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REFINERY MATERIAL BALANCE
6960-000-DS-0011 PAGE 1 of 4 REV: D4
5.000.DS.0011_D4.doc
REVISION 01 D1 D2 D3 D4 DATE JUL 00 Jul 00 30 April 04 7 July 04 30 August 04 ORIG. BY A J Creek A J Creek A. Sirven P. Nyvlt A. Sirven APP. BY A J Creek A J Creek S. Glavas S. Glavas S. Glavas SIGNATURE A J Creek STATUS For FDC
Approval Issue for
FDC Issue for
FDC Pages modified under revision D2 : All Pages modified under revision D3 : 2,3,4 Pages modified under revision D4 : 2,3
Contract: 7303 N
Client’s Name: VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)
Project Title: DUNG QUAT REFINERY PROJECT – FEED
DEVELOPMENT CONTRACT Project Location: DUNG QUAT, VIETNAM
CONTENTS
SECTION SUBJECT 1. INTRODUCTION
2. REFINERY EXPECTED MATERIAL BALANCE
3. CDU STREAM DATA
4. MATERIAL BALANCE LIMITING CONSTRAINTS
Attachments 1A Bach Ho crude - RFCC operating in maximum distillate mode 1B Bach Ho crude - RFCC operating in maximum gasoline mode 1C Mixed crude - RFCC operating in maximum distillate mode 1D Mixed crude - RFCC operating in maximum gasoline mode 2A CDU Stream Data - Bach Ho 2B CDU Stream Data - Mixed Crude
6960-000-DS-0011 PAGE 2 of 4 REV: D4
REFINERY MATERIAL BALANCE
5.000.DS.0011_D4.doc
1. INTRODUCTION
This document presents the refinery expected material balances for the following four refinery operating cases:
• Bach Ho crude - RFCC operating in maximum distillate mode
• Bach Ho crude - RFCC operating in maximum gasoline mode
• Mixed crude - RFCC operating in maximum distillate mode
• Mixed crude - RFCC operating in maximum gasoline mode
The mixed crude case is defined as the refinery processing a mix of Bach Ho and Dubai crude in the ratio of 5.5 million tonnes per annum of Bach Ho to 1 million tonnes per annum of Dubai crude. The refinery material balances have been prepared considering minimum benzene gasoline mode of operation (i.e. light naphtha cut of C5 – 82°C from NHT naphtha splitter is sent to the Isomerisation Unit). The refinery material balances are presented in Attachments 1A, 1B, 1C & 1D attached. The material balances include mass and liquid volume flows corresponding to the Stream Numbers included on the Process Flow Diagram - Refinery Flow Scheme - Doc No. 6960-000-20-0001. The refinery material balances also include Product Blending Balances for each operating case. The Blending Balances present a summary of the key intermediate and final product flows and product qualities. The overall material balances have been produced using process data from the crude assays and the individual process unit expected material balances and stream data. The refinery intermediate streams were used to calculate the finished product flow rates. The product blending was optimized against a given set of constraints inclusive of product specifications. For example Kerosene can be routed to Jet A-1 sales or can be used for blending into Auto Diesel to balance the pour point properties of the heavier gas oils. Attachment 2A & 2B present the key CDU stream property data for the CDU processing either 100% Bach Ho crude or the refinery processing mixed crude. The material balances mass and volume flow rates are based on calculated flows based on stream days. The refinery design is based on all processing units operating for 8000 hours annually, which is equivalent to stream factor of 0.913.
2. REFINERY EXPECTED MATERIAL BALANCE
The refinery expected material balances are presented for two different crude processing operations and two different RFCC operating modes. The CDU Basis of Design document 6960-011-PS-0002 defines basis used for the cut points on the crude unit. These are also presented on the CDU key stream properties included in Attachments 2A and 2B.
REFINERY MATERIAL BALANCE
6960-000-DS-0011 PAGE 3 of 4
REV: D4
5.000.DS.0011_D4.doc
The RFCC operating modes - Maximum Distillate and Maximum Gasoline - are defined in the RFCC BED Package for Unit 15. The refinery material balances are presented in Attachments 1A, 1B, 1C & 1D. The following notes further explain the basis used and set out any assumptions required in producing these material balances.
• Flows are predicted actual operating flows based on crude assay data and licensor expected yields and do not necessarily represent unit design capacities. For example the Basis of Design for the NHT/CCR includes a design margin on the quantity of heavy naphtha that can be processed. The material balances presented are based on processing all the heavy naphtha available.
• Minimum benzene gasoline mode of operation (i.e. light naphtha cut of C5 – 82°C containing benzene precursors from NHT naphtha splitter is sent to the Isomerisation Unit).
• Stream properties are based on crude assay data and licensor expected values
• For each of the four Refinery Operating cases, expected Gasoline Blending balances present two alternate cases: production of RON 95 and RON 90 Mogas or production of RON 92 and RON 90 Mogas simultaneously. All gasoline blending calculation results are presented for summer gasoline grade.
• All refinery fuel oil is assumed to be DCO. Refinery fuel oil consumption is based on Power Plant operation at nominal design power generation capacity (i.e. power supply to the Polypropylene Plant and/or power export to the EVN grid if possible). Refinery fuel oil requirements consider that excess C4s are sent to the fuel gas system (see section 4).
• It is assumed all kerosene not used for blending to diesel and fuel oil is sold as Jet A1 (i.e. no kerosene sales)
• The following margins were used for limiting constraints to account for test method repeatability:
0.2 for Mogas RON and MON 3.2 kPa for Mogas RVP 2° C for Auto Diesel 90% vol. boiling temperature (ASTM D86) 2.5° C for Fuel Oil Pour Point
For the Bach Ho - Max Gasoline case and for mixed crude max gasoline case - a minimum quantity of Jet A-1 has been included as a constraint to the refinery balance. The minimum Jet A-1 production is set at 659 Tonnes per stream day.
