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CRUDE DISTILLATION BASIS OF DESIGN

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FOSTER WHEELER ENERGY LTD PROCESS DOCUMENT

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4.8.9 Unit metallurgy .................................................................................................................. 11 4.8.10 Trays ................................................................................................................................. 11 4.8.11 Exchanger cleaning .......................................................................................................... 11 4.8.12 Effluent streams ................................................................................................................ 11 4.8.13 Waste minimisation........................................................................................................... 11 4.8.14 Flushing ............................................................................................................................ 11 4.8.15 Water wash injection......................................................................................................... 11 4.8.16 Heater ............................................................................................................................... 11 4.8.17 Preflash drum.................................................................................................................... 12 5. BATTERY LIMIT CONDITIONS........................................................................................ 12 ATTACHMENT 1 - CDU DESIGN MATRIX ................................................................................. 14


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1. INTRODUCTION

1.1 Use of this document

This document defines the basis of design for the Crude Distillation Unit (CDU).

1.2 Unit processing objectives

The objective of the CDU is to provide primary separation of crudes to produce straight run blendstocks of distillate products (after suitable downstream treatment processes) and feedstocks for other downstream process units.

2. UNIT INDEPENDENCE

The Unit requires the simultaneous operation of the LPG Recovery Unit to stabilize naphtha, subject to feedstock and utility availability.

3. DESCRIPTION OF UNIT

Crude oil feedstock is preheated against product and pumparound streams before being routed to a fired heater. Primary fractionation is carried out in the preflash vessel/ main crude column fractionator and associated side stream strippers. Overhead naphtha is further stabilised in the naphtha stabiliser column in the LPG Recovery Unit. Products are cooled and rundown to product blending, intermediate storage or further processing as appropriate.

4. DESIGN BASIS

4.1 Design objectives

The design of the CDU is consistent with the overall refinery objective of maximising distillates and minimising residue. The design incorporates flexibility in distillate production, will allow for minor variations in feed quality, and will enable consequent flexibility in refinery blending operations.

There are two design cases and the kerosene production is designed to accommodate the specifications of both aviation and non-aviation kerosene from the same draw (refer to section 4.7). However, Kerosene product flash point and ASTM-D86 IBP specifications shall be achieved at KHDS Unit.

The design incorporates features for optimising energy utilisation and heat recovery consistent with product fractionation.


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The Unit shall produce the following streams:

An overheads gas stream routed to the LPG Recovery Unit.

A full range unstabilised naphtha stream routed to the LPG Recovery Unit for further processing.

A kerosene stream routed to the Kerosene Hydrodesulphurisation Unit (KHDS) or to Slops in case of KHDS shutdown.

A gas oil stream routed to the Gas Oil Hydrodesulphurisation Unit (GOHDS) or to GOHDS intermediate tankage.

An atmospheric residue stream routed hot to the Residue Hydrodesulphurisation Unit (RHDS) for further processing or to intermediate tankage.

The Unit shall receive the following stream:

A combined wild naphtha stream from the Kerosene Hydrodesulphurisation Unit

(KHDS) and Gas Oil Hydrodesulphurisation Unit (GOHDS) into the Crude Column Overhead Receiver.

4.2 Design feedstocks

Design case CDU feedstock is 100% Kuwait Export crude.

The crude assay for the design is included in document number 3550-8110-PD-0003. A maximum of 0.5% by volume water is assumed to be present in the crude.

Capacity of CDU for 85 liq. vol% Kuwait Export Crude/15 liq. vol% Murban is 200,000 BPSD.

4.3 Design Capacity

4.3.1 Annual throughput

The CDU has been designed to process an average of 9.66 Million Tonnes per Annum (MTA) of the design feedstock defined under section 4.2.

4.3.2 Operating Factor

The CDU capacity is based on an average of 8320 hours operation per year giving an operating factor of 0.95. The target operating factor is 0.97.

4.3.3 Nameplate capacity

The CDU nameplate capacity is 200,000 Barrels Per Stream Day (BPSD - Dry basis), set by operation on Kuwait Export crude as per section 4.2.


