2. Introduction
Important terms
Reformer design specifications
Combustion fundamentals
Typical burner configuration
Effect of potassium promotion
Troubleshooting
Course contents:
Reformer convection section
Alarm set points
COD
Combustion hazards
Methods of control
Reformer monitoring
3. Steam reformer represents the core operating unit of most large scale hydrogen
production facilities. Therefore, its furnace combustion safety is fundamental to
overall safe operation of these plants. They can be operated with natural gas,
refinery-off gas, naphtha and other light-hydrocarbon streams.
Radiant section is the portion of furnace in which the heat is transferred to the
tubes, primarily by radiation
Convection section is that portion of reformer, downstream of the furnace, where
flue gas passes over heat exchangers and heat transfer occurs via radiation and
convection.
Introduction:
5. 1. Burner: Device for the introduction of fuel and air into a combustion chamber
at a required velocity and concentration to maintain ignition and combustion
of fuel.
2. Burner Management System(BMS): Control system dedicated to
combustion safety and operator assistance in starting, stopping and
preventing mis operation of fuel preparation and combustion equipment
3. Casing: Metal plate used to enclose the fired heater.
4. Draft: Negative pressure(vacuum) measured at any point in the furnace,
typically expressed in mm of water column.
Important terms:
6. 5. Duct: Conduit for air or flue gas flow
6. Excess air: Air supplied for combustion in excess of theoretical air. Frequently
expressed as percentage above stochiometric requirements.
7. Flame detector: Device that senses the presence or absence of flame and
provides a useable signal.
8. Flue gas: Gaseous products of combustion including excess air.
9. Furnace: Portion of the reformer where the combustion process takes place.
10.Steam reformer: Processing unit where steam reacts with hydrocarbons over a
nickel catalyst at high temperature to produce hydrogen and carbon oxides.
Important terms:
7. Potassium as a promoter to increase the rate of carbon gasification
(1.5-2.5%)𝐾2𝑂 present in top 45% of our active nickel catalyst
Ensure carbon removal rate is faster than carbon formation rate
For a supported nickel catalyst, addition of dopant would increase the surface
basicity which aids in preventing carbon formation and reducing carbon formation to
a greater extent.
Potassium forms hydroxide species in presence of steam that prevents any carbon
build-up on the surface
Effect of potassium promotion:
8. Combustion fundamentals:
Fuel, air and an ignition source are required for combustion to occur.
Combustion reactions involving organic compounds and oxygen takes place
according to stoichiometry combustion principles.
Steam reforming reactions are overall endothermic. As a result, a fired
heater type furnace provides the necessary heat of reaction. Heat transfer is
predominantly by infrared radiation. The furnace consists of radiant tubes
filled with nickel based reforming catalysts. Therefore steam reformer is a
complex combination of catalyst reactor and heat exchanger.
10. • Following are the reactions:
2CO = C + CO2 1
Heat
CO + H2 = C + H2O 2
CH4 = C + 2 H2 3
Heat
C2H6 = 2C + 3H2 4
Carbon formation:
11. • Following are the reactions:
C + 2H2O = CO2 + 2H2
Regeneration:
12. Typical burner configuration:
1. Top-fired steam reformers:
Burners are located in the furnace ceiling and the flue gas is extracted
at the bottom of the furnace
Coffin tunnels to ensure even flow of flue gas through the furnace.