3. CDU STREAM DATA
The CDU key stream property data for Bach Ho and mixed crude processing is presented in Attachments 2A and 2B respectively. The data presented is based on the crude assay data and from the CDU process unit simulations.
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REFINERY MATERIAL BALANCE
5.000.DS.0011_D4.doc
4. MATERIAL BALANCE LIMITING CONSTRAINTS During preparation of the refinery expected material balances the following material constraints were noted:
• The RVP of summer grade gasoline (60 kPa) and minimum C3 content of LPG (20% mol) specifications does not enable all C4s to be used in Refinery products and consequently some C4s are sent to Fuel Gas.
• For the production of 95 RON Gasoline, the 50% vol. boiling temperature (120°C) is very close to limiting the production due to the relatively large quantity of reformate required in this blend.
• Due to the large quantity of LCO which is available for Auto Diesel production during Maximum Distillate operation, the diesel Pour Point is not a constraint. However, the quantity of HGO which can be blended in Auto Diesel is limited by the 90% vol. distillation temperature (370°C) and some HGO must be sent to Fuel Oil product.
VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)DUNG QUAT REFINERY PROJECTFEED DEVELOPMENT CONTRACT 7303N05-000-DS-0011ATTACHMENT 1A
Page 1 of 5
BLOCK FLOW DIAGRAM EXPECTED MASS BALANCE CRUDE BLEND : 100% Bach Ho OPERATING CASE : Max Distillate
STREAM 1 2 3 4 5 6 7 8 9 10 11 12 13DESCRIPTION Sweet
CrudeSour
CrudeCDU
OffGasLight
Naph to Isom
Total Naphtha
Raw Kero Light Gas Oil
Heavy Gas Oil
Atom Residue
CDU LPG RFCC Naph
LCO DCO From RFCC
TPSD 19500 - 7 683 2668 1223 4216 1722 9623 44 3137 3901 660BPSD 147976 - - 6361 23215 9920 32775 13041 68482 485 27601 28401 4327
STREAM 14 15 16 17 18 19 20 21 22 23 24 25 26DESCRIPTION LTU Feed Treated
LPGProp ylene
Propane Mixed C4's
C4's to LPG
C4's to Sphere
LPG to Sales
Naph to CCR
CCR LPG Reform ate
RFCC Naph
95 RON to Sales
TPSD 1348 1347 321 147 864 680 184 882 1975 55 1761 3137 2706BPSD 15009 15000 3866 1782 9163 7221 1948 9634 16856 638 13392 27601 22727
STREAM 27 28 29 30 31 32 38 39 40 41 42 43 44DESCRIPTION Jet A1 to
SalesKero to
Auto Diesel
LGO to Auto
Diesel
HGO to Auto
Diesel
LCO to Auto
Diesel
Auto Diesel
LGO to Fuel Oil HGO to
Fuel OilLCO to Fuel Oil Fuel Oil
NHT gas to RFCC
DCO to Fuel Oil
TPSD 1223 0 4216 1017 3808 9041 - - 705 95 971 14 171BPSD 9920 0 32775 7700 27846 68321 - - 5341 693 7156 - 1122
STREAM 45 47 48 49 50 51 52 53 54 55 61 62 71DESCRIPTION
90 RON to Sales
C4's to 95 RON
Isomerate to 95 RON
Reform to 95 RON
RFCC Naph to 95 RON
C4's to 90 RON
Isomerate to 90 RON
Reform to 90 RON
RFCC Naph to 90 RON
Excess C4 HDT LCO
ISOMERATE
LGO to LCO HDT
TPSD 2923 43 489 1291 883 34 164 470 2255 107 3902 653 -BPSD 25349 452 4690 9820 7765 365 1576 3572 19836 1131 28539 6266 -
VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)DUNG QUAT REFINERY PROJECTFEED DEVELOPMENT CONTRACT 7303N05-000-DS-0011ATTACHMENT 1A
Page 2 of 5
BLOCK FLOW DIAGRAM EXPECTED MASS BALANCE CRUDE BLEND : 100% Bach Ho OPERATING CASE : Max DistillateSTREAM 81DESCRIPTION HGO to
LCO HDTTPSD -BPSD -
VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)DUNG QUAT REFINERY PROJECTFEED DEVELOPMENT CONTRACT 7303N05-000-DS-0011ATTACHMENT 1A
Page 3 of 5
Total23 19 17 21
CCR LPG C4's to LPG
Propane LPG to Sales
Flow TPSD 55 680 147 882Flow BPSD 638 7221 1784 9634RVP kPa 1113 441 1255 667C3 Content Mol% 35.6 0.8 87.5 20SG 0.544 0.592 0.518 0.576
Total
47 48 49 50 26C4's to 95
RONIsomerate to 95 RON
Reform to 95 RON
RFCC Naph to 95
RON
95 RON to Sales
Flow TPSD 43 489 1291 883 2706Flow BPSD 452 4690 9820 7765 22727RON 98.7 86.4 102 91.7 95.2MON 88.4 84.4 90 79.6 85.2Sulphur wt % 0.001 0 0 0.001 < 10 ppmDensity kg/m3 593 656 827 715 749RVP kPa 441 88 18 51 57Olefins Vol% 58 0 1 43 16Benzene Vol% 0 0 1 1 1Aromatics Vol% 0 0 77 15 38
