You are currently viewing: Q&A
Number: 262
Display:
We have a black sludge formation at the interphase of naphtha and water in OVHD accumulator. But all the OVHD paramters like pH, Iron and Chloride are normal. The crude unit has a partail condensation ovhd system and the black sludge is observed in the second boot (Cold reflux boot). There is a CI dosing in the accumulator upstream. What could be the reason for this sludge?
Replies: 1
Can we add valave Before Flash zone in CDU, to use it when we have a maintenance on the heater without the need to empty the tower?
Regional shifts in higher refinery capacity seem to correspond with the need for more intensive water treatment programmes involving wastewater recycle processes while protecting heat exchangers and linked assets from fouling and corrosion. At what level of investment have you seen refinery operators commit to plant water quality while reducing its consumption?
Can high-grade needle coke (such as P66 or Seadrift) be used for synthetic graphite in EV battery anode materials? If the quality exceeds specifications and needs to be downgraded, is it easy to modify the needle coke manufacturing process? Or, is it easy to source lower-grade decant oil?
Replies: 2
For a residue hydrotreater, feedstock about 360C+, what would be accaptable values for TI (toluene Insoluble) following ASTM D 4072? We encounter often pressure drop issues in the first reactor and we would like to sample the feed mix for TI. But there is no guideline what is acceptable and what is too much. Any idea?
Why does NiMo catalyst has more hydrogenation potential than CoMo? What nature of it is enabling it to do so?
Why does Nitrogen molecules in hydrotreating units takes the path of hydrogenation followed by hydrogenolysis instead of direct hydrogenolysis unlike sulphur molecules which gets hydrogenolysis directly?
Between CoMo and NiMo, Which catalyst has more deactivation rate and why?
What are the ways or methods to ensure that sulphiding of the Diesel and VGO hydrotreater units catalyst is completed? What are the check points?
1. Is it purely by injecting the stoichiometric required DMDS into the reactor that decides sulphiding is completed?
2. Is there any thumb rule for quantity of dmds that needs to be dosed during first stage of sulphiding at 220degC or quantity of dmds that needs to be injected for second stage of sulphiding at 330degC?
Please share any references which provides the guidelines regarding process variable alarm value for H HH L LL specifically to pressure and temperature.
At DHT RX Eff/ Separator Liquid exchange train got leaked once and we plan to install pressure transmitter on sep liquid side to detect any leakage.
We have low PH (3 to 4) in the CDU overhead but in same time we have low chloride values ( 3 to 10 ) and already we injected high values of neutralizing amine and corrosion inhibiter. What is the reason that causes this drop in PH value?
Replies: 8
How can I know there is weak acids in crude oil and what's the effect of weak acid on the overhead conditions in the crude distillation unit?
Replies: 6
What are some of the most effective compressor performance strategies for improving the mean time between failure (MTBF)?
What heat exchanger fouling prediction frameworks do you see benefiting refinery and petrochemical operations?
Replies: 3
With global hydrocracking unit capacity and feedstock diversity increasing, what strategies are available to prevent reactor runaway and increase overall unit safety?
Replies: 5
What optimal hydrocracking catalysts and operating strategies are needed to co-hydroprocess waste oils with VGO?
What are the optimal routes to valorisation of olefins-rich FCC unit and coker unit off-gas?
How to confirm the run away reactions in Diesel and Vaccum Gas Oil hydrotreater units reactors? Is it localized phenomena at particular location or gets spread on wide area of the catalyst?
As the 1st bed hydrotreater bed exotherm for our unit already stays at above 40degC during normal operation, I would like to understand how to confirm the run away phenomenon and take necessary actions like actuation of EDPS. Kindly guide.
In Diesel and VGO hydrotreaters, after feed pump failure, feed introduction is advised to be done within 15minutes, in case feed introduction is not done in 15minutes, it is advised to take normal shutdown by cooling of the reactor. What's wrong in feed introduction after 15minutes at high temperature?
Diesel hydrotreater feed introduction to Reactor is designed to be done at 180 to 200 DegC. Is there any issue, if feed introduction is done at 240degC or 260degC during Normal startup (Assuming HP Loop contains above Minimum prescribed H2S 2000 ppm).