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4.3.4 Turndown

The Unit is capable of operating at a maximum turn-down ratio of 50% of design feed as per section 4.2, at the design capacity stated in section 4.3 while meeting product specifications defined in section 4.7. Any additional facilities or non-standard operations required to achieve this are clearly identified.

4.4 Design Cases

4.4.1 Base Case

CDU is designed for TBP cut points stated in section 4.6 and products specifications in section 4.7. The overflash has been specified at 5% and performance guarantees are based on this case only.

4.4.2 Minimum Kerosene Case

CDU shall be able to increase wild naphtha production at the expense of kerosene cut in order to maximise profits in the Aromatics Complex. This case complies with the CDU LP Model’s economics and Employer’s requirements (overflash has been reduced from 5.0 to 2.3 %).

4.5 Check Cases

4.5.1 Maximum Kerosene Case

CDU shall be capable to produce a wider range of kerosene draw of acceptable quality in order to take advantage of market changes. This corresponds to 17% more kerosene production than the Base Case described in section 4.4.1.

4.5.2 Cold Reflux Case

CDU shall have the flexibility to operate with 5 wt% cold reflux ratio (cold naphtha/hot top pumparound). This facility consists of wild naphtha stream from the column overhead receiver routed into the top pumparound return.

CDU will operate under this scenario during start-up, cleaning and off-design operation. TBP cut points as per Base Case.

4.5.3 Murban Case

CDU design shall be checked for an alternative feed of 85 liq. vol% Kuwait Export Crude/15 liq. vol% Murban. TBP cut points as per Base Case.


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4.6 Product cut points

The CDU is based upon the following TBP cut points:

Products TBP cut point (°C)

Base Case / Cold Reflux / Murban Case

(Note 1)

Maximum Kero Case

Minimum Kero Case

Naphtha / Kerosene 165 160 176 Kerosene / Gas Oil 220 224 220 Gas Oil / Atm. Residue 360 360 360

Notes:

1. CDU performance guarantees are against the Base Case.

4.7 Product specification and fractionation

The CDU is designed to meet the following specifications and fractionation performance when processing the design feeds referred to in section 4.2, at the design capacity stated in section 4.3, and at the design TBP cut points stated in section 4.6. The fractionation is based upon measurements by the ASTM D86 test method.

The list below shows the expected properties of the feedstock streams to the downstream processing units.


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Cases Products

Product Spec

(Note 1) Base Case

(Note 3)

Minimum Kero

(Note 3)

Maximum Kero

(Note 3)

Murban

(Note 3)

Full Range Naphtha

ASTM D86 90%vol (°C) 155 max (Note 5) 144 154 142 144

Kerosene

ASTM D86 IBP (°C) 144 min (Note 4) 143 148 143 144

ASTM D86 10%vol (°C) 205 max 176 183 174 176

ASTM D86 90%vol (°C) 230 max 217 219 219 217

ASTM D86 EP (°C) 300 max 234 236 236 234 Flash point ASTM D56 / D-3828 (°C)

38 min (Note 4) 38 43 36 38

Atmospheric Gasoil

ASTM D86 90%vol (°C) 360 max (Note 2) 350 360 350 348

Flash point ASTM D93 / D-3828 (°C) 55 min 84 85 85 83

Fractionation Value

(Note 2)

Gap between 5 vol% ASTM D-86 of Kerosene and 95 vol% ASTM D-86 of Naphtha minus material 5°C min.

Gap between 5 vol% ASTM D-86 of Atmospheric Gas Oil and 95 vol% ASTM D-86 of Kerosene 0°C min.

Notes:

1. Refer to Product Specification Doc. 3550-8110-PD-0004.

2. CDU performance guarantees are against the Base Case.

3. Data from CDU simulation output.

4. Kerosene ASTM D86 (IBP) and flash point shall be met in KHDS Unit.

5. Target specification for Naphtha and Aromatic Complex.


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4.8 Specific design requirements

4.8.1 Design margins

CDU Design Matrix (Attachment 1) shall be used as a guideline for equipment design margins. Margins are based on the CDU design cases stated in section 4.4, but having enough flexibility to cover the check cases described in section 4.5. Criteria for design margins are based on the Process Engineering Design Guidelines 3550-8110-PD-0007, section 10.