Total51 52 53 54 45
C4's to 90 RON
Isomerate to 90 RON
Reform to 90 RON
RFCC Naph to 90
RON
90 RON to Sales
Flow TPSD 34 164 470 2255 2923Flow BPSD 365 1576 3572 19836 25349RON 98.7 86.4 102 91.7 92.9MON 88.4 84.4 90 79.6 81.2Sulphur wt % 0.001 0 0 0.001 < 10 ppmDensity kg/m3 593 656 827 715 725RVP kPa 441 88 18 51 57Olefins Vol% 58 0 1 43 35Benzene Vol% 0 0 1 1 1Aromatics Vol% 0 0 77 15 23
Stream NoStream Name
Stream Name
Product 90 RON GasolineComponents
Product Blending BalancesBach Ho Maximum Distillate Case - Expected Balance
Stream NoStream Name
Product LPGComponents
Stream No
Product95 RON - 90 RON GASOLINE POOL
95 RON GasolineComponents
VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)DUNG QUAT REFINERY PROJECTFEED DEVELOPMENT CONTRACT 7303N05-000-DS-0011ATTACHMENT 1A
Page 4 of 5
Product Blending BalancesBach Ho Maximum Distillate Case - Expected Balance
Total47 48 49 50 26
C4's to 92 RON
Isomerate to 92 RON
Reform to 92 RON
RFCC Naph to 92
RON
92 RON to Sales
Flow TPSD 72 653 1704 2895 5325Flow BPSD 765 6266 12960 25470 45461RON 98.7 86.4 102 91.7 94.0MON 88.4 84.4 90 79.6 83.2Sulphur wt % 0.001 0 0 0.001 < 10 ppmDensity kg/m3 593 656 827 715 737RVP kPa 441 88 18 51 57Olefins Vol% 58 0 1 43 25Benzene Vol% 0 0 1 1 1Aromatics Vol% 0 0 77 15 30
Total
51 52 53 54 45C4's to 90
RONIsomerate to 90 RON
Reform to 90 RON
RFCC Naph to 90
RON
90 RON to Sales
Flow TPSD 5 - 57 242 304Flow BPSD 53 - 432 2131 2616RON 98.7 86.4 102 91.7 93.5MON 88.4 84.4 90 79.6 81.2Sulphur wt % 0.001 0 0 0.001 < 10 ppmDensity kg/m3 593 656 827 715 731RVP kPa 441 88 18 51 57Olefins Vol% 58 0 1 43 36Benzene Vol% 0 0 1 1 1Aromatics Vol% 0 0 77 15 25
90 RON GasolineComponents
Stream Name
Components Stream No
Stream Name
Stream No
92 RON - 90 RON GASOLINE POOLProduct 92 RON Gasoline
Product
VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)DUNG QUAT REFINERY PROJECTFEED DEVELOPMENT CONTRACT 7303N05-000-DS-0011ATTACHMENT 1A
Page 5 of 5
Product Blending BalancesBach Ho Maximum Distillate Case - Expected Balance
Total27 27
Jet A1 to Sales
Jet A1 to Sales
Flow TPSD 1223 1223Flow BPSD 9220 9920Density kg/m3 775 775Sulphur wt ppm 50 50Flash Point C 48 48Smoke Point mm 31 31Freeze Point C -52 -52
Total28 29 30 31 32
Kero to Auto
Diesel
LGO to Auto
Diesel
HGO to Auto
Diesel
LCO to Auto
Diesel
Auto Diesel
Flow TPSD 0 4216 1017 3808 9041Flow BPSD 0 32775 7700 27846 68321Density kg/m3 775 809 831 860 832Sulphur wt ppm 50 200 290 50 147Pour Point C -58 -3 20 -19 -2ASTM D86 90% C 204 322 405 340 368Cetane Index 47 60 64 42 53
Total38 39 40 41 44 42
Kero to Fuel Oil
LGO to Fuel Oil
HGO to Fuel Oil
LCO to Fuel Oil
DCO to Fuel Oil
Fuel Oil
Flow TPSD - - 705 95 171 971Flow BPSD - - 5341 693 1122 7156Density kg/m3 - - 831 860 960 854Sulphur wt ppm - - 290 50 700 339Pour Point C - - 20 -19 20 19
Stream NoStream Name
Components
Jet A1Components
Auto DieselProduct
Product
Stream NoStream Name
Stream Name
Fuel OilComponents
Product
Stream No
VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)DUNG QUAT REFINERY PROJECTFEED DEVELOPMENT CONTRACT 7303N05-000-DS-0011ATTACHMENT 1B
Page 1 Of 5
BLOCK FLOW DIAGRAM EXPECTED MASS BALANCE CRUDE BLEND 100% Bach Ho OPERATING CASE: Max Gaso
STREAM 1 2 3 4 5 6 7 8 9 10 11 12 13DESCRIPTION Sweet
CrudeSour
CrudeLPG off
CDULight
Naph to Isom
Total Naphtha
Raw Kero Light Gas Oil
Heavy Gas Oil
Atom Residue
CDU LPG RFCC Naph
LCO DCO From RFCC
TPSD 19500 0 7 683 2668 1223 4216 1722 9623 44 5101 1345 699BPSD 147976 0 - 6361 23215 9920 32775 13041 68482 485 43837 9287 4216
STREAM 14 15 16 17 18 19 20 21 22 23 24 25 26DESCRIPTION LTU Feed Treated
LPGProp ylene
Propane Mixed C4's
C4's to LPG
C4's to Sphere
LPG to Sales
Naph to CCR
CCR LPG Reform ate
RFCC Naph
95 RON to Sales