It is well understood that the Mimium Pressurization Temperature is the temperature below which the steel is assumed to be brittle due to H2 Embrittlement in hydrotreating units.
How to understand conceptually, why beyond MPT value, H2 embrittlement is not an issue or reactor is not suspectible to loss of ductility, eventhough pressure after MPT value will be higher than before. Can someone please guide me?
What measures or techniques do you employ to optimise the cooling of coke bed in drum and mitigate the occurrence of hot-spots? If you are performing pressurised quenching, what specific pressure levels do you maintain within the drum during the initial water quench ramp?
Replies: 0
What is the basis for maintaining minimum wetting rates in vacuum column (whether based on vacuum charge or design condition?) What will happen if minimum wetting rates are not adhering to?
What is the impact in the product quality if circulating refluxes return temperatures are not maintaining at design temperatures? Is it wise to reduce heat recovery in pre heat network for maintaining design pump around return temp at the expense of pre heat?
What is the expected volumetric efficiency in the diesel product treating only SRGO? (It is understood that it is less than 103.4% due to the decrease in the content of aromatics and olefins)
What is the best solvent to be used in a carbon capture train of syngas placed between the HTS and PSA unit?
We have loaded the catalyst (IP- 632) of our Isomerization Unit. So, what procedures must be taken before Startup? And what are the most important instructions to be followed?
How can I know the water mole fraction in the overhead stream in the CDU? I need it to know the optimum temperature of the top reflexes.
For a desalter system with low performance, we made an RCA that revealed multiple issues to the desalter hardware, including that the equipment is undersized and electro-coalescne not happening, while grid is still ON. Could anybody advise equipment retrofitters to shift the existing desalter almost electrodynamic type to low velocity type ?
I would like to learn about the usage of Pyrolysis oil produced from Ethylene Cracker in the Delayed Coker Unit. I would like to use this pyrolysis oil which is around 2.5 wt% of total feed as a feed in the Delayed Coker Unit. Do you know any applications like this? If it is, have you encountered any issue to process pyrolysis oil to the coker unit?
In addition, what if I use this pyrolysis oil as wash oil stream in the coker fractionator column instead of using as a feed? Do you know any applications or example?
Replies: 4
Is CCR value directly linked with asphaltene content? In hyrocracker feed specification why limit is fixed for both CCR and Asphaltene content? Why both parameters are measured separately?
How to resolve high differential pressure issue in FCC amine absorber?
Is there some way of reversing silicon poisoning in our hydrotreating catalyst?
Please share an article on processing of used engine oil distillate through Hydroprocessing. How long the catalyst lasts? Do we need to put metal trap separtely?
In our Hydrogen plant designed by KT, we have 2 steam drums and during every start up, we face severe hammering in both steam drums intially. I worked before in other Hydrogen plants and have never experienced such hammering?
I am in Hydrotreater, I want to know how much stripping steam is required in stripper, during startup we use excess steam in stripper to achieve diesel doctor test negative, is it beneficial or adversely affect steam stripping?
We are experiencing frequent amine carry-over from our high pressure amine absorber. What are the possible causes and solutions?
In catalytic reforming Process: - increasing the initial boiling point leads to increasing in hydrogen production. Any Explanation ? - How can we increase the purity of the hydrogen (recycle gas) ? - What is the maximum allowable moisture (ppm) in the feed (Heavy Naphtha) ?
Can we use biofeedstocks without co-processing them with conventional crudes to produce drop-in fuels?
Unloading contractor encountered fire due to vacuum unloading of HDS reactor. Unloading a fixed bed hydrotreater reactor is classically done under Nitrogen atmosphere in order to avoid any fire due to deposit FeS. And FeS in nearly inavoidable in older units due to corrosion in the upstream equipment. Normally avoiding any fire is ensured by putting the reactor and the unloading nozzles until the drum dedicated to the unloaded catalyst under N2. Sometimes it is necessary to unload the reactor from the top by vacuum (e.g. sampling of spent catalyst is needed, or there are baskets on the distributor tray).
In that case, how the unloading company can avoid that the catalyst comes in contact with air? Can their vacuum facility be operated under N2?