Co-current flow of process gas and flue gas
13. Typical burner configuration:
2. Side-fired steam reformers:
Burners are located along the entire side wall of furnace and the flue gas
exhaust is at the top of the furnace
Based on the concept of uniform heat flux by positioning the catalyst tubes
in the centre of furnace cell
Cross-current flow of process gas and flue gas
14. Typical burner configuration:
3. Bottom-fired steam reformers:
Burners are located in the floor level and the flue gas is extracted
From the top
Firing arrangement is opposite of a top-fired unit
Co/counter-current flow of process gas and flue gas
15. Combustion hazards:
Cause Hazard
1. Flame instability:
Fuel pressure or fuel mixing insufficient
Deviation of fuel composition from design
Uneven distribution of fuel gas in furnace
Incomplete combustion
Flame impingement that can damage
tubes, refractory etc
2. Flame lift-off:
Fuel pressure too high
Reformer draft is too high
Flame is extinguished
Uncombusted fuel accumulation in the
furnace
Severe potential damage and pulsation in
the furnace
3. Back burning:
Fuel pressure drops in fuel line below the
burner design parameters
Enables the flame to travel from burner
tip into the fuel supply in the line
Potential for unintended energy release
16. Combustion hazards:
Cause Hazard
4. After burning:
Lack of combustion air or insufficient
mixing of fuel and air
Incomplete combustion of fuel near
burner.
Fuel-rich flue gas reacts with oxygen
and burns, resulting combustion in
convection section
Damage to convection equipment and
refractory materials
5. Fuel accumulation:
Accumulation of combustible gases
upon mixing with sufficient air
Energy release result in total
destruction of furnace
Severity of energy release depending
on air to fuel ratio
17. Methods of control:
• Reformer draft: The reformer draft is controlled by modulating the stack damper (or ID fan damper if
installed), the more the damper is opened the higher the draft becomes (more negative).
•Plant capacity control: The plant capacity control scheme is configured to maintain a ratio between
steam and feed and to ensure an excess of steam when changing demand capacity of the reformer.
•Ratio controller: The ratio controller maintains a ratio between steam and feed flows. The lead/lag
system ensures that on-capacity demand increases, the steam flow increases first followed by an
increase in feed flow. On-capacity demand decreases the lead/lag system ensures that the feed flow
decreases first followed by a decrease in the steam flow.
•Reformer firing: The reformer firing is controlled by modulating the fuel gas pressure or flow control
valve from the DCS. In AUTOMATIC Mode, the reformer process outlet temperature and the reformer
crossover temperature controls the firing.
•PSA purge gas: PSA purge gas and supplemental fuel gas flows, with their heating values, are used
to calculate the total main burner firing rate.
18. Methods of control:
1. Effective fire control:
To maintain flue and process temperatures within the desired operating
range and equipment design limits. The steam reformer firing control scheme is used to
achieve appropriate operating temperatures by balancing the firing rate with the heat
demand of the steam reforming reaction.
Typically PSA tail gas provides the majority of the firing duty requirement. An auxiliary
fuel(naphtha) gas is adjusted to make up the balance of the firing duty required to
maintain the appropriate operating temperature.
The use of feed-forward controllers or model predictive controllers can adjust firing to
respond to changes in variables such as process feed rate, combustion air flow and
temperature and PSA tail gas flow and heating value.
19. Methods of control:
2. Over firing protection:
Over firing, particularly at startup or during rate changes, can result in overheating and
potential damage to tubes. Alarms and/or interlocks may be used to mitigate the risk.
There are multiple parameters that may be used to set overfiring protection limits,
including:
FGT/ROT rate of rise
Temp diff between ROT & FGT
Min steam flow during s/u
Comparison of calculated energy requirements with theoretical reforming requirements
FGT based on system mechanical limitations
20. 1. Tube skin temperature(TST):
An optical/infrared pyrometer to be used as a device to read the tube wall temp with
emissivity set to1.0
Increase in temp could be result of excessive firing, swing in feed/fuel, burner issue,
catalyst deactivation, improper flow distribution through the reformer
Tube discoloration or hotspots could represent carbon formation or sulfur poisoning of
catalyst or flame impingement on the tubes
Especially brighter areas of tubes should be watched closely to ensure they don’t exceed
their design temp
An external inspection to ensure uniform expansion of tubes
REFORMER MONITORING:
21. 2. Excess Oxygen:
To ensure complete combustion of fuel streams
Incomplete combustion can lead to further ignition in case of oxygen ingress in flue gas
duct or in stack with potential of damage to equipment
Oxygen analyzer at the exit of radiant section to measure the oxygen levels and
minimize the possible effect of air ingress
Typical set points are 1.2-2.0%, approx. corresponding to excess air values of 10%
Flue gas oxygen controlled though manipulation of comb air flow via FD fan damper
position and lead lag arrangement
REFORMER MONITORING:
22. 3. Draft control:
ID fan maintains box pressure and pressure sensing device directly connected to box
To protect personnel from exposure to hot combustion gases
To ensure uniform flame pattern and heat distribution to tubes
4. Fuel gas pressure:
Controlled within apt range as defined by burner design so as to avoid low pressure
flame instability or loss of flame or high pressure over firing protection
Measurement should be made by pressure sensing device
REFORMER MONITORING:
24. • Depending on the design, the convection section can contain
numerous coils that provide a different service. The following
are typically provided and are listed in the order that the flue gas
comes into contact with them.
