Relax the assumptions regarding the split of components at the flash tank by incorporating the information below into your calculations. Using all other conditions given in Problem 13.20, reestimate the composition and flow rate of the purge stream. We have the following values at the high pressure separator (y_i/x_i):

Problem 13.20

Perform an analysis of the converter loop by determining the composition and flow rate of the purge stream using a basis of 100 kmol of feed from the MUG compressor.

a. Assume that the feed has a composition that is 3 mole% methane, 8% CO₂, 15% CO, and the remainder hydrogen.

b. Revise the feed composition to that calculated in Problem 13.12. As given in the Process Description, the molar flow rate of material to the MSR is 7.8 times the flow rate of fresh feed.

c. To simplify calculations, assume that the liquid leaving the flash drum contains no methane, CO₁, CO, or hydrogen and that the gas contains no water or methanol. The single-pass conversions of CO and CO₂ are 15% and 10%, respectively. You may be assisted in your calculations by assuming flow rates of components in the recycle stream mixed with fresh synthesis gas entering the converter loop. In this approach the recycle stream is known as a tear stream, and an iterative solution will be required to determine the requested values. Such calculations are easily performed using a simulation program of the type described in Chapter 10, or you may write your own program or spreadsheet to obtain the desired results. If you develop a spreadsheet to perform the calculations, direct substitution of calculated values of component flow rates in the tear stream for new estimates may suffice. (This is the method of successive substitution described in Appendix A.2.)

Problem 13.12

As covered in the Process Description, there are three primary reactions that occur in the MSR. These are given by Equations 13.3, 13.4, and 13.5. However, determination of chemical equilibrium among the species H₂, CO, CO₂, H₂O, and CH₃OH involves only two of the three reactions because each reaction is a linear combination of the other two. Cherednichenko gives an approximation for the equilibrium relationships in Equation 13.3 (see Problem 13.13) and in Equation 13.5:

The equilibrium Ka_13.5 constant is defined by the relationship

Where T is in kelvin and K_ϕ13.5 accounts for nonideal behavior of the gas phase.

Transcribed Image Text:

Component CH4 CO2 CO H2 H2O CH3OH K 29.8 5.12 39.9 86.3 2.85 X 10-3 6.80 X 10-3