to be removed from the plant and disposed of in anenvironmentally safe manner.

KVA:RNER~

•Feasibility Study Report - Volume 2 of2EA TCO - Suez Petrochemical Complex GTPProjectSuez, Egypt

14.3 Solids Discharges

Catalysts and Adsorbents

Section 14 Page 5

June, 2000

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Periodically, there will be a need to discharge spent catalysts and adsorbents fromthe facility. Manufacturers' recommendations regarding the safe handling anddisposal of such items should be followed. Certain catalysts will require recyclingto recover their metals content.

Catalyst Fines

The MTO process will generate catalyst fmes, these fines will need to be disposedof in accordance with the catalyst manufacturers' recommendations.

Sludge

A waste solid from the bio-treat pond will require disposal from the facility.


14.4 Potential Major Hazards Summary

General

Section 14 Page 6

June, 2000

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This section qualitatively identifies the potential major hazards associatedwith the installation and operation ofthe GTP Plant.

The predominant major hazard to the plant, plant personnel and thesurrounding environment is a leak of one of the process fluids. The designand layout of the facility should be to minimize inadvertent emissions to theatmosphere through the implementation of control safeguards as well as theuse ofwell-trained operations and maintenance personnel.

The technologies utilized for the facility are based upon proven operatingplants around the world and information gained from the operation of theseplants will form the basis ofthe design and operation ofthe SPC facility.

Plant Location

The plant is to be located in an industrial complex near Suez, Egypt. Nearbyfacilities will include other petrochemical plants, the port of Ain EI Sokhnaand the main highway form Suez to Zaafrana.

Plant Layout Considerations

The preliminary plant layout indicates the basic layout of the complex.Detail layout reviews will be required to ensure adequate spacing ofequipment for access by plant operations, maintenance and safety personnel,maintenance equipment and emergency vehicles.

In the preliminary plant layout, the facility has been orientated so as to takeinto account the effect of the prevailing wind in the region. This willminimize the effect ofstack emissions on the reminder ofthe facility.

Fire-fighting Requirements

All local fire-fighting codes and regulations will need to be followed duringthe detailed design and subsequent operation of the facility. The feasibilitystudy has incorporated electric and diesel powered firewater pumps togetherwith an emergency bypass to utilize seawater as the fire-fighting medium.


Construction Considerations

Section 14 Page 7

June, 2000

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All local codes and regulations will need to be followed during theconstruction period. During construction, efforts should be made to containthe effects ofearth movement and to minimize the effect of run-off from thenew facility into existing drainage ditches.

Fuel storage will require containment to prevent contamination of the localenvironment in the event ofa leak from the storage vessel.

Plant Operation Considerations

Process Chemicals

The following summarizes the chemicals that are used and/or producedduring operation ofthe various processes employed in the facility.

The methanol plant utilizes the steam reforming of natural gas,consisting mainly of methane, to produce a synthesis gas mixture whichcontains primarily hydrogen, carbon monoxide and carbon dioxide. Thesynthesis gas mixture is converted in a recycle synthesis loop to producea methanol-water mixture, which will also contain a small amount ofdimethylether and traces ofreactant gases.

The MTO process utilizes the methanol-water mixture to produceprimarily ethylene and propylene together with some C4/C5+hydrocarbons and oxygenates such as dimethylether. The higherhydrocarbons are removed in the light olefin recovery process and aresent to the fuel system.

The propylene and ethylene are converted into their respective polymerswithin the polymer plant.

The utilities/offsites plant is concerned primarily with the handling andtreatment of the various facility water streams as well as the generationof steam and chemical storage. Chemicals such as sulfuric acid, causticsoda, boiler and water treatment chemicals will be utilized in this area

•Feasibility Study Report - Volume 2 oj2EA TCO - Suez Petrochemical Complex GTP ProjectSuez, Egypt

Process ()peration

Section 14 Page 8

June, 2000

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Within the methanol plant, the reformer control system is designed tominimize the possibility of carbon laydown and subsequent damage tothe reformer catalyst. Safeguards are also included to minimize thepossibility ofoverfiring the reformer with the potential ofdestroying thereformer tubes. The methanol synthesis loop reaction is inherently selflimiting.

