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Heat transfer phase changes, evaporators
Rudolf Žitný, Ústav procesní a zpracovatelské techniky ČVUT FS 2010
HEAT PROCESSESHP8
Heat transfer at phase changes (boiling and condensation). Evaporation and evaporators. Powerpoint presentation of evaporators (falling, climbing film, multiple effects, vapour recompression). Mass and enthalpy balances. Boiling point temperature and its elevation. Design of thermal vapour recompression (Laval nozzle and Ts diagram). Vacuum cooling.
HEAT transfer condensationHP8
Dropwise condensation
Film condensation
Duchamp
HEAT transfer film condensationHP8
Film condensation (Nusselt)
2 2
( ) GL
T T gq x dm dx d
h
2
2
3 2( ) ( )
2
u y yu y
3 u
g
gravity Viscous force at wall
Transversal parabolic velocity profile and balance of forces
Transversal linear temperature profile, heat and mass fluxes
2 3
3
gm u
2 3 24
4GL GL
T g T gdx d x
h h
Thickness of film determines the heat transfer coefficient
2 3
4( )4GLh g
xTx
Tw
Ts=Tw+T
x
dx
dmMass flow rate of condensed steam
Gravity acting in the flow direction
increases
The following analysis holds only for laminar films (Re<1800). It is usually sufficient, because majority of practical cases are laminar.
HEAT transfer film condensationHP8
41.13 cosc
2 3
4
0
1( ) ( )
4
LGLh g
L x dx cL TL
Enthalpy balancing of a condenser requires mean value of heat transfer
The coefficient c is theoretically c=2/32=0.94 but experiments indicate that the actual value should be about 20% higher, therefore c=1.13
c=0.725
Horizontal pipe4
0.725c
N
Inclined wall N-rows of horizontal pipes
See also M.N.Ozisik: Heat transfer, a basic approach, McGraw Hill, 1985
The increased film thickness
decreases heat transfer
HEAT transfer dropwise condensationHP8
Kakac S.: Boilers, evaporators, and condensers, Wiley 1991
D.W. Tanner, C.J. Potter, D. Pope, D. West: Heat transfer in dropwise condensation—Part I The effects of heat flux, steam velocity and non-condensable gas concentration International Journal of Heat and Mass Transfer, Volume 8, Issue 3, March 1965, Pages 419-420, IN5, 421-426
=liquid-solid
Dropwise condensation (Schmidt) yields much higher heat
transfer coefficients than the film condensation, however special smooth or hydrophobic coatings (large contact angle and very low surface energy of wall) of heat transfer surfaces must be provided.
Gold plated surface
Schmidt, E., Schurig, W. and Sellschop, W., Versuche uber die kondensation von wasserdampf und film und tropfenform. Tech. Mech. Thermodynamiks, Berlin,1930, 1, 53-63.
M. ABU-ORABI: Modeling of heat transfer in dropwise condensation. Int. J. Heat Mass Transfer. Vol. 41, No. 1, pp. 81-87, 1998
HEAT transfer dropwise condensationHP8
H.M.Steinhagen: Smart surfaces for improved heat exchangers. Institute for Thermodynamics and thermal engineering, University of Stuttgart (presentation)
HEAT transfer pool boilingHP8
Nukyama curve (q-TSAT) see A.Bejan, A.Kraus: Heat transfer handbook. Willey 2003
Boiling crisis of the first kind
HEAT transfer pool boilingHP8
m
LSCNu PrRe
1 3/2
,D
NuL
b
,Du
ReL
LbL
.a
PrL
L
Nucleate (pool) boiling Rohsenow (1952)
Exponent m is 0,7 for all liquids with the exception of water (m=0). The coefficient CLS depends upon the combination surface-liquid (tables see Özisik (1985)) and for
the most common combination steel-water CLS=0,013.
