Qayyum Khan Galfar Engineering & Contracting SAOG, Lead Process Engineer Email: [email protected] Tel.: +968 24525424 GSM-95942025 Fax: +968 24525385 Always remember: "Do not draw conclusions until you know all the facts''
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Qayyum KhanGalfar Engineering & Contracting SAOG, Lead Process Engineer
Email: [email protected] Tel.: +968 24525424 GSM-95942025
Fax: +968 24525385 Always remember: "Do not draw conclusions until you know all the facts''
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Hot In Hot Out
Cold Out Cold In
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Hot In Hot Out
Cold Out Cold In
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.
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Pr.60 bar Temp
201°CPr.1 bar
Temp 15°C Pr.60 bar Temp
50°C
Pr.1 bar
Temp 15°C
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TheThe two fluids flow right angle to each other .two fluids flow right angle to each other .
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Parameters Hot fluid Cold fluid SI units
Mass flow rate M m Kg/s
Inlet temperature T1 t1 C or K
Outlet temperature T2 t2 C or K
Inlet enthalpy H1 h1 J/Kg
Average specific heat C c J/Kg K
Heat flow rate Q Q W
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.t2 Cold.t2 Cold OutOut
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T
H
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Streams Locations Typical values Comments
A Tube –to- baffle <20%
B Main (cross flow) Min. 60% for turbulentflow & 40% for laminar
flow
Should bemaximum
C Bundle –to –shell <10% Add sealing strips
a e-to- e < se ou esegmental baffles
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= tube itch,
d 0 = tube outside diameter,
Ds = shell inside diameter, m,
I B = baffle spacing, m.
Gs= Ws/As
Us= Gs/
,
Ws = fluid flow on the shell side Kg/s
As=cross flow area m 2
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= 2‐
Re= Usde / μUs= Gs/
L= Tube length
Jf= friction factor
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Advantage Advantage-- True countercurrent flow,True countercurrent flow, CanCan handle large Temperaturehandle large Temperaturecrosscross DisadvantageDisadvantage-- Required large plot area.Required large plot area.
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Types of shellTypes of shell-- andand-- tube Heat Exchangerstube Heat Exchangers-- – –
22--UU--TubeTube33--FloatingFloating --headhead
Advantage Advantage-- Can handle high Temp, pressure and flow ratesCan handle high Temp, pressure and flow rates DisadvantageDisadvantage-- vibrationsvibrations
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Advantage- less operating cost, CW saving Disadvantage- High capital cost, more hot fluid outlet T, more plot area
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Advantage- less plot area, T cross, close temp approach m tat on - an e up to ar, , ew ven or
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Advantage- very less fouling, good flow
distribution, true countercurrent Limitation- can handle up to 25 bar, 400 °C,
few vendor
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1.1. Stat ionary HeadStationary Head -- ChannelChannel 14.14. Float ing Head Cover Floating Head Cover
2.2. Stationary Head FlangeStationary Head Flange -- Channel or BonnetChannel or Bonnet 15.15. Floating Head Cover FlangeFloating Head Cover Flange
.. ..
4.4. Stationary Head NozzleStationary Head Nozzle 17.17. Tie Rods & SpacersTie Rods & Spacers
5.5. Stat ionary Tube SheetStationary Tube Sheet 18.18. BafflesBaffles
.. ..
7.7. ShellShell 20.20. Pass Part it ionPass Partition
8.8. Shell Cover Shell Cover 21.21. Vent ConnectionVent Connection
.. e angee ange -- a onary ea na onary ea n .. ra n onnec onra n onnec on
10.10. Shel l FlangeShell Flange -- Rear Head EndRear Head End 23.23. Instrument ConnectionInstrument Connection
11.11. Shel l NozzleShell Nozzle 24.24. Suppor ting SaddleSupporting Saddle
12.12. Shel l Cover FlangeShell Cover Flange 25.25. Lifting LugLifting Lug
13.13. Float ing Tube SheetFloating Tube Sheet
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Δ P D E C
E A S E
F R O M E T
X
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SINGLE &DOUBLE SEGMENTAL BEFFLESSINGLE &DOUBLE SEGMENTAL BEFFLES
PRESSURE DROP IS LESSER FOR DSB THAN THE SSBPRESSURE DROP IS LESSER FOR DSB THAN THE SSB
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Window
Window
PRESSURE DROP FOR NTIW IS LOWER THAN DSB AND SSBPRESSURE DROP FOR NTIW IS LOWER THAN DSB AND SSB
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Preferred for single-phase applications Preferred for condensers and vaporisers
Horizontal Vertical
Baffle cut is the height of the segment removed form the baffle.
Baffle cuts from 15 to 45% are used but 20 to 25 % is optimum generally.
