1. Project Work Week 2 Terry A. Ring Chemical Engineering

2. Project Schedule

3. Progress Report Memo Introduction Body Give and Report on the Old Gantt Chart State past progress and list what has been finished Discuss the progress since the last progress report. Explain any overdue problems Why they occurred Implication on project Efforts you will use to overcome problems Conclusion Give prognosis for total project

4. Progress Report Ghantt Chart Activity 15 Jan. 2003 15 July 2003 15 Dec. 2003 15 Jan. 2004 15 Feb. 2004 15 March 2004 15 April 2004 Set up envelopes for various expenses x Adjust investment portfolioxxxx Collect all Expenses x Purchase Tax Software x Collect W2, Capital Gains, 1099, K-1 (partnership) forms xx Compile expenses x Use tax software to fill in forms xx Pay IRA’s, self-employed pension plan x Check tax forms, Pay tax due and file tax forms x

5. AIChE Contest Problem Price of Chemical from Lab Supply company 100 gm at $100 = $1,000/kg What should be the price when I buy in bulk Typically a 100% markup for the lab supply industry $500/kg

6. Methanol Process Purge 500 psia T=? T=250C P=? T=?

7. Purge on Loop Design Spec Failure Some feed is leaving with the liquid Set design spec with Purge + liquid loss at HP flash = feed

8. Reactor Impurities Dimethyl ether Methyl formate Butanol Easiest way Add a side stream after reactor with a flow of each of these chemicals after you have determined the flow of methanol out of the reactor More complicated way but a bit more rigorous Add a RStoic reactor with 3 reactions Set a design specification on reaction conversion to get the amount of impurity needed 2CO + 4 H 2  C 2 H 6 O + H 2 O (dimethyl ether) 0.00024 lb/lb methanol 2CO + 2H 2  CH 3 OCOH(methyl formate) 0.0012 lb/lb methanol 4CO + 8H 2  C 4 H 9 OH + 3 H 2 O(butanol)0.00026 lb/lb methanol

9. Reactors Size of Reactor Very Long Large number of tubes Break up reactor into sizes that makes sense Put reactors in Series or Parallel All reactors are plug flow so you can break these up as you like

10. Turbine in place of Valve Turbines in Aspen are typically used to generate work for Gas Systems Gas Turbine You may get some errors if you us a turbine on a liquid stream Apologies to Jason McHan (and others) When we talked I mistook his stream for the gas stream when talking about adding a turbine

11. Separation System Having trouble with the complex Distillation Column #2 Hard Way – PetroFrac with extra side streams You do not need to use PetroFrac, etc with extra side streams Easy Way – Sequence of Distillation Columns You can use a sequence of distillation columns

12. Separation Problem ComponentsBP(C) CO CO2 N2 H2 CH4 H2O100C Methanol65C Dimethyl ether-24C Methyl formate32C N-Butanol117C (n) 98C (2-butanol) 83C(t-butanol) 107C(i-butanol) HP/LP Flash System

13. Distillation Sequence – Tower 1 Dimethyl ether-24C Remove in HP/LP Flash System or PC on First Tower Methyl formate32C Methanol65C H2O100C N-Butanol117C (n) 98C (2-butanol) 83C(t-butanol) 107C(i-butanol) LK HK

14. Distillation Sequence – Tower 2 Methyl formate32C Methanol65C H2O100C N-Butanol117C (n) 98C (2-butanol) 83C(t-butanol) 107C(i-butanol) HK could bet-butanol LK HK

15. Week 1 slides

16. Kinetics Problem Statement Rate in kmole/m^3/s Partial pressure in kPa Aspen Help LHHW Kinetics gives Aspen’s Required Units Rate basis = reactor volume (or kg of catalyst rate [kmole/kg/s]) Rate has units kmole/m^3/s Concentration Basis Partial Pressure has units of N/m^2 or Pa This assumes that the equilibrium constants, K i ’s, are pressure equilibrium constants, K p with units in Pa^(-n) ln(K)=A+B/T+C ln(T)+DT A=ln(K), K is K p made unitless by multiplying by Pa^n

17. Kirk-Othmer Methanol.pdf in ARTICLES section of Course Website

18. Manufacturing Process

19. Methanol Conversion Reactor – Steam Generator 500,000 Tonne/yr