CDU Fired Heater shall have 10% design margin on duty and flow.

4.8.2 Overflash

The CDU is designed for a maximum of 5% overflash. Overflash is defined as the ratio of liquid leaving the tray above the flash zone to the whole crude charge, expressed as a liquid volume (LV) percentage at 15°C.

4.8.3 Distillate Stripping

Distillate sidestreams from the main fractionator are stripped to improve fractionation.

4.8.4 Heat integration

Heat exchange across the temperature pinch point between hot and cold streams is minimised as far as practicable. The global approach temperature for the crude preheat train at the pinch point is set to ensure economic heat recovery.

The number of pumparounds and their duties are selected to maximise heat recovery whilst meeting fractionation requirements (see also section 4.8.6). Full utilisation of pumparound heat is made where practical.

Where heat exchanger leakage may result in product contamination, provision for repair while the Unit remains on line shall be made. Provision for on-line cleaning shall be provided so as to maintain energy efficiency over a four year run length (see also section 4.8.10).

4.8.5 Fouling Factors

Fouling factors are set as shown below:


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Crude Fouling Factor (m2°C/kW) 0-121 °C 121 -177°C 177-232 °C 232 °C and over

Velocity (m/s) Velocity (m/s) Velocity (m/s) Velocity (m/s) Crude

<0.6 0.6 - 1.2 >1.2 <0.6 0.6-1.2 >1.2 <0.6

0.6-1.2 >1.2 <0.6 0.6-1.2 >1.2

Salt 0.528 0.352 0.352 0.881 0.704 0.704 1.057 0.881 0.881 1.233 1.057 1.057Dry 0.528 0.352 0.352 0.528 0.352 0.352 0.704 0.528 0.528 0.881 0.704 0.704

Service Fouling Factor (m2°C/kW) Top Pumparound 0.352 Kerosene 0.352 LAGO PA 0.352 AGO 0.352 HAGO PA 0.528 Atm Residue 0.704 Desalter Water Effluent 0.528 (veloc<1 m/s) or 0.352 (veloc>1m/s) Makeup Water 0.176 (Service Water) / 0.352 (Stripped Water) Cooling Water 0.430 Tempered Water 0.176

4.8.6 Desalter

Two-stage desalting is provided to reduce the salt level of the crude, and hence the atmospheric residue, to the minimum practicable level consistent with RHDS operation. Water is recycled within the desalter system to reduce overall water requirement. The desalter shall be supplied with stripped water from the sour water stripper (SWS). If required, the balance shall be supplied by “oxygen scavenged” service water.

The desalter is specified to handle the range of salt contents specified below:

Water and sediment content 0.5 vol%

Normal salt content (Kuwait Export crude) 15 PTB (49 ppm wt)

Maximum salt content 80 PTB (262 ppm wt)

Water wash ratio: 7 vol% of crude feed.

Water to upstream feed preheat: 20% of makeup

The desalter is specified to meet the following treated crude specification: Free water and sediment content (maximum) 0.2 vol%

Crude salt content (maximum) 2.0 ppm wt (0.6 PTB)


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4.8.7 Pumparound circuits

The design includes a top pumparound. This is intended to offload duty from the overheads condenser. Other pumparound circuits are provided to maximise heat recovery whilst maintaining the required fractionation.

4.8.8 Process Chemicals

Facilities are specified for introducing the following process chemicals:

Demulsifying agent

This is to be introduced upstream of cold crude feed pre-heat train and downstream of first stage desalter in order to aid separation of any oil/water emulsions that cannot be resolved by electrostatic action alone. Actual operating experience will determine the basis on which the demulsifier will have to be injected, i.e. whether intermittent or continuous.

Anti fouling agent

This is to be introduced into the second stage desalter outlet in order to reduce fouling of the hot pre-heat train.

