materi alat penukar kalor_teknik mesin ujb
TRANSCRIPT
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Alat Penukar Kalor
(Heat Exchanger)
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Tujuan Pembelajaran
• Mengenal jenis-jenis alat penukar kalor
• Mengetahui jenis APK yang paling baik untuk
aplikasi industri yang ada • Mengerti parameter kunci dalam desain APK
• Mampu mengestimasi ukuran dan harga APK
• Memiliki latarbelakang untuk menggunakansoftware komersial untuk mendesain APK
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Pendahuluan Heat Exchangers
Untuk apakah Alat Penukar Kalor?
Jenis-Jenis Alat Penukar Kalor
Bagaimana Alat penukar kalor
diklasifikasikan?
Dasar-dasar perencanaan Alat Penukar
Kalor?
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Contents
• Mengapa kita membutuhkan APK
• Konstruksi APK
• Macam-macam APK
• Proses Desain APK
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Apakah fungsi APK itu ?
• Untuk memperoleh aliran fluida padatemperatur yang tepat untuk proses berikutnya
•Untuk mengkondensasikan uap
• Untuk menguapkan fluida
• Untuk memanfaatkan panas buang
•Untuk pembangkitan daya
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Typical crude oil distillation
E2
E1
E3
E4
E5 E6
E2
E5
Storage
Kerosene
Desalter
Top pump
around
Top pump
around
Naphtha
and gases
Kerosene
Furnace
Reduced crude
Light
gas oil
Heavy
gas oil
Reduced
crude
Heavy gas oil
Light gas oil
Bottom pumparound
D i s t i l l a t i o n t o w e r
Bottom
pump
around
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Geothermal Power cycle
Feedwater
heater
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Nuclear Power Plant
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Ocean Thermal Energy Conversion
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Heat utilities
• Hot utilities – Boiler generating service steam (maybe a combined
heat and power plant)
– Direct fired heaters (furnace)
– Electric heaters
• Cold utilities
– Cooling tower (wet or dry) providing service cooling
water
– Direct air-cooled heat exchanger
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Contoh sebuah APK
Bundle for shell-and-tube exchanger
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KATEGORI UTAMA ALAT PENUKAR KALOR
Heat exchangers
Recuperators Regenerators
Wall separating streams Direct contact
Kebanyakan Alat Penukar Kalor memiliki 2 aliranfluida, hot dan cold , tetapi beberapa memilikilebih dari dua aliran fluida
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Recuperators dan regenerators
Recuperative
Has separate flow paths for eachfluid which flow simultaneouslythrough the exchangertransferring heat between thestreams
Regenerative
Has a single flow path which the hotand cold fluids alternately passthrough.
Rotating wheel
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Compactness
• Can be measured by the heat-transfer area per unit volume or by channel size
• Conventional exchangers (shell and tube)have channel size of 10 to 30 mm givingabout 100m2/m3
•
Plate-type exchangers have typically 5mmchannel size with more than 200m2/m3
• More compact types available
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Compactness
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Double Pipe
Simplest type has one tube inside another - inner
tube may have longitudinal fins on the outside
However, most have a
number of tubes in the outertube - can have very many tubes
thus becoming a shell-and-tube
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Shell and Tube
Alat Penukar Kalor tipe shell and tube yang biasadigunakan pada industri proses
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Shell-side flow
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Baffle
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Complete shell-and-tube
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Plate-fin exchanger
• Made up of flat plates (parting sheets) andcorrugated sheets which form fins
• Brazed by heating in vacuum furnace
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Cooling Towers
•Large shell with packing at the bottom over whichwater is sprayed
• Cooling by air flow and evaporation
• Air flow driven by forced or natural convection
• Need to continuously make up the cooling water lost by evaporation
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Exchanger specification
• Heat load (duty) along with the terminal
temperatures of the streams
• Maximum pressure drop each streams – liquids - 0.5 bar
– gases/vapours below 2bar - 10% of inlet pressure
• Design pressures and temperatures
• Size/weight constraints
• Standards to apply
– General standards like ISO, TEMA, ASME, API etc – Companies own standards
• Other requirements
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The designer must supply an exchanger which
• Meets the stated specification
• Has reasonable initial costs and operating
costs (most exchangers are bought on the basis of the cheapest tender)
• Has a reasonable lifetime
– no damaging vibration – no thermal fatigue
– no unexpected fouling or corrosion
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Pemilihan Heat Exchanger
Choosing the best exchanger for a
given process application
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Langkah-langkah
• “Coarse filter” – Buang Jenis Alat Penukar Kalor yang
