New Approach to Optimizing Fired Heaters • Ashutosh Garg, Furnace Improvements Sugar Land Texas, USA Energy Consumption • Petroleum Refining ▫ 7.5% of the total energy consumption in USA • 0.40 MMBtu/ BBL of oil • Total Energy consumed in refining- 7.1 Quadrillion BTU/yr • Energy cost -$6/MMBtu • Total Energy Cost- 42 Billion /yr • Fired heaters -40-70% of the energy Energy Consumption • • • • A Typical refinery process 100,000 BPD Consumption of 0.40 MMBTU/BBL $6 per MMBTU Energy bill of $ 87.6 million per year. Potential Saving • 1% Efficiency improve • $876,000/Year Fired Heaters • Essential component in Petrochemical and Chemical Plants • Each refinery has ≈ 20-50 fired heaters • Design efficiency - 70-90% ▫ Operating efficiency is even less than design. Maintaining Design Operation • Maintain the design conditions (very difficult) • In the field, heater loads change constantly due to variations in: ▫ ▫ ▫ ▫ Feed flow rate Feed temperature Fuel composition Ambient temperature • The heater will be operating a non-optimal conditions • Requires optimization 24/7 How to Maintain the Design Efficiency? • When the heater conditions change, adjustments in the heater are required. • Manual adjustments are provided- not adequate • Optimizing the fired heater will: ▫ Reduce Energy Consumption ▫ Increase run length ▫ Minimize maintenance • FIS has proposed two prong approach • Software based- Heater Performance Index • Hardware based- Draft & Excess O2 Control Fired Heater • Heat liberated by the combustion of fuels is transferred to fluids contained in coils • Fired Heater: ▫ Radiant Section ▫ Convection Section ▫ Stack www.heatflux.com Typical heater efficiency • Natural Draft- 70-84% • Balance Draft-90-92% • Natural Draft heaters in Industry- 86% • Balanced Draft heaters in Industy-12% • Typical stack temperature – 500-800 F • Typical stack Oxygen- 2-10% • Target Oxygen-2-3% • Plenty of room for optimization Combustion • Combustion Requires ▫ Air ( 0.21O2 + 0.79 N2) ▫ Fuel ▫ Ignition source • Complete Combustion ▫ Excess air • Incomplete Combustion ▫ Energy Loss ▫ CO and H2 are released Draft • Pressure inside the heater ▫ Combustion air is drawn inside the heater through the burner’s air register ▫ Hot Flue gas flows out of the heater through the stack • Types of Draft ▫ ▫ ▫ ▫ Natural Draft (ND) Forced Draft (FD) Induced Draft (ID) Balanced Draft > 80% < 1% ≈ 10% ≈ 10% Draft • Stack Dampers helps control the draft STACK EXIT LOSS STACK (SE)a STACK EFFECT IN STACK ________ Pc • Excess or shortage of draft is not acceptable (SE)c CONVECTION SECTION RADIANT SECTION • Arch is the highest pressure point in the heater 0.05"- 0.1" W.G. DRAFT DRAFT AT RADIANT SECTION OUTLET, R0 NEGATIVE PRESSURE 0.05"- 0.1" W.G. AT TOP OF RADIANT SECTION Pb (SE)r Pa BURNERS NEGATIVE POSITIVE PRESSURE PRESSURE 0 Burner Operation • Correct combustion in firebox include: ▫ The firebox is clear ▫ No smoky appearance ▫ Burners flames are steady and well-formed • Check burners regularly • Adjusting burner registers to control air intake Air Leakages • Air entering in to furnace from a number of places: ▫ ▫ ▫ ▫ Peepholes Header box doors Tube guide