avoid syn gas catalyst mal-operation wsv
DESCRIPTION
syngasTRANSCRIPT
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Avoiding SyngasCatalyst Mal-Operation
ByGerard B. Hawkins
Managing Director, C.E.O.
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Objective
This presentation covers frequent and costly incidents related to catalysts mal-operation with the focus of providing the plant operator with recommendations to avoid plant outages and catalyst losses.
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Process Information Disclaimer
Information contained in this publication or as otherwise supplied to Users is believed to be accurate and correct at time of going to press, and is given in good faith, but it is for the User to satisfy itself of the suitability of the Product for its own particular purpose. GBHE gives no warranty as to the fitness of the Product for any particular purpose and any implied warranty or condition (statutory or otherwise) is excluded except to the extent that exclusion is prevented by law. GBHE accepts no liability for loss or damage (other than that arising from death or personnel injury caused by GBHEs negligence or by a defective Product, if proved), resulting from reliance on this information. Freedom under Patent, Copyright and Designs cannot be assumed.
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Content
Review of incidents by reactor Primary reforming Secondary reforming HTS LTS Methanator
Reactor loading Support media Some general comments on alternative actions when a
plant gets into abnormal operation
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Reformer Catalyst Loading
UNIDENSETM is now established as key to an even reformer loading
However UNIDENSE requires some care to achieve its full potential
A reformer in South America was loaded by an inexperienced team and had to be unloaded and reloaded with 20 % catalyst losses.
Lesson check experience of UNIDENSE loading supervisors
UNIDENSE is a trademark of Yara International ASA
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Reforming Burners Lighting
Lighting burners during start-up is a critical activity The clear requirement is to increase the number of lit
burners as the plant rate is increased and ensure the pattern of burners always gives an
even heat input Obvious but was one component leading to this:
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Reforming Burners Lighting
Lesson light only the number of burners you need at each stage of start-up and keep the pattern/heat generation even
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Reformer - Carbon
Carbon deposition will occur when excess hydrocarbons are introduced
There are several ways to do this: Inadequate purging during a plant trip can lead to feed
being stored in the desulfurization vessel / pipe work Then introducing nitrogen purge pushes this
hydrocarbon into the reformer Naphtha fed plants have a high risk of feed condensing
and sitting in dead legs until some motive force pushes this into the furnace
Erroneous feed flow measurement more critical in low steam ratio plants
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Reformer Carbon from Naphtha
Introduction of nitrogen during a start-up increased the reformer pressure drop from 1.4 to 7 bar in 2 minutes
The nitrogen feed line was 100mm diameter and around 1km long, capable of holding up to 10te of naphtha
A spectacle plate was not swung during earlier operation On previous occasions a drain valve was opened on the
nitrogen compressor this time the valve was not operable
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Reformer Naphtha in Dead LegsSituation After Plant Trip
Steam to Reformer
Flow Feed CV
Feed ESDV
Steam to Preheat Coil
FM
Final ZnO Bed
Feed
To Collector or Flare
PCV
S Pt
Trapped Feed After Plant Trip
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Reforming - Carbon from Liquid HCs
A couple of ammonia plants in South America had problems before the natural gas condensate removal plant was installed
These plants took their feed off the bottom of the supply line and hence took any liquids that were present
The liquid did not register in the flow meters which were orifice plate type thereby reducing the actual steam to feed ratio
Non-alkalized catalysts lasted as little as 6 weeks and when replaced by alkalized products lasted a 2 year run
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Reforming - Carbon from Liquid HCs
Lessons Gas flow meters largely ignore the presence
of condensed higher hydrocarbons Note also that during startup flowmeters may
read in error if not compensated for temperature and pressure
Alkalized reforming catalysts give very significant additional margin against carbon formation in primary reformers
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Reforming Tube Failure from Higher Hydrocarbons
A plant in North America was the sole user of gas that came down a branch that went under a river
During a start-up after an extended shutdown - when lighting burners liquid was seen flowing from a few burners onto tubes
While the operator exited and radioed the control room to shut off the fuel - a tube burst leading to significant damage to the furnace/tubes
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Reforming Tube Failure from Higher Hydrocarbons
It was thought that hydrocarbons had condensed in the cooler section of pipe under the river
Lessons: Consider potential for condensation of higher
hydrocarbons, especially If lines are cooled below normal If levels of higher hydrocarbons increase
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Reforming Failure from Condensation
We have another example of catalyst breakage from condensation on start-up
A naphtha fed plant was not able to provide nitrogen purge for the initial phase of start-up and so heated the reformer using steam
Around 20 start-ups from cold eventually led to breakage of catalyst, poor flow distribution, hot spots and required catalyst change
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Reforming Failure from Condensation
Lesson: Reforming catalyst should be warmed up to
50C above the dew point before introduction of steam
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Secondary Reforming