Within the polyolefins process, the gas phase reaction is inherently selflimiting. Unlike liquid phase processes, reaction upsets cannot lead toover-pressurization of equipment. In a power failure, the reaction isautomatically terminated very quickly.

Process Hazards

Plant Personnel Safety

The process fluids are typically contained within the pressurized processplant. The various process plants operate at elevated temperatures andpressures and care will need to be taken to prevent operator andmaintenance staff coming into contact with the hot process and utilitypiping.

In the event of a release to the atmosphere of one or more of the reactiongases, there is the potential for the generation of a vapor cloud, whichcould result in a catastrophic explosion. Siting and/or design ofoccupied buildings will need to address the potential consequences ofsuch an incident. The electrical classification of the facility will have totake into account the fluids normally contained within the process toensure the correct electrical devices are incorporated into the facilitydesign.

Area gas detection devices will be required to monitor for gaseousemissions from the plant; these will include carbon monoxide andhydrocarbon detection systems.

Safety-showers/eyewash stations will be required at locations wherepersonnel can come into contact with chemicals within the facility.Adequate personnel protective equipment will need to be worn byplant personnel when handling chemicals in the facility.

There will be the need for noise reduction in the plant due to the use ofhigh-speed machinery. Noise reduction can be effected by designwhere possible, and also by the use of adequate personnel safetyequipment.


Section 14 Page 9

June, 2000

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Plant Overpressure

Over-pressure in any of the process units can occur due to anyone ofseveral reasons, for example a blocked outlet, coolant failure, powerfailure, external fire etc. In the event of an overpressure incident, theprocesses are to be equipped with relief valves designed to vent theoverpressure to a control device, e.g. a flare, to prevent a release to theatmosphere ofone or more ofthe reaction fluids.

Spill Containment

In the event of a process liquid spill it may be necessary to contain theliquid to prevent potential environmental contamination. In such areas,it will be necessary to curb the process areas and to drain the liquid awayfrom the process equipment to prevent possible 'liquid pooling' and theresultant fire hazard around equipment.

Chemical Storage

The storage of the reaction feedstocks and products should be such thatemissions to the environment are minimized. Vents from such tanksshould be sent to an approved control device, e.g. a flare. Separation ofand diking requirements for storage tanks containing flammablematerials will require siting per the local codes and regulations.

FeasibilityStudyReport - Voiume2of2EATCO - Suez Petrochemical Complex GTPProjectSuez, Egypt

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15. Technology Information

15.1 Commercial Experience Lists15.2 Perfonnance Guarantees15.3 Technology Fees

Section 15 Page 1

June, 2000

Page 2

Page 13

Page 14


15.1 Commercial Experience Lists

Section 15 Page 2

June, 2000

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The Suez Petrochemical Complex is planned to utilize well proven commerciallyestablished technologies for the conversion of gas to methanol and olefins topolyolefms.

Methanol

Since its introduction in 1967, the Imperial Chemical Industries (lCI) LowPressure Methanol Process has accounted for more than 60% of the world's newmethanol plant capacity. Kvaemer has extensive experience in the design andconstruction of methanol process units and offers the ICI Process. Methanolplants in which Kvaemer has been involved have a combined production capacityequivalent to over 70% of the installed capacity of plants built using ICItechnology and over 45% ofthe total world's methanol capacity installed.

This unique record has been established by the combination of ICI basictechnology and the vast experience of Kvaemer since the early 1960's in thedesign and construction of numerous plants all around the world for theproduction of methanol, ammonia, hydrogen, carbon dioxide, and Towns gas.This includes 30 methanol plants built since 1968 with a total capacity of over42,000 STPD of methanol, including 10 plants capable of producing over 2,000STPD. This technology is supported by 30 years of experience in steamreforming involving the supply of over 200 reformers in 25 different countriesmaking Kvaemer the world's most experienced steam reformer designer.