opening Feed tubes entering and exits ▫ Not pressure tight structure Heater Optimization • Target set 2-3% O2 in the flue gas. • Operating conditions fluctuates : ▫ Manual control /adjustments ▫ Operators Number going down Experience going down Need training Optimisation Case Study -1 • FIS performed a tuning job for a refinery. • Heater: ▫ Depentanizer reboiler heater ▫ Horizontal tube box ▫ Absorbed heat duty - 87 MMBtu/hr ▫ 15 up fired burners ▫ The stacks is connected to a large common stack ▫ Two off take ducts provided with manual dampers Optimisation Approach • Check draft ▫ Adjust using off-take dampers • Check excess O2 ▫ Adjust burner register • Check burners ▫ Light up all burners ▫ Check Flames/Firebox Draft 0.7 Draft , in H2O 0.6 0.5 0.4 0.3 0.2 0.1 10:48 12:00 13:12 Time (7/22/09) 14:24 Excess Oxygen Excess Oxygen, % 6.0 5.5 5.0 4.5 4.0 3.5 3.0 2.5 2.0 10:48 12:00 13:12 Time (7/22/09) 14:24 Stack Temperature, °F Stack Temperature 645 635 625 615 605 Stack Temp. A Stack Temp. B 595 10:48 12:00 13:12 Time (7/22/09) 14:24 Thermal Efficiency Thermal Efficiency, % 83.0 82.0 81.0 80.0 79.0 78.0 10:48 12:00 13:12 Time (7/22/09) 14:24 Crude Heater Tuning Case Study -2 • Natural Draft Crude Heater • Horizontal tube • Up-fired burners • 11 burners 3440 20 3420 18 3400 16 14 3380 12 3360 10 3340 3320 8 Flue Gas Flow, MSCFD 6 3300 3280 4 Fuel Gas Pressure, psig 2 3260 0 11:15 AM 11:30 AM 11:45 AM 12:00 PM 12:45 PM 1:00 PM 1:15 PM 1:30 PM Fuel gas pressure, psig Fuel gas flow, MSCFD Fuel gas Flow and Pressure Before & After Tuning Tube Skin Temp Before & After Tuning 760 740 720 T Skin, °F 700 680 660 640 620 600 580 11:15 AM 11:30 AM 11:45 AM 12:00 PM 12:45 PM 1:00 PM 1:15 PM 1:30 PM Observations in Refineries • • • • Furnace working off design conditions Poor quality of dampers Lower number of operators Operator without sufficient training Recommendations • Software ▫ Heater Performance Index (HPI) • Hardware ▫ Draft control system ▫ Excess O2 control system Heater Performance Index • Analyzes the performance of Fired Heater 24/7 • Built into DCS • Generates guidelines • Built in intelligence • Customized modeling ▫ Thermal Efficiency ▫ Fuel gas rate, ▫ Draft, ▫ Excess O2, ▫ Tube skin temperatures, ▫ Feed flow rate, ▫ Pressure drop, ▫ Coking rate, ▫ Air preheater performance Crude Flow Rates TAG No. SERVICE UNITS SET POINT 8/15/2009 8/16/2009 8/17/2009 Data 1 Data 2 Data 3 PROCESS 57FC0009.PV Total Crude Flow BPH 4337.6 5249.1 4807.3 4637.7 57FC0001.PV Crude Flow to Pass 1 BPH 542.2 709.5 711.6 668.0 57FC0002.PV Crude Flow to Pass 2 BPH 542.2 676.5 725.0 725.0 57FC0003.PV Crude Flow to Pass 3 BPH 542.2 670.8 671.1 635.6 57FC0004.PV Crude Flow to Pass 4 BPH 542.2 729.1 731.1 686.3 57FC0005.PV Crude Flow to Pass 5 BPH 542.2 729.1 731.2 686.3 57FC0006.PV Crude Flow to Pass 6 BPH 542.2 695.1 710.1 680.2 57FC0007.PV Crude Flow to Pass 7 BPH 542.2 737.4 743.8 711.8 BPH 542.2 706.7 717.7 684.7 Average Coil Inlet Pressure TAG No. SERVICE UNITS SET POINT 8/15/2009 8/16/2009 8/17/2009 Data 1 Data 2 Data 3 PROCESS 57PI0054.PV Crude Inlet Pressure (Pass 1) psig 147.9 278.9 287.4 286.0 57PI0055.PV Crude Inlet Pressure (Pass 