What a careless mistake on my part! The hydrogen must dissolve in the liquid phase to convert the vacuum residue; it makes sense to me now.
But doesn’t this mean that the unconverted H2 ends up in the top stream from the flash separator? The compositions in the table would correspond to the...
It makes sense to me expressing the makeup in terms of the recycle stream but not for the purge stream.
Shouldnt the Molar H2 makeup to the reactor=Molar H2 in top stream from the the flash separator + Molar H2 in Purge + H2 Consumed
Molar H2 Feed=Molar H2 Make up+ Molar H2 Recycle
Molar H2...
The problem states that the non-H₂ components cannot be removed as liquid-phase products from the flash separation unit. Therefore, 1.0779 kmol of non-H₂ components produced during hydroconversion will end up in the gaseous stream. This gaseous stream is split into a low-pressure purge and...
But If the partial pressure of H2 in the recycle stream is 8 MPa I think the total system pressure would not be 10 MPa. According to Daltons law
Partial pressure of H2=Mole fraction of H2*Total pressure in the system
8=0.9725*Total pressure in the system
Total pressure in the...
How can I deduce that from the problem givens? I think the 1000 m³ of H₂/m³ of residue feed is referring to the rate of the feed to the ebullated reactor. This was the solution posted for the problem. However, I am not sure how the mole fraction of H₂ in the recycle stream is 0.8 when the...
Unfortunately, no flow diagram is provided in the problem. I would imagine a simplified diagram of the process to look like the image below. I used 1030 kg as the basis because the questions are asking for the purge and fresh rates per m³ of residue feed, which is equivalent to 1030 kg. However...
1.1) 1 m3 of residue feed has a mass of 1030 kg.
Mass of H2 consumed=(1.27 kg of H2 consumed/100 kg of residue feed)*1030 kg of residue feed=13.081 kg
We can treat H2 as an ideal gas to calculate its volume at normal conditions
101325*V=(13.081/2.016)*1000*8.3145*273.15
V=145.436 m3 normal/m3...
Storage tank leaks are caused by the failure of the pressure relief valve, tank body, or tank piping.
If the pressure relief valve fails, can't it contribute to tank body and/or piping failure from overpressure? But the tank body and tank piping can fail by other mechanisms (mechanical...
I have collected data on crude oil incidents from the CONCAWE cross country European oil pipeline. The database includes incidents for 3 types of service: crude, refined products, and heated black products (hot oil) over 1971-2021. However, I have used the data from 2001-2002 because as this...
After researching for the past few days, I found that internal corrosion is one of the leading types of pipeline failure. I read that crude oil is not corrosive by itself, but crude oil contains water and sediments limited to <0.5 % wt, and the solid particles tend to be encapsulated by a layer...
I tried searching for risk assessments on the US Department of Transportation site, and I found a document on how to perform pipeline risk modeling. I will definitely use it in my report. However, I forgot to clarify that I am using data from a paper that developed a methodology for performing...
Currently, I am working on a project that necessitates a quantitative risk assessment (frequency analysis and consequence analysis) of buried crude oil pipelines, considering specific hazard scenarios.
Most of the hazard analyses I have come across were conducted on gas pipelines, and there...
Are the concentration and temperature axial derivatives not equal to zero because the composition of A is changing due to the homogeneous reaction?
Will Rs be given by the following formula?
Yes. If we now consider a heterogeneous reaction, the mole and energy balance equations remain the same.
$$ C_{A}(r,0)=C_{A_{0}}; T_{f}(r,0)=T_{0}=T_{s}(r,0)\hspace{0.2cm} \text{at z=0} $$
$$ \frac{\partial C_{A} }{\partial z}=\frac{\partial T_{f} }{\partial z}=\frac{\partial T_{s} }{\partial...
My attempt:
Species fluid and solid phase balances for a tubular reactor in which there is a homogeneous first order reaction and a heterogeneous reaction on the external surface of non-porous catalyst coated along the reactor wall.
Mole balance equation for the fluid phase
The heterogeneous...