Kvaemer design engineers have thorough knowledge of all aspects of methanolplant operation, from water and gas treatment through reforming to final productloading. A Kvaemer designed plant ensures easy operation, not only duringnormal operation but also through all stages of start-up and shutdown conditions.

Kvaemer's patented furnace design offers one of the best temperature profiles inthe industry. The improved profile reduces localized stress and lengthens catalysttube life.

The highly selective synthesis catalyst minimizes feedstock usage and undesirableby-product formation. The catalyst is demonstrably more active and has longerlife than any other competitive catalyst. Plants with ICI catalyst have operated formore than six years with the same catalyst charge. ICI catalyst is not subject tothe variable quality problems of competing catalysts, which have led to the needfor their early replacement.

ICI and Kvaemer provide training facilities for operation and consulting servicesboth onsite and at their engineering offices. Regularly organized symposia atvarious locations for users of the ICI methanol process provide forums for newdesigns and operating techniques. Once a plant is commissioned, these backupservices by ICI and Kvaemer continue to be available for clients.


Section 15 Page 3

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Kvaemer is continuously developing its methanol plant design to achieve betterefficiencies, improved availability, better control, simpler operation, and lowercapital and production costs. Many Kvaemer developments are now an acceptedpart of modem high efficiency plant design and new designs under developmentwill continue this progress in providing cheaper, more reliable, more efficient, andlarger single-steam methanol plants.

The following table lists the Kvaemer experience with the ICI methanoltechnology:

KV~RNER~


KVAERNERlICI METHANOL EXPERIENCE LIST

Section 15 Page 4

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Year Client Location Capacity--(STPD)

1997 Methanex Chile 3100

1995 TIMC Trinidad 1800

1995 Methanex Chile 2950

1995 Sterling/BP Chemicals USA 1500

1992 BHP Australia 180

1992 Supennetanol Venezuela 2200

1990 Coastal Chern Inc. USA 222

1989 Caribbean Methanol Co. Trinidad 1650

1988 Deepak Fertilizers Limited India 330

1980 Mobil R&D New Zealand 2x2425

1980 Air Products USA 500

1980 ARCO Chemical Company USA 2000

1979 Ocelot Industries Canada 1350

1978 Sabic/Celanese Texas Eastern (SCT) Saudi Arabia 2300

1978 Borden Chemical USA 1900

1977 IMC/Air Products USA * 1500

1977 Techmashimport Tomsk, USSR 2750

1977 Techmashimport Gubaha, USSR 2750

1976 Methanor Holland 1100

1976 Celanese Chemical Co. (Expansion USA 22001800 to 2200 STPD)

1975 Celanese Chemical Co. USA ** 1300

1973 Taesung Methanol Industries Co. Korea 1100

1973 Induquimica (Subsidiary of CEPSA) Spain 660

1972 Metanor Camacari, Brazil 200

1971 PCUK (Ugine Kuhlmann) France 660

1971 Methanol Chemie Nederland Holland 1100

Year Client Location Capacity--(STPD)

1969 Chang Chun Petrochemical Co. Taiwan 165

1969 Celanese Chemical Co. USA 150011800

1969 Georgia Pacific Corp. USA 1200

1968 Taesung Lumber Industries Co. Korea 165

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* Project Shelved; ** Revamp Project

Section 15 Page 5

June, 2000


Methanol to Olefins (MTO)

Section 15 Page 6

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The conversion of methanol to oletins is a technology offered by UOP, the largestprocess licensing organization in the world, providing more than 65 licensedprocesses for the hydrocarbon processing industries. For more than 80 years, UOPhas been a world leader in developing and commercializing technology for licenseto the oil refining, petrochemical and gas processing industries. UOP has createdtechnologies that have led to advances in such diverse industries as motor fuels,plastics, detergents, synthetic fibers and food preservatives. Since its beginnings,UOP has been awarded more than 30,000 patents as a result of its dedicated researchand development commitment.