TPSD 1827 1825 462 172 1170 790 379 1018 1975 55 1761 5101 2604BPSD 20298 20286 5562 2093 12408 8384 4024 11108 16856 638 13392 43837 21770
STREAM 27 28 29 30 31 32 38 39 40 41 42 43 44DESCRIPTION Jet A1 to
SalesKero to
Auto Diesel
LGO to Auto
Diesel
HGO to Auto
Diesel
LCO to Auto
Diesel
Auto Diesel
LGO to Fuel Oil HGO to
Fuel OilLCO to Fuel Oil Fuel Oil
NHT gas to RFCC
DCO to Fuel Oil
TPSD 659 564 4216 359 1802 6941 - - 740 166 1128 14 223BPSD 5347 4573 32775 2714 13134 53197 - - 5601 1210 8154 - 1344
STREAM 45 47 48 49 50 51 52 53 54 55 61 62 71DESCRIPTION
90 RON to Sales
C4's to 95 RON
Isomerate to 95 RON
Reform to 95 RON
RFCC Naph to 95 RON
C4's to 90 RON
Isomerate to 90 RON
Reform to 90 RON
RFCC Naph to 90 RON
Excess C4 HDT LCO
ISOMERATE
LGO to LCO HDT
TPSD 5135 64 443 1189 908 159 210 572 4193 159 1968 653 -BPSD 44090 675 4250 9040 7805 1690 2016 4352 36032 1659 14344 6266 -
VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)DUNG QUAT REFINERY PROJECTFEED DEVELOPMENT CONTRACT 7303N05-000-DS-0011ATTACHMENT 1B
Page 2 Of 5
BLOCK FLOW DIAGRAM EXPECTED MASS BALANCE CRUDE BLEND 100% Bach Ho OPERATING CASE: Max GasoSTREAM 81DESCRIPTION HGO to
LCO HDTTPSD 624BPSD 4726
VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)DUNG QUAT REFINERY PROJECTFEED DEVELOPMENT CONTRACT 7303N05-000-DS-0011ATTACHMENT 1B
Page 3 Of 5
Total23 19 17 21
CCR LPG C4's to LPG
Propane LPG to Sales
Flow TPSD 55 790 172 1018Flow BPSD 638 8384 2093 11108RVP kPa 1113 440 1255 663C3 Content Mol% 35.6 0.8 87.5 20SG 0.546 0.593 0.518 0.576
Total47 48 49 50 26
C4's to 95 RON
Isomerate to 95 RON
Reform to 95 RON
RFCC Naph to 95
RON
95 RON to Sales
Flow TPSD 64 443 1189 908 2604Flow BPSD 675 4250 9040 7805 21770RON 98.7 86.4 102 91.8 95.2MON 88.3 84.4 90 79.6 85.2Sulphur wt % 0.001 0 0 0.001 < 10 ppmDensity kg/m3 593 656 827 732 752RVP kPa 440 88 18 34 57Olefins Vol% 58 0 1 33 14Benzene Vol% 0 0 1 1 1Aromatics Vol% 0 0 77 26 41
Total51 52 53 54 45
C4's to 90 RON
Isomerate to 90 RON
Reform to 90 RON
RFCC Naph to 90
RON
90 RON to Sales
Flow TPSD 159 210 572 4193 5135Flow BPSD 1690 2016 4352 36032 44090RON 98.7 86.4 102 91.8 92.8MON 88.3 84.4 90 79.6 81.2Sulphur wt % 0.001 0 0 0.001 < 10 ppmDensity kg/m3 593 656 827 732 733RVP kPa 440 88 18 34 57Olefins Vol% 58 0 1 33 29Benzene Vol% 0 0 1 1 1Aromatics Vol% 0 0 77 26 29
Components Product
95 RON - 90 RON GASOLINE POOL
90 RON Gasoline
Stream No
Stream NoStream Name
95 RON GasolineComponents
Stream Name
Stream NoStream Name
Product
Product Blending BalancesBach Ho Maximum Gasoline Case - Expected Balance
LPGComponents
Product
VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)DUNG QUAT REFINERY PROJECTFEED DEVELOPMENT CONTRACT 7303N05-000-DS-0011ATTACHMENT 1B
Page 4 Of 5
Product Blending BalancesBach Ho Maximum Gasoline Case - Expected Balance
Total47 48 49 50 26
C4's to 92 RON
Isomerate to 92 RON
Reform to 92 RON
RFCC Naph to 92
RON
92 RON to Sales
Flow TPSD 131 653 1420 2912 5117Flow BPSD 1390 6266 10800 25025 43481RON 98.7 86.4 102 91.8 93.8MON 88.3 84.4 90 79.6 83.2Sulphur wt % 0.001 0 0 0.001 < 10 ppmDensity kg/m3 593 656 827 732 740RVP kPa 440 88 18 34 57Olefins Vol% 58 0 1 33 21Benzene Vol% 0 0 1 1 1Aromatics Vol% 0 0 77 26 34
Total51 52 53 54 45
C4's to 90 RON
Isomerate to 90 RON
Reform to 90 RON
RFCC Naph to 90
RON
90 RON to Sales
Flow TPSD 92 - 341 2189 2622Flow BPSD 975 - 2592 18812 22379RON 98.7 86.4 102 91.8 93.3MON 88.3 84.4 90 79.6 81.2Sulphur wt % 0.001 0 0 0.001 < 10 ppmDensity kg/m3 593 656 827 732 737RVP kPa 440 88 18 34 57Olefins Vol% 58 0 1 33 30Benzene Vol% 0 0 1 1 1Aromatics Vol% 0 0 77 26 31
Components Stream No
Stream Name
Components Stream No
Stream Name
Product 90 RON Gasoline
92 RON - 90 RON GASOLINE POOLProduct 92 RON Gasoline
VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)DUNG QUAT REFINERY PROJECTFEED DEVELOPMENT CONTRACT 7303N05-000-DS-0011ATTACHMENT 1B
Page 5 Of 5
