New patented split flow technology increases the capacity of catalytic reformer heaters at a fraction of the cost of traditional revamps. Furnace Improvements has installed this technology in four reformer heaters at US refineries. This technology has also been used in several other heaters and one of the main benefits is lower pressure drop at increased capacity thus saving your pump or compressors.
2. Catalytic Reforming Units
Catalytic Reforming Unit is an important unit in most
refineries
It converts Straight Run Naphtha from Low Octane to
High Octane in Presence of Hydrogen
The reaction occurs in the presence of catalyst.
The reaction is endothermic in nature.
The reaction is carried out in 3 or 4 stage reactors.
Feed needs to be heated in the charge heater and then to
the interheaters before reactors.
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3. Catalytic reforming units initially
operated at very high pressure and
over the last 50 years the pressure has
gradually reduced from 1000 psig to
almost 50 psig.
Feed volume increases substantially
as the pressure goes down.
Typical pressure drop across each
stage is only 3-4 psi.
Pressure drop is very critical as it
determines recycle gas compressors.
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4. Catalytic Reforming Heaters
Most of the heaters have charge in the radiant
section only
Inlet all vapor, large manifolds provided
Low pressure drop required, multiple passes
High inlet temperature 850-900 F, outlet temperature-
950-1050 F
Convection section has waste heat recovery
Mostly steam generation –bfw preheating, steam
generation and steam superheater
Some have stripper and stabilizer reboilers coils
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5. Construction
Most heaters are natural draft
configuration
Tall stack providing draft in the
radiant section
Air preheating also installed in
some heaters
Typical heat flux
15,000-20,000 Btu/hr.ft2
Tubes are single fired or double
fired
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Convection Section
Stack
Damper
6. Most Clients
want to
Increase
Heater Duty
Clients are want to increase the
capacity of their units
Increase in charge rate means increase
of pressure drop in the heater
Limited in pressure drop and cannot
push more charge
Limited in firing rate/permit limit
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7. Conventional Approach
Increase tube size to reduce pressure drop
Upgrade tube metallurgy to increase TMT limits
Both options require complete radiant section
retubing including manifold
Increase heat transfer area in radiant section
Extend existing radiant section
Add new radiant section
Both these options are extremely expensive
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Process Feed In
Process Feed Out
Waste Heat
Recovery Unit
1,600°F
750°F
250°F
750°F
1000°F
8. Conventional Approach to Increasing Capacity
Extend radiant cell and add more radiant coils & burners
Provide additional radiant cells with new coils and burners
H-20
H-21
H-22
H-20
(NEW)
H-21
(NEW)
H-21
(NEW)
H-20 H-21 H-22
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10. Split Flow* Fired Heater
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*Patented
Feed In Feed Out
450 °F 600 °F
Radiant Section
Convection
Section - I
1,650 °FFlue gas 3,200 °FFlue gas
1,650 °FFlue gas
500 °F
Convection
Section- II
750 °FFlue gas
Flue gas
Flue gas
Split Flow in
Split Flow out
450 °F 600 °F
500 °F
11. Reformer Heater - Split Flow
Radiant Section
Parallel Passes
Heat 70% of process feed
Convection Section
Heat 30% of Process Feed
Waste heat recover
• HC Reboiler
• Steam Generation Service
Pressure drop is maintained
11
Process Feed In Process Feed Out
Split
Flow in
Split Flow Out
Waste Heat
Recovery Unit
1,600°F
1,100°F
250°F
400°F
12. Reformer Heater – Flexible Split Flow
Radiant Section
Parallel Passes
Heat 70% + of process feed
Convection Section
Heat up to 30% of Process Feed
Waste heat recovery
• HC Reboiler
• Steam Generation Service
Pressure drop is kept same even
at increased charge rate.
