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4.7.15 Process Control, Safety and Shutdown Systems 15
4.7.16 Flare Loads and Flare Design 15
4.8 Utilities 15
4.8.1 Wash Water 16
4.9 Other Raw Material Requirements 16
5. BATTERY LIMIT CONDITIONS 17
6. PROCESS GUARANTEES 20
7. ATTACHMENTS 21


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1. INTRODUCTION
1.1 Unit Processing Objectives
The Naphtha and Aromatics Complex shall be designed to process a stabilised
feedstock of full range naphtha with the following objectives:
• To maximise Paraxylene yield for product sale.
• To produce a yield of Benzene for product sale.
• To recover Liquefied Petroleum Gas (LPG) from the CCR Platforming Unit.
• To produce an Isomerate stream for gasoline blending
• To produce a hydrotreated light and heavy naphtha stream to control the
feedstock quality to the aromatics and isomerate producing units.
• To produce Hydrogen at (99.9% mole) purity for use on other refinery units.
• To have the facilities to route Toluene or HA column overheads to gasoline
blending, if required.
The overall design philosophy of the Naphtha and Aromatics Complex maximises
economic Paraxylene production.
1.2 Use of Document
This document shall be used as the basis for the process design of the Naphtha
and Aromatics Complex only.
The design requirements specified in this document are considered to be the
minimum required. Where Licensor is applying more onerous requirements or
more beneficial operation than those specified, these shall be notified to Employer
prior to implementation.
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2. NAPHTHA AND AROMATICS COMPLEX SCHEMATIC
Figure 2-1 shows a schematic of the Naphtha and Aromatics Complex. Licensor
shall provide a process unit configuration to meet this duty specification.
NHT
CCR
Penex
Paraxylene
CDU
HN
Reformate
Benzene
Off Gas
Heavy Aromatics
LPG
Isomerate
LN
KHDS Naphtha
RHDS Naphtha
GOHDS Naphtha

LPG
Recovery
Unit
LPG
LPG
FRN
HDS Off gases
NHT Off Gas
Aromatics
Complex
LICENSOR SCOPE OF WORK
Hydrogen
H
2
Rich
Gas
Raffinate
LPG
Treater
De-
ethaniser
H
2
H
2
H
2
Toluene /
A9/A10
NHT

CCR
Penex
Paraxylene
CDU
HN
Reformate
Benzene
Off Gas
Heavy Aromatics
LPG
Isomerate
LN
KHDS Naphtha
RHDS Naphtha
GOHDS Naphtha
LPG
Recovery
Unit
LPG
LPG
FRN
HDS Off gases
NHT Off Gas
Aromatics
Complex
LICENSOR SCOPE OF WORK
Hydrogen
H
2
Rich

Gas
Raffinate
LPG
Treater
De-
ethaniser
H
2
H
2
H
2
Toluene /
A9/A10

Figure 2-1 Naphtha and Aromatics Complex Schematic
The Naphtha and Aromatics Complex comprises of the following units:
• Naphtha Hydrotreater
• Penex
• CCR Platforming
• CCR Platforming – Regeneration Section
• Xylenes Fractionation
• Parex
• Isomar
• Tatoray
• Sulfolane
• Benzene Toluene Fractionation
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3. UNIT DEPENDENCE
The Naphtha and Aromatics Complex shall be capable of operating independently
subject to the availability of hydrocarbon feedstocks, hydrogen make-up and
utilities.
Sufficient intermediate storage capacity will be available to enable continued
production of Paraxylene and Benzene products in the event of either Naphtha
Hydrotreater unit or CCR short term outage, and continued operation of the
Naphtha and Aromatics Complex during short term outage of the CDU and LPG
Recovery Unit.
Paraxylene and Benzene products shall rundown cold to Product Storage.
Isomerate shall rundown cold to Product Component Storage. Heavy Aromatics
shall rundown cold to Fuel Oil Blending storage. Toluene and A9/A10 Aromatics
shall normally be direct hot feed for the Tatoray Unit but shall also have the
facilities to rundown cold to Product Component Storage.
The following Intermediate, Product, and Product Component Storage Tanks will
be available and are excluded from Licensor’s scope:
• FRN (Full Range Naphtha) Tanks
• Desulphurised Heavy Naphtha Tank
• Reformate Tank
• Light Reformate Tank