Product Blending BalancesBach Ho Maximum Gasoline Case - Expected Balance
Total27 27
Jet A1 to Sales
Jet A1 to Sales
Flow TPSD 659 659Flow BPSD 5347 5347Density kg/m3 775 775Sulphur wt ppm 50 50Flash Point C 51 51Smoke Point mm 31 31Freeze Point C -52 -52
Total28 29 30 31 32
Kero to Auto
Diesel
LGO to Auto
Diesel
HGO to Auto
Diesel
LCO to Auto
Diesel
Auto Diesel
Flow TPSD 564 4216 359 1802 6941Flow BPSD 4573 32775 2714 13134 53197Density kg/m3 775 809 831 863 821Sulphur wt ppm 50 200 290 50 154Pour Point C -58 -3 20 5 0ASTM D86 90% C 204 322 405 385 348Cetane Index 48 60 64 41 55
Total38 39 40 41 44 42
Kero to Fuel Oil
LGO to Fuel Oil
HGO to Fuel Oil
LCO to Fuel Oil
DCO to Fuel Oil
Fuel Oil
Flow TPSD - - 740 166 223 1128Flow BPSD - - 5601 1210 1344 8154Density kg/m3 - - 831 862 1043 870Sulphur wt ppm - - 290 50 1000 395Pour Point C - - 20 5 20 19
Auto Diesel
Stream No
Jet A1Components
Components
Stream Name
Product
Stream No
Product
Stream NoStream Name
Stream Name
Fuel OilComponents
Product
VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)DUNG QUAT REFINERY PROJECTFEED DEVELOPMENT CONTRACT 7303N05-000-DS-0011ATTACHMENT 1C
Page 1 of 5
BLOCK FLOW DIAGRAM EXPECTED MASS BALANCE CRUDE BLEND : Mixed Case OPERATING CASE : Max Dist
STREAM 1 2 3 4 5 6 7 8 9 10 11 12 13DESCRIPTION Sweet
CrudeSour
CrudeLPG off
CDULight
Naph to Isom
Total Naphtha
Raw Kero Light Gas Oil
Heavy Gas Oil
Atom Residue
CDU LPG RFCC Naph
LCO DCO From RFCC
TPSD 16500 3000 8 684 2673 1221 4146 1695 9635 61 3051 3888 606BPSD 125210 21697 - 6373 23294 9881 32075 12732 67625 677 26695 27763 3834
STREAM 14 15 16 17 18 19 20 21 22 23 24 25 26DESCRIPTION LTU Feed Treated
LPGProp ylene
Propane Mixed C4's
C4's to LPG
C4's to Sphere
LPG to Sales
Naph to CCR
CCR LPG Reform ate
RFCC Naph
95 RON to Sales
TPSD 1422 1421 332 165 908 759 150 979 1979 55 1764 3051 3041BPSD 15835 15824 3993 2001 9653 8058 1589 10691 16890 639 13419 26695 25540
STREAM 27 28 29 30 31 32 38 39 40 41 42 43 44DESCRIPTION Jet A1 to
SalesKero to
Auto Diesel
LGO to Auto
Diesel
HGO to Auto
Diesel
LCO to Auto
Diesel
Auto Diesel
LGO to Fuel Oil HGO to
Fuel OilLCO to Fuel Oil Fuel Oil
NHT gas to RFCC
DCO to Fuel Oil
TPSD 1221 0 4146 952 3767 8865 - - 743 93 912 14 76BPSD 9881 0 32075 7150 27389 66614 - - 5582 673 6737 - 482
STREAM 45 47 48 49 50 51 52 53 54 55 61 62 71DESCRIPTION
90 RON to Sales
C4's to 95 RON
Isomerate to 95 RON
Reform to 95 RON
RFCC Naph to 95 RON
C4's to 90 RON
Isomerate to 90 RON
Reform to 90 RON
RFCC Naph to 90 RON
Excess C4 HDT LCO
ISOMERATE
LGO to LCO HDT
TPSD 2520 51 549 1415 1025 39 106 350 2026 60 3859 655 -BPSD 21808 545 5265 10760 8970 412 1012 2659 17725 632 28062 6277 -
VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)DUNG QUAT REFINERY PROJECTFEED DEVELOPMENT CONTRACT 7303N05-000-DS-0011ATTACHMENT 1C
Page 2 of 5
BLOCK FLOW DIAGRAM EXPECTED MASS BALANCE CRUDE BLEND : Mixed Case OPERATING CASE : Max DistSTREAM 81DESCRIPTION HGO to
LCO HDTTPSD -BPSD -
VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)DUNG QUAT REFINERY PROJECTFEED DEVELOPMENT CONTRACT 7303N05-000-DS-0011ATTACHMENT 1C
Page 3 Of 5
Total23 19 17 21
CCR LPG C4's to LPG
Propane LPG to Sales
Flow TPSD 55 759 165 979Flow BPSD 638 8058 2001 10691RVP kPa 1113 438 1255 662C3 Content Mol% 35.6 0.8 87.5 20SG 0.546 0.592 0.518 0.576
Total
47 48 49 50 26C4's to 95
RONIsomerate to 95 RON
Reform to 95 RON
RFCC Naph to 95
RON
95 RON to Sales
Flow TPSD 51 549 1415 1025 3041Flow BPSD 545 5265 10760 8970 25540RON 98.4 86.4 102 92.0 95.2MON 88.4 84.4 90 79.5 85.2Sulphur wt % 0.001 0 0 0.001 < 10 ppmDensity kg/m3 592 656 827 719 749RVP kPa 438 88 18 48 57Olefins Vol% 58 0 1 45 18Benzene Vol% 0 0 1 2 1Aromatics Vol% 0 0 77 12 36
Total51 52 53 54 45
C4's to 90 RON
Isomerate to 90 RON
Reform to 90 RON
RFCC Naph to 90
RON
90 RON to Sales