2) psig 147.9 296.0 309.6 309.8 57PI0056.PV Crude Inlet Pressure (Pass 3) psig 147.9 275.9 282.8 284.8 57PI0057.PV Crude Inlet Pressure (Pass 4) psig 147.9 286.0 294.8 293.0 57PI0058.PV Crude Inlet Pressure (Pass 5) psig 147.9 281.7 290.4 288.7 57PI0059.PV Crude Inlet Pressure (Pass 6) psig 147.9 283.8 292.4 290.2 57PI0060.PV Crude Inlet Pressure (Pass 7) psig 147.9 298.2 310.0 306.8 psig 147.9 285.7 295.3 294.1 Average Fluids Cross-over Temperatures. TAG No. SERVICE UNITS SET POINT 8/15/2009 8/16/2009 8/17/2009 Data 1 Data 2 Data 3 PROCESS 57TI0583 Crude Inlet Temperature o 542 557.2 553.8 555.3 57TI0590 Cross-over Temp. (Pass-1) o 610 585.1 581.9 583.6 57TI0591 Cross-over Temp. (Pass-2) o 610 589.7 586.9 587.9 57TI0592 Cross-over Temp. (Pass-3) o 610 592.0 589.4 590.3 57TI0593 Cross-over Temp. (Pass-4) o 610 597.1 594.2 595.8 57TI0618 Cross-over Temp. (Pass-5) o 610 594.5 591.9 593.2 57TI0619 Cross-over Temp. (Pass-6) o 610 590.9 588.4 589.7 57TI0620 Cross-over Temp. (Pass-7) o 610 594.4 591.1 593.0 610.0 590.9 588.0 589.4 AVERAGE Cross-over Temp. F F F F F F F F o F Coil Outlet Temperatures TAG No. SERVICE UNITS SET POINT 8/15/2009 8/16/2009 8/17/2009 Data 1 Data 2 Data 3 PROCESS 57TI0633 Coil Outlet Temp. (Pass 1) o 730 686.8 687.0 687.4 57TI0634 Coil Outlet Temp. (Pass 2) o 730 678.6 678.3 677.5 57TI0635 Coil Outlet Temp. (Pass 3) o 730 680.2 680.6 679.0 57TI0636 Coil Outlet Temp. (Pass 4) o 730 678.5 678.6 679.9 57TI0629 Coil Outlet Temp. (Pass 5) o 730 683.4 683.5 683.7 57TI0630 Coil Outlet Temp. (Pass 6) o 730 670.1 670.0 670.9 57TI0631 Coil Outlet Temp. (Pass 7) o 730 683.0 682.2 683.3 730.0 679.9 679.9 680.1 AVERAGE Coil Outlet Temp. F F F F F F F o F Heater Performance Index. Remarks Operating- Data 1 Operating- Data 2 Operating- Data 3 Operating- Data 4 Operating- Data 5 Operating- Data 6 Operating- Data 7 Design CLEAN Design FOULED Metallurgical Limit RADIANT COIL TUBE METAL TEMP. CRUDE HEATER 537-F-001 Temperature, Deg F 1200.00 1100.00 1000.00 900.00 800.00 700.00 PASS1 PASS2 PASS3 PASS4 PASS 5 PASS 6 PASS 7 PASS 8 Heater Performance Index. Remarks THERMAL EFFICIENCY CRUDE HEATER 537-F-001 90.60 Thermal Efficiency, (%) 90.40 90.32 90.25 90.20 90.00 89.73 89.80 89.57 89.56 89.60 89.69 89.35 89.40 89.26 89.20 89.00 88.80 88.60 Design Data 1 Data 2 Data 3 Data 4 Data 5 Data 6 Data 7 Heater Performance Index Oxygen & Draft Control System (Natural Draft Heater) Draft Control System Stack dampers • • • • Reliable Correctly sized Pneumatically operated Opposed blades Reliable Dampers Opposed blades vs. Parallel Blades Excess O2 Control • Control air supply to burners • Pneumatically operated dampers or registers • Provide proper control scheme • Damper opening is provided based on ▫ Draft ▫ Excess O2 ▫ Firing rate ▫ Other parameters • Savings realized through out the day Summary • Manual controls are not adequate • Energy prices are high • Advanced Controls possible • Use DCS based or PLC based • Provide adequate safe guards • Intelligent analysis of heater parameters • Substantial savings can be realized • Payout will be less than a year in most cases Thank you very much • Questions and comments are welcome