All incidents on secondary reformers are related to the burners
The problem of increasing plant rate to the point that there is inadequate mixing zone is well understood but requires detailed CFD modelling to predict
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Secondary Burner Problems
Cost of Problems:
7-10 day turnaround
Short Catalyst life $52K/yr less than 10yr
Mechanical repairsEstimated $65K/year
Poor mixing Burner failure
Bed damage Refractory damage
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Secondary Burner Solution
Small flame cores from all nozzles
No flame attachment to rings
Good mixing of the process gas and air
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HTS
The main problem with HTS reactors is upstream boiler leaks
We have another case where dehydration of the catalyst has lead to an exotherm on startup
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HTS - Boiler Leaks
This is a potential problem on ammonia plants with high pressure boilers upstream of the HTS
Boiler leaks put stress onto the HTS catalyst by: rapid wetting/drying and pressure-drop build-up from accumulated boiler solids
These leaks are inevitable with steam pressures of 100bar A serious leak will occur approximately every 12 years
Selecting a catalyst with high in-service strength significantly improves probability of survival
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HTS VSG-F101 Resists Boiler Leaks
A plant in China suffered a complete tube failure that tripped the plant F101 was unaffected by this incident:
0
20
40
60
80
100
120
0.0 50.0 100.0 150.0
Nor
mal
ized
Tem
pera
ture
% Bed Depth
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HTS - Dehydration
A plant in China had kept a charge of HTS catalyst in a spare reactor for 1 year but had left this reactor open to the air so the catalyst had adsorbed water
The start-up required nitrogen heating for 2 days to dry the whole bed and in doing so dehydrated the catalyst in the top/bulk of the bed
100% steam was switched into the reactor against our advice of 5% An exotherm started and then (unrelated) the plant tripped (site power
trip) which held the reactor with 100% steam The exotherm reached 530C, and look several hours to cool down
with N2 The final activity when on-line looked good, with expected low
pressure-drop.
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HTS Lessons
Do not leave catalysts exposed to damp atmospheres
VSG-F101 give the best survival of boiler leak and over-reduction incidents
Incorporate the GBHE VULCAN Series procedures when over-reduction is suspected
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LTS
A plant in North America had to top skim its LTS bed due to high pressure drop
The main cause was poor atomization of quench water
This was not helped by the competitive catalyst installed which developed very poor strength when wetted
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LTS
Lessons: Ensure quench water nozzles are on the
shutdown inspection list Check for adequate pipe length for
vaporization Use catalyst with good strength after
wetting
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Methanator
The main hazards when methanation reactors are shutdown are nickel carbonyl (see plant safety presentation on nickel Carbonyl) and self heating when exposed to air
An example of self heating comes from a methanator on an olefin cracker
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Methanator self heating
The plant was shut down and purged with nitrogen
The inlet and exit valves and thermocouples were removed for repair
Open ends were covered in plastic sheet Catalyst was in reduced state, with N2 purge
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Methanator Self-heating
A reading of 454C/850F was seen on re-connection of the thermocouples The plastic sheeting was not adequate isolation Air entered the vessel and
A downward purge of nitrogen then gave a reading of 649C/1200F on the bottom thermocouple
Decided to change catalyst as needed 5 yr run GBHE had product on site within 4 days
(including a weekend)
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Methanator Learning
Reduced methanation catalyst becomes very hot when exposed to air
Secure isolation/inert purge is essential for maintenance on vessels containing reduced catalyst
With little or no gas flow, thermocouples do not show the peak temperature
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Support Media
Dont spoil a ship for a few cents worth of tar! Below Bed:
Support media does a key job preventing catalyst pass through the exit collector and doing this with low pressure-drop
Above Bed: Support media placed on top of the bed protects
catalysts from high inlet gas velocities - which have the potential to break catalysts through disturbance and milling
High voidage media can also be used to reduce the effects of boiler solid build-up
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Support Media - problems
A plant decided to use some old support balls that had been stored outside for some years
This was a LTS duty so either alumina or silica-alumina would be suitable
Shortly after start-up the reactor pressure-drop started to increase
This eventually required a shutdown to address
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Support Media - problems
Investigation showed failure of the support media
The catalyst had to be replaced Cause is believed to have been rapid
drying of support that had got wet during storage
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Support Media use of Si/Al
Silica-alumina support is cheaper A plant decided to use silica-alumina balls in a high
temperature shift bed It was thought that this would be a low enough
temperature for silica migration not to be an issue Not true silica migrated downstream and
collected on the tubes of the exchanger before the LTS which required regular shutdowns to clean
A recent enquiry associated with HDS and HTS catalysts simply specified ceramic balls
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Support Media Catalyst Protection
For the most severe duties, including secondary reformers GBHE recommends fused alumina lumps High density High strength Inert (high purity alumina) Difficult to blow around!