Flow TPSD 39 106 350 2026 2520Flow BPSD 412 1012 2659 17725 21808RON 98.4 86.4 102 92.0 93.1MON 88.4 84.4 90 79.5 81.2Sulphur wt % 0.001 0 0 0.001 < 10 ppmDensity kg/m3 592 656 827 719 727RVP kPa 438 88 18 48 57Olefins Vol% 58 0 1 45 38Benzene Vol% 0 0 1 2 1Aromatics Vol% 0 0 77 12 19
Components Stream No
Stream Name
Stream NoStream Name
95 RON - 90 RON GASOLINE POOL95 RON Gasoline
Components
90 RON Gasoline
Stream NoStream Name
Product
Product Blending BalancesMixed Crude Maximum Distillate Case - Expected Balance
Product LPGComponents
Product
VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)DUNG QUAT REFINERY PROJECTFEED DEVELOPMENT CONTRACT 7303N05-000-DS-0011ATTACHMENT 1C
Page 4 Of 5
Product Blending BalancesMixed Crude Maximum Distillate Case - Expected Balance
Total47 48 49 50 26
C4's to 92 RON
Isomerate to 92 RON
Reform to 92 RON
RFCC Naph to 92
RON
92 RON to Sales
Flow TPSD 90 655 1764 3051 5561Flow BPSD 960 6277 13419 26695 47351RON 98.4 86.4 102 92.0 94.2MON 88.4 84.4 90 79.5 83.35Sulphur wt % 0.001 0 0 0.001 < 10 ppmDensity kg/m3 592 656 827 719 739RVP kPa 438 88 18 48 57Olefins Vol% 58 0 1 45 27Benzene Vol% 0 0 1 2 1Aromatics Vol% 0 0 77 12 28
Total51 52 53 54 45
C4's to 90 RON
Isomerate to 90 RON
Reform to 90 RON
RFCC Naph to 90
RON
90 RON to Sales
Flow TPSD - - - - -Flow BPSD - - - - -RON 98.4 86.4 102 92.0 -MON 88.4 84.4 90 79.5 -Sulphur wt % 0.001 0 0 0.001 -Density kg/m3 592 656 827 719 -RVP kPa 438 88 18 48 -Olefins Vol% 58 0 1 45 -Benzene Vol% 0 0 1 2 -Aromatics Vol% 0 0 77 12 -
Components
Components
Stream NoStream Name
Product 90 RON Gasoline
92 RON - 90 RON GASOLINE POOLProduct 92 RON Gasoline
Stream NoStream Name
VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)DUNG QUAT REFINERY PROJECTFEED DEVELOPMENT CONTRACT 7303N05-000-DS-0011ATTACHMENT 1C
Page 5 Of 5
Product Blending BalancesMixed Crude Maximum Distillate Case - Expected Balance
Total27 27
Jet A1 to Sales
Jet A1 to Sales
Flow TPSD 1221 1221Flow BPSD 9881 9881Density kg/m3 777 777Sulphur wt ppm 310 310Flash Point C 48 48Smoke Point mm 30 30Freeze Point C -52 -52
Total28 29 30 31 32
Kero to Auto
Diesel
LGO to Auto
Diesel
HGO to Auto
Diesel
LCO to Auto
Diesel
Auto Diesel
Flow TPSD 0 4146 952 3767 8865Flow BPSD 0 32075 7150 27389 66614Density kg/m3 777 813 837 865 837Sulphur wt ppm 310 2000 3710 350 1482Pour Point C -57 -4 20 -17 -3ASTM D86 90% C 204 321 404 340 368Cetane Index 46 59 62 37 50
Total38 39 40 41 44 42
Kero to Fuel Oil
LGO to Fuel Oil
HGO to Fuel Oil
LCO to Fuel Oil
DCO to Fuel Oil
Fuel Oil
Flow TPSD - - 743 93 76 912Flow BPSD - - 5582 673 482 6737Density kg/m3 - - 837 865 994 851Sulphur wt ppm - - 3710 350 8350 3756Pour Point C - - 20 -17 20 19
Auto Diesel
Jet A1Components
Components Stream No
Stream NoStream Name
Product
Product
Stream NoStream Name
Stream Name
Fuel OilComponents
Product
VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)DUNG QUAT REFINERY PROJECTFEED DEVELOPMENT CONTRACT 7303N05-000-DS-0011ATTACHMENT 1D
Page 1 of 5
BLOCK FLOW DIAGRAM EXPECTED MASS BALANCE CRUDE BLEND : Mixed Crude OPERATING CASE : Max Gaso
STREAM 1 2 3 4 5 6 7 8 9 10 11 12 13DESCRIPTION Sweet
CrudeSour
CrudeLPG off
CDULight
Naph to Isom
Total Naphtha
Raw Kero Light Gas Oil
Heavy Gas Oil
Atom Residue
CDU LPG RFCC Naph
LCO DCO From RFCC
TPSD 16500 3000 8 684 2673 1221 4146 1695 9635 61 4798 1402 726BPSD 125210 21697 - 6373 23294 9881 32075 12732 67625 677 41007 9526 4182
STREAM 14 15 16 17 18 19 20 21 22 23 24 25 26DESCRIPTION LTU Feed Treated
LPGProp ylene
Propane Mixed C4's
C4's to LPG
C4's to Sphere
LPG to Sales
Naph to CCR
CCR LPG Reform ate
RFCC Naph
95 RON to Sales
TPSD 1813 1812 448 188 1156 857 299 1099 1979 55 1764 4798 3122BPSD 20184 20170 5384 2277 12260 9093 3174 12001 16890 639 13419 41007 26090
STREAM 27 28 29 30 31 32 38 39 40 41 42 43 44DESCRIPTION Jet A1 to
SalesKero to
Auto Diesel
LGO to Auto
Diesel
HGO to Auto
Diesel
LCO to Auto