• Heavy Reformate Tank
• Isomerate Tanks
• Heavy Aromatics Tanks (Toluene and A9/A10 Aromatics)
• Paraxylene Storage Tanks
• Benzene Storage Tanks
• Refinery or Utility Fuel Oil Tanks
The Naphtha and Aromatics Complex will normally operate with 100% hot direct
feeds to maximise energy efficiency, but provision shall be made to accept partial
or entire feed 'cold' from storage whilst meeting all product specifications.
Similarly, Naphtha and Aromatics complex intermediates are normally rundown
hot to the downstream units, but provision shall be made for intermediates to run
down cold to available storage.
LPG from the CCR shall be routed to the De-ethaniser in the LPG Recovery Unit
(outside the scope of Licensor). Offgas from the NHT shall be fed to the LPG
Recovery Unit (outside the scope of Licensor).
The battery limit conditions required for each intermediate, product and by-product
are outlined in Section 5 below.
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4. BASIS OF DESIGN
4.1 Design Objective
The Naphtha and Aromatics Complex shall be designed to process a full range
naphtha feedstock to produce Paraxylene and Benzene products at a purity
suitable for sale and an Isomerate stream suitable for gasoline blending.
The CCR of the complex will produce hydrogen with a purity of 99.9 mol% that will
be routed to the refinery Hydrogen Compression and Distribution System for use
throughout the refinery.
LPG from the CCR shall be routed to the De-ethaniser in the LPG Recovery Unit.
The design philosophy of the Naphtha and Aromatics Complex is to maximise
economic Paraxylene production. Benzene is treated as a paraxylene by-product
and is 2
nd
priority. Benzene production should float in favour of paraxylene.
There is no target for Isomerate production volume, the isomerate production
volume can decrease in favour of paraxylene and benzene production.
Production of Heavy Aromatics should be minimised to obtain further paraxylene
and benzene production.
4.2 Design Capacity
The Naphtha and Aromatics Complex shall be designed to process the following
quantities of the design feedstock.
Table 4-1: Feedstocks to the Naphtha Hydrotreater
Feedstock
Flow rate, te/
stream day
Full Range Naphtha 5500
The properties of the above feedstock are listed below in Table 4-2 below.
4.3 Design Feed Cases
The design feed case for the Naphtha and Aromatics Complex is 100% straight
run naphtha with the feed specifications as shown in Table 4-1.

For the Naphtha Hydrotreater, an alternative (C4 spike) design case is required for
the design of the Naphtha Stripper and associated equipment. The basis for the
C4 spike case is 1 vol% of C4 in the feed.
An additional (rich) design case for the CCR Platforming Unit is required. The
basis for the Rich feed case is 10% additional Naphthenes (on a PONA basis) in
the CCR Platforming Unit feed.
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The Naphtha and Aromatics Complex will normally operate with 100% hot direct
feed from the LPG Recovery Unit to maximise energy efficiency, but provision
shall be made to accept partial or entire feed 'cold' from storage whilst meeting all
product specifications. The design basis for Hot and Cold Feeds is provided in
section 4.7.4 below.
The feedstock pressures and temperatures are provided in section 5 below.
Properties of the Naphtha and Aromatics Complex feedstock are given in Section
Table 4-2 below.
It should be noted that the Licensor may be requested, during the Licensor PDP
phase, to provide estimates of product yields and main properties, operation
conditions, probable bottlenecks (identification of constraining equipment) and

maximum throughput for various Performance Cases. These Performance Cases
may concern feeds or operating objectives different from the Design Case.
4.4 Feedstock Properties
The design properties of the 100% straight run, full range naphtha feedstock to the
Naphtha and Aromatics Complex, processed from Kuwait Export Crude, are
detailed in Table 4-2 and Table 4-3 below.
Table 4-2: Properties of Naphtha feed to the Naphtha Hydrotreater
Parameter Units
Full Range
Naphtha

API Gravity API 64.8

Nominal Cut Range °C C5 - 180

Specific Gravity
@60°F 0.721
Molecular Weight 103.0


D-86 IBP °C 45
D-86 5% °C
D-86 10% °C 75
D-86 20% °C
D-86 30% °C 98
D-86 50% °C 117
D-86 70% °C 138
D-86 80% °C
D-86 90% °C 164
D-86 95% °C

