4. Steam Reforming limited by
Heat transfer
Catalyst activity
Kinetic rate
Equilibrium
5. Approach to Equilibrium
770 780 790 800 810 820
2
4
6
8
10
12Methaneslip(%)
Gas
Exit TEq'm T
ATE
(1418) (1454)(1436) (1472) (1490)
Temperature Deg C (Deg F)
Exit CH4
6. Approach to Equilibrium
CH4 + H2O <=> CO + 3H2
Approach Tms = Actual T gas - EquilibriumT
gas (A.T.E.)
measured calculated
•Measure of catalyst activity
–If ATE = O, system at equilibrium
–As catalyst activity decreases, ATE
increases
7. Kinetics
•Reversible action, zero rate at equilibrium
•Reforming reaction very fast
•Limited to pellet surface only-diffusion limit
•Depends upon catalyst GSA
•Depends upon gas composition
•Exponential with temperature
•C2, C3 & C4 considered as not reversible
9. Steam Reforming Catalysis
Key Reaction Steps
1. Fast - Diffusion of the molecules in the bulk gas
phase
2. Slow - Diffusion of the molecules through the
gas film
3. Slow - Diffusion through catalyst pores
4. Fast - Absorption of the molecules onto the Ni
sites
5. Fast - Chemical reaction to produce CO and H2
10. Kinetics - Natural Gas
•Kinetic model used for natural gas feeds
•Methane kinetics well validated
•C2 ,C3, & C4 kinetics ok for natural gas tail only
•NOT to be used for LPG feeds
•Kinetics for steam reforming reactions
•Shift reaction taken to be at equilibrium
•Shift very fast compared to reforming
11. Kinetics - Natural Gas
•Form of equation as below:
R[CH4] = K.GSA.Ract.exp(T).P[CH4].(Kp’-Kp)
P[H2O]
R[CH ] = Rate of methane reaction T = Temperature
K = Constant P[X] = Partial pressure
Ract = Catalyst relative activity Kp' = Equilibrium constant of gas
GSA = GSA Kp = Equilibrium constant at T
12. Geometric Surface Area
• GSA for short
–Area per unit volume
–Typically 200-500 m2/m3
• Important as apparent activity is a
very strong function
• Function of
–shape
–size
–number
13. Kinetics
•Major points of interest
–Steam is a poison
–Kp’- Kp can be changed to approach
–GSA term is included
–Relative activity term is included
14. Kinetics
•For higher hydrocarbons
•R[C2H6] = K.GSA.Ract.exp(T).P[C2H6]
•R[C3H8] = K.GSA.Ract.exp(T).P[C3H8]
•R[C4H10]= K.GSA.Ract.exp(T).P[C4H10]
•Simple first order kinetics-non reversible
•Hence limit to natural gas tail only
17. Catalyst Applications
• VSG-Z101
–Other light feeds - refinery offgas
–Light duties e.g. side fired reformers
–Use up to butane at 4.0 S:C ratio
–Use in top fired reformers at tube top
18. Steam Ratios for
Catalyst/Feedstock Combinations
Feedstock Natural Gas
Reforming
Non-
alkalised
Associated Gas
Ref
Lightly
alkalised
Dual Feedstock
Reforming
Moderately
alkalised
Naphtha
Reforming
Heavily
alkalised
Non-alkalised Low alkali Moderate alkali High alkali
Naphtha 3.0-3.5
Light Naphtha 6.0-8.0 3.0-4.0 2.5-3.0
Butane 4.0-5.0 2.5-3.5 2.0-3.0
Propane, LPG 3.0-4.0 2.5-3.0 2.0-2.5
Refinery Gas 6.0-10.0 3.0-4.0 2.0-3.0 2.0-2.5
Associated
Gas
5.0-7.0 2.0-3.0 2.0-2.5
Natural Gas 2.5-4.0 1.5-2.0 1.0-2.0
Pre-reformed
Gas
2.0-3.0 1.0-2.0 1.0-2.0
19. Pre - reduction
• This will maximize the activity of a catalyst
• The start up will be easier and quicker
• Catalyst should remain more active at
tube top
• Useful for low inlet temperature reformers
20. Catalyst Support -
Reduction Temperatures
AlphaAlumina
CalciumAluminate
MagnesiumAluminateSpinel
Temperature
(Deg F)
Temperature
(Deg C)
800 1000 1200 1400 1600