Diesel
Auto Diesel
LGO to Fuel Oil HGO to
Fuel OilLCO to Fuel Oil Fuel Oil
NHT gas to RFCC
DCO to Fuel Oil
TPSD 659 562 2530 160 3750 7002 - - 632 148 1135 14 354BPSD 5333 4548 19572 1201 27815 53135 - - 4747 1100 7890 - 2043
STREAM 45 47 48 49 50 51 52 53 54 55 61 62 71DESCRIPTION
90 RON to Sales
C4's to 95 RON
Isomerate to 95 RON
Reform to 95 RON
RFCC Naph to 95 RON
C4's to 90 RON
Isomerate to 90 RON
Reform to 90 RON
RFCC Naph to 90 RON
Excess C4 HDT LCO
ISOMERATE
LGO to LCO HDT
TPSD 4320 78 529 1387 1127 146 125 377 3671 75 3898 655 1616BPSD 36995 830 5075 10550 9635 1552 1202 2869 31372 792 28914 6277 12503
VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)DUNG QUAT REFINERY PROJECTFEED DEVELOPMENT CONTRACT 7303N05-000-DS-0011ATTACHMENT 1D
Page 2 of 5
BLOCK FLOW DIAGRAM EXPECTED MASS BALANCE CRUDE BLEND : Mixed Crude OPERATING CASE : Max GasoSTREAM 81DESCRIPTION HGO to
LCO HDTTPSD 903BPSD 6784
VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)DUNG QUAT REFINERY PROJECTFEED DEVELOPMENT CONTRACT 7303N05-000-DS-0011ATTACHMENT 1D
Page 3 Of 5
Total23 19 17 21
CCR LPG C4's to LPG
Propane LPG to Sales
Flow TPSD 55 857 188 1099Flow BPSD 639 9093 2277 12001RVP kPa 1113 438 1255 660C3 Content Mol% 35.6 0.8 87.5 20SG 0.546 0.593 0.518 0.576
Total
47 48 49 50 26C4's to 95
RONIsomerate to 95 RON
Reform to 95 RON
RFCC Naph to 95
RON
95 RON to Sales
Flow TPSD 78 529 1387 1127 3122Flow BPSD 830 5075 10550 9635 26090RON 98.5 86.4 102 92.1 95.2MON 88.3 84.4 90 79.9 85.2Sulphur wt % 0.001 0 0 0.001 < 10 ppmDensity kg/m3 593 656 827 736 753RVP kPa 438 88 18 32 57Olefins Vol% 58 0 1 33 15Benzene Vol% 0 0 1 1 1Aromatics Vol% 0 0 77 26 41
Total51 52 53 54 45
C4's to 90 RON
Isomerate to 90 RON
Reform to 90 RON
RFCC Naph to 90
RON
90 RON to Sales
Flow TPSD 146 125 377 3671 4320Flow BPSD 1552 1202 2869 31372 36995RON 98.5 86.4 102 92.1 93.0MON 88.3 84.4 90 79.9 81.2Sulphur wt % 0.001 0 0 0.001 < 10 ppmDensity kg/m3 593 656 827 736 735RVP kPa 438 88 18 32 57Olefins Vol% 58 0 1 33 30Benzene Vol% 0 0 1 1 1Aromatics Vol% 0 0 77 26 28
Stream NoStream Name
Product 90 RON GasolineComponents
Stream NoStream Name
Product
Stream No
95 RON - 90 RON GASOLINE POOL95 RON Gasoline
Components
Stream Name
Product Blending BalancesMixed Crude Maximum Gasoline Case - Expected Balance
Product LPGComponents
VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)DUNG QUAT REFINERY PROJECTFEED DEVELOPMENT CONTRACT 7303N05-000-DS-0011ATTACHMENT 1D
Page 4 Of 5
Product Blending BalancesMixed Crude Maximum Gasoline Case - Expected Balance
Total47 48 49 50 26
C4's to 92 RON
Isomerate to 92 RON
Reform to 92 RON
RFCC Naph to 92
RON
92 RON to Sales
Flow TPSD 177 655 1634 3682 6149Flow BPSD 1880 6277 12430 31470 52057RON 98.5 86.4 102 92.1 94.0MON 88.3 84.4 90 79.9 83.2Sulphur wt % 0.001 0 0 0.001 < 10 ppmDensity kg/m3 593 656 827 736 743RVP kPa 438 88 18 32 57Olefins Vol% 58 0 1 33 22Benzene Vol% 0 0 1 1 1Aromatics Vol% 0 0 77 26 34
Total51 52 53 54 45
C4's to 90 RON
Isomerate to 90 RON
Reform to 90 RON
RFCC Naph to 90
RON
90 RON to Sales
Flow TPSD 47 - 130 1116 1293Flow BPSD 503 - 989 9537 11029RON 98.5 86.4 102 92.1 93.3MON 88.3 84.4 90 79.9 81.2Sulphur wt % 0.001 0 0 0.001 < 10 ppmDensity kg/m3 593 656 827 736 738RVP kPa 438 88 18 32 57Olefins Vol% 58 0 1 33 31Benzene Vol% 0 0 1 1 1Aromatics Vol% 0 0 77 26 29
Product 90 RON GasolineComponents
Components Stream No
Stream Name
92 RON - 90 RON GASOLINE POOLProduct 92 RON Gasoline
Stream NoStream Name
VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)DUNG QUAT REFINERY PROJECTFEED DEVELOPMENT CONTRACT 7303N05-000-DS-0011ATTACHMENT 1D
Page 5 Of 5
Product Blending BalancesMixed Crude Maximum Gasoline Case - Expected Balance
Total27 27
Jet A1 to Sales
Jet A1 to Sales
Flow TPSD 659 659Flow BPSD 5333 5333Density kg/m3 777 777Sulphur wt ppm 310 310Flash Point C 51 51Smoke Point mm 30 30Freeze Point C -52 -52