The UOPIHYDRO MIO process is based on a well proven fluidized catalyst bedstyle reactor design, which is similar to UOP's Fluidized Catalytic Cracking (FCC)process technology. UOP has licensed over 200 FCC units with numerousinnovative developments in this technology over the years. The MIO processperformance has been demonstrated in a 0.75 MI/day demonstration unit at NorskHydro's facilities near Oslo Norway. In addition, UOP has much experience in thedesign and supply of equipment for the production of polymer-grade ethylene andpropylene. UOP's experience in these related areas is shown in the followingexperience summary:

UOPIHYDRO MIO Process

UOP FCC Process

UOP Ethylene & PropyleneSplitters

1 demonstration unit initially operated in 1995.

More than 70 units on-stream since 1970 andover 200 units on-stream since 1942.

More than 180 projects completed.

•

The table on the following page indicates the commercialization experience ofUOP:

KV)ERNER~

•Feasibility Study Report - Volume 2 of2EATCD - Suez Petrochemical Complex GTP ProjectSuez, Egypt

UOP COMMERCIALIZATION EXPERIENCE - PARTIAL LIST

Section 15 Page 7

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Process Description Year 1st Unit Number ofPlaced in Units--Operation Licensed

Catalytic Condensation Gasoline/Higher Olefins 1935 300+

FCC Gasoline/Cycle OillLPG 1942 200+

HF Alkylation - Motor Fuel Gasoline 1943 100+HF Detergent Alkylation Alkylation ofBenzene 1948 33Platfonning Catalytic Refonning 1949 700+

Butamer Butane Isomerization 1955 50+

Merox Mercaptan Extraction 1958 1700+

Styrene Ethylbenzene Dehydro. 1960 14Molex n-Paraffm Recovery 1964 30+Sulfolane BTX Extraction 1965 100+

Pacol Olefin Production 1969 30+

Parex p-Xylene Recovery 1971 60+

MTBE-Ethennax MTBEIETBE 1976 30+

Penex Lt. Naphtha Isom. 1983 100+

KLP Acetylene Hydrogenation 1986 8

Oleflex Lt. Paraffm Dehydro. 1990 14

Cyclar BTX Production 1990 2

Detal Alkylation ofBenzene 1994 4Q-Max Cumene 1996 4

InAlk Gasoline 2001 3

KVA:RNEIf


Polyolefins

Section 15 Page 8

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Union Carbide offers the UNIPOL technology for both polyethylene andpolypropylene production. The UNIPOL PE and PP processes are simple, flexible,economical, safe, and superior to alternative technologies.

The simplicity of the UNIPOL PE and PP processes derives from advanced gasphase, fluidized bed technology and advanced catalyst technology. These systemsare very stable and flexible and use simple equipment. They produce a full rangeofcommercial products with no variation in capacity, and provide broad turndownwith uniform product properties.

The UNIPOL PE and PP processes produce granular resins of a consistent,predictable particle size distribution, that are conveyed, transported, and processedin conventional materials handling equipment. This granular resin may bepelletized in efficient, low energy UNIPOL pelleting equipment.

The UNIPOL PE and PP continuous resin handling facilities are simple, efficient,and inexpensive to operate, and require minimum investment. These advantagesdirectly result from reaction stability and product consistency. This productconsistency allows for continuous conveying of product from reaction/pelletingdirectly to bulk distribution or packaging feed hoppers. Trim resin from start-upor grade transitions, when available, is also metered and continuously mixed intoaim-grade resin. By contrast, batch resin handling facilities required by otherpolyethylene and polypropylene technologies are typically complex, inefficient,expensive to operate, and require much greater investment than UNIPOL PE andPP facilities.

From an operating point of view, the simplicity of the process and equipmentleads to reduced requirements for operating and maintenance staff, low energyconsumption and high efficiency. From a project point of view, the simplicityleads to significantly reduced capital requirements. A UNIPOL PE or PP plant iscompact, requiring relatively small land area. It includes no exotic equipment and,except for pelleting, only one major piece of rotating equipment for each reactor.The net result is a shortened project schedule, low investment, and simple startup.

The high safety standards of the UNIPOL PE and PP Processes are indicated byseveral hundred reactor-years of safe operation. The processes are designed with ahigh emphasis on safety and, as gas phase processes, are inherently safer thanalternative technologies

Kvaemer has undertaken almost 150 major polymer projects worldwide and hasmore experience in designing and constructing these plants than any otherengineering and construction company in the world.