400 500 600 700 800 900
Magnesium Aluminate
spinel material usually
supplied pre-reduced
22. Carbon Formation
•Carbon formation formed by side reactions
•Totally unwanted due to damage caused
•Catalyst break up and deactivation
•Catalyst tubes overheated - hot bands
–Premature tube failure
–Catalyst activity reduction
–Pressure drop increases
23. Carbon Formation
•Carbon forms when
–Steam ratio is too low
–Catalyst has too little activity
–Higher hydrocarbons are present
–Tube walls are hot - high flux duties
–Catalyst has poor heat transfer coefficient
26. Heavier Feedstocks
•Steam reforming
–Not practical to increase steam to carbon
ratio using gas reforming catalysts
–Carbon formation more problematic
Need promoters to limit carbon
and/or increase its removal once
formed
Carbon formed not just by cracking
but also by polymerisation of
intermediates
29. Heavier Feedstocks
•Carbon removal (heavy feed reforming)
–Potash (alkali) incorporated into catalyst
support
Inhibits cracking rate
Accelerates carbon gasification
Needs to be “mobile” to remove carbon
on the inside tube wall surface - Potash
released by complex chemical
Release reaction controlled by
temperature
Required only in the top section of the
reformer tube - Lower section of catalyst
absorbs liberated potash
30. Heavier Feedstocks
•Potash Addition (Heavy feed reforming)
–Reduces catalyst activity
Need extra Ni
–MgO/NiO solid solution
Low Polymerization activity - reduces
carbon formation
MgO must be “fixed” so as to avoid
hydration of the “free” MgO to
magnesium hydroxide - weakens
catalyst pellet severely (cannot steam
catalyst!)
31. Carbon Formation
•Use of potash to prevent carbon formation
•Increases the rate of carbon removal
•Does not stop the formation from cracking
•Potash catalyzes the rate of steam
gasification
•Balance of kinetics altered to favour removal
•Can steam with care
33. Role of Alkali - Lightly Alkalized
For light feeds and LPG etc using lightly
alkalized catalyst
–Potash is chemically locked into catalyst
support
–Potash required only in top 30-50% of the
reformer tube
Catalyst life influenced by
–Poisoning
–Ni sintering
– Process upsets etc
Lightly alkalized
Non-alkalized
34. Carbon Formation and Prevention
Top Fraction Down Tube Bottom
Non-Alkalised
Catalyst
Ring Catalyst
Optimised Shape
(4-hole Catalyst)
Inside Tube Wall
Temperature
920
(1688)
820
(1508)
720
(1328)
0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1.0
Alkalised
Catalyst
Carbon Forming
Region
Optimized Shape
VSG-Z101
35. Potash and Activity
•However, potash is a catalyst poison
–Potash does reduce activity
•At low levels 2%, the effect is minimal
•Use a gas type catalyst in bottom of tube
•Use naphtha catalyst in top of tube for carbon
•Therefore no carbon and low exit approach
36. Potash Levels in Heavy Feed Steam
Reforming Catalyst
0 20 40 60 80 100
0
1
2
3
4
5
6
7
% Down Reformer Tube
wt% Potash
2 year
1 year
0 years
Potash Promoted Non-akalised
37. Must watch the interface temperature
At >650°C Potash leaching too high
Leads to
◦ Fouling of WHB etc
◦ Loss of carbon resistance
◦ Hot banding etc
40. When to Use and Why
• Used when major feedstock variations
– NG to LPG
• Feedstock flexibility
– When 650oC limit is reached
• Problem of Potash Leaching
42. Sock Loading - Measurements
• Key part of charging procedure
• Aim to pack catalyst to uniform voidage