Total28 29 30 31 32
Kero to Auto
Diesel
LGO to Auto
Diesel
HGO to Auto
Diesel
LCO to Auto
Diesel
Auto Diesel
Flow TPSD 562 2530 160 3750 7002Flow BPSD 4548 19572 1201 27815 53135Density kg/m3 777 813 837 848 829Sulphur wt ppm 310 2000 3710 350 1020Pour Point C -57 -4 20 4 0ASTM D86 90% C 204 321 404 381 350Cetane Index 46 59 62 49 53
Total38 39 40 41 44 42
Kero to Fuel Oil
LGO to Fuel Oil
HGO to Fuel Oil
LCO to Fuel Oil
DCO to Fuel Oil
Fuel Oil
Flow TPSD - - 632 148 354 1135Flow BPSD - - 4747 1100 2043 7890Density kg/m3 - - 837 848 1092 905Sulphur wt ppm - - 3710 350 10300 5330Pour Point C - - 20 4 20 19
Product
Stream NoStream Name
Jet A1Components
Auto DieselComponents
Product
Stream NoStream Name
Stream Name
Fuel OilComponents
Stream No
Product
VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)DUNG QUAT REFINERY PROJECTFEED DEVELOPMENT CONTRACT 7303N05-000-DS-0011ATTACHMENT 2A
Page 1 of 1
KEY STREAM PROPERTIES
Property Whole Crude LPG/offgas Light naphtha (1) Heavy naphtha (1) Kerosene LGO HGO Residue
Cut start temperature (OC) - - 15 70 165 205 330 >370Cut end temperature (OC) - <15 70 165 205 330 370 -
Wt% Yield on crude 100 0.3 2.7 10.6 6.3 21.4 8.6 50.1Production kT/annum 6500 20 175 689 410 1391 559 3256Production T/stream day 19500 59 526 2067 1229 4173 1677 9769
Specific gravity (15/15) 0.8289 - 0.65 0.741 0.776 0.811 0.830 0.882Sulphur wt% 0.03 - 0.001 0.001 0.005 0.020 0.029 0.054Aromatics wt% - - - 12.7 11.3 9.6 - -Flash point (OC) - - - - 51 77 150 -Freeze Point (OC) - - - - -52 4 29 -Cloud Point (OC) - - - - -56 0 26 -Pour Point (OC) 33 - - - -58 -2 24 -Cetane index (D976) - - - - 48.9 62.7 64.1 -Kinematic viscosity at 38OC (cst) 6.75 - - - 1.1 3 8.3 -Kinematic viscosity at 50OC (cst) - - - - 0.8 2.4 5.8 -RON - - 58.9 42.6 - - - -MON - - 58.9 40.5 - - - -ppm Ni 0.22 - - - - - - 1ppm V 0.02 - - - - - - 0RVP (kPa) 20.2 - 75.6 7.1 - - - -
ASTM D86 distillation (oC at vol% recovered)5% - - 47 90 177 220 322 35210% - - 49 107 181 230 332 37230% - - 55 122 186 253 355 42650% - - 60 130 188 275 368 46770% - - 64 140 194 296 379 53990% - - 68 156 204 322 405 73395% - - 78 165 213 331 414 794
Notes : 1- Light Naphtha and Heavy Naphtha are produced as one stream from Unit 11 (Full Range Naphtha from CDU Stripper bottom)
100% Bach-Ho
VIETNAM OIL AND GAS CORPORATION (PETROVIETNAM)DUNG QUAT REFINERY PROJECTFEED DEVELOPMENT CONTRACT 7303N05-000-DS-0011ATTACHMENT 2B
Page 1 of 1
KEY STREAM PROPERTIES
Property Whole Crude LPG/offgas Light naphtha (1) Heavy naphtha (1) Kerosene LGO HGO Residue
Cut start temperature (OC) - - 15 70 165 205 330 370Cut end temperature (OC) - <15 70 165 205 330 370 -
Wt% Yield on crude 100 0.4 2.7 11.0 6.3 21.1 8.5 50.0Production kT/annum 6500 27 177 713 407 1371 553 3255Production T/stream day 19500 82 531 2139 1221 4114 1658 9765
Specific gravity (15/15) 0.835 - 0.646 0.741 0.778 0.815 0.837 0.893Sulphur wt% 0.35 - 0.003 0.010 0.031 0.200 0.371 0.550Aromatics wt% - - - 12.7 12.4 12.3 - -Flash point (OC) - - - - 49 76 153 -Freeze Point (OC) - - - - -52 2 27 -Cloud Point (OC) - - - - -55 -2 23 -Pour Point (OC) 27.6 - - - -57 -4 21 -Cetane index (D976) - - - - 47.8 61.3 62.0 -Kinematic viscosity at 38OC (cst) - - - - 1.1 3 8.3 -Kinematic viscosity at 50OC (cst) - - - - 0.8 2.4 5.8 -RON - - 60.3 43.4 - - - -MON - - 60.1 41.2 - - - -ppm Ni 1.06 - - - - - - 5ppm V 4.33 - - - - - - 10.5RVP (kPa) 6.64 - 75.1 7.4 - - - -
ASTM D86 distillation (oC at vol% recovered)5% - - 43 90 173 219 320 35310% - - 48 106 180 228 331 37230% - - 50 119 185 252 354 42750% - - 52 128 187 275 367 47070% - - 64 138 198 295 378 53990% - - 69 155 204 321 404 73195% - - 78 164 212 331 413 807
Notes : 1- Light Naphtha and Heavy Naphtha are produced as one stream from Unit 11 (Full Range Naphtha from CDU Stripper bottom)
85% Bach-Ho/15% Dubai mix