Db is the Laplace constant characterizing diameter of bubble ( )bL G
Dg
)(
12
12)(
3
GLGL g
DD
gD
All parameters are related to liquid L
uL - velocity of liquid surface
LLG L
qu
h
Interpretation of Db follows from the equilibrium of surface stress and buoyancy forces
Rohsenow W.M., Trans.ASME, Vol.74,pp.969-975 (1952)
HEAT transfer boiling onsetHP8
.D
ppDD
)pp(b
bbb
b
4
4
2
Pressure difference pb –p can be calculated from the temperature difference using
Clausius Clapeyron equation
( )b LG G LG
SAT G L SAT SAT
p p h hdp
T dT v v T T
Substituting into the balance of forces gives the final result4
.SATb
G LG SAT
TD
h T
The nucleate boiling (bubble boiling) regime is optimal for boilers or evaporators. How to specify its onset (or the level of superheating necessary for bubble formation on the heat transfer surface)?
pb corresponds to saturated steam temperature at
Tw=TSAT+TSATp corresponds to saturated
steam temperature TSAT
-surface tensionDb diam. of a microcavity on heat transfer surface
Balance of forces: overpressure – surface tension
HEAT transfer boiling crisisHP8
Bubble flow regime ends at such a high intensity of evaporation that a more or less continuous layer of vapor is formed and creates a thermal barrier between the heat transfer surface and liquid. Critical heat flux
1/4( ) .krit LG G L Gq c h g
Theoretical solution Zuber (1958) predicts coefficient c=0,131 , experimental data suggest little bit greater value c=0,18 , Rohsenow (1973). The relation for critical heat flux shows that the boiling crisis can be delayed by increasing pressure (and therefore density G) or by acceleration pressing liquid layer towards the heat transfer surface
(this is utilised in centrifugal evaporators).
Theoretical prediction of boiling crisis is based upon stability analysis of a liquid layer (thickness H2) sitting above the light layer of vapor (H1). A small disturbance of initially planar interface increases area of interface (and therefore potential energy of surface tension W ) but at the same time decreases gravitational potential energy Wg. At the stability limit (neutral stability) the differential of the total potential energy is zero, This condition determines wavelength of disturbance causing disruption of continuous layer, and location of steam jets breaking through the liquid layer (it can be shown that the distance of these parallel jets is a multiple of the Laplace constant Db). Following stability analysis of these steam jets, based upon variation of potential energy of surface tension and kinetic energy, yields the previous expression for the critical heat flux.
HEAT transfer flow boilingHP8
Flow boiling in vertical pipes is characterized by gradual changes of flow regime and the vapor quality x increase along the pipe
, ,L SAT
LG
h hx
h
Enthalpy of liquid at saturation
temperature
Vapor quality x<0 means subcooled liquid, vapor quality x=0 liquid at the beginning of evaporation, x=1 state when all liquid is evaporated and x>1 superheated steam.
Heat transfer by forced convection (e.g.Dittus Boelter)
Nucleate boiling (bubbles), e.g.
Rohsenow correlation
Slug flow
Annular flow (rising film)
Vapor quality is related to the Martinelli’s parameter (ratio of pressure drops corresponding to liquid and vapor)
0,10,50,9( / ) 1
.( / )
GL L
G L G
p z xX
p z x
Vapor quality and Martinelli’s parameter are used in most correlations for convective boiling heat transfer.
HEAT transfer flow boilingHP8
The previous slide introduced two basic characteristics of two phase liquid- vapor flows: vapor quality x and the Martinelli’s parameter X. Their relationship follows from the following reasoning:
Gradient of pressure dp/dz for one phase flow is proportional to (see dArcy Weisbach equation)
21 2
Rem m m
m
p uu
z
Exponent m=0.25 for low Re (Blasius), m=0.2
for high Reynolds numbers
therefore1 2
0,51 22
1 2
1( )
( / ) 1.
( / ) ( )
m m m mmL L
GL L L
m m mG L GG G
G
xp z x
Xxp z x
and you can see that the corresponding exponent of Reynolds number in the correlation for pressure drop is m=0.2. It is obvious that the Martinelli’s parameter is a decreasing function of vapor quality (its value is infinity for liquid).