• Measure pd
– Not outage in tube at any one time
– Not weight per tube
– Not catalyst density
– After 50%
– After full loading
• Use defined and consistent procedure
throughout
43. DP Measurement
• Use VSC Pressure Drop Rig
• If too high then
– suck out catalyst and recharge
• If too low then
– Vibrate tube
– Top up if outage too great
44. Pressure Drop Measurement
• Fixed flow of air (choked flow through orifice)
• Mass flow rate through orifice function of
– Upstream pressure
– Orifice diameter (known)
– Temperature (known)
• Downstream pressure is measure of pd
47. Sock Loading - Vibration
• Electric or pneumatic vibrators
–rotating cams are noisy
• Soft-faced shot-filled hammer
–need consistent blows
48. “UNIDENSE” Method
• Developed by Norsk Hydro
– licensed to a number of organisations
• Tried in a number of plants
– ammonia, hydrogen and DRI
• Leads to “denser” packing
– less pd variation
• more uniform gas flows
– easier procedure
• shorter loading time (70%)
– slightly higher pd
• effect on throughput?
50. Pigtail Nipper
This hydraulic device designed by ICI
is operated at a safe distance from the
leaking tube and squeezes the pigtail
flat with the plant still operating.
Allows furnace to stay on line.
No thermal cycle.
57. GHR History
• Developed for ammonia process - LCA
• Early 1980's - Paper exercise
• Mid 1980's - Sidestream unit at Billingham
• Mid 1980's - LCA design developed
• Late 1980's - ICI Severnside plants start up
• 1991 - BHPP LCM plant designed
• 1994 - BHPP plant start up
• 1998 - AGHR Start Up
• 1998 - MCC Start Up
58. GHR Shellside Design
•Shellside heat transfer usually poor
•Minimize tube count with expensive alloys
•Tubes are externally finned
•Designed as double tubes
- Sheath tube
•Produces much smaller tube bundle
•Allows scale up to higher capacities
65. Uprate Capabilities
•GHRs can be used in parallel to existing
primary reformer
•Potential to uprate capacity by 40%
•Severely impacts steam system
•Most applicable to hydrogen plants
•No changes to radiant or convection
sections of reformer / fans burner etc.
•New WHB may be required
•Rest of plant must be uprated
68. Keys to Good Performance
•Burner Design
•Mixing Space
•Catalyst
69. Poor Mixing Performance
• Good mixing is absolutely essential
• Poor mixing in combustion zone gives high
approach and high methane slip
• Problem is poor mixing can not be
differentiated from poor catalyst performance
UNLESS thermocouples are in the bed.
•Bed temps will show divergence
•Bed temps will show odd behaviour
70. Catalyst Bed Sizing
•Based on a space velocity technique
•Wet Gas Space Velocity (WGSV)
•Uses exit flow with steam included
•See attached graph
•Modify space velocity by catalyst GSA
•See table for relative catalyst GSA
75. Metal Dusting Key features
•Catastrophic carburization
•Occurs at "low" temperatures 700 - 450°C
•Induction period sometimes required
•Often local pitting - pits coalesce
•Can have general corrosion
•Can be very rapid 3mm/year
•Carbon formation occurs
77. Mechanism of Metal Dusting
Initiation
•Gas has propensity to deposit carbon
2 CO=> CO2 + C (Boudouard)
CO + H2 => H2O + C (CO Reduction)
•Oxide film breakdown exposes active Fe,
Ni, Co sites
•Carbon deposits at active sites
78. Metal Dusting and GBHE
•GBHE have great experience
•GBHE have a solution
•Proven to work in operation