Explosion doors are required for safety reasons; it will minimize the impact of an explosion effect by allowing expansion waves going up rather than blasting everybody underneath around the heater.
Vortex meters are more accurate for wide range requirements, like the ones for heaters pass steam velocity.
As far i know, no many cokers have a feed tk; last coker i was had one as part of the unit; it was designed to allow about 24 hr recovery for, either coker or vacuum unit short trips; tk level was allowed to increase from 50 to 80% in the case of coker shutdown; or, from 50 to 20% for the case of vacuum units shutdown. The tk was provided with 2-60% capacity pumps; about 70-80% of total vacuum bottoms was directly fed to the coker and the remaining was going thru the TK via coker feed.
Regarding location, the preference should be to be closer to the coker unit as possible and letting coker to control inventory.
it is highly important providing the tk with temperature indicators to be used as cross-check for level readings; 2 radar were used, one for control and one for indication.
Could you please provide a brief description of the system and symptoms to help understanding the problem? I’d like to know if Fractionator bottom nozzle for fines removal system is of a typical vortex braker or stand-pipe? is the coke fines stream pumped back to fractionator bottom or to heaters charge pump suction? how big are your filters? are you catching any coke? has frequency being reduced? what evidences do you have for coke buildup inside the tower?
Here is a website link for information regarding two methods used for HKGO PSD: Light Scattering and Lasser Diffraction. Choice of the method depends on the matrix, the particle size, etc.
http://www.coultercounter.com
Thi is really sad news and will add to upcoming inflation due to gas and diesel higher prices.
Any information about why Valero Delaware decided keeping the Fluid Coker down for that long? it sounds like was time or getting close to general maintenance; I know the unit was having problems, but no sure if refinery was on preparation for turnaround
sir,
there is not a general answer to your questions since it depends on fouling level; for design purposes my rule is that horizontal piping equivalent lenght should not belonger than 100 ft and turns should be minimized as possible; when required for stress or piping arrangement constrainsts, then long 120 degree ells should be used and cleaning connection located to the ell closest to the 100 ft; the connection size should be min 6 inches and max 10″, and located in horizontal position and tangential to bottom of the pipe.
jesse
After working with Corrosion team, considering tracing and insulating to prevent condensation and hence avoid corrosion highly depends on the levels of CO2 or NH4HS or O2 or HCl, which are the ones may cause significant corrosion rates. For Coker gas the only component found is CO2 typically below 0.5mol%; however, using the DeWaard-Milliams curve, the predicted corrosion rate based on the CO2 Partial Pressure and temperature is relatively low, and would be reduced further, as H2S also present somewhat reduces CO2 corrosion rates. Hence, the predicted corrosivity is not great enough to justify an absolute requirement for tracing and insulation.
Yeap. There is always a chance for smoking coke conveyors due to hot coke; most of the time is just heat released or fire without flames “smoldering”, as reported by Mr. Neil to the dailybreeze reporter.
http://www.dailybreeze.com/ci_11771365
Sorry.. It was me..just forgot to sign in.
Lucky
The new coker design i’m working on would be out of single deck.
Lucky
I’m also interested in knowing about Heavy Gas Oil PSD Lab Test
Anyone out there checking HGO for particle distribution?
Lucky
I have effectively used Nalco EC 9019A , 60000 cst, which continues to be the preference for new Cokers…I keep hearing about 100,000 cst being more effective, but have not tried yet.
Consumption may vary depending unit operation; it ranges from 3-5 LBS/MBbl feed (average of 0.5 Gal/MBbl feed). I’ve heard units with high consumption reporting up to 1 Gal/Mbbl
Lucky
In my last coker AOS performed a three months cutting/quench water corrosive and erosive evaluation; findings indicated no issues with coke fines (suspended solids were below 50 wppm), but corrosion rates were high (high 45 – low 35 mpy, as measured by corrosion coupons)
Id suggest working towards getting rid-off of additional fines production; few areas to start looking include watching cutting process techniques, like cutting too fast and/or poor cutting nozzle condition. There also key operational requirements, like using 2-3 ft coke dams in front of the water drains at the end of the coke pit to improve maze efficiency by keeping fines/foam out of the maze. You may also consider watching/sampling whats coming out of your tank when draining and evaluating either frequency or how hard you dump water back to maze; of course, once your tank is full of coke, then it may be better cleaning it out before starting putting in place any new measures. One more area to look for is your heaters; either bad fighting, flame impeachment or simply poor operation due to high asphaltene feedstock, could lead to bad coke formation and/or fueling further fines generation.
None Delayed Cokers I have been deal with excessive coke fines in water nor using hydroclones; the only one Im aware using Hydroclones is for Slurry made in Flexicoker units; so, just adding hydroclones may not be the solution if the root cause has not been detected and eliminated.
Lucky
I wonder if anybody have experienced bad fouling downstream of SP3 up to Fractionator inlet?
Good news for Flexicokers…Hellenic Petroleum keeps on track
No doubt Delayed Cokers continue ahead regarding new units…surprised about Spain
I find also really sad the number of unexpected shutdowns, specially the ones catching on fire
Lucky
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