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Pilot-scale CFP Commissioning: Creative Problem Solving and Lessons Learned
Katherine Gaston
tcbiomassplus2019
October 8, 2019
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NREL | 2
Staged Multi-Scale Evaluation Improves Research Efficiency
Catalyst: 1g
Biomass: 25 mg/run
Microscale Reactor
Uses/Purpose:• Rapid catalyst screening• Preliminary product analysis
(no condensed oil)• Batch experiments• Mechanistic insight
• Catalyst evaluation with continuous biomass feed
• Assess operating conditions• Full product/yield analysis• Extended time on stream• Fixed/Fluidized bed (not
representative of riser)
• Process evaluation / integration with industrially-relevant riser
• Assess operating conditions compared to lab-scale
• Co-processing of biomass and petroleum feeds (liq. and gas)
• Evaluation of process operability / uptime
• Identification & assessment of scale-up challenges & impacts
• Generate significant product quantities
R-Cubed (Pilot Scale)DCR (Small Pilot Scale)Laboratory Scale Fluid/
Fixed Bed Reactor
Process and catalyst evaluation at multiple scales:• Improves research efficiency, thus reducing cost• Provides data that is directly transferrable to industry partners• Allows for a tiered catalyst and process development approach
500g
0.5 kg/h
2kg
3 kg/h
100kg
20 kg/h
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NREL | 3
TCPDU Process Flow Diagram
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NREL | 4NREL | 4
Challenges / Creative Problem Solving
• Design Constraints
• Measuring & controlling catalyst flow rate
• Pressure & level control
• Plugging in exit lines
• Air regeneration – complete coke combustion for catalyst efficiency
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NREL | 5
Design Constraints
• Must have built-in flexibility• Ceiling height limit
– Must account for thermal expansion
• Floor loading limit (Techlok flanges)
• BPVC: limited to 6-in. diameter pipe
• Highly fluidizable catalyst (Zeolite)
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NREL | 6
R3 Process Flow Diagram
4-inRiser
AirRegen. (FBR)
SteamStripper
3-inTransferRiser
Gas Exits
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NREL | 7
R3 Process Flow Diagram
Catalyst Level measured by DP
Regen. DP
Stripper DP
Riser DP
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NREL | 8
How to Measure Catalyst Mass Flow
0
5
10
15
20
25
30
35
12:30 13:00 13:30 14:00
Cat
alys
t Le
vel,
kPa
Time
• Loaded 5 kg shots of catalyst
• 1 kg = 0.64 kPa at 60 kPa
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NREL | 9
How to Measure Catalyst Mass Flow
0
5
10
15
20
25
30
35
12:30 13:00 13:30 14:00
Cat
alys
t Le
vel,
kPa
Time
• Loaded 5 kg shots of catalyst
• 1 kg = 0.64 kPa at 60 kPa
y = 0.64x + 13.42R² = 1.00
0
5
10
15
20
25
30
35
0 5 10 15 20 25 30
Cat
alys
t Le
vel,
kPa
Weight catalyst loaded, kg
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NREL | 10
R² = 0.994
R² = 0.998
R² = 0.999
0
50
100
150
200
250
0.0 0.1 0.2 0.3 0.4 0.5 0.6 0.7C
alcu
late
d C
atal
yst
Flo
wra
te, k
g/h
Riser DP, kPa
HIGH MID LOW
Catalyst mass flow required for kinetics
• Timed the transfer of catalyst from one FBR to other
• Simulated high/mid/low process gas flows with N2
ሶ𝑀 = ∆𝑃𝑠𝑡𝑎𝑟𝑡 − ∆𝑃𝑒𝑛𝑑 ×1 𝑘𝑔
0.64 𝑘𝑃𝑎×
1
∆𝑡
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NREL | 11
Controlling catalyst flow via slide valves
• First generation: temperature at Riser exit (TE709B) controlled catalyst flow
– Difficult due to thermal mass of riser & external heaters (thermocouple not sensitive to catalyst flow)
• Next generation: keeps catalyst flowrate constant, as measured by DP across riser (PDIT700)
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NREL | 12
Pressure Control in Fluidized Beds (Regen/Stripper)
DP across slide valve must be positive
y = 0.97x - 3.81R² = 0.99
0
1
2
3
4
5
6
7
8
0 5 10 15
CYC
LON
E D
P, k
Pa
LEVEL, kPa
3.3 kPa
7.2 kPa
MUST BE GREATER THAN
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NREL | 13
Level Control & Maximum Level in FBRs
0
5
10
15
10:50 11:00 11:10 11:20
Flu
idiz
ed B
ed
Leve
l, kP
a
Regen. St. Stripper
25
50
75
Pre
ssu
re, k
Pa
Regen. Cyclone Outlet
Regen. Headspace
Regen. Level increases as Stripper Level decreases
DP across cyclone inverts
~13 kg of catalyst out cyclone gas exit
Max level in Regenerator plugs
Sidearm
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NREL | 14
Hot Gas Filtration