D-86 FBP °C 180


Paraffins wt%
Olefins wt%
Naphthenes wt%
See Table
4-3 below

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Parameter Units
Full Range
Naphtha
Aromatics wt%


Sulphur ppmw 500
Hydrogen Sulphide ppmw 0.4

Mercaptans ppmw 104
Nitrogen ppmw 1
Carbonyl Number mg/l Note 2
Carbonyl Sulphur ppmw Note 2
Peroxide mg/kg Note 2
Chlorides ppmw Note 2
Bromine number g/100g Note 2
Total oxygen ppmw Note 2
Diene Value Note 2
Copper ppbw Note 2
Lead ppbw < 4
Arsenic ppbw 1
Mercury ppbw 1
Silicon ppmw Note 2
Total metals ppbw Note 2
Note 1 – Deleted
Note 2 - Licensor is requested to assume other feedstock impurities, not limited to
those in this table, based on their experience of processing Kuwait Export Crude,
and state the assumptions used.
Table 4-3: Estimated wt% PIONA of Feedstocks to the Naphtha Hydrotreater Unit
n-P i-P O N5 N6 A Total
C5
4.28 6.51 0.00 0.00 0.00 0.00 10.79
C6
5.02 7.64 0.00 0.73 0.73 0.92 15.04
C7
5.81 8.91 0.00 1.89 1.90 2.63 21.14
C8
4.28 6.46 0.00 2.44 2.46 3.61 19.24
C9

3.58 4.98 0.00 2.95 2.96 2.39 16.87
C10
0.00 10.46 0.00 1.77 1.74 1.30 15.26
C11+
0.00 1.66 0.00 0.00 0.00 0.00 1.66
Total
22.97 46.62 0.00 9.79 9.79 10.84 100.00
Licensor is requested to estimate the composition of the full range naphtha based
on the properties and PIONA distribution above.
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4.5 Product Specifications
4.5.1 Paraxylene
For the design feedstock and flowrate, the Naphtha and Aromatics Complex shall
meet the Paraxylene product specifications outlined below in Table 4-4.
Table 4-4: Paraxylene Product Specification
Property Unit Specification Test method
Appearance
Clear liquid free

of sediment
Visual Inspection
Minimum Purity wt% 99.7 min.
(1)
ASTM D-3798
Metaxylene wt% 0.2 max. ASTM D-3798
Orthoxylene wt% 0.1 max. ASTM D-3798
Non-aromatics wt% 0.05 max. ASTM D-3798
Total Sulphur content ppmw 0.5 max. ASTM D-4045
Distillation @ 760mm Hg
(abs)
°C
2.0 max.
including 138.4
ASTM D-850
SG (15.6°C/15.6°C) 0.864 - 0.867 ASTM D-3505/4052
Acid Wash Colour 2 max. ASTM D-848
Bromine Index mg/100g 20 max. ASTM D-1492
Chloride ppmw 1 max. ASTM D-5808 / UOP-395
Cu Corrosion Pass ASTM D-849
Colour (Pt-Co) Scale 10 max. ASTM D-1209
Note 1: Paraxylene purity is linked to 97% recovery from Parex-Isomar loop at design
Naphtha feed rate
4.5.2 Benzene
For the design feedstock and flowrate, the Naphtha and Aromatics Complex shall
meet the Benzene product specifications outlined below in Table 4-5.
Table 4-5: Benzene Product Specification
Property Unit Specification Test method
Appearance
Clear liquid free

of sediment
Visual Inspection
Purity wt% 99.96 min ASTM D-4492
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Property Unit Specification Test method
Non-aromatics wt% 0.04 max ASTM D-4492
Sulphur ppmw 0.2 max ASTM D-4045
Sulphur compounds
Free of
H2S/SO2
ASTM D-853
Distillation @ 760 mmHg
(abs)
°C
1.0 max.
including 80.1
ASTM D-850
SG (15.6°C/15.6°C) 0.882 - 0.886 ASTM D-4052