HEAT transfer flow boiling ChenHP8
Chen (1966) calculates the flow boiling heat transfer coefficient as the weighted sum of nucleate boiling b and the convective heat transfer in liquid film c
cb
,S FZb
.F DBc
0,24 0,75 0,45 0,49 0,79
0,5 0,290,00122 .SAT pL L LSAT
FZLG G L
p cT
h
0,8 0,4 4 (1 )0,023Re Pr , Re ,DB
L L LL L
D M x
D
TP
TPTP
Re,,
Re,,)(ReS
5
7
1067101
10677051
.X,,)X(F ,75401522620
1.25Re ReTP LF
.x
x
)z/p(
)z/p(X
,
G
L
,
L
G,
G
L
1050901
Forster Zuber correlation for nucleate boiling (Chen’s concept was later modified by different correlations for nucleate regime, for example by Rohsenow correlation for pool boiling)
Dittus Boelter correlation for convective heat transfer
Chen J.C.: A correlation for boiling heat transfer to saturated fluids in convective flows. Industrial and Engineering Chemistry, Process design and development, Vol.5, no.3, (1966), pp.322-329
HEAT transfer flow boilingHP8
Chen’s method is probably the most frequently used, but it seems that his correlation overpredicts the effect of nucleation and many modifications were therefore suggested. These modifications replace the Forster Zuber pool boiling correlation by Rohsenow’s correlation and the suppression factor S and the convective enhancement factor F were correlated with other system variables
Kandlikar S.G.: A general correlation for saturated two phase flow boiling heat transfer inside horizontal and vertical tubes. Journal of Heat Transfer, Vol.112, pp.219-228 (1990)
Bennett D.L., Chen J.C.: Forced convective boiling in vertical tubes for saturated pure components and binary mixtures. AIChE J., Vol.26, pp.454-461 (1980)
Shah M.M.: A new correlation for heat transfer during boiling through pipes. ASHRAE Transactions, Vol.82, Part.II, pp.66-86 (1976)
Shah (1976) introduced correlations based upon boiling number Bo, convection number Co (that replaces the Martinelli’s parameter) and Froude number Fr
LG
qBo
G h
0.8 0.51
( ) ( )G
L
xCo
x
G is the mass flux, kg/m2s
Viscosity ratio (see Martinelli’s parameter)
seems to be unimportant
2
2
L
GFr
gD
HEAT transfer flow boilingHP8
Heat transfer correlations for the film condensation (Nusselt) and the flow boiling (Chen) are used in the following Excel program designed for modeling of a climbed film evaporator (Kestner).
Procedure:
Tube is divided to short sections z. At each section (starting from bottom, feed input) are calculated: heat transfer coefficient at outer surface, heat flux, wall temperature, enthalpy change h, steam quality x, Martinelli’s parameter, and heat transfer coefficient using Chen’s method. Temperature dependence of all thermophysical properties is considered.
EvaporatorsHP8
Condenstation of saturated
steam
Evaporation of water (pool or flow boiling)
feed
concentrate
condensate
Saturated steam
Vapours (brüden)
Minton P.E.: Handbook of evaporation technology. Noyes Publ., New Jersey, 1986
fm
HP8
f cm m W fm
Nomenclature
What to do with vapor: 1. It can be condensed in a direct (spray), shell
and tube or plate condensers
2. It can be used for heating the following evaporator unit (multiple effects evaporators)
3. It can be recompressed (by mechanical or thermo-compressor) and used for heating
fm
W
D
cm
f f c cm m
0 0 0
0 0 0
0 ( ) ( ) ( )
f f f c c c v v
f f c c v
m h h m h h W h h kS T
m h m h Wh
f dissolutionm h
Mass balances
Enthalpy balance
dissolution heat
Overall mass flow rate
mass flow rate of dissolved solid
=cc(Tc-T0)
Evaporators
HP8
Natural circulation in short pipes
Climbed film
Robert’s basket Vogelbusch
Kestner
Wiegand Müller
Centritherm
condensate condensatecondensate
condensate
vacuumvacuumvacuum
steam
steam
Circulation pump
condensate
Wiped filmFalling film Centrifugal
POOL boiling prevails Long residence times
Suppressed boiling (flash evaporation) High velocity in HE-low fouling
Short residence times Only for low viscosities Viscous
liquids
Centrifugal forces promote dropwise condensation and increase critical heat flux
External heater Forced circulation
Very small T
Evaporators
HP8
Multistage evaporators (latent heat of vapor is used for the next effect heating)
T1 T2
T1 T2
Counter currentLow viscosity feed flows to the
second stage at lower temperature (advantageous from point of view
of heat transfer).
