Fresh Air Firing
Fresh Air Firing
Often fresh air firing is resorted to generate steam when the gas turbine is not in operation. However, it should be noted that using ambient air for generating steam in an HRSG is not an efficient process and must be used sparingly or for emergency reasons only and not for continuous operation. It must be clearly understood that in HRSGs, the ratio of gas flow to steam is much larger than in conventional steam generators. Hence, a large amount of energy is wasted by raising the temperature of air from ambient conditions and exhausting the gas at a higher temperature at the stack. One may wonder that we do the same thing in
a steam generator. However, keep in mind that the ratio of flue gas to steam is about 1.1 in a steam generator, while in an HRSG, it will be in the range of 6–8, and so a large amount of exhaust gas is heated from ambient conditions relative to steam generation and then vented to the atmosphere. The sizing of the HRSG should be such that the exhaust gas flow in fresh air mode also should be in the same range as the exhaust gas flow with gas turbine opera- tion or else the gas velocities can be much lower causing nonuniformities in gas flow at the heat transfer surfaces and poor heat transfer. It can be slightly lower than the turbine exhaust gas flow say by 10%–20% but not much lower. The following examples give an idea of the performance in fresh air mode with two different air flows, and one can see the issues here.
Example 5.13
The HRSG in Example 5.1 is to be operated in fresh air mode. Check the performance when 100,000 kg/h of air and 80,000 kg/h of air are used to generate 12,000 kg/h.
The results for both the cases are presented in Figure 5.16a and b. It can be seen that the efficiency is higher when the air flow is lower and vice versa. However, the firing temperature increases with lower air flow. If the HRSG had been designed to accept higher firing temperatures, then we can further lower the air flow and generate the same amount of steam more efficiently. However, we cannot reduce the air flow too much due to gas maldistribution concerns. When sizing the fan, about 80% of the turbine exhaust flow should be adequate. While locating the fan and duct, one should ensure that the flow nonuniformity is minimized as the fan is generally located at right angles to the main duct or at an angle. Grid plates with variable openings may be inserted in the duct,
300 Steam Generators and Waste Heat Boilers: For Process and Plant Engineers
Project—hh Units—Metric case—B Remarks - Amb. temp., °C = 25 Heat loss, % = 1 Gas temp. to HRSG C = 25 Gas flow, kg/h = 80,000
% vol CO 2 =.H 2 O = 1. N 2 = 78. O 2 = 21. SO 2 =. ASME eff., % = 69.85 tot duty, MW = 9.2 Surf.
Gas temp.
Pstm. Pinch Apprch. US Module no. in/out °C
Wat./Stm. Duty
Pres. Flow
°C kcal/h °C Burn 25 551
in/out °C
MW kg/cm 2 a kg/h
Stack gas flow = 80,932 % CO 2 = 2.05 H 2 O = 5.02 N 2 = 76.41 O 2 = 16.49 SO 2 =.
Fuel gas: vol % Methane = 97 ethane = 3
LHV - kcal/cv m = 11 LHV - kcal/kg = 6,623 aug air - kg/h = 0
Sh. Evap. Eco. Project—hh Units—Metric case—B Remarks -
Amb. temp., °C = 25 Heat loss, % = 1 Gas temp. to HRSG C = 25 Gas flow, kg/h = 100,000 % vol CO 2 =.H 2 O = 1. N 2 = 78. O 2 = 21. SO 2 =. ASME eff., % = 62.9 tot duty, MW = 9.
Surf. Gas temp.
Pstm. Pinch Apprch. US Module no. in/out °C
Wat./Stm. Duty
Pres.
Flow
°C kcal/h °C Burn 25 486
in/out °C
MW kg/cm 2 a kg/h
Stack gas flow = 101,016 % CO 2 = 1.79 H 2 O = 4.52 N 2 = 76.61 O 2 = 17.06 SO 2 =.
Fuel gas: vol % Methane = 97 Ethane = 3 LHV - kcal/cv m = 105 LHV - kcal/kg = 11,922 aug air - kg/h = 0
FIGURE 5.16
Fresh air firing cases with 80k and 100k kg/h air flow.
and by measurement of static pressure, one can get an idea of the velocity profile across the cross section at the burner. The profile should also be checked for turbine exhaust gas. The velocity profile cannot be optimized for both turbine exhaust and fresh air as the flow directions are at nearly 90° to each other. Some compromise must be accepted depending on how often fresh air firing is used. More on fresh air firing is discussed in Chapter 4.