– Mixed Feed Preheat Coil
– Steam Superheat Coil
– Steam Generating Coil
– Air Pre-Heaters
Major Components:
25. Faults Consequences Remedies
Draft is high (to negative) Possible burner flame out caused
by flame lifting off the burner tip
Adjust ID fan damper to bring the
draft down.
Draft is low (to positive) Possible injury to personnel who
are on the reformer caused by hot
flue gases
Adjust ID fan damper to increase
the draft .
Reformer Inlet Temp too High Thermal cracking of feed gas on
the inlet system resulting in carbon
deposition on the catalyst
Remove the feed gas and steam
catalyst at elevated temperature.
Fuel gas pressure too high High reformer tube metal
temperatures
Reduce the fuel gas pressure.
Fuel gas pressure too low Poor reaction and conversion Increase the fuel gas pressure.
Consequence of deviation:
26. Faults Consequences Remedies
Steam-to-Carbon ratio
too low
Possible carbon deposition on to the
catalyst
Increase the process steam flow or
reduce feed gas flow.
Steam-to-Carbon ratio
too high
Reduction in methane slip leading to high
tube metal temperatures (TMTs)
Reduce the process steam flow or
increase the feed gas flow.
Low excess O2 in the flue
gas
Possible afterburning If reformer box draft is low, open the
ID fan damper a little. If reformer
box draft is high, open the FD fan
damper.
High excess O2 in the flue
gas
Possible high TMTs wasting fuel If reformer box draft is low, close the
FD fan damper a little. If reformer
box draft is high, close the ID fan
damper a little.
Consequence of deviation:
27. Faults Consequences Remedies
Burner flame is impinging
on the radiant tubes
Overheating of the tubes,
leading to tube failure
Remove the burner and
check that the tip it is not
partially plugged.
Burner flame is lazy and
yellow
Inefficient mode of
operation, low heat
transfer to the process
side
Check draft and excess
O2, make adjustments
accordingly
Consequence of deviation:
Steam reforming of methane is an endothermic reversible reaction, whilst steam reforming of higher hydrocarbons is not reversible. The activity of the catalyst installed is critical in determining the reaction rate within the reformer. However, the steam reforming reaction is diffusion limited, so the geometric surface area of the installed catalyst is directly related to the catalyst activity. This article will show the mechanisms by which carbon can form on a catalyst and how a potassium dopant can prevent this and aid catalyst recovery following carbon formation.
Due to the temperatures at which steam reformers operate, carbon is constantly being formed from the hydrocarbon feedstock, with the primary route being through cracking reactions. However, there are also carbon removal (or gasification) reactions that simultaneously occur which remove the carbon laid down, meaning there is no net accumulation of carbon in a well-run plant.
With a given catalyst loading in the reformer, the rate of gasification is fixed by the catalyst type and the process conditions. However, the rate of carbon laydown is a function of a number of conditions such as the catalyst activity, degree of sulfur poisoning and heat input to the tubes. The rate of laydown is therefore more likely to vary compared to the rate of gasification. The selected catalyst should have appropriate activity or alkali promoters to ensure that the carbon removal rate is faster than the carbon formation rate, which would result in no net carbon laydown.
t is well known that carbon formation on a surface, whether the support or catalyst, is affected by the acidity of that surface. Positively charged acidic sites on a surface will increase the rate of carbon formation, which is partly due to acidic sites catalysing the cracking reaction. Alpha alumina, which is a common catalytic support, contains acidic sites and adding Group 2 metals such as magnesium or calcium neutralises these making the surface less acidic.