Co currentHigh viscosity concentrate flows
to the second stage at lower temperature (suitable for heat
sensitive products).
T1>T2 therefore p1>p2 and it is necessary to use a pump
Number of effects 1 2 3 4 5
kg steam/kg of evaporated water 1,1 0,6 0,4 0,3 0,25
Evaporators
HP8
Number of effects is limited by range of temperatures (feed – condensate)
T1-T2 = THE + Tpch + Tp
T1 T2 T3
T1 > T2 > T3
Temperature drop corresponding to pressure
drop (frictional losses). Usually small ~ 10C
Physico chemical elevation of boiling point temperature (solution boils at
elevated temperature). Can be large, depends on concentration
Temperature difference on heat transfer surface (rising film >100C, falling film >40C)
Tpch
Sugar 0.5~3
NaCl 10
NaOH 16
Evaporators
HP8
TI TII
Tf,mf,f
m1,1
mc,c
WI WII
D,TS
kISI kIISII
What is given (it is assumed that the temperature TII is determined by condenser and is the same as the temperature of boiling solution in the second effect and the temperature of product):
Tf mf f – temperature, mass flowrate, mass fraction of feed
TII c – temperature and mass fraction of product
TS – temperature of steam
What is to be calculated (9 variables):
D,WI,WII – mass flowrates of steam and vapours
m1,mc – mass flowrates of solution from the 1st and 2nd effect
1- mass fraction of solution after 1st stage
TI –temperature of boiling solution in the 1st effect
kISI, kIISII- heat transfer surfaces in both effects
1 1 1
1 1 1
f I f f
c II c c
m m W m m
m m W m m
1 1
1 1
( ) ( ) ( )
( ) ( ) ( )
f f I I S I I I S cond I I S I
II II I II c c II II I I cond II II I II
h m k S T T h m h W D h h k S T T
h m k S T T h m h W W h h k S T T
Mass balances Enthalpy balances
1st stage
2nd stage
There exist only 8 equations for 9 parameters – one of them can be selected (for example boiling temperature in the first stage T I).
This degree of freedom can be used for optimisation (for minimisation of the heat transfer surface or consumption of steam).
Optimisation of a two effects evaporator
Evaporators
HP8
Design of a two effect co-current evaporator can be implemented in Excel program
Select substance and boiling point elevation
Specify temperature of
steam and feed
CALC starts calculation
Heat transfer surface will be
result
Select temperature in the first effect TI
Evaporators
Evaporators MVRHP8
MVR Mechanical Vapor Recompression
AC
D
Root’s blower
Condensate injection
F=1.8C+32
BTU=1.054 kJpsi=6.9 kPa
It would not be a good idea to use superheated steam for
heating, because will be too small. Saturated steam and condensation is achieved by
water injection
Evaporators TVRHP8
TVR Thermal Vapor Recompression
1
5
2
Thermocompressor
.hhu 454 2
.hhu 313 2
1 3 1 2 4.m u m m u
3 1 32
1 4 5 4
1 1.e
u h hmf
m u h h
1
11
1 2 221
55 25
22
11
1 1 1.1
1
k
k
pe k
p k
pTc T T pT
fTc T T
pT
p
The most important equation is the momentum balance (mixing chamber)
Entrainment ratio fe (mass flowrate of entrained
vaports to the mass florate of motive steam) follows from the momentum balance
Power R.: Steam jet ejectors for the process industries. Mac Graw Hill, New York, 1994
Evaporators TVRHP8
Power R.: Steam jet ejectors for the process industries. Mac Graw Hill, New York, 1994
Design diagram for TVR
Motive steam presure
Suction pressure
Discharge pressure
Previous analysis determined only the entrainment ratio . To complete the TVR design it is necessary to calculate the mass flowrate of motive steam through the Laval nozzle (given inlet pressure). Laval nozzle is characterised by converging and diverging section and the mass flowrate depends only upon the cross section of throat (the smallest cross section S*) where the speed of sound is achieved.
