steam reforming - (atm) approach to equilibrium
DESCRIPTION
Equilibrium Effects - Methane Steam - Water Gas Shift Relationship of Kp to Temperature Relationship of WGS Kp to Temperature Effect of Temperature on Methane Slip Approach to Equilibrium Reaction Path and Equilibrium Effect of Pressure Increase Operating Parameters - Pressure - Temperature - Feed Rate - Steam to Carbon Effect of Exit Temperature Spread Useful Tools Calculating ATMTRANSCRIPT
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Gerard B. Hawkins Managing Director Kp
Temperature
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The aim of this presentation is to • Give an understanding of equilibrium ◦ Methane Steam ◦ Water Gas Shift
• Explain what affects equilibrium • Explain concept of approach to equilibrium
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• There is an equilibrium effect • Limits the reaction rate • Point at which forward and reverse reactions are
equal • Defined by
[ ] [ ]
[ ] [ ]CO.PHPOH.PCHPKp 3
2
24=
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• Can rearrange into a more useful form
• So now we can relate partial pressure of methane to other parameters
• But can simplify again to
• This is the most useful form
[ ] [ ] [ ]O]P[H
CO.PHPKpCHP2
32
4 =
[ ] [ ] [ ]O][H
CO.HPKpCH2
32
2
4 =
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• Equilibrium defined by
• We can see therefore ◦ Methane slip is proportional to Kp ◦ Methane slip is proportional to P² ◦ Methane is inversely proportional to steam fraction Reason why SC Ratio is high
• So we can now determine cause and effect by using this simple expression
[ ] [ ] [ ]O][H
CO.HPKpCH2
32
2
4 =
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• Kp is inversely proportional to temperature • Therefore to achieve a good equilibrium position
need to use a high temperature
Kp
Temperature
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• Water Gas Shift (WGS) is also equilibrium limited • Equilibrium defined by
• Which can be rearranged to
P[CO2] P[H2] Kp = ____________ P[CO] P[H2O]
[CO2] x [H2] [CO] = _________ Kp x [H2O]
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• [CO] not dependant upon pressure
• [CO] α 1/[H2O] ◦ Higher steam to carbon ratio gives lower CO content
◦ Higher steam to carbon ratio gives higher CO2 content
• Kp is related to temperature
• High exit temperature gives more CO and conversely less CO2
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Water Gas Shift (WGS) is at equilibrium at exit of the reformer
Reaches equilibrium very fast
Kp
Temperature
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By using equation earlier can relate methane slip to temperature
770 780 790 800 810 4
6
8
10
12
Met
hane
slip
(%)
(1418) (1454) (1436) (1472) (1490) Temperature °C (°F)
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770 780 790 800 810 4
6
8
10
12
Met
hane
slip
(%)
(1418) (1454) (1436) (1472) (1490) Temperature °C (°F)
Exit CH4
Equilibrium Temperature
Gas Exit Temperature
ATE
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Approach to Equilibrium (ATE) is therefore defined by
ATE = Actual temperature - Equilibrium temperature
ATE is 0°F when gases at equilibrium This never happens Usually ATE in in range 5-20°F ATE rises as the catalyst ages
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Can translate this graph to give
0 0.2 0.4 0.6 0.8 1 200
300
400
500
600
700
800
900
Fraction down tube
Tem
pera
ture
°C Gas Temp
Eq'm Temp
390
570
750
930
1110
1290
1470
1650
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Can then superimpose the reaction path
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6
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Met
hane
slip
(%)
(1418) (1454) (1436) (1472) (1490) Temperature °C (°F)
Equilibrium Line
Reaction Path
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770 780 790 800 810 4
6
8
10
12
Met
hane
slip
(%)
(1418) (1454) (1436) (1472) (1490) Temperature °C (°F)
ATE
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770 780 790 800 810 4
6
8
10
12
Met
hane
slip
(%)
(1418) (1454) (1436) (1472) (1490) Temperature °C (°F)
Equilibrium Line
Increasing pressure
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770 780 790 800 810 4
6
8
10
12
Met
hane
slip
(%)
(1418) (1454) (1436) (1472) (1490) Temperature °C (°F)
Increasing pressure
ATE
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• A reformer is essentially an equilibrium reactor ◦ Low ATE’s are achieved at the exit
• Any change that affects the equilibrium position will affect the performance of the catalyst/reformer ◦ Will affect the approach ◦ Will affect the methane slip
• Raising the outlet pressure will ◦ Increase kinetic rate which will reduce ATE ◦ But equilibrium position is worse
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770 780 790 800 810 4
6
8
10
12
Met
hane
slip
(%)
(1418) (1454) (1436) (1472) (1490) Temperature °C (°F)
Equilibrium Line
Reaction Path
Effect of Raising Exit Temperature
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• So raising the exit temperature ◦ Reduces the methane slip ◦ Tightens the approach to equilibrium
• But ◦ Will increase tube temperatures ◦ May reduce tube wall margin
• Classic trade off between maximizing production but sacrificing tube life
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• Any increase in feed rate will ◦ Increase exit temperature or methane slip Depends on operating policy ◦ Increase pressure drop ◦ Increase ATE - lower residence time ◦ Increase maximum tube wall temperatures Hence reduce tube life ◦ Increase fluegas flow ◦ Increase temperature Reduced contact time
• Converse is also true
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• Reducing steam to carbon ratio ◦ If methane slip is held constant will require an increase in
exit temperature ATE will reduce Maximum tube wall temperature will rise ◦ If exit temperature is held constant will cause methane
slip to rise ATE will increase ◦ Pressure drop will be reduced
• Converse is also true
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770 780 790 800 810 4
6
8
10
12
Met
hane
slip
(%)
(1418) (1454) (1436) (1472) (1490) Temperature °C (°F)
Cold Zone
Hot Zone
Actual Operating Point
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Effect of such a spread is • Tight approaches in both hot and cold zones • Methane slip is average of both zones • Temperature is average of both zones • Approach for ‘mixed’ gas is high • Appears as if catalyst is not working well
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From the above, there are conflicts as defined below
Temperature Pressure Steam to
Carbon
Kinetics Equilibrium Overall
Conflict ?