Solidification Point
(anhydrous)
°C 5.39 min. ASTM D-852
Thiophene ppmw 0.2 max. ASTM D-7011
Water ppmw 175 max. ASTM E-1064
Acidity None detected ASTM D-847
Acid Wash Colour 1 max. ASTM D-848
Chloride ppmw 0.2 max. ASTM D-5808 / UOP-395
Copper Corrosion Pass 1a or 1b ASTM D-849
Colour (Pt-Co) Scale 20 max. ASTM D-1209
Toluene ppmw 150 max. ASTM D-4492
Bromine Index mg/100g 20 max. ASTM D-1492
Total basic nitrogen (as N) ppmw 0.1 max. ASTM D-6069 / UOP-971

4.5.3 Component Blend Products
Licensor shall target the following component blend products to be of suitable
blend quality to meet the gasoline product specification shown in section 7:
• Isomerate from the Penex unit
• Toluene from the BT Fractionation Unit (Normally No Flow)
• A9/A10 Stream from Heavy Aromatics Column overheads (Normally No Flow)
During Normal Operation the Toluene and A9/A10 streams will form feeds to the
Tatoray Unit.
In addition, the Isomerate from the Penex unit shall have a minimum RON of 88
and the
ASTM D86 endpoint of the A9/A10 stream shall be less than 210 °C.
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4.5.4 Heavy Aromatics Stream
The Heavy Aromatics produced in the Naphtha and Aromatics Complex will be
used as fuel oil and routed to the Refinery Fuel Oil Tank.
4.5.5 Hydrogen Product
Hydrogen produced in the Naphtha and Aromatics Complex will be routed to the
refinery Hydrogen Compression and Distribution system (HCDS). The hydrogen
sent to HCDS shall meet the specification as detailed in Table 4-6 below.
Table 4-6: Hydrogen Specification
Parameter Unit Value
Hydrogen purity, min vol% 99.9
CO+CO
2
content ppmv 10 max.
CO content ppmv 1 max.

Methane / Nitrogen ppmv Balance
Chlorides ppmv Nil
Oxygen ppmv Nil
Water ppmv Nil
4.5.6 CCR Platforming Unit LPG
The treated LPG product specification is outlined in Section 7 below for
information purposes. CCR Platforming LPG is routed to the De-ethaniser column

in the LPG Recovery Unit.
The CCR Platforming Unit LPG should contain less than 1.1mol% C5+.
4.6 By-product Specifications
The following by-products are expected to be produced in the Naphtha and
Aromatics Complex:
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• Off-gas from NHT Unit to LPG Recovery Unit (by others)
• Fuel Gas from Isomar and Tatoray Units to the Fuel Gas Distribution (by
others)
• Tail Gas from the PSA unit within the CCR Platforming Unit to the
Hydrogen Manufacturing Unit (by others)
• Sour water and water contaminated with hazardous hydrocarbons to
treatment facilities
• Flue Gas from fired heaters within the Naphtha and Aromatics Complex
• Vent Gas from CCR Platforming Regeneration Section
Licensor shall provide the process conditions and composition of the above
streams in addition to any further by-product streams not stated above.
For Flue Gases, particulate emission shall be restricted to less than 50mg/Nm³

max.
Removal of Chlorides and HCl from the CCR Platforming Regeneration Section
Vent Gas by Chlorsorb
TM
shall be a minimum of 97 wt%.
Table 4-7 below shows the specifications required for Fuel Gas. Fuel gas streams
from the Naphtha and Aromatics Complex are required to meet this specification.
Table 4-7: Fuel Gas Specification
Property Unit Specification Test Method
H
2
S ppmw 50

4.7 Specific Design Requirements
4.7.1 On stream factor
The Naphtha and Aromatics Complex shall be designed for a minimum on-stream
factor of 0.95. This is equivalent to 8320 hours operation per calendar year.
On stream factor is defined as follows:
On stream Factor = (1) / ((1) + (2))
(1) = total duration of productive operation
(2) =total duration for repairs and maintenance including turnaround, catalyst
change-out and typical trip outage.
Licensor to advise minimum unit downtime required for catalyst replacement.
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4.7.2 Turndown
The Naphtha and Aromatics Complex shall be designed to operate satisfactorily in
the range 50% to 100% of design feed rate for the feed cases defined in section
4.3 and 4.4 while meeting all product specifications.
4.7.3 Cycle length
Catalysts shall be specified for a minimum of 4 years operation between major
turnarounds. All equipment shall be specified and spared to support 4 years
continuous operation.
Paraxylene adsorbent shall be designed for a minimum of three full cycle lengths
(12 years) without changeout.
4.7.4 Hot and cold feeds
Normal operation will utilise hot feed. The basis for hot and cold feeds is outlined
below in Table 4-8.
Table 4-8: Hot and Cold Feed Design Basis