Section 15 Page 9

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The range of projects handled includes polypropylene, high and low densitypolyethylene, linear low-density polyethylene, PVC, polyester, elastomers andvarious intermediates for these final products

Kvaemer has an extensive track record in polymers and particularly in polyolefinplants completed and in hand using Univation's UNIPOL technology. The totalnameplate capacity of UNIPOL Polypropylene and Polyethylene Plants engineeredby Kvaemer now exceeds 3,500,000 te/annum. In addition, studies and otherengineering and operating assistance have been carried out for Union Carbide andother Clients. Kvaemer engineers frequently join Union Carbide development andstart-up teams.

The following pages include a listing of the plants that have licensed the UnionCarbide UNIPOL technology for polyethylene and polypropylene production. Theplants with which Kvaemer has been associated are indicated by *. Projects inwhich Kvaemer has been associated with via other services, e.g. Process DesignPackages, Commissioning Services etc., have been indicated by **.

•Feasibility Study Report - Volume 2 of2BATCO - Suez Petrochemical Complex GTP ProjectSuez, Egypt

UNIPOL PE EXPERIENCE LIST

Section 15 Page 10

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UNIPOL PE Facilities Location Start-up ReactorUnits in Operation Year Lines

UCC LPPE-l USA 1969 1Borealis #1* Sweden 1971 3Qenos* Australia 1972 2UCCLP-l USA 1976 1Chemopetrol* Czech Republic 1976 4Chevron USA 1977 1Nova Canada 1977 2Borealis #2* Sweden 1978 1Russia PE #1* Russia 1980 3UCCLP-2 USA 1980 2Polisur Argentina 1981 1UCCLP-3 USA 1981 2Polifin* South Africa 1982 1ExxonMobil USA 1982 2Borealis #3* Sweden 1983 2ExxonMobil #2 USA 1983 2NUC Japan 1983 1Japan Polychem #1 Japan 1983 1Russia PE #2* Russia 1983 3Imperial Oil-ESSO** Canada 1983 1Nova #2 Canada 1984 2Kemya Saudi Arabia 1984 2Equistar#1 USA 1984 1Yanpet PE #1 ** Saudi Arabia 1985 3Sharq #1 Saudi Arabia 1985 1HCC#1 Korea 1986 1Borealis* Austria 1986 1Buna Gennany 1987 1Qilu* China 1987 2Daqing China 1988 1USI Far-East** Taiwan 1989 1HCC#2 Korea 1989 1UCCLP-5 USA 1989 1ExxonMobil #3* USA 1990 1Equistar#2 USA 1990 1

UNIPOL PE Facilities Location Start-up ReactorUnits in Operation Year Lines

Qilu#2 China 1990 1Petromont Canada 1991 1ShowaDenko Japan 1992 1MCCPE#2 Japan 1992 1OPP Brazil 1992 2CIPEN* France 1992 1Qenos Australia 1992 1Titan Malaysia 1993 1Sharq#2 Saudi Arabia 1994 1Chandra Asri Indonesia 1995 1Tianjin China 1995 1UCCLP-6 USA 1995 1Jilin China 1996 1Maoming China 1996 1Zhongyuan China 1996 1Kalush Ukraine 1996 1Equistar#3 USA 1996 1ASPELL Polymeres France 1997 1Polimeri Europa Italy 1997 2Guangzhou China 1997 1Equate Kuwait 1997 2Hyundai Petrochemical Korea 1997 1J. G. Summit** Philippines 1998 2Rasco Libya 1998 2

UNIPOL PE Facilities Location Start-up ReactorUnits in Design Year Lines

Yanpet PE #2** Saudi Arabia 2000 2DSM* Germany 2000 1UCCLP-7 Canada 2000 2ExxonMobil** Singapore 2000 1Chemopetrol** Czech Republic 2001 1Yangzi Petrochemical** China 2002 1Rio Polimeros Brazil 2002 2ExxonMobil/Pequiven Venezuela 2003 1

