1. Institutt for kjemisk prosessteknologi, NTNU
Professor De Chen
Institutt for kjemisk prosessteknologi, NTNU
Gruppe for katalyse og petrokjemi
Kjemiblokk V, rom 407

2. Kjemisk reaksjonsteknikk Chemical Reaction Engineering
H. Scott Fogler: Elements of Chemical Engineering
University of Michigan, USA
Time plan:
Week 34-47, Tuesday: 08:15-10:00
Thursday: 11:15:13:00
Problem solving: Tuseday:16:15-17:00

4. Kjemisk reaksjonsteknikk Chemical Reaction Engineering
Chemical Reaction Engineering (CRE) is the field that studies the rates and mechanisms of chemical reactions and the design of the reactors in which they take place.

5. Lecture notes will be published on It’s learning after the lecture
(Pensumliste ligger på It’s learning
Deles ut på de første forelesningene)
Øvingsopplegget ligger på It’s learning
Deles ut på de første forelesningene

6. Felleslaboratorium Faglærer: Professor Heinz Preisig
For information: It’s learning
Introduction lecture:
Place :  in PFI-50001, the lecture room on the top of the building Date:    Tuesday 21 of August Time:    12: :00

7. TKP4110 Chemical Reaction Engineering
Øvingene starter onsdag 26 august kl 1615
i K5.
Lillebø, Andreas Helland:
Stud.ass.:
Kristian Selvåg : Øyvind Juvkam Eraker: Emily Ann Melsæther: 

8. Kjemisk reaksjonsteknikk Chemical Reaction Engineering
Lecture 1
Kjemisk reaksjonsteknikk
Chemical Reaction Engineering
Industrial reactors
Reaction engineering
Mass balance
Ideal reactors

9. Steam Cracking (Rafnes)

10. Batch reactor

11. Fixed bed reactor

12. CSTR bioreactor

13. Artificial leaf, photochemical reactor

14. Chemical Engineering Momentum transfer Reaction engineering
Mass transfer
Heat transfer

16. Reaction Engineering Mole Balance Rate Laws Stoichiometry
These topics build upon one another 16

17. No-ideal flow Heat Effects Isothermal Design Stoichiometry Rate Laws
Mole Balance 17

18. Chemical kinetics and reactor design are at the heart of
producing almost all industrial chemicals
It is primary a knowledge of
chemical kinetics and reactor design that
distinguishes
the chemical engineer from other engineers

19. Reaction Engineering
Week 34, Aug. 21, chapter 1, Introduction, mole balance, and ideal reactors,
Week 34, Aug. 23, chapter2, Conversion and reactor size
Week 35, Aug. 28, chapter 3, Reaction rates
Week 35, Aug. 30, chapter 3, Stoichometric numbers
Week 36, Sept. 4, chapter 4, isothermal reactor design (1)
Week 36, Sept. 6, chapter 4, isothermal reactor design (2)
Week 37, Sept. 11, chapter 10, catalysis and kinetics (1)
Week 37, Sept. 13, chapter 10, catalysis and kinetics (2)
Week 38, Sept. 18, chapter 10, catalysis and kinetics (2)
Week 38, Sept. 20, chapter 5,7, kinetic modeling (1)
Week 39, Sept. 25, chapter 5,7, kinetic modeling (2)
Week 39, Sept. 28 chapter 6, multiple reactions (1)
Week 40, Oct. 2, chapter 6 multiple reactions (2)
Week 40, Oct. 4, summary of chapter 1-7, and 10

20. Reaction Engineering
41 (9/10, 11/10) (JPA) Reaktorberegninger for ikke-isoterme systemer.
42 (16/10, 18/10) 8.3 – 8.5 (JPA) Energibalanser, stasjonær drift. Omsetning ved likevekt. Optimal fødetemperatur.
43 (23/10, 25/10) (JPA) CSTR med varmeeffekter og flere løsninger ved stasjonær drift, ustabilitet.
44 (30/10, 1/11) (JPA) Masseoverføring, ytre diffusjonseffekter i heterogene systemer.
45 (6/11, 8/11) (JPA) Fylte reaktorer (packed beds). Kjernemodellen (shrinking core). Oppløsning av partikler og regenerering av katalysator.
46 (13/11, 15/11) (JPA) Diffusjon og reaksjon i katalysatorpartikler, Thieles modul, effektivitetsfaktor.
47 (20/11,22/11) (JPA) Masseoverføring og reaksjon i flerfasereaktorer Oppsummering.
50 (Mandag 13/12) Eksamen, kl

21. Chemical Identity and reaction
A chemical species is said to have reacted when it has lost its chemical identity. There are three ways for a species to loose its identity:
1. Decomposition CH3CH3  H2 + H2C=CH2
2. Combination N2 + O2  2 NO
3. Isomerization C2H5CH=CH2  CH2=C(CH3)2 21

22. Reaction Rate
The reaction rate is the rate at which a species looses its chemical identity per unit volume.
The rate of a reaction (mol/dm3/s) can be expressed as either:
The rate of Disappearance of reactant: rA
or as
The rate of Formation (Generation) of product: rP 22

23. Reaction Rate
Consider the isomerization A  B rA = the rate of formation of species A per unit volume -rA = the rate of a disappearance of species A per unit volume rB = the rate of formation of species B per unit volume 23

24. Reaction Rate
For a catalytic reaction, we refer to -rA', which is the rate of disappearance of species A on a per mass of catalyst basis. (mol/gcat/s)
NOTE: dCA/dt is not the rate of reaction 24

25. Reaction Rate Consider species j:
rj is the rate of formation of species j per unit volume [e.g. mol/dm3s]
rj is a function of concentration, temperature, pressure, and the type of catalyst (if any)
rj is independent of the type of reaction system (batch, plug flow, etc.)
rj is an algebraic equation, not a differential equation
(e.g. = -rA = kCA or -rA = kCA2) 25

26. General Mole Balance
Fj0 Fj Gj
System Volume, V 26

27. General Mole Balance
If spatially uniform
If NOT spatially uniform 27

28. General Mole Balance
Take limit 28

29. General Mole Balance General Mole Balance on System Volume V FA0 FA GA29

30. Batch Reactor Mole Balance
Well Mixed 30

31. Batch Reactor Mole Balance
Integrating
when t = 0 NA=NA0
t = t NA=NA
Time necessary to reduce number of moles of A from NA0 to NA. 31

32. Batch Reactor Mole BalanceNA t 32

33. CSTR Mole Balance
CSTR
Steady State 33

34. CSTR Mole Balance Well Mixed
CSTR volume necessary to reduce the molar flow rate from FA0 to FA. 34

35. Plug Flow Reactor Mole Balance35

36. Plug Flow Reactor Mole Balance
Rearrange and take limit as ΔV0
This is the volume necessary to reduce the entering molar flow rate (mol/s) from FA0 to the exit molar flow rate of FA. 36

37. Alternative Derivation – Plug Flow Reactor Mole Balance
PFR
Steady State 37

38. Alternative Derivation – Plug Flow Reactor Mole Balance
Differientiate with respect to V
The integral form is:
This is the volume necessary to reduce the entering molar flow rate (mol/s) from FA0 to the exit molar flow rate of FA. 38

39. Packed Bed Reactor Mole Balance
PBR
Steady State 39

40. Packed Bed Reactor Mole Balance
Rearrange:
The integral form to find the catalyst weight is:
PBR catalyst weight necessary to reduce the entering molar flow rate FA0 to molar flow rate FA. 40

41. Reactor Mole Balance Summary
Differential
Algebraic
Integral
Batch NA t
CSTR
PFR FA V 41 41