Corrosion inhibitor

This is to be introduced into the main fractionator overhead vapour line and top pumparound circuit in order to protect the main column overhead system against corrosion by chlorides and hydrogen sulphide.

Neutraliser

This is to be introduced into the main fractionator overhead vapour line to neutralise acid gases and assist in the protection of the main column overhead system against corrosion and fouling. Ammonia not to be used for safety reasons.

Caustic Injection

Caustic shall be injected downstream of second stage desalter to protect the crude tower overhead system against corrosion by the formation of acid chlorides from salt carry over from desalter.

Anti foam

Anti foam is to be added at the inlet of the Preflash Drum to prevent foaming.

Bisulphite

The bisulphite as an oxygen scavenger is injected at the service water line to the Desalter Water Surge Drum.


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Nitrite

Nitrite is introduced into the tempered water closed system through the Tempered Water Pump suction line as a corrosion inhibitor. The same facility shall be used for Biocide dosing during system re-fill after a shutdown.

4.8.9 Unit metallurgy

The metallurgy for the Unit is based upon the 100% Kuwait Export Crude case only.

Equipment design life follows the requirements included in the Basic Engineering Design Data 3550-8820-SP-0001.

4.8.10 Trays

All CDU columns are specified with suitable conventional valve trays. All draw- off trays are of the non-fractionating type.

4.8.11 Exchanger cleaning

Provision for on-line cleaning of exchangers prone to fouling shall be incorporated into the design where applicable.

4.8.12 Effluent streams

All solid, liquid and gaseous effluent streams are identified in terms of composition, flowrate and hazardous character for both normal and abnormal modes of operation.

4.8.13 Waste minimisation

Waste minimisation techniques are incorporated, in order to minimise emissions to air, water and land from both normal and abnormal modes of operation.

4.8.14 Flushing

Provision shall be made for flushing out of high pour point circuits in the event of an unplanned and extended shutdown of the CDU.

4.8.15 Water wash injection

Provision shall be made for stripped water wash injection (intermittent) at the inlet of the CDU overhead condenser when fouling is causing heat transfer constraints or as part of regular washing. The water washing operation is not considered as part of the condenser design duty.

4.8.16 Heater

Horizontal tube type is required. Maximum allowable average heat flux is 12000 Btu/hr/ft2 (for tubes fired on one side). Heater to be equipped with air preheating to maximise heater efficiency.


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4.8.17 Preflash drum

A preflash drum has been selected to reduce fired heater pressure drop (less vaporisation), save in pumping costs and reduce fouling at the hot end of heat exchangers by water removal.

Operating pressure is controlled via a control valve.

5. BATTERY LIMIT CONDITIONS

The design of the CDU allows the reception of crude from, and the delivery of products to the battery limits, at the following conditions, measured at grade. Maximum temperature means that a lesser temperature shall be acceptable. Maximum pressure refers to the maximum backpressure that may be imposed at the CDU battery limits by the downstream system. Contractor shall ensure that the CDU can deliver product at up to this pressure at all times, and also that CDU can control satisfactorily throughout the entire operating range, should a lesser backpressure be imposed.


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Stream Origin / destination Temperature °C

Pressure KPa(g)

Crude feed From storage 30 max (2) 2564

Wild Naphtha From KHDS / GOHDS to Column Ovhd Receiver 50 - 55 155

CDU overhead gas stream To LPG Recovery Unit 55 max 30

Full range Naphtha To LPG Recovery Unit 55 max 1374

Sour water To SWS 55 max 400

Kerosene To KHDS

To Slops

84 - 89

42

750

600

Atmospheric Gas Oil

To GOHDS

To GOHDS interm. tankage

87 - 89

55

750

600

Atmospheric

Residue

To RHDS

To intermediate tankage

114 - 117 (1)

80

850

600

Desalter Effluent To Effluent Treatment Plant 38 500

Notes: 1. Temperature after heat recovery on the CDU. 2. Design checked at minimum crude storage temperature of 16 °C.


