The boss has decided the (AM) option is not practical.
Sector 5 etank upgrade#
Options include: (AM) add steel mass of (kg) (DU) discontinue tank use (LP) limit fill pressure to _ (kPa) (RM) Routine maintenance (UV) upgrade valve area by _ % (OR) other suggestions. Pressure (kPa) 2010 Final Pressure (kPa) 652 (after 5 minute exposure) Final Temperature (K) 975 (after 5 minute exposure) Recommended Actions (RM) Changing the scenario to pass the safety check is not an option. Note: Debug your analysis/spreadsheet so that your results match the given results for (H2) Summary Compressed Gas Storage Tank Emergency Venting Predictions for "Worst Case Scenario" Gas Hydrogen Argon Methane Neon Oxygen H2 Ar CHE Ne O2 Meets safety limit (yes/no) YES Max.
6) HANDCHECK EXCEL for H2 & CH4 cases for the first TWO increments (0 to 10 sec.) Check each column. 5) EXCEL tabulations for Osts 300 sec with At increments of 5 seconds for H2 & CH. 4) COMPLETE GOAL PROBLEM WRITE-UP (for Hz), clearly show basic egns. Mark-up the plot and circle any failure points. > Set-up one plot for each gas including labels. 3) PLOTS of the time history for each gas show p (kPa).
shutdown plant, stop using the tanks, revise filling limits, etc. Discuss/recommend specific immediate changes to stay within the fixed (Px. SO consider options other than valve replacement. Please retype the table or "cut & paste 3) Recommendations/Conclusions/Comments: Write a few brief paragraphs with "bullet points" Is the plant safe? Which gases are safe? Which are not? Note that it will take months to order & upgrade the valves. PaAsity ) VTANK = 100 m Q = 10000 kJ/s CASE STUDY Assignment (work with 1 partner) - CHECKLIST → Turn in these items (in order) 1) Cover Sheet with a title, both of your names, current date 2) First the completed SUMMARY TABLE (below). Determine if the relief valves are adequate by using meast) TRANSIENT CONTROL VOLUME ANALYSIS and an APPROXIMATE Eevit) INCREMENTAL NUMERICAL SIMULATION to estimate tank pressure, Toas(T) temperature and mass for the 300 second interval of the worst case" conditions. However, the relief valves have not been certified for venting the other gases now stored in the tanks. 1) vent the gas at a rate sufficient to prevent the tank pressure from exceeding 3000 kPa 2) vent the gas at a rate sufficient to prevent the tank temperature from exceeding 1000 K The tanks were originally set-up to only store hydrogen gas (Hz), and the relief Tank, Valve & Tall Vent valves meet the safety specifications if the tanks are filled with hydrogen gas. The relief valves open when the pressure exceeds 2000 kPa to vent gases out the tall stacks (away from the fire) and must meet the following specifications to prevent a tank failure during the initial 5 minute (300 second) interval following the start of the fire. Emergency fire crews are expected to arrive, isolate and cool the tanks within a 5 minute response time. The fire causes a steady heat transfer rate of 10000 kJ/s to each of the tanks.
Sector 5 etank full#
Each tank has a pressure relief valve that must prevent damage during a "worst case accident", defined as the tanks being full at 2000 kPa and 300 K, when a fire occurs on the site, coupled with a simultaneous failure of the emergency sprinkler system. A single tank burst may damage/injure other tanks, critical components or personnel nearby.
The tank pipe flanges or the entire tank may burst if pressure exceeds 3000 kPa or temperature exceeds 1000 K. The tanks are normally filled to capacity at a pressure of 2000 kPa and a temperature of 300 K. The tanks store hydrogen gas (H2), oxygen gas (O2), methane gas (CH4), neon (Ne) and argon gas (Ar). A chemical plant has eight identical spherical high-pressure gas storage tanks, each fabricated of 6666 kg of stainless steel with identical pressure relief valves and tall vent stacks. Transcribed image text: MET MTANK ME212 Chp 4 Case Study Problem: Transient Tank Venting (effect of changing gas composition) Consider the safety of the following situation.