High High
High
No
High Low
?
Yes
Low High
?
Yes
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• Pressure - defined by other issues ◦ CAPEX of reformer High pressure = thicker tubes ◦ Size of synthesis gas compressor High pressure reduces size of synthesis gas machine But increases the size of the air compressor ◦ Methane slip is increased But secondary reduces the effect Does represent an inefficiency
• Classic balance between CAPEX and OPEX
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• Steam to Carbon - defined by other issues ◦ Must raise HP steam for synthesis gas machine Do get MP steam from extraction from turbine Try to minimise capacity to reduce CAPEX - more steam
raising requires more coils/heat exchangers ◦ HTS operation - over reduction ◦ CO2 removal - reboiler heat load ◦ Metal dusting is a problem at low steam to carbon ratio’s
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508
203
102
Equi
libriu
m %
CH
4 (d
ry b
asis
)
Pres
sure
(psi
g)
Pres
sure
(bar
g)
Steam Ratio
2.0
3.0
4.0
5.0
35
14
7
1.0
2.0
5.0
10
20
50
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Equilibrium exit CH4 at these conditions ?
P= 30bar (435psi) T = 850°C (1562°F) Steam/Carbon = 3.5
508
203
102
Equi
libriu
m %
CH
4 (d
ry b
asis
)
Pres
sure
(psi
g)
Pres
sure
(bar
g)
Steam Ratio
2.0
3.0
4.0
5.0
35
14
7
Equilibrium CH4 = ~5.6% 1.0
2.0
5.0
10
20
50
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CH4 slip is a function of ◦ Catalyst activity ◦ Reformer exit temperature ◦ Reformer exit pressure ◦ S:C Ratio ◦ varies with operating conditions
Assessment of catalyst performance ◦ CH4 slip alone is not a good measure of performance ◦ ATE is a better guide ◦ will not change dramatically with operating conditions
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Take inlet and exit gas samples for analysis Measure steam reformer exit T & P Measure reformer inlet steam and feed flows Need to calculate reformer exit dry gas flow ◦ all carbon in the feed ends up in the dry gas ◦ hence we can calculate exit dry gas rate by carbon
balance
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Need to calculate the reformer exit steam flowrate ◦ can be done by Hydrogen balance across the
reformer Can also do a balance on O2 as a cross check Calculate exit wet gas composition and then Kp Calculate Equilibrium Temperature Calculate Approach to Equilibrium
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Assumes measured data is correct In practise always errors in measured data ◦ feed flow ◦ feed analysis ◦ steam flow ◦ exit analysis ◦ exit pressure ◦ exit temperature
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770 780 790 800 810 4
6
8
10
12
Met
hane
slip
(%)
(1418) (1454) (1436) (1472) (1490)
Temperature °C (°F)
Exit CH4
Equilibrium Temperature
Gas Exit Temperature
ATE
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770 780 790 800 810 4
6
8
10
12
Met
hane
slip
(%)
(1418) (1454) (1436) (1472) (1490)
Temperature °C (°F)
Exit CH4
Gas Exit Temperature
Pressure
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770 780 790 800 810 4
6
8
10
12
Met
hane
slip
(%)
(1418) (1454) (1436) (1472) (1490)
Temperature °C (°F)
Worst ATE CH4
Gas Exit Temperature
Actual ATE
Best ATE
Pressure
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Need to do a consistency check on the data Check data for a consistent H & M balance ◦ GBHE VULCAN CERES H & M Balance reconciliation
WGS at reformer exit temperatures ◦ At high temps, WGS reaction should be at Equilibrium
◦ We can similarly calculate approach to WGS equilibrium
Often WGS appears to not be at equilibrium ◦ Suggests errors in exit analysis and exit T
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• Well ◦ Use VULCAN CERES
◦ Use VULCAN TP3
◦ Use VULCAN REFSIM
◦ And most of all Think !
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