We are designing a submarine pipeline to transfer heavy fuel oil from a off-shore mooring. Does anyone here has a reference chart on the viscosity of HFO no. 6 (bunker c)at various temperatures. We are aware of the temperature at offload and the related viscosity, however after pumping, and some amount of time/days passing the oil contained in the pipeline would fall to sea temperature. Sea temperature is around 27 deg C or 80 deg F
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HFO no 6 (bunker C) viscosity vs temperature
- Thread starter msamuels
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maybe this one,
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"Pumping accounts for 20% of the world’s energy used by electric motors and 25-50% of the total electrical energy usage in certain industrial facilities."-DOE statistic (Note: Make that 99% for pipeline companies)
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"Pumping accounts for 20% of the world’s energy used by electric motors and 25-50% of the total electrical energy usage in certain industrial facilities."-DOE statistic (Note: Make that 99% for pipeline companies)
Maybe this will help...
The thread 21121956 refers to makes an interesting read.
I should say that Electricpete's comments on the spreadsheet where explained in another thread.... The spreadsheet calculates the values of A and B from the input data, it does not look these values up and the input temperature may be in degC but the calculation converts to Kelvin.
The point Skogs was making about his discussions with Shell.
I think he meant that there was no equation that allowed you to find the viscosity at a temperature knowing only the viscosity at a single temperature; you need the viscosity at two temperatures to solve the Walther equation (which is the basis of the ASTM D341 calculation) but the more accurate description of temperature viscosity behaviour is in the Vogel equation.... but this is even less handy to use.
The problem for process engineers is that what they'd like to do is measure a property online at whatever conditions exist and calculate the property at a reference temperature.
You can dot his for density, for example, and many other properties, but not viscosity. It complicates process measurements no end and either you control the temperature as with the process capillary viscometers which have a temperature bath, or you are looking at multiple viscometers measuring at different temperatures.... a reasonable option when dealing with the Walther equation, you need two viscometers, but far less practicable when dealing with the Vogel equation.
So back to Skogskurra's discussion with Shell. This is kind of ironic becuase SHell produced an equation called the Shell V50 equation which was designed to produce the viscosity at 50deg C from the viscosity measured at one other temperature..... but for fuel oils. Skog's discussion was about lubes. Lubricants are complicated by the manipulation of viscosity index so you could have two oils with convergent temperature viscosity curves so that at one temperature they have the same viscosity.
With fuels oils this doesn't happen. They exhibit a vi that changes with the viscosity a 50degC in such a manner taht we can aproximate the calculation of viscosity at one temperature, based on the measurement of viscosity at another temperature, reasonably well - provided we stay within certain guidelines... this works fine for fuel oisl where the reference temperature is 50degC and the measured temperature is somewhere bewteen 40 and 60degC (e.g. on barges, in terminals) but not where the process temp is 90-130degC (e.g. in refineries).
JMW
I should say that Electricpete's comments on the spreadsheet where explained in another thread.... The spreadsheet calculates the values of A and B from the input data, it does not look these values up and the input temperature may be in degC but the calculation converts to Kelvin.
The point Skogs was making about his discussions with Shell.
I think he meant that there was no equation that allowed you to find the viscosity at a temperature knowing only the viscosity at a single temperature; you need the viscosity at two temperatures to solve the Walther equation (which is the basis of the ASTM D341 calculation) but the more accurate description of temperature viscosity behaviour is in the Vogel equation.... but this is even less handy to use.
The problem for process engineers is that what they'd like to do is measure a property online at whatever conditions exist and calculate the property at a reference temperature.
You can dot his for density, for example, and many other properties, but not viscosity. It complicates process measurements no end and either you control the temperature as with the process capillary viscometers which have a temperature bath, or you are looking at multiple viscometers measuring at different temperatures.... a reasonable option when dealing with the Walther equation, you need two viscometers, but far less practicable when dealing with the Vogel equation.
So back to Skogskurra's discussion with Shell. This is kind of ironic becuase SHell produced an equation called the Shell V50 equation which was designed to produce the viscosity at 50deg C from the viscosity measured at one other temperature..... but for fuel oils. Skog's discussion was about lubes. Lubricants are complicated by the manipulation of viscosity index so you could have two oils with convergent temperature viscosity curves so that at one temperature they have the same viscosity.
With fuels oils this doesn't happen. They exhibit a vi that changes with the viscosity a 50degC in such a manner taht we can aproximate the calculation of viscosity at one temperature, based on the measurement of viscosity at another temperature, reasonably well - provided we stay within certain guidelines... this works fine for fuel oisl where the reference temperature is 50degC and the measured temperature is somewhere bewteen 40 and 60degC (e.g. on barges, in terminals) but not where the process temp is 90-130degC (e.g. in refineries).
JMW
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