Normal
operation
Turndown
operation (50%)
for the S/U
Hot / Cold
Design Case
Feed rate,% 100% 50% 100%
Unit Hot, % Cold, % Hot, % Cold, % Hot, % Cold, %

NHT Unit 100 0 0 100 0 100 (1)
PENEX Unit 100 0 0 100 100 0
CCR-PL Unit 100 0 0 100 0 100
Xylenes Fractionation Unit 100 0 0 100 50 50
Parex Unit 100 0 0 100 50 50
Isomar Unit 100 0 - - - -
Tatoray Unit 100 0 - - - -
Sulfolane Unit 100 0 0 100 50 50
Benzene Toluene Fractionation
Unit
100 0 - - - -
Note (1) - 100% Cold = All feed to NHT from FRN Tank, i.e. zero fresh direct
naphtha feed from LRU and zero direct raffinate feed from Sulfolane
4.7.5 Hydrogen Distribution
A common Hydrogen Compression and Distribution System (HCDS) will be
available to take purified Hydrogen from the CCR Platforming Unit PSA.
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4.7.6 Process and Heater Efficiency

The Licensor’s design shall optimise the consumption of energy and utilities.
Licensor’s process design shall incorporate a high level of heat integration in order
to contribute to optimum refinery efficiency.
Fired heaters shall be specified with air preheat facilitates using waste heat
available from flue gas, unless Licensor demonstrates the addition of air preheat is
uneconomic or detrimental to the unit operation.
Steam is expected to be used for reboiler duties, where heat integration with
process streams is not possible.
4.7.7 Purification of Off-gas Streams
The use of amine absorbers for removal of H2S from sour off-gas streams is
excluded from the Naphtha and Aromatics Complex scope.
4.7.8 Design Guidelines for Process and Equipment
Guidelines for the design of process and equipment are listed in Doc. No. 3550-
8110-PD-0007. The guidelines are used to achieve a consistent design approach
across the project. These are not intended to supersede the Licensor’s design
requirements, or any criteria which may impact the Licensor’s guarantees.
4.7.9 Major Compressor Driver Selection
Major compressor driver selection shall be specified by the Licensor with
justification for the selection between steam turbine or motor drives.
4.7.10 Catalyst Regeneration and Handling
Licensor shall specify the required method for regeneration and replacement of all
catalysts used in the Naphtha and Aromatics Complex.
Licensor shall specify all permanent facilities required for storage, loading and
unloading of catalysts. Licensor to advise any plot layout/space required for new
catalyst handling
Licensor shall provide guidance as to any special conditions relating to these
operations and any effluent problems that might be expected.
The units that require in-situ catalyst regeneration, or pre-sulphiding shall be
designed accordingly, including any additional equipment if required.
4.7.11 Chemicals

Licensor shall specify facilities for the storage and preparation of chemicals (if any)
required for the normal operation of the complex, or required to facilitate unit
shutdown and maintenance.
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4.7.12 Effluents and Emissions
Licensor shall identify all effluent streams (gaseous, liquid and solid) arising from
the process during normal operation and significant abnormal operations.
Estimated rates and compositions shall be provided for each stream, together with
recommendations for safe treatment and disposal.
Specifically vent gas and wastewater streams should be treated to remove
dioxins, if present, within the Licensor’s units.
4.7.13 Purging and flushing
Licensor shall specify any special facilities required for the purging and flushing of
equipment and instruments. Licensor shall identify purging and flushing mediums
and estimated rates of consumption.
4.7.14 Start-up and shutdown
Licensor shall specify any special facilities required to facilitate smooth and safe
start-up of the complex, and complex shutdown. This shall include shutdown of