tidak memenuhi ketentuan tekanan dan
temperatur operasi, fluid-materialcompatibilitas, kondisi termal yang
extrem
• “Fine filter” – Estimasi Harga
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“Coarse filter”
• Use information on next few slides to reject
those exchangers which are clearly out of
range or are otherwise unsuitable• The information is summarised in the table
• At this stage, if in doubt, include the
exchanger (poor choices are likely to turnout expensive at the “fine filter” stage)
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Point-point utama
•
Tube /pipa dan cylinders dapat menahan tekananyang lebih besar dibanding dengan plates
• Jika APK dapat dibangun dengan material yang
bervariasi, berarti anda dapat menentukan metal
yang dapat tahan terhadap temperatur yang extremdan fluida-fluida yang korosif
• APK yang khusus hanya memiliki supplier yang
sangat sedikit, waktu pengiriman barang yang
lebih lama dan harus diperbaiki oleh orang yang
sangat ahli.
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Thermal effectiveness
T T T T
in out
in in
1 1
1 2
, ,
, ,
Stream temperature rise divided by the
theoretically maximum possible
temperature rise
T 1 ,in T 1 ,out
T 2 ,out T 2,in
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Double PipeTipe APK ini adalah yang paling simpel, memiliki satu tube di
dalam dan satu tube pada bagian luar, Tube paling dalam bisa
memiliki sirip secara longitudinal pada bagian luarnya
Walaupun demikian terdapat
pula jenis APK ini yangmemiliki beberpa tube didalam
tube luarnya.
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Double pipe
• Ukuran Normal
– 0.25 to 200m2
(2.5 to 2000 ft2
) per unit – Note multiple units are often used
• Built of carbon steel where possible
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Advantages/disadvantages of double-pipe
• Advantages
– Easy to obtain counter-current flow
– Can handle high pressure
– Modular construction
– Easy to maintain and repair
– Many suppliers
• Disadvantage
– Become expensive for large duties (above
1MW)
S f d bl i
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Scope of double pipe• Maximum pressure
– 300 bar(abs) (4500 psia) on shell side – 1400 bar(abs) (21000 psia) on tubeside
• Temperature range
– -100 to 600oC (-150 to 1100oF) – possibly wider with special materials
• Fluid limitations
– Few since can be built of many metals
• Maximum = 0.9
• Minimum DT = 5 K
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Shell and tube
• Size per unit 100 - 10000 ft2 (10 - 1000 m2)• Easy to build multiple units
• Made of carbon steel where possible
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Advantages/disadvantages of S&T
• Advantages
– Extremely flexible and robust design
– Easy to maintain and repair
– Can be designed to be dismantled for cleaning
– Very many suppliers world-wide
• Disadvantages
– Require large plot (footprint) area - often need
extra space to remove the bundle
– Plate may be cheaper for pressure below 16 bar
(240 psia) and temps. below 200oC (400oF)
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Scope of shell and tubeEssentially the same as a double pipe
• Maximum pressure – 300 bar(abs) (4500 psia) on shell side
– 1400 bar(abs) (21000 psia) on tubeside
•Temperature range – -100 to 600oC (-150 to 1100oF)
– possibly wider with special materials
• Fluid limitations
– Few since can be built of many metals
• Maximum = 0.9 (less with multipass)
• Minimum DT = 5 K
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Heat exchanger costing - “fine filter”
• Full cost made up of
– Capital cost
– Installation cost
– Operating cost
• The cost estimation method given here is basedonly on capital cost - which is the way it is often
done
• Note: installation costs can be as high as capital
cost except for compact exchangers
• Installation cost considerations can predominate
on offshore plant
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Quick sizing of heat exchangers
We estimate the area from
DT aDT b
A Q
U T
DWhere
D D
D D D
D D
T F T
T T T
T T
T m
m
a b
a b
ln( / )
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FT correction factor
• This correction accounts for the two streams not
following pure counter-current flow• At the estimation stage, we do not know the detailed
flow/pass arrangement so we use
– F T = 1.0 for counter flow which includes most compact and
double-pipe
– F T = 0.7 for pure cross flow which includes air-cooled and
other types when operated in pure cross flow (e.g. shell-and-
tube)
– F T = 0.9 for multi-pass
– F T = 1.0 if one stream is isothermal (typically boiling and
condensation)
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Estimating U
• This may be estimated for a given exchanger typeusing the tables
• These tables give U values as a function of Q/DT (the significance of this group will become clear
later)
• Example: high pressure gas cooled by treated
cooling water in a shell-and-tube, where
Q/DT = 30 000 W/Kgives U = 600 W/m2K
• This includes typical fouling resistances
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Estimating cost
• This has often been done by multiplying the
calculated area, A, by a “cost per unit area” • But, when comparing exchangers, U and A
vary widely from type to type. It is also
difficult to define A if there is a complicatedextended surface.