To determine the flow rate m1 as a function of S* and the inlet pressure p1 it is necessary to solve the complete velocity and pressure profiles along the Laval nozzle.
Evaporators TVRHP8
TVR Thermal Vapor Recompression
1
5
2
Thermocompressor
2 1/ef m m
Evaporators TVRHP8
Mixing chamber
Laval nozzle
Diffuser
Speed of sound
Motive steam
Suction
Thermocompressor and Laval nozzleUnknown profiles along the Laval nozzle: p(x), v(x)-or density, T(x), u(x)-velocity, and h(x), together 5 unknowns
Available equations:
pv=RT - state equation
pv=p1v1 - isoentropic flow (without friction)
dh=-du2/2 - Bernoulli equation
dh=cpdT
By selecting any of the parameters, for example the pressure p, it is possible to calculate all other variables, for example the velocity u
2 2 2 2p p
pdv vdpdu dh c dT c
R
v and dv is to be eliminated (expressed in terms of p)
1/ 1/1 11 1( ) ( )
p p dpv v dv v
p p p
2 1/ 1/1 11 1
2( ( ) ( ) )pc p pdp
du v v dpR p p p
By integration we obtain St.Venant Wanzel equation
12
1 11
2 (1 ( ) )1
pu p v
p
Ideal gas!
Evaporators TVRHP8
Mass flowrate is independent of axial coordinate1 1 2 1
11 1 1 1
1 1 1 1 1
( ) ( ) 2 ( ) ( )( ) ( ) ( ) ( ) 2 1 ( ) .
1 1
pp z p z p z p zm u z S z z S z S z p
p p p p
2 1 ** *
1*1
2 12 1 * ** * 1 11 1
2 1
0.22
11
dPm P P
dzmdS d
dz dz pp P PP P
Introducing dimension pressure P*=p(z)/p1 the throat geometrical constraint (minimum cross section S) is
,P* 1
1
2
2 1 1
1 1 1* *1 1
1 1 1
2 2 2 2.
1 1 1 1
pm S S p
zS*
Solution of this (algebraic) equation is and corresponding mass flowrate
H2O molecule riding inside a Laval nozzleHP8
zS*
0
1
2
3
4
5
6
7
00.10.20.30.40.50.60.70.80.91
p(z)/p1
S(z
)
S=1/(2*kappa/(kappa-1)*(A3 (̂2/kappa)-A3 (̂(kappa+1)/kappa)))^0.5)2 1
1 1 11 1
2 ( ) ( )( ) / .
1
p z p zS z m p
p p
H2O molecule riding inside a Laval nozzleHP8
zS*
Slow, nice, eliptic ride, clear view
Approaching speed of sound, view is misty
Speed of sound and still accelerating, Molecule is blind, nothing is seen (only the rear mirror view is clear)
Collision with different pressure at outlet of Laval nozzle (wrong design, of course not by our students)
Mass flowrate through a gap with cross section S at subsonic
flow
Evaporators St Venant WanzelHP8
St Venant Wanzel equation is quite useful and not only for the Laval’s nozzle design. It is applied for example for estimation of an evaporator or a condenser leakage
2 1
1 1 11 1
2.
1
p pm S p
p p
1
1
2
1
p
p
1
1
1 1 1
2.
1m S p
p
p1
Evaporator chamber operating at underpressure
Leakage at sonic flow (choking). Mass
flowrate is independent of vacuum level p.
Vacuum cooling LIQUIDSHP8
Evaporation is also used for rapid cooling of food materials. Material containing water (liquid solutions, but also porous solids like flowers, vegetables, meat) can be cooled down by evaporation of water at a decreased pressure. Assuming uniform temperature Tf(t) of the cooled material the enthalpy balance can be written as
Foam separator
Condenser
Vacuum pump
cooker
Condensatepump
Heatingjacket
ff pf LG
dTM c m h
dt
Mass flow rate of evaporated water
M. Dostal, K. Petera: Vacuum cooling of liquids: mathematical model. Journal of Food Engineering 61 (2004) 533–539
conduction Convection (n is mass flux)
Area of liquid surface
There still exist controversial opinions concerning interpretation of thermal and mass transfer resistances at surface
Vacuum cooling WATERHP8
Technical realization is similar to vacuum evaporators, only without heating of evaporated liquid. Jet pumps (steam ejectors) are usually used.