• Catalyst + water = Mud = Plugged Sidearms = Catalyst out
• Hot Catalyst + water vapor = ok
• Required on ALL exit streams
CRITICAL TO SUCCESS OF OPERATION
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NREL | 15Upsized diameter of entire line
Upgraded exit lines to remove catalyst particles while hot
Added heat exchangers in parallel
Added filtersAddedblowdown
Cyclone moved upstream
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NREL | 16
Insufficient Regen Air
• Initial Design: Coke loading estimated from preliminary results on Bench-scale FBR
• No O2 measured on regen exit
• Limited by reactor geometry:
– Exit line too small diameter
– Too much carryover (elutriation) at higher air flow
0
2
4
6
8
10
12
vol%
CO CO2 O2
0
10
20
30
40
50
60
0 50 100 150
slm
Time (min)
Air flow into reactor
Early experiments, max air 50 slm
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NREL | 17
120, 43
1
10
100
1000
75 100 125 150 175 200 225 250 275
Elu
tria
tio
n R
ate,
kg
/hr
Total Gas Flow, SLPM
Elutriation of Catalyst at Increased Air Flow
Credit: Bruce Adkins (ORNL) (using PSRI models)
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NREL | 18
Add Cyclone Return into Regenerator
• Increased air flow carries over MUCH more catalyst
• Effectively increased Regen. diameter
• Installed cyclone to return catalyst into reactor
• Tricky design: must keep horizontal section of return pipe fluidized
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NREL | 19
Air Regeneration Results
Coke on Catalyst (%C by wt) Insufficient
Regen
Post-stripper, after ~2 hours 0.94%
Post-regen, after ~2 hours 0.66%
Insufficient Regen
Complete Regen
Post-Stripper Post-Regen
Post-Stripper Post-Regen
0
5
10
15
20
20:00 21:00 22:00 23:00 00:00
vol %
CO CO2 O2
Coke on Catalyst (%C by wt) Insufficient
RegenComplete
Regen
Post-stripper, after ~2 hours 0.94% 0.58%
Post-regen, after ~2 hours 0.66% 0.01%
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NREL | 20
Catalyst mass flow rate, which is critical for VPU kinetics,
– can be empirically determined by change in level in fluidized bed reactors,
– then correlated to differential pressure across Riser,
– as long as gas flow rate stays constant
Lessons Learned
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NREL | 21
• Pressure in top of fluidized beds varies linearly with level of catalyst in bed
• D Pressure across Regen. cyclone must be positive
- Flowrate out sidearm must be greater than flow in, or pressure flips and catalyst empties
Lessons Learned
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NREL | 22
DON’T PLUG SIDEARMS
- Don’t overflow fluidized beds
- Filter catalyst particles out while hot (mud plugs lines & is difficult to clean out)
Lessons Learned
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NREL | 23
NEED PLENTY OF O2 FOR REGENERATION
- High-risk to scale up using bench-scale data from dissimilar reactor system
- We mitigated catalyst elutriation out of Regen. by adding a cyclone
- Ideally, disengagement zone (freeboard) keeps catalyst in reactor
- Pure oxygen is dangerous & expensive, but plausible
Lessons Learned
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NREL | 24
Acknowledgements
NREL: Danny Carpenter, Tim Dunning, Chris Golubieski, Rebecca Jackson, Ray Hansen, Matt Oliver, Jessica Olstad, Marc Pomeroy, David Robichaud, Kristin Smith
CCPC: Bruce Adkins, Jim Parks (ORNL)Xi Gao, Bill Rogers (NETL)
DOE Advanced Development & Optimization program (ADO)
10/9 @ 4pm Jessica Olstad (NREL)Co-Processing Catalytic Fast Pyrolysis Oils with Vacuum Gas Oil in a Davison Circulating Riser – Upgrading Track
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www.nrel.gov
Questions?
This work was authored by the National Renewable Energy Laboratory, operated by Alliance for Sustainable Energy, LLC, for the U.S. Department of Energy (DOE) under Contract No. DE-AC36-08GO28308. Funding provided by U.S. Department of Energy, Office of Energy Efficiency and Renewable Energy, Bioenergy Technologies Office. Theviews expressed in the article do not necessarily represent the views of the DOE or the U.S. Government. The U.S. Government retains and the publisher, by accepting the article for publication, acknowledges that the U.S. Government retains a nonexclusive, paid-up, irrevocable, worldwide license to publish or reproduce the published form of this work, or allow others to do so, for U.S. Government purposes.