• Note, from our basic heat transfer equation
UA = Q / DT
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Steps in calculation
•Calculate
DT ln and hence estimate
DT
• Determine Q/DT
• Look up C value from table
– To determine C at intermediate Q/DT , use logarithmic
interpolation - see next slide
• Calculate exchanger cost from - Cost = C (Q/DT )
• Taking the last shell-and-tube example, C = 0.4.
Hence, Cost = £ 0.4 X 30 000 = £12 000• Make sure that you take account of footnotes in
tables
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Logarithmic interpolation
C ln C C C V V
V V
exp ( ) ln( / ) ln( / )
ln( / )1
1 2 1
1 2
ln(C 1)
ln(C 2)
ln(C )
ln(V1) ln(V) ln(V2)
Where the V s are the values of Q/ T. V 1 and V 2
are the values either side of the required value V
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Desain Termal
Alat Penukar Kalor
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Harga Lokal dan harga rata-rata
• “Overall” artinya dari “the hot side” ke “ the
cold side” termasuk semua termal resistan
• Titik khusus pada alat penukar kalor adalah local
• Jadi kita memiliki lokal, overall coefficient
LOKAL
KESELURUHAN ALAT PENUKA KALOR
mT mT T AU Q
T U q
D
D
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Q = U A DTk
Thot
Tcold
1 1 1
U r
yr
cold
cold w
w
hot
hot
yw
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Definisi dari harga rata-rata (mean values )
Dari slide sebelumnya
Bandingkan dua sides
Q
T U A
dQT
UdA
T
m
m T
Q AT T
D
D
1 1
D DT Q
dQ
T m T Q
U A
UdAmT AT
1
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Kasus Khusus dimana Ts linear terhadap Q
• Eqn. integrates to
give log. mean
temperaturedifference - LMTD
DT a
D D D D
D DT T
T T
T T m LM
a b
a b
ln( / ) DT b
Q
T e m p e r a
t u r e
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Pararel Flow
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Counter Flow
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Cross Flow
M lti h
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Multipass exchangers
• Untuk single-phase duties,Faktor correction teoritis,
F T , sudah diturunkan (lihar
referensi)
• Harga F T Kurang dari 1
• Jangan Merancang untuk F T
kurang dari 0.8
Q
T e m p .
T 1
T 2
t 1
t 2
D DT F T m T LM
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Thermal effectiveness
T T T T
in out
in in
1 1
1 2
, ,
, ,
Stream temperature rise divided by the theoretically
maximum possible temperature rise
T 1 ,in T 1 ,out
T 2 ,out T 2,in
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Tube layouts
• Typically, 1 in tubes on a 1.25 in pitch or 0.75 in
tubes on a 1 in pitch• Triangular layouts give more tubes in a given shell
• Square layouts give cleaning lanes with close pitch
pitchTriangul
ar
30o
Rotated
triangul
ar
60o
Squar e
90o
Rotate
dsquare
45o