Parts
» For Process and Plant Engineers
» A Few Typical Solved Problems
» Excess Air from Flue Gas Analysis
» Simplified Combustion Calculations
» Relating Oxygen and Energy Input in Turbine Exhaust Gases
» Evaluating Fuel Quantity Required to Raise Turbine Exhaust Gas Temperature
» Simplified Formulae for Boiler Efficiency
» Firing Fuels with Low Heating Values
» Boiler duty and efficiency calculations
» Acid Dew Point Temperature T dp
» Steam Generator Furnace Design
» Advantages of Water-Cooled Furnaces
» Furnace Exit Gas Temperature Evaluation
» Empirical Formula for Furnace Duty Estimation
» Distribution of Radiation to Tube Banks
» External Radiation to Heat Transfer Surfaces at Furnace Exit
» Correlations for CHF (Critical Heat Flux) and Allowable Steam Quality
» Guidelines for Good Circulation System Design
» Emissions Affect Steam Generator Designs
» Adding Condensate Heater to Improve Boiler Plant Efficiency
» Understanding Boiler Surface Areas
» Steam Generators for Oil Sands Application
» Radiant versus Convective Superheaters
» Steam Inlet and Exit Nozzle Location
» Case Study of a Superheater with Tube Failure Problems
» Problem at Low Loads with Inverted-Loop Superheaters
» Data Required for Performing Steam Generator Analysis
» Evaluating Part Load Performance
» Tube Wall Temperature Estimation at Economizer Inlet
» Methods to Minimize Low-Temperature Corrosion Problems
» Water Chemistry, Carryover, Steam Purity
» Sizing and Performance Calculations
» Flue Gas Composition and Gas Pressure
» Heat Recovery in Sulfur Plants
» Heat Recovery in Sulfuric Acid Plant
» Heat Recovery in Hydrogen Plants
» Combining Solar Energy with Heat Recovery Systems
» Natural versus Forced Circulation HRSGs
» Optimizing Pinch and Approach Points in HRSGs
» HRSG Performance and Evaluating Field Data
» Advantages of Supplementary Firing in HRSGs
» Performance with and without Export Steam
» Cement Plant Waste Heat Recovery
» Fluid Heaters and Film Temperature
» Boiling Heat Transfer Coefficient h o
» Off-Design Performance with Addition of Economizer
» Simulation of Fire Tube Boiler Performance
» Simplified Approach to Evaluating Performance of Fire Tube Boilers
» Heat Transfer Inside and Outside Tubes
» Specifying Waste Heat Boilers
» Understanding Pinch and Approach Points
» Estimating Steam Generation and Gas–Steam Temperature Profiles
» Why Cannot We Arbitrarily Select the Pinch and Approach Points?
» Off-Design Performance Evaluation
» Single- or Multiple-Pressure HRSG
» Cogeneration Plant Application
» Water Dew Point of Flue Gases
» Condensation Heat Transfer Calculations
» Condensation over Finned Tubes
» Drum Coil Heater: Bath Heater Sizing
» Checking Heat Transfer Equipment for Noise and Vibration Problems
» Steam Drum Calculations Steam Velocity in Drum
» Flow Instability in Two-Phase Circuits
» Superheater Design and Off-Design Calculation
» NTU Method of Performance Evaluation (Number of Transfer Units)
» Appendix B: Tube-Side Heat Transfer Coefficients and Pressure Drop
» Another Method of Estimating h c for Water
» Importance of Streams in Superheater, Economizer
» Simplified Procedure for Evaluating Performance of Plain Tube Bundles
» Appendix D: Nonluminous Heat Transfer Calculations
» Determination of Heat Transfer Coefficient h c Convective Heat Transfer Coefficient
» How Is Life of Superheater Affected by High Tube Wall Temperatures?
» Effect of h i on Fin Selection
» Reduce Weight of Tube Bundles Using Smaller Tubes
» Effect of Outside Fouling Factor
» Effect of Fin Thickness and Conductivity
» Why Are Fins Not Used in Gas–Gas Exchangers?
» Appendix F: Properties of Gases
» Flue Gas Mixture Properties Calculation
» Appendix G: Quiz on Boilers and HRSGs with Answers
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