where we go wrong in distillation towers l.
Download
Skip this Video
Loading SlideShow in 5 Seconds..
Where We Go Wrong In Distillation Towers PowerPoint Presentation
Download Presentation
Where We Go Wrong In Distillation Towers

Loading in 2 Seconds...

play fullscreen
1 / 29

Where We Go Wrong In Distillation Towers - PowerPoint PPT Presentation


  • 309 Views
  • Uploaded on

Where We Go Wrong In Distillation Towers. Dick Hawrelak Presented to ES317Y in 1999 at UWO. Introduction. 3% of large property damage losses are caused by failures in process towers. Average Trended Loss was $53.8MM, the largest of all unit operations. Distillation Tower Problems.

loader
I am the owner, or an agent authorized to act on behalf of the owner, of the copyrighted work described.
capcha
Download Presentation

PowerPoint Slideshow about 'Where We Go Wrong In Distillation Towers' - reynold


An Image/Link below is provided (as is) to download presentation

Download Policy: Content on the Website is provided to you AS IS for your information and personal use and may not be sold / licensed / shared on other websites without getting consent from its author.While downloading, if for some reason you are not able to download a presentation, the publisher may have deleted the file from their server.


- - - - - - - - - - - - - - - - - - - - - - - - - - E N D - - - - - - - - - - - - - - - - - - - - - - - - - -
Presentation Transcript
where we go wrong in distillation towers

Where We Go Wrong In Distillation Towers

Dick Hawrelak

Presented to ES317Y in 1999 at UWO

introduction
Introduction
  • 3% of large property damage losses are caused by failures in process towers.
  • Average Trended Loss was $53.8MM, the largest of all unit operations.
distillation tower problems
Distillation Tower Problems
  • The following list of problems have been drawn from my personal experience as a design engineer with Dow Chemical for 33 years (1960 - 1993).
poor mass balances
Poor Mass Balances
  • Normal mass balance.
  • Start-up, shut down or upset.
  • Re-run of off-spec material.
tower variables
Tower Variables
  • Poor understanding of tower variables, reflux, downcomers, reboilers, condensers.
  • VLE data can be confusing and misleading during design.
  • Tower configuration not the best - Seadrift tower explosion kills one operator.
tower controls
Tower Controls
  • Process controls not adequate for upset conditions.
  • Often dual level controls are required on bottoms of towers.
reboilers
Reboilers
  • Poor reboiler selection.
  • High rate of fouling due to high steam temperatures.
  • Reboiler stall due to loss of level in tower - Seadrift tower explosion.
  • Reboiler lines too small and choke recirculation.
condensers
Condensers
  • Pressure drops higher than design due to fouling.
  • Hydrates form and plug condenser.
  • Entrainment from tower not considered in design.
  • Inerts blanket condenser, failure to remove heat cause PSVs to blow.
mechanical design of tall towers
Mechanical Design of Tall Towers
  • Tower shell thickness not suitable to prevent sway in high winds, tower topples.
impurities in tower feed
Impurities In Tower Feed
  • Impurities not considered in design, exothermic reaction destroys tower - Seadrift
flammable inventory
Flammable Inventory
  • Designers specify excessive inventory in reflux drum when tower logistics not well understood.
  • Large bottoms inventory may promote formation of unwanted polymerization products.
tower operation at low rates
Tower Operation at Low Rates
  • Ballast tray units experience high rate of wear due to low unit reference. Broken valves plug downcomers or end up in pump suction causing further upsets.
vacuum operation
Vacuum Operation
  • Designers too optimistic about air leakage. Vacuum pump or steam jets too small to pull required vacuum.
  • Poor management of pressure drop.
recessed sumps on trays
Recessed Sumps On Trays
  • Vendors often specify recessed sumps to save 6 inches on tower diameter.
  • Recessed sumps are perfect traps to collect solids and plug downcomers.
packed towers
Packed Towers
  • Poor vapor and liquid distribution affects HETP. Dow wins $3MM lawsuit.
  • Vendors predict high HETP over wide range of flow. Customers beware.
  • Poor rangeability in packed tower operation.
data collection
Data Collection
  • Grab samples not suitable to check tower performance.
  • Require sample range over 24 hour period.
  • Troubleshooting difficult because of poor instrumentation.
tower internals
Tower Internals
  • Flashing tower feeds not considered in feed tray design.
  • Feed distributors do not work.
  • Demisters often required but are ignored.
  • Vortex breakers omitted in tower bottoms.
tower optimization
Tower Optimization
  • Select a process sequence.
  • Mass balances to match product specs.
  • Thermal condition of the feed.
  • Minimum reflux ratio.
  • Minimum no. of trays.
  • No. trays versus reflux ratio.
optimization cont d
Optimization Cont’d
  • Feed tray location.
  • Tray efficiency.
  • Valve tray tower design.
  • Select tower internals.
  • Repeat optimization for a packed tower.
previous exam problem
Previous Exam Problem
  • The students were presented a paper on Union Carbide’s Seadrift, Texas, EO tower explosion. They were asked to comment on the explosion with respect to what they had learned in this safety course.
other possible exam questions
Other Possible Exam Questions
  • Why do designers often specify abnormally large flammable inventory in the reflux drum?
  • Why should the designer minimize the reboiler steam temperature in a flammable distillation tower?
  • What are the main problems with packed towers?
summary
Summary
  • This short list is indicative of some of the problems caused by poor engineering discipline in distillation tower design.
  • Recommend you obtain a copy of the Chemical Plant Design programs and follow the procedures built into the spreadsheets.