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ATTACHMENT 1 - CDU DESIGN MATRIX


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Equipment PFD Stream No. Base Min Kero Max Kero 5% Cold Reflux (CR)

85%KWEC/ 15%Murban Base MinKero MaxKero 5% Cold

Reflux (CR)85%KWEC/ 15%Murban Proposed Design Margins Remarks Cases to be reported in

Process Specification

Pumps Rated Flow

010-P-001A/B/C: Offsite Crude Charge Pumps 1 1347 1347 1347 1347 1347 1482 91 91 91 91 91 Flow: 110% base case Total flow reported (3 x 50% pumps considered) Base case

010-P-003A/B: Desalter water Make-up Pumps 76 94 94 94 94 94 103 91 91 91 91 91 Flow: 110% base case Base case

010-P-004A/B: Desalter Water Circulation Pumps 74 81 81 81 81 81 89 91 91 91 91 91 Flow: 110% base case Base case

010-P-005A/B/C: Flashed Crude Pumps 20 1463 1454 1461 1463 1466 1610 91 90 91 91 91 Flow: 110% base case Total flow reported (3 x 50% pumps considered) Base case

1948 1580 2262 1643 1975 2714 72 58 83 61 73 Rated Flow:120% MaxK case Not recommended

1948 1580 2262 1643 1975 2337 83 68 97 70 84 Rated Flow:120% Base caseRecommended. Total flow reported (3 x 50% pumps

considered)

010-P-007A/B: Kerosene PA Pumps 37 1273 1220 1234 1275 1290 1528 83 80 81 83 84 Flow: 120% base case Typ. margin on PA pumps Base case

131 105 152 131 137 168 78 62 91 78 82 Flow: 110% MaxK case Not recommended

131 105 152 131 137 157 83 67 97 83 87 Flow: 120% base case Recommended

010-P-009A/B: LAGO PA Pumps 48 825 740 820 786 804 990 83 75 83 79 81 Flow: 120% base case Typ. margin on PA pumps Base case

010-P-010A/B: AGO Product Pumps 53 345 345 334 345 353 379 91 91 88 91 93 Flow: 110% base case Base case

1207 696 1230 1186 1237 1449 83 48 85 82 85 Flow: 120% base case2 x 100% pumps

Not recommended (turndown issues)

1207 696 1230 1186 1237 1670 72 83 74 71 74 Flow: 120% minkero caseRecommended. Total flow reported (3 x 50% pumps

considered)010-P-012A/B: Atm. Residue Pumps 63 786 781 786 786 754 864 91 90 91 91 87 Flow: 110% base case Base case

010-P-013A/B: Tempered Water Pumps 69 406 406 406 406 406 446 91 91 91 91 91 Flow: 110% base case Base case

288 316 275 340 306 374 77 84 73 91 82 Flow: 110% CR case Not recommended

288 316 275 340 306 379 76 83 73 90 81 Flow: 120% minkero case Recommended

010-P-015A/B: CDU Sour Water Pumps 31 27 26 28 27 26 30 91 88 93 91 88 Flow: 110% base case Base case

Heat Exchangers / Air Coolers / Fired Heater Design Duty/Flow

010-E-001: Cold Crude / Top Pumparound Duty - 22.1 22.6 22.3 21.7 23.4 24.8 112 110 111 114 106 Duty: 110% minK case

Shell Side Flow 3 1365 1365 1365 1365 1365 1502 110 110 110 110 110 Flow: 110% base case

Tube Side Flow 33 1574 1206 1877 1262 1570 1889 120 157 101 150 120 Flow: 120% base case Typ. margin on PA HXs flow

010-E-002: Cold Crude / Kero Product Duty - 4.2 3.8 4.7 4.3 4.4 4.8 115 125 103 112 108 Duty: 115% base case

Shell Side Flow 41 131 105 152 131 137 157 120 150 103 120 115 Flow: 120% base case Kero prod pump margin

Tube Side Flow 5 421 421 421 421 422 463 110 110 110 110 110 Flow: 110% base case

010-E-003: Cold Crude / AGO Product Duty - 12.4 12.2 12.2 12.8 12.8 13.7 110 112 112 107 107 Duty: 110% base case