individual units where the process allows.
Licensor to advise procedures associated with these activities, especially
sulphiding and oil purging.
Licensor shall advise expected start-up and shutdown periods (including heat up
and cool down time/rates).
4.7.15 Process Control, Safety and Shutdown Systems
The Naphtha and Aromatics Complex design shall incorporate the use of modern
state-of-the-art process control systems and shutdown logic systems. Licensor
shall specify all necessary process control systems and safety shutdown logic
systems required to support the safe operation and maintenance of the complex.
4.7.16 Flare Loads and Flare Design
Licensor shall specify all safety / pressure relief valves required to protect plant
and equipment within the complex. Licensor shall quantify the relief loads arising
from controlling, common mode and significant relief scenarios for each
safety/pressure relief valve (e.g. utility failure, blocked-in, external fire, etc).
4.8 Utilities
Design data for available utility supplies are given in the Basic Engineering Design
Data (BEDD) document 3550-8820-SP-0001.
Licensor shall identify all utility consumption requirements and provide estimated
rates of consumption for normal operation and for significant abnormal operations.
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4.8.1 Wash Water
Condensate and stripped sour water shall be used as wash water in the Naphtha
and Aromatics Complex in accordance with recommendations established by the
process Licensor.
4.9 Other Raw Material Requirements
Licensor shall specify all other raw materials required for the Naphtha and
Aromatics Complex in addition to the feedstock, hydrogen, catalysts, chemicals
and utilities discussed in this document. This specification shall include materials,
hazard data, method of use, frequency of use and consumption. The design shall
include all specialised equipment required for their use.
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5. BATTERY LIMIT CONDITIONS
The key battery limit stream conditions for the Naphtha and Aromatics Complex
operating at design throughput are provided in the tables below.
Licensor shall provide a full list of all battery limit streams and conditions.

Table 5-1: Naphtha Hydrotreater Unit Battery Limit Conditions
Process Streams From To
Pressure,
kPa (g) Temp, °C
Full Range Naphtha LPG Recovery Unit NHT 325 75
Full Range Naphtha Intermediate Storage NHT 550 42
Sulfolane Raffinate Sulfolane Unit NHT Note 2 Note 2
Make-up Gas
CCR Plat. Unit
NHT Note 2 Note 2
Stripped Sour Water Sour Water Stripper NHT 450 55
Wash Water Cold condensate NHT 450 50
Sour water NHT Sour Water Stripper 400 52
Unstabilised Net
Overhead Liquid
NHT LPG Recovery Unit 1300 40
Off-gas NHT LPG Recovery Unit 500 40
Light Naphtha NHT Penex Unit Note 2 Note 2
Light Naphtha NHT Intermediate Storage Note 2 42
Heavy Naphtha NHT Intermediate Storage 600 47
Heavy Naphtha
(1)
Intermediate Storage NHT Note 2 47
Heavy Naphtha NHT
CCR Plat. Unit
Note 2
Note 2
Note 1: Processing of Heavy Naphtha from intermediate storage will require
routing through the fractionation section of the NHT prior to the CCR Platforming
Unit

Note 2: Specified by Licensor
Table 5-2: Penex Unit Battery Limit Conditions
Process Streams From To
Pressure,
kPa (g) Temp, °C
Light Naphtha NHT Penex Unit Note 1 Note 1
Make-up Hydrogen CCR PSA Penex Unit Note 1 Note 1
Caustic Supply
Caustic Supply
System
Penex Caustic
Dilution Tank
215 40
Spent Caustic
Penex Degassing
Drum
Neutralisation Tank 500 Note 1
Isomerate Penex Unit
Product Component
Storage
700 42
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Off gas Penex Unit Fuel Gas Distribution 500 Note 1
Note 1: Specified by Licensor
Table 5-3: CCR Platforming Unit Battery Limit Conditions
Process Streams From To
Pressure,
kPa (g) Temp, °C
Heavy Naphtha NHT CCR Plat. Unit Note 1 Note 1
Hydrogen CCR PSA Hydrogen Distribution 2450 45 max.
Reformate
CCR Plat. Unit

Xylenes Fractionation Note 1 Note 1
Reformate
CCR Plat. Unit

Intermediate Storage 600 47
LPG
CCR Plat. Unit

LPG Recovery Unit 2200 Note 1
Tail Gas
CCR Plat. Unit

Hydrogen Manuf. Unit 500 82
Note 1: Specified by Licensor
Table 5-4: Aromatics Units Battery Limit Conditions

