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Last 10 active questions:


Question No : 5913  Date Posted :8/11/2017 View detailsView details and responses  
Category : Refining Operations Submit a responseSubmit a response  
  Subject : UOP395
  Can anyone please tell me how Colorimetry performs for Total Chloride in Petroleum Distillates?

How effective is it?

Can we test light naphtha and heavy naphtha?

Number of responses: 1


Question No : 5912  Date Posted :8/7/2017 View detailsView details and responses  
Category : Refining Operations Submit a responseSubmit a response  
  Subject : Fluoride in Naphtha
  Can anyone tell me the qualitative test for fluoride content in Naphtha or even Quantitative without ASTM D7359. CIC equipment? It is an urgent requirement before startup of PENEX.
Number of responses: 1


Question No : 5911  Date Posted :7/30/2017 View detailsView details and responses  
Category : Refining Operations Submit a responseSubmit a response  
  Subject : Hydrocracker Dump Valves operation
  In CLG technology, on activation of EDPS (dump valves), feed pumps will not trip. Rather, it is used as a cooling agent to the reactor.

When it comes to UOP operation feed pump will trip to avoid catalyst damage. What causes this trip in UOP? What causes CLG to recommend not stopping the pump?

Number of responses: 0


Question No : 5910  Date Posted :7/28/2017 View detailsView details and responses  
Category : Refining Submit a responseSubmit a response  
  Subject : Gasoline antioxidant interference mercaptan measurement
  RCCG, one of our gasoline blend components from RFCC unit, after sweetening process for removing Mercaptan, we inject antioxidant (N, N'-Di-Sec-Butyl-P-Phenyldiamine) before the storage tank.

Mercaptan is 4ppmw before injecting antioxidant, but Mercaptan rises to 20 ppmw after injection. The method for Mercaptan measurement is ASTM D3227.

Q1. Did anyone ever faces such problem?
Q2. How to solve this problem?

Number of responses: 2


Question No : 5909  Date Posted :7/26/2017 View detailsView details and responses  
Category : Refining Submit a responseSubmit a response  
  Subject : Desalter transformer
  What is the reason for no increase in secondary voltage of desalter transformer?
Number of responses: 1


Question No : 5908  Date Posted :7/25/2017 View detailsView details and responses  
Category : Refining Operations Submit a responseSubmit a response  
  Subject :
  "Sand-type" coke morphology:
Typically, we process high asphaltenes, high-MCR vacuum residues in our Delayed Coker, that produce a shot-coke morphology.

But in one of our Delayed Coker Units we have recently changed feedstock quality, to light (low-MCR, low asphaltenes). This light VR is producing a transition coke (asphaltenes/MCR ratio about 0.6) with low particle size (less than 1 mm), quite loose, that looks like "sand". This coke give us a lot of problems during coking cycle: high level alert that is not consistent with coke yield and drum filling (it seems as coke "floats" or is withdrawn with coking vapors) and more severe problems during decoking cycle: problems during cooling (high level measurement, it seems as coke "floats" in water), difficulties in cooling (more time required, it seems as coke release more heat that usually), plugging problems in drainage line and bed collapse during coke cutting.

For sure, the coke bed formed is very loose, not compact and "mobile".

We suspect that it is due to:
1) Excessive velocity in the coke drum (due to higher gas production);
2) Light feedstock require more time in order to obtain a compact coke.

How can we improve the coke morphology to avoid this problem? Which should be the changes in operating conditions to avoid these problems?

Number of responses: 0


Question No : 5907  Date Posted :7/24/2017 View detailsView details and responses  
Category : Refining Submit a responseSubmit a response  
  Subject : Request for Technical Assistance - Defining the Land required for Grass Root Refinery
  I am trying to find an expert opinion guiding me to estimate the adequate size of land to establish the below refinery project, I appreciate providing me any valuable information you have in this regard.

Planned barrels processed- 60,000+/day, 3 million +/year
Type of Refinery project: Grass Root/Green Field; built from scratch
Refinery Complexity: medium conversion.
Oil Supply- light sweet/medium sweet crude from GCC area.
Planned output- to be checked
Refinery Location: East Africa
Primary Target Markets: East Africa
Secondary/future Target Market- Neighbours in Africa.
Construction Employment- 1400+ construction jobs.
Construction period: 3 to 4 Years.
Operation/Permanent Employment: around 1,000 persons.

Number of responses: 0


Question No : 5906  Date Posted :7/19/2017 View detailsView details and responses  
Category : Refining Operations Submit a responseSubmit a response  
  Subject : High TAN Crude Processing
  Good Day all, I am new to this site. To introduce myself, I am a chemical engineer with 10 years experience. I work for a Petronas company in downstream refining in South Africa. I am a crude distillation engineer.

I would like to know if anyone has had experience in crude processing with Higher TAN crudes such as USAN (West African). Typically, are there any challenges with USAN blended with Arab Light crudes in terms of overheads corrosion, desalter operation or boot water pH etc.

This is just for information as I am currently processing a higher TAN crude as a test run - USAN crude specifically.

Number of responses: 2


Question No : 5905  Date Posted :7/14/2017 View detailsView details and responses  
Category : Other Submit a responseSubmit a response  
  Subject : Nitrogen mixing with water
  I was doing a very basic simulation:

Mixing 25000 Nm3/hr Nitrogen with 7 kmol/hr of liquid water at 6 barg and 40 DegC in PROII. The results are a bit confusing:

Mixed stream temperature dropped to 30 DegC and most of the water got evaporated (only 0.01 mol% water left in liquid phase). Can anyone explain this to me?

Number of responses: 0


Question No : 5904  Date Posted :7/3/2017 View detailsView details and responses  
Category : Refining Submit a responseSubmit a response  
  Subject : Kerosene Hydrotreaters
  What is the typical EOR operating temperature for kerosene stream? Can there be RSH recombination at EOR, if the unit is processing SR kerosene and targeting 8 wpm Sulfur in the stream?
Number of responses: 2


 


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