010-E-004: Cold Crude / Kero Pumparound Duty - 12.2 11.3 12.0 12.4 12.2 13.5 110 119 112 108 111 Duty: 110% base case

Shell Side Flow 39 810 604 810 801 795 971 120 161 120 121 122 Flow: 120% base case Typ. margin on PA HXs flow


010-E-005: Cold Crude / Atm. Residue Duty - 32.2 30.2 32.4 32.5 30.2 35.4 110 117 109 109 117 Duty: 110% base case


Tube Side Flow 45%Stream 4 631 632 631 631 632 694 110 110 110 110 110 Flow: 110% base case

010-E-006: Desalter Water Feed / Effluent Duty - 9.7 9.3 9.5 9.7 9.7 10.6 110 115 112 110 110 Duty: 110% base case



010-E-007: Desalter Effluent Water Cooler Duty - 1.9 1.9 1.9 1.9 1.9 2.0 110 110 110 110 110 Duty: 110% base case


010-E-008: Desalted Crude / Kero Pumparound Duty - 4.6 5.7 4.1 4.7 4.9 6.3 138 110 155 136 128 Duty: 110% minK case



010-E-009: Desalted Crude / AGO Product Duty - 10.3 11.1 10.2 10.2 10.3 12.2 119 110 119 119 119 Duty: 110% minK case

Shell Side Flow 53 345 345 334 345 353 380 110 110 114 110 107 Flow: 110% minK case


010-E-010: Desalted Crude / LAGO Pumparound Duty - 14.4 12.5 14.3 13.5 13.2 15.8 110 127 111 117 120 Duty: 110% base case



010-E-011: Desalted Crude / Atm. Residue Duty - 18.8 17.6 19.0 18.8 17.7 20.7 110 118 109 110 117 Duty: 110% base case



010-E-012: Flashed Crude / LAGO Pumparound Duty - 6.7 7.5 7.3 7.1 7.4 8.3 124 110 114 117 112 Duty: 110% minK case



010-E-013: Flashed Crude / HAGO Pumparound Duty - 26.1 17.0 26.6 26.1 26.1 28.7 110 169 108 110 110 Duty: 110% base case



010-E-014: Flashed Crude / Atm. Residue Duty - 20.7 17.7 20.8 21.2 20.3 22.8 110 129 109 107 112 Duty: 110% base case

Shell Side Flow 45%Stream 20 658 654 658 658 660 724 110 111 110 110 110 Flow: 110% base case


010-E-015: Flashed Crude / Atm. Residue Duty - 29.7 32.1 29.5 29.4 28.4 35.3 119 110 120 120 124 Duty: 110% minK case



010-E-016: Atm. Residue / Temp. Wat Cooler Duty - 12.8 11.9 12.6 12.8 11.3 14.0 110 118 112 109 125 Duty: 110% base case



010-E-017: Kerosene Product Trim Cooler Duty - 0.68 0.54 0.79 0.68 0.71 0.81 120 151 103 120 115 Duty: 120% base case

Shell Side Flow 44 117 93 137 117 122 141 120 151 103 120 115 Flow: 120% base case Kero prod pump margin

010-AC-001: Top PA Return Air Cooler Duty - 4.1 3.7 4.8 0.0 4.7 5.0 120 136 102 - 106 Duty: 120% base case

Tube Side Flow 34 1511 1143 1812 1200 1503 1813 120 159 100 - 121 Flow: 120% base case Typ. margin on PA HXs flow

010-AC-002: Desalter Effluent Air Cooler Duty - 0.59 0.58 0.77 0.63 0.58 0.65 110 112 85 104 112 Duty: 110% base case

Tube Side Flow 71 94.1 94.5 94.2 94.1 94.0 104 110 110 110 110 110 Flow: 110% base case

010-AC-003: Tempered Water Air Cooler Duty - 12.8 11.9 12.6 12.9 11.3 14.1 110 118 112 109 125 Duty: 110% base case


010-AC-004: Kero Product Air Cooler Duty - 1.8 1.3 2.1 1.7 1.8 2.1 120 169 99 124 115 Duty: 120% base case