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1 2 BGM
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1:2 BGM
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.t2 Cold.t2 Cold OutOut .t1 Cold.t1 Cold InIn
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-- HTRIHTRI (Heat Transfer Research Inst itute operated by United State)(Heat Transfer Research Inst itute operated by United State)
--
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DESIGN
RATING SIMULATION
CALCULATION
MODE
Heat Trans er Research Institute HTRI Xist software
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FLUID VELOCITY IN BOTH TUBE AND SHELL SIDE
TUBE SIDE HEAT TRANFER COEFFICIENT
SHELL SIDE HEAT TRANSFER COEFFICIENT
SHELL SIDE PRESSURE DROPFLOW-INDUCED VIBRATION
STREAM ANALYSIS
OVER DESIGN
.
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. .
1 Heat exchanger selection guide line EP-2005-5186
2 Fouling resistance to heat transfer equipments DEP-20.21.00.31
3 Shell and tube heat exchangers DEP-31.21.01.30
4- HTRI Manual
5 American Tubular Heat Exchanger Manufactures Association Team standard
6 British standard BS 3274
7 Coulsion and Richardson Volume -1 and 6
8 Shell and Tube Heat Exchanger for General Refinery Services API-660
9 Air-cooled Heat Exchangers for General Refinery services API-661
10 Plate Heat Exchangers for General Refinery services - Part -1Plate and Frame Heat Exchan er
API-662
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60
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To Improve Tube side Heat TransferCoefficient:Decrease number of tubesDecrease number of tubes
Change to larger diameter tubes for laminar flowChange to larger diameter tubes for laminar flow
Decrease tube length for laminar flowDecrease tube length for laminar flow
ange u a oca onange u a oca on
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To ReduceTo Reduce Shell sideShell side Pressure Drop:Pressure Drop:
Increase Baffle Spacing within limitsIncrease Baffle Spacing within limits
Increase baffle cut percentageIncrease baffle cut percentageChange baffle type to double segmental or NTIWChange baffle type to double segmental or NTIWChange shell type from E to J or X Change shell type from E to J or X Increase no. of shellsIncrease no. of shells--inin--parallelparallelDecrease no. of shellsDecrease no. of shells--inin--seriesseriesncrease s e ame erncrease s e ame er
Increase shell nozzle sizeIncrease shell nozzle sizeProvide annular distributorsProvide annular distributors
Change tube layout to square from triangularChange tube layout to square from triangularIncrease tube pitchIncrease tube pitch
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Decrease Baffle Spacing within limitsDecrease Baffle Spacing within limitsProvide sealin stri s or dumm rodsProvide sealin stri s or dumm rodsDecrease baffle cut percentageDecrease baffle cut percentageChange baffle type to single segmental, if otherwiseChange baffle type to single segmental, if otherwise Apply tight clearances Apply tight clearances
ange s e ypeange s e ypeIncrease no. of shellsIncrease no. of shells--inin--seriesseriesDecrease shell diameterDecrease shell diameterChan e fluid allocationChan e fluid allocation
Change tube layout to triangular from squareChange tube layout to triangular from squareDecrease tube pitchDecrease tube pitchIf shellIf shell--side fluid is clean gas, use fin tubesside fluid is clean gas, use fin tubes
ecrease num er o tu esecrease num er o tu esIncrease number of tube passesIncrease number of tube passes
Change fluid allocationChange fluid allocation
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--Draft : Forced vs. InducedDraft : Forced vs. Induced
Advantages of forced draft
Easier accessibility for maint.
Lower power consumption
Advantages of induced draft
Better air distributionReduced hot air recirculation
Better stack effect
Better protection from the elements
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Process Requirements:-
Exchanger should give satisfactory thermal & hydraulic performance from thestart of operation to shut-down.
-
Exchanger should withstand mechanical stresses during installation, start-up,
- , ,Exchanger also should withstand thermal stresses induced by temperaturedifferences
Maintenance Re uirements:-
Exchanger configuration should be such that it permits
vulnerable to corrosion, erosion or vibration damage.
temperature differences.
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Cost Requirements:-
Exchanger should be most economically designed utilizing the allowablepressure drop as much as possible
Other Requirements:-
m a ons on exc anger ame er, eng , we g , u e spec ca ons ueto client requirements, site requirements, lifting & servicing capabilities orinventory considerations require thorough evaluation.