Example: GEA Wiegand GmbH, 2-stage steam jet cooling plant of compact design, cooling 44 m3/hr of water from 30 to 10 °C.
Spray cooling WATERHP8
Cooling ponds JETE
3[ ( ) ( )]LG wA wA A
p
dTh T T
dt r c
Vacuum cooling MEATHP8
Relatively new vacuum cooling technology is applied also to porous solids, for example meat.
The visualised cross-section of the cooked meatL. Wang, D.-W. Sun / International Journal of Refrigeration 25 (2002) 862–871
Mathematical modelling is usually based upon FK equation for heat transfer
Mass transport of vapour is expressed in terms of pressure P Heat flux
D.-W. Sun, L. Wang / Journal of Food Engineering 77 (2006) 379–385
There exists doubt about this approach. It was objected that this model doesn’t recognize moving front between the boiling and diffusive regions. T.X. Jin, L. Xu / Energy Conversion and Management 47 (2006) 1830–1842
Mass flux Evaporation rate
Evaporators papersHP8
K.R. Morison, Q.A.G. Worth, N.P. O’dea Minimum Wetting and Distribution Rates in Falling Film Evaporators Food and Bioproducts Processing, Volume 84, Issue 4, December 2006, Pages 302-310
Falling film evaporators are used extensively in the food industry for their ability to process heat sensitive liquids. A coherent liquid film is required to maintain heat transfer efficiency and minimize fouling. It is likely that most evaporator fouling occurs after film breakdown as the substance within the evaporator dries out. The minimum flow rate required to maintain a film is known as the minimum wetting rate which is defined as the minimum mass flow rate per unit circumference. In this work, minimum wetting rates were determined in a 1 m long, 48 mm internal diameter, vertical, stainless steel tube. Water and aqueous solutions of glycerol, alcohol and calcium chloride were used. These substances were chosen so as to give a wide range of properties such as viscosity (0.5–39 mPa s), density (950–1410 kg m-3), surface tension (35–90 mN m-1) and contact angle (64–980). In a separate set of experiments, the minimum flow rate required to distribute liquid and completely wet the top of industrial evaporator tubes was measured using a range of sucrose solutions. The tube wetting results obtained fitted a dimensionless power law relationship well. Surface tension and contact angle had a strong influence on the wetting rate but viscosity and density were found to have very little effect. The minimum flow rates for distribution were found to nearly always exceed the minimum wetting rates showing that more attention needs to be given to distributor design.
Nii S.et al: Membrane evaporators. Journal of membrane science, 201 (2002), 149-159
Almost the same result can be derived from the Weber
number limit2
2u
We
Evaporators papersHP8
Susumu Nii, R. Selwyn Jebson, E. L. Cussler Membrane evaporators Journal of Membrane Science, Volume 201, Issues 1-2, 31 May 2002, Pages 149-159
We have built and tested a flat-sheet membrane evaporator for removing water from dilute feed streams likemilk and orange juice. The energy for the water’s evaporation comes from steam channels next to the feed channels, so that the operation differs sharply from other forms of “membrane distillation”. The membrane evaporator retains flavors effectively. Because it has an overall vapor phase mass transfer coefficient of about 1 cm/s, it is only 68% efficient: only about 0.68 kg water is evaporated per kg steam condensed. This efficiency should be over 95% for a membrane which is 10 times more permeable.
Evaporators papersHP8
S. Sharma, G.P. Rangaiah, K.S. Cheah Multi-objective optimization using MS Excel with an application to design of a falling-film evaporator system Food and Bioproducts Processing, Available online 9 February 2011
An Excel-based MOO (EMOO) program is developed based on the elitist non-dominated sorting genetic algorithm (NSGA-II) and tested on benchmark problems. It is then applied for MOO of design of a falling-film evaporator system, consisting of a pre-heater, evaporator, vapor condenser and steam jet ejector, for milk concentration. The EMOO program gave well-distributed Pareto-optimal solutions for the MOO problems tested. Design equations and results for two bi-objective optimization problems are presented and discussed.