Tube Side Flow 42 121 96 141 121 126 145 120 151 103 120 115 Flow: 120% base case Kero prod pump margin

010-AC-005: AGO Product Air Cooler Duty - 4.7 4.6 4.3 4.6 5.0 5.8 125 127 135 127 117 Duty: 125% base case margin based on sensitivity study


010-AC-006: Crude Column Ovhd Condenser Duty - 41.7 44.7 40.5 46.6 43.0 53.7 129 120 132 115 125 Duty: 120% minK case

Tube Side Flow 28 67043 69245 65879 72203 68416 83094 124 120 126 115 121 Flow: 120% minK case

010-H-001: Crude Charge Heater Duty - 72.1 73.7 71.3 72.9 73.2 81.0 112 110 114 111 111 Duty: 110% minK case 10% margin OK based on sensitivity study.

Flow 25 1657 1619 1657 1659 1665 1823 110 113 110 110 109 Flow: 110% base case

Desalter / Vessels / Column / Strippers Design Duty/Flow

010-A-001: 1st & 2nd Stage Desalters 11 1512 1506 1513 1513 1514 1663 110 110 110 110 110 Liq Flow: 110% base case Base case

010-V-001: Desalter Water Surge Drum 76 94 94 94 94 94 103 110 110 110 110 110 Liq Flow: 110% base case Base case

010-V-002: Pre-flash Drum Liq Flow 20 1463 1454 1461 1463 1466 1610 110 111 110 110 110 Liq Flow: 110% base case Base case

Vap Flow 27 16990 16583 17170 16557 16764 18689 110 113 109 113 111 Vap Flow: 110% base case Base case

010-V-005:Crude Column Ovhd Receiver Liq Flow upstream 30 288 316 275 340 306 379 132 120 138 111 124 Liq Flow: 120% minK case

Vap Flow upstream 29 4866 4120 5241 4873 4276 5839 120 142 111 120 137 Vap Flow: 120% base case

Water Flow upstream 31 27.2 26.3 27.8 27.3 26.5 29.9 110 114 108 110 113 Liq Flow: 110% base case Base case

010-C-001: Crude Distillation Column / 010-C-002: Kerosene Stripper / 010-C-003: AGO Stripper

10% on trays load (pumparound trays

sensitivity with 20% margin on normal liquid flow)

Column and strippers sizing checked considering the tray loading data for each case.

Since this is a main equipment, it is recommended to report all cases (Base Case / Min Kero Case / Max Kero Case & CR).

Vendor to advise.

Notes:

1. The purpose of the CDU Design Matrix is to specify the governing case and design margin per equipment only. All equipment process specifications shall be consistent with CDU H&MBs.

Base case & MinK case. Note to be added: Pump flow design margin to cover 7%CR

case.

Base case & MinK case. Note to be added: Duty design

margin covers MaxK case.

Normal Operating Flow (Am3/h) Pump Operation Flow % (Normal / Rated)

Base case

Base case Note to be added: Pump flow design margin to cover MaxK

case.

% (Design / Normal)Normal Operating Duty (MW) / Flow (Am3/h)

Base case & MinK case

Base case & MinK case. Note to be added: Design margin to cover MaxK & 7% CR cases

010-P-014A/B: CDU Ovhd Liquids Pumps 30

010-P-011A/B/C: HAGO PA Pumps 59

Base case

Base case


Base case (pumps: 2op,1sp) / MinK case (pumps:1op,2sp)


010-P-006A/B/C: Top PA Pumps 32

010-P-008A/B: Kerosene Product Pumps 41


margin covers MaxK case.




Base case

CDU DESIGN MATRIX

Check Cases Design Cases Check Cases

Process Flows / Duties MarginsDesign

ParameterDesign Cases

(Note 1)



margin to cover MaxK case.



Base case


Base case





Base case

Normal Operating Flow (Am3/h) % (Design / Normal)

Base case & MinK case. Note to be added: Duty&flow design margins to cover 7% CR case.

Base case

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