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a. Overdesign
b. Shell side and tube side
velocity, heat transfer
100o
112,000 kg/h
.
c. Stream analysis40o 70o
75o
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Performing the design for a specified dutyPerforming the design for a specified duty
Hot stream:Hot stream:Flow rate = 112 000Flow rate = 112 000
kg/h = 31.11 kg/seckg/h = 31.11 kg/secTin = 100Tin = 100 °°C, Tout =C, Tout =
°°
100o
112,000 kg/h
Physical propertiesPhysical properties
Cold stream:Cold stream:40o 70o
, ,
= 28.39 kg/sec= 28.39 kg/secTin = 40Tin = 40 °°C, Tout = 70C, Tout = 70
°°
75o
Physical propertiesPhysical properties
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Predicting the performance of a specified heat
exc anger or a g ven se o n e or ou e con ons
Nil overdesignb. Shell side and tube side velocit
heat transfer coefficient and pr.
drop
100o
112,000 kg/h
.
40o ?
?
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Questions: Why are gas htc’sQuestions: Why are gas htc’slow?low?
Are gas htc’s always low? Are gas htc’s always low?
low thermal conductivity, h α k low thermal conductivity, h α k 0.670.67
low densitylow densityPressure drop α GPressure drop α G22/ρ/ρ
Therefore, if ρ is low, G (ρ V) is required to be low.Therefore, if ρ is low, G (ρ V) is required to be low.
Since h α GSince h α G0.80.8 , a low G means a low HTC. , a low G means a low HTC.
I gas pressure s g , ts HTC w e muc g er.I gas pressure s g , ts HTC w e muc g er.
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1.1. SimpleSimple construction, lowconstruction, low
2. Differential expansion not2. Differential expansion notpossiblepossible
. uts e o tu es cannot. uts e o tu es cannotbebe mechanically cleanedmechanically cleanedbut inside tube cleaning isbut inside tube cleaning is
ossible.ossible.1.
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◦◦ Cleaning insideCleaning insidetu estu es s cu ts cu t
◦◦ Low costLow cost
◦◦ bundlebundle
◦◦ Permits thermalPermits thermalexpansionexpansion
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Removable tubeRemovable tubebundlebundle
Permits thermalPermits thermalexpansionexpansion
Tube cleaningTube cleaningpossible inside andpossible inside andoutsideoutside
High costHigh cost
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UU – – Overall Heat Transfer CoefficientOverall Heat Transfer Coefficient
Depends onDepends on
Exchanger configurationExchanger configuration
Operating ParametersOperating Parameters
ou ng ac orou ng ac or
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AIR AIR--COOLED HEAT EXCHANGER COOLED HEAT EXCHANGER
Induced draftInduced draft
OPTIMISE AIR AND WATER COOLINGOPTIMISE AIR AND WATER COOLINGOnly water cooling: both in/out temps low, e.g., 50 C/45 COnly water cooling: both in/out temps low, e.g., 50 C/45 C(Air + water) cooling: inlet temp high, outlet temp. low, e.g., 100 C/40 C(Air + water) cooling: inlet temp high, outlet temp. low, e.g., 100 C/40 C
n y a r coo ng: ot n et an out et temp s g , e.g.,n y a r coo ng: ot n et an out et temp s g , e.g.,
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Multiple shells in seriesMultiple shells in series
-- Handle temperature crossHandle temperature cross--
-- Reduce penalty due to temp.Reduce penalty due to temp.
profile distortionprofile distortion
-- en s e s are requ re anyway,en s e s are requ re anyway,examine putting them in series.examine putting them in series.
-- Advantageous when MOC Advantageous when MOC
varies with temperaturevaries with temperature
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Determine operating envelope
Eliminate types that can not meet envelope
ze ea exc anger an anc ary equ pmen ers)
Eliminate types that don't fit any shape and weight restrictions
Estimate Capex, Opex and potential deferments for each remaining type
Select type with the required availability and lowest life cost cycle cost
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ssume
Calculate MTD
Find A from Q = U.A.MTD
From tube OD and length, determine no. of tubes, tube pitchand no. of tube passes.
Size nozzles
Determine shell ID and assume baffle type/spacing/cut
Run rating program and see results for velocities, streamanalysis, pressure drop, overdesign and vibration
Re-run until design is optimum
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Process Requirements(Thermal and Hydraulic)
Mechanical Requirements(Mechanical &Thermal stress)
Cost Requirements (Capex+Opex)
Other Requirements
I. L/D Ratio
II. Weight
I. Lifting and servicing capabilities
7/22/2019 Process Presentation Shell and Tube Heat Exchanger Galfar
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Q‐In which service impingement plates shall be used?
‐ u u v y u
abrasive particles .
Q‐why we are using log mean temperature difference instead of normal difference?Ans – As the temperature of fluids changes along the length of the heat exchanger
so the properties of the fluids also changes with the length .LMTD gives the most
accurate result in compression of ∆T.
Qayyum KhanGalfar Engineering & Contracting SAOG, Lead Process Engineer
Email: [email protected] Tel.: +968 24525424 GSM-95942025
Fax: +968 24525385 Always remember: "Do not draw conclusions until you know al l the facts''