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Support Media - advice
Lessons: Store support media to the same standard as
catalysts the cost will be the same if they fail!
Only use high purity alumina support above 300C in steam environments
Use GBHE A2ST for protection against accumulation of boiler solids from boiler leaks
Use fused alumina lumps for the ultimate protection against bed disturbance
A2ST Advanced Alumina Support Technology
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Reactor loading Dont be tempted to put that last bit in! A methanol plant with a water cooled reactor experienced an
increasing pressure-drop on a new charge of catalyst Eventually the plant had to be shut down Inspection showed that catalyst had been loaded on top of
the tube-sheet as well as in the tubes Removal of the catalyst on top of the reactor and 150mm
down the tubes restored the pressure-drop to normal
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Reactor overloading
A hydrogen plant in Europe implemented a plant up-rate and as part of this increased the HTS volume (we advised it could be lowered)
In order to maximize the catalyst volume the hold-down system was removed!
Milling then increased the pressure-drop A reactor inlet distributor is better described as inlet gas
momentum destruction device Lesson gas distribution/bed protection requires careful
design along with the rest of a plant up-rate
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Reactor loading
A plant with a HTS reactor with two beds (one vessel) went with a short load and split the short load equally between each of the two beds.
The net effect was a bed L/D of 0.2 a long way below the minimum recommendation of 1.0
The charge had to be replaced after 2 years One can debate the merits of two beds with L/D
of 0.2 with gas mixing in-between or one bed with an L/D of 0.4
The key is neither but to load the bed(s) carefully:
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Reactor Loading
The ideal catalyst loading method is by sock with the minimum or raking
Any raking will introduce density differences that will lead to early discharge of the catalyst due to the uneven flow distribution produced
Lesson: allowing your loading company to rake catalyst is equivalent to throwing catalyst away
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Priorities When Things go Wrong
There is no universal advice but some up-front thinking can lead to faster more confident decisions
A number of incidents have involved exotherms on catalysts which threatened the integrity of their reactors
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Example exotherm and action Hydrogen was being removed from a process
stream using a copper oxide catalyst During commissioning a hydrogen stream was
mistakenly introduced and the catalyst temperature rose to 1000C
GBHE staff on site advised immediate depressurization
Vessel damage was avoided There were problems later on downstream mol
sieve driers from water produced which accumulated in a dead leg
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Depressurization vs Purging
With the previous example in mind it is worth reflecting on the merits of depressurization and purging
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Depressurization
Several advantages: It decreases the partial pressure of
reactants which may help slow the temperature rise
It reduces the stress on equipment enabling the handling of higher temperatures
No motive force is required so it is reliable
Lowering the pressure makes purging more effective
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Depressurization
Risks Depressurization can generate high gas
velocities enough to fluidize catalyst beds Fluidized catalyst beds can lose their top
protective layer (into the bed) and suffer: flow distribution problems or pressure drop increase if loss of the top layer
allows milling
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Purging
Advantages Can maintain plant pressure (but is
better if pressure reduced) Fluidization risks to catalyst beds much
lower
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Purging
Disadvantages Difficult to achieve high flow-rates steam is
often the purge gas with highest availability Steam can deactivate catalysts through
oxidation and in some cases sintering Nitrogen is a good inert material but often
the available flow is limited Need to consider trace oxygen in nitrogen
Ideal is nitrogen with enough hydrogen to ensure reducing conditions
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Conclusions
The incidents here suggest: Selecting the right catalyst has a significant
impact on the ability of a plant to continue operation through an unplanned event
Operator training/procedures are key to avoiding incidents
Avoiding Syngas Catalyst Mal-Operation ObjectiveProcess Information DisclaimerContentReformer Catalyst LoadingReforming Burners Lighting Reforming Burners LightingReformer - CarbonReformer Carbon from NaphthaReformer Naphtha in Dead LegsReforming - Carbon from Liquid HCs Reforming - Carbon from Liquid HCsReforming Tube Failure from Higher HydrocarbonsReforming Tube Failure from Higher HydrocarbonsReforming Failure from CondensationReforming Failure from CondensationSecondary ReformingSecondary Burner ProblemsSecondary Burner SolutionHTSHTS - Boiler LeaksHTS VSG-F101 Resists Boiler LeaksHTS - DehydrationHTS LessonsLTSLTSMethanatorMethanator self heatingMethanator Self-heatingMethanator LearningSupport MediaSupport Media - problemsSupport Media - problemsSupport Media use of Si/AlSupport Media Catalyst ProtectionSupport Media - adviceReactor loadingReactor overloadingReactor loadingReactor LoadingPriorities When Things go WrongExample exotherm and actionDepressurization vs PurgingDepressurizationDepressurizationPurgingPurgingConclusions