Under normal operating conditions this catalyst does not produce carbon. Plant incidents, such as power failures, instrument malfunctions and equipment failures can bring about operating conditions that can form carbon. Under these circumstances, the following reactions produce carbon formation:
Under certain conditions, in mixture of carbon monoxide, carbon dioxide, hydrogen, methane, and water free carbon is thermodynamically possible and carbon can be formed from Reactions 1 and 2. This carbon is usually referred to as thermodynamic carbon or Boudouard carbon.
Carbon can also be formed as a result of thermal cracking of hydrocarbons as illustrated in Reactions 3 and 4.
Thermodynamic carbon can give rise to the most difficult problems at a plant. There is a critical level of steam-to-carbon ratio depending on operating conditions, below which carbon from this reaction is formed instantaneously in the catalyst pores. Deposition of carbon causes physical breakdown of the catalyst. When this occurs, immediately shut down the plant and change the catalyst.
The amount of carbon formed from hydrocarbon cracking depends on the relative rates of deposition and removal of carbon. The higher the number of carbon atoms in the hydrocarbon feed, the faster the rate of decomposition to form carbon, and the higher the steam-to-carbon ratio the faster the rate of removal of carbon. The likelihood of carbon deposition increases with increasing molecular weight of the feedstock and decreasing the steam-to-carbon ratio. The value of steam-to-carbon ratio at which the amount of carbon deposited becomes significant, depending on the feedstock composition. With a light feedstock, the value is below the normal design minimum steam-to-carbon ratio of 3:1. As the amount of heavier hydrocarbons present in the gas increases, the minimum operable steam-to-carbon ratio needs to be raised and levels maintained for long periods of trouble-free (that is carbon deposition-free) operation.
Carbon resulting from hydrocarbon cracking does not usually form in the inner pores of the catalyst so that a total breakdown of the rings does not take place. The outer surface of the rings is weakened, and the surface layers often fall off during operation or on discharge. This gives the rings a characteristic eroded appearance, which after the carbon is steamed off during operation or shutdown, is the only indication that carbon formation occurred.
Most reformers have alarm settings and trip systems connected to the steam-to-carbon ratio controller. To protect the catalyst from damage by carbon deposition that results from operation at a low steam-to-carbon ratio. With a design steam-to-carbon of 3:1, the alarm is usually set at 2.8:1 and the trip at 2.5:1.
If only a small amount of carbon deposition occurred, as indicated by reformer tube appearance or increased pressure drop, catalyst activity can be recovered by steaming.
It is usually sufficient to shut off the hydrocarbon flow for several hours and maintain the exit temperature in the range of 1380–1472F (750–800C). Removal of carbon during the regeneration may be checked by monitoring the carbon dioxide concentration at the reformer exit.
If high s/c ratio is maintained then at the same time fuel has to be increased so as to maintain ROT and methane slip. If only high s/c and no fuel increase then it may result in high TST.
2. Afterburning results when there is insufficient excess air for complete combustion in the radiant firebox. Air leakage into the furnace combines with any remaining excess air to react with uncombusted fuel downstream of the firebox. This overheats the heater internals and may subsequently cause permanent damage. Afterburning may not be visible and may only be evidenced by a rapid increase in stack temperature. Afterburning is a potentially dangerous condition. Take immediate remedial action. Reduce the firing rate (cut fuel), and then open both the ID fan and FD fan dampers to admit more combustion air while maintaining a negative draft. If afterburning continues, continue to decrease the firing.
Air leakage into the furnace should be minimized for optimal combustion conditions because by design all combustion air should enter through the burners. Keep all observation (peep) doors and pressure relief (explosion) doors closed when not in use. If leakage continues to be significant, a program of sealing all heater penetrations is appropriate.