Recent content by Chestermiller

The hard part of attacking physical is to articulate in words the physical mechanisms involved and translate these into a set of equations. Solving the equation(s) is supposed to be a gimme.

Are you saying that you don't know how to solve this linear first order ordinary differential equation and that you want. us to solve it for you?

It goes like this: $$MC_p\frac{dT}{dt}=-kS(T-20)$$The initial temperature is 1500 C and, apparently, your final temperature is supposed to be 40C.

In thess equations, the 0.9724 should be 0.8

If you person on the free surface with a spoon, the system will no longer be in equilibrium, and the spoon will begin descending into the fluid. The fluid at the surface of the spoon will be moving at the spoon velocity, while the fluid further away will be moving more slowly, and the fluid at...

I don't think so. I think that the makeup is equal to the converted H2 in the bottom liquid product plus the H2 in the purge stream. I don't thnk so. The H2 from the separator is equal to the H2 in the recycle plus the H2 in the Purge. The H2 makeup should be the the H2 leaving in the purge...

Copper tubing has substantial bending stiffness, which is not present in a thin rope or wire.

After further thought, here's my tae on this: Let M = molar makeup H2 feed to reactor/m^3 residue feed Let R = molar recycle feed to reactor/m^3 residue feed Let P = molar purge rate /m^3 residue feed Then $$M=\frac{13.081}{2.016}+0.8P$$ $$M+0.8R=44.615$$ Does this make sense to you?

The problem statement, in my judgment, is not precise enough to allow unambiguous solution.

The mole fraction of H2 in the recycle is not 0.9725.

what are your thoughts so far?

I'm finally understanding the problem statement better. The basis of the calculation is 1 m^3 of residue stream. Ir seems to me everything you've shown in the calculations so far makes sense.

The composition of the recycle steam is exactly the same as the purgee stream. If the partial pressure of H2 is 8 MPa and the total pressure in the system is 10 MPa, the mole fraction of H2 is 0.8.

Maybe that mole ratio is in the feed to the reactor

Can you please provide a flow diagram? You chose as a basis for the calculation 1030 kg residual feed, and you calculated a H2 consumption of 6.49 moles. If the H2 to residue feed ratio is 1000 m^3/m^3, that is a mole ratio of 1000. These two results don't seem consistent to me. What am I...