Process Streams From To
Pressure,
kPa (g) Temp, °C
Reformate CCR Plat. Unit
Xylenes
Fractionation Note 1 Note 1
Reformate Intermediate Storage
Xylenes
Fractionation
Note 1 47
Light Reformate Intermediate Storage Sulfolane Unit Note 1 47
Light Reformate Xylenes Fractionation Intermediate Storage 600 47
Heavy Reformate Intermediate Storage
Xylenes
Fractionation
Note 1 50
Heavy Reformate Xylenes Fractionation Intermediate Storage 600 50
Make-up Hydrogen Hydrogen Distribution Isomar Note 1 55
Make-up Hydrogen Hydrogen Distribution Tatoray Note 1 55
Raffinate Sulfolane NHT Note 1 Note 1
Raffinate Sulfolane Intermediate Storage 600 42
Toluene BT Fractionation
Product Component
Storage
600 47
A9/A10 Xylenes Fractionation
Product Component
Storage
600
50

Paraxylene Product Parex Product Storage 600 50
Benzene Product BT Fractionation Product Storage 600 47
Heavy Aromatics Xylenes Fractionation
Refinery Fuel Oil
Storage
600 50
Offgas Isomar
Xylenes Column
Reboiler Heater
Note 1 Note 1
Fuel gas Tatoray Fuel Gas Distribution 500 Note 1
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DUTY SPECIFICATION

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Note 1: Specified by Licensor
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DUTY SPECIFICATION

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6. PROCESS GUARANTEES
The process performance guarantees are expected to include the following:
• Unit Capacities
• Paraxylene product specification and production rate
• Benzene product specification and production rate
• LPG quality and production rate
• Hydrogen purity and production rate
• Isomerate quality and production rate
• Catalyst and adsorbent life
• Utility consumptions based on the utility summary at completion of design
• Hydrogen consumption
A complete list of process performance guarantees for the Naphtha and Aromatics
Complex shall be specified by the Licensor in the guarantee agreement.

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7. ATTACHMENTS
Table 7-1: NSRP Gasoline Specification
Property Unit Specification Test Method
RON 92 / 95 ASTM D-2699
MON 82 / 85 ASTM D-2700
Lead g/l Nil ASTM D-3237
Distillation IPB °C Report ASTM D-86
10% vol °C 70 max.
50% vol °C 120 max.
90% vol °C 190 max.
FBP °C 210 max.
Residue vol % 1.5 max.
Copper strip corrosion
(3hrs, @ 50°C)
1 max. ASTM D-130
Existent gum mg/100ml 4 max. ASTM D-381
Oxidation stability mins 480 min. ASTM D-525
Sulphur wt ppm 50 max. ASTM D-2622 /ASTM D-5453
RVP (@ 37.8°C) kPa 60 max (summer)
75 max (winter)
ASTM D-4953 /ASTM D-5191
Benzene vol % 1.0 max. ASTM D-3606 /ASTM D-4420
Aromatics vol % 40 max. ASTM D-1319 /ASTM D-6839
Olefins vol % 30 max. ASTM D-1320 /ASTM D-6839
Oxygen wt % 2.7 max. ASTM D-4815 /ASTM D-6839

SG (@ 15°C) 0.72 - 0.76 ASTM D-1298 /ASTM D-4052
Appearance Clear ASTM D-4176

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Table 7-2: LPG Product Specification
Property Unit Specification Test Method
Density (@15deg C) kg/l 0.5 min. ASTM D-1657/ ASTM D-2598
Vapour Pressure (@37.8 deg
C)
kPa 1,430 max. ASTM D-1267/ASTM D-2598
Vapour Temp. (95% vol) deg C 2.2 max. ASTM D-1837
Ethane % mol 3 max. ASTM D-2163
Propane % mol 20~50 ASTM D-2164
Butane % mol 50~80 ASTM D-2165
Pentane heavier % mol 1.5 max. ASTM D-2166
Olefin Content vol. % 20 max. ASTM D-2163
Composition of 100 ml
vaporized residue

ml 0.05 max. ASTM D-2158
Copper Strip Corrosion - 1 max. ASTM D-1838
Sulphur ppmw 100 max. ASTM D-2784/ASTM D-6667
Hydrogen Sulphide - Pass ASTM D-2420
Free Water - Nil -
Mercaptan ppmw 20 max. ASTM D-3227