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Section 15 Page 11

June, 2000


UNIPOL PP EXPERIENCE LIST

Section 15 Page 12

June, 2000

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UNIPOL PP Facilities Location Start-up ReactorUnits in Operation Year Lines

UCCP-l USA 1985 11. G. Caltex Korea 1988 1Huntsman #1 USA 1989 1Polychim #1 * France 1989 1Propilco Colombia 1990 1Epsilon USA 1991 1Montell Australia 1991 1Montell Germany 1991 1Huntsman #2 USA 1991 1TPI#1 Indonesia 1992 2DSM Germany 1992 1MCCPP Japan 1992 1Solvay #1* Belgium 1992 1Propylene Malaysia Malaysia 1992 1IbnZahr* Saudi Arabia 1993 1TPI#2 Indonesia 1995 1Reliance* India 1996 2Epsilon #2 USA 1996 1Solvay #2 USA 1996 1Hyosung T&C Ltd. Korea 1996 1PIC Kuwait 1997 1J. G. Summit** Philippines 1998 1Reliance #2* India 1999 2ARCO USA 1999 1Epsilon #3 & #4 USA 1999 2Reliance #3* India 1999 1Stavropol Polymers* Russia 2000 1

UNIPOL PP Facilities Location Start-up ReactorUnits in Design Year Lines

YanpetPP** Saudi Arabia 2000 1OPC Egypt 2000 1Ibn Zahr #2 Saudi Arabia 2001 1TOSCO* USA 2001 2


15.2 Performance Guarantees

Section 15 Page 13

June, 2000

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It is expected that guarantees will be provided for the overall perfonnance of theplant and for the perfonnance of the individual process units. The most likelystructure is that the engineering procurement and construction (EPC) contractor willprovide the project schedule and plant perfonnance guarantees. The plantperfonnance guarantees will include the plant's production capacity for polyolefins,polyolefm product quality, natural gas feedstock consumption, and utilityconsumption. Individual process unit perfonnance would be guaranteed by eachprocess licensor to the EPC contractor. These guarantees would cover similarrequirements for each process unit (capacity, product quality, feed consumption, andconversion or utility consumption).

Guarantee Values

The actual guarantees and associated values for each process unit will be developedduring the engineering phase ofthe project.

Catalyst

In addition to the aforementioned perfonnance guarantees, the licensors of theprocess units will be expected to provide guarantees on the catalyst consumptionand/or stability. These guarantees would provide that the consumption and/orstability of the catalysts be such that the equivalent average annual cost of thecatalysts will not exceed the amounts indicated in this report.

Guarantee Liabilities

Failure to meet the represented guarantees would typically require the guarantors tomake changes to the plant to enable it to meet the guarantees or they would beobligated to pay liquidated damages to the owner. These changes could include thedesign, procurement, shipping, and installation or modification ofequipment asnecessary. The amount of liquidated damages payable would depend on the extentofthe perfonnance deficiency. The total liability would be limited to a percentageofthe relevant contract value.

Liabilities for failure to meet guarantees on catalyst consumption and/or stabilitywould obligate the licensors to provide a portion of replacement catalyst to theowner. The amount of such replacement catalyst would be in proportion to thepart of the guarantee not achieved.

•Feasibility Study Report - Volume 20/2EATCO - Suez Petrochemical Complex GTP ProjectSuez, Egypt

15.3 Technology Fees

Section 15 Page 14

June, 2000

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The Suez Petrochemical Complex is planned to utilize the following licensedprocesses:

a) Kvaemer Reforming/ICI Low Pressure Methanol Processb) UOPIHYDRO MTO Processc) Union Carbide UNIPOL Polyethylene Processd) Union Carbide UNIPOL Polypropylene Process

The technology fees associated with the licensing ofthese processes will befinalized in license agreements between the owner and licensor ofeach process.

The payment schedule oftechnology fees will be determined with the respectiveprocess licensor. It is expected that these fees will be paid in installments over acertain period rather than in one lump sum.

eatco_suez petrochemicals complex_gas to polyolefins ii

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