www.heatflux.com
Split Flow with Flexibility
13. Split Flow Technology - Advantages
Low Cost Solution for:
Increasing Capacity
Improving Efficiency
Lower Pressure Drop
Lower Revamping Cost
Flexible Operation
Maximum Process Duty
Maximum Steam Generation
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14. Case Study 1
Three stage catalytic reformer ( reactor) unit
First cell – Feed heater, Rest 3 cells- interheater
Feed- Mixture of Naphtha and Recycle gas
Inlet Temperature- 842-990 °F
Outlet Temperature-1010 °F
Inlet Pressure-231 psig
Outlet Pressure- 228 psig
Pressure drop /stage- 3 psi
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15. Revamp Objectives
Improve Efficiency
Stack temperature was 1100 ºF
No steam generation
No air preheater
Gas prices touched
$10/MSCF
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16. Arrangement - Original Heater
Process flow before revamp
StackStackStack
Stabilizer
Btms
Stabilizer
Btms
Stripper Btms
Stripper Btms
To Plat. RX To Plat. RX
From Plat. RX.
To Plat. RX
From Plat. RX
Stripper Btms
From Plat.
RX
To Plat. RX
Stripper Btms
BURNERS
428°F
840°F
459°F
1010°F
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17. Reformer Heater Conventional
Revamp
Increase heat transfer surface in
convection section
Pressure drop – more than twice
of existing
Large size piping requirement
Larger convection sections
Increased stack height
High cost ($6 Million) Reformer Heater
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18. Split-Flow Arrangement
Split Flow Technology Design
StackStackStack
Burners
#1 In
#1 Out
In
#2 In
#2 Out
#3 In
#3 Out
#4 In
#4 Out
In
Out
Out
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19. Heater Data Comparison
Heater after revamp
Reformer Heater Data Comparison
Item Units Before After
Capacity BPD 18,500 24,000
Heat Duty MMBtu/hr 158 194.5
Heat release MMBtu/hr 234 225
Stack temp. °F 1,092 478
Efficiency % 67.5 86.6
Fuel savings $/annum 5.8 Million
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20. Case Study-2
Process heating-all Radiant
Steam Generation in Convection
Natural Draft
Firing rates were very high
Heater efficiency lower than design
value by 10% to 15%
Stack temperature -650℉ (320 ℉
higher than design)
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21. Radiant Section
3 Cells
52/56/48 tubes in cells 1/2/3
P22 tubes
Inverted U tubes
Single fired design
Bottom inlet/outlet
2.5 inch tubes at 5 inch pitch
Total -23 Burners (7 , 9 and 7 in cell 1/2/3)
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22. Convection Section
Steam Generator Bank
BFW Preheater Bank
Steam Generation: 53,650 lbs/hr@300 psig
8 tubes per row
Eleven rows
Two future rows
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23. Revamp Objectives
Increase heater capacity from 12,000 to
18,000 BPD
Improve thermal efficiency
Maintain NOx emissions
Improve Reliability
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24. Proposed Process Heat Duties (MMBtu/hr)
at 18000 BPD
Heater Section
Existing Heat
Duty
Proposed
Duty
Extra Duty
Required
70-H-1 27.7 37.5 9.8
70-H-2 33.4 44.7 11.3
70-H-3 22.9 30.9 8.0
Stem Gen. 51.6 47.8 -
Total Process 84 113.1 29.1
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29. Proposed Scheme Advantages
25-30% process feed of Cells 1 & 2 is heated in split flow coils
Heater to be operated at two modes:
Normal operation/Maximum process absorbed duties
Dry run operation/Maximum steam generation
To maximize steam production, process absorbed duties reduced
Split flow coils are run dry to shift convection heat duties for steam
generation
It gives flexibility in steam production and process duties as per
requirement
No change in firing rates
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30. General Advantages of FIS
Flexible Split Flow Technology
Improved Capacity and Flexible Operation
Higher Efficiency
Lower Pressure Drop (process)
Lower Firing Rate
Lower Fire Box Temperatures
Lower Radiant Heat Fluxes
Lower TMT
Lower Turnaround Time
Lower Installation Cost
www.heatflux.com
www.heatflux.com
31. Furnace Improvement Services Inc.
Low Cost Solutions for Fired Heaters and Boilers
1600 Hwy 6 South Ste. 480
Sugar Land, TX 77479
Tel: (281) 980-0325
www.heatflux.com
Thank you very much.
Questions and Comments are welcome.