Evaporators papersHP8
Tarif Ali Adib, Bertrand Heyd, Jean Vasseur: Experimental results and modeling of boiling heat transfer coefficients in falling film evaporator usable for evaporator design Chemical Engineering and Processing: Process Intensification, Volume 48, Issue 4, April 2009, Pages 961-968The aim of this paper is to describe the variation laws of the boiling heat transfer coefficient (h) versus the main process parameters, using a pilot scale falling film evaporator as found in many food industries. Sugar solutions at different concentrations are used as a model of Newtonian liquid food. The studied parameters affecting boiling heat transfer coefficient (h) in the falling film evaporator are: the dry matter concentration XDM (or Brix for sugar solution), the evaporating temperature (L) or pressure (P) taking into account the boiling point elevation (BPE), the heat flux or the temperature difference between the heated surface and boiling liquid temperature () and the specific mass flow rate per unit of perimeter length ( ). The nature of heated surface is kept constant (stainless steel) and the effect of the emitted vapor velocity is not taken into account in our study. The variations of h with or , are given for pure water and sugar solutions at different concentrations (10%, 30%, 50% and 70%), and interpreted in relation with the two boiling regimes (non-nucleate and nucleate). The transition between non-nucleate regime and nucleate regime has also been visually observed. The critical specific mass flow ( cri) for water and sugar solution at dry matter concentration 50% has been studied.
Variation of h as a function of temperature difference at P = 1010mbar and = 0.56 kg s−1 m−1 for pure water and sugar solution X = 10%, 30%, 50% and 70% DM.
Evaporators papersHP8
Xianchang Li, Ting Wang, Benjamin Day: Numerical analysis of the performance of a thermal ejector in a steam evaporator Applied Thermal Engineering, Volume 30, Issues 17-18, December 2010, Pages 2708-2717
Ejectors have been widely used in many applications such as water desalination, steam turbine, refrigeration systems, and chemical plants. The advantage of an ejector system lies in its extremely reliable operation due to the complete absence of moving parts. However, the performance depends on a number of factors, among which the flow channel configuration/arrangement is critical. To improve the performance of an existing thermal compressor in a steam evaporator, a comprehensive study was conducted in this paper with a main focus on the sensitivity of performance to the geometric arrangement. Numerical simulation was employed to investigate the thermal-flow behavior. The performance is measured by the entrainment ratio, i.e., the secondary (suction) flow rate from a vapor plenum over the primary steam jet flow. It is observed that any downstream resistance will seriously impede the suction flow rate. In addition, the entrainment ratio is sensitive to the location of the jet exit, and there is an optimum location where the primary flow should be issued. A well-contoured diffuser can increase the entrainment ratio significantly. However, the size of suction opening to the plenum is less important, and a contoured annular passage to guide the entrained flow shows little effect on the overall performance. Based on the numerical results the steam entrainment rate of the best case in the confinement of the current study is approximately 430% of the jet flow rate, while some cases with mediocre design can only produce an entrainment of 24% of the primary jet flow.
Fluent
HP8
EXAMHP8
Phase changes
Evaporators
Thermocompressors
What is important (at least for exam)HP8
T
w Ts=Tw+T
xdx
dm
Mass flow rate of condensed steam
2 3
4( )4GLh g
xTx
Nusselt correlation for film condensation
m
LSCNu PrRe
1 3/2
( )bL G
Dg
Rohsenow correlation for pool boiling
Laplace constant Db is used as a characteristic dimension in Nu and Re
What is important (at least for exam)HP8
Condensation of saturated steam
(Nusselt correlation)
Evaporation of water (pool or flow boiling).
Use Rohsenow or Chen correlations
feed
concentrate
condensate
Saturated steam
Vapours (brüden)
f cm m W
f f c cm m
0 0 0 0 0 0
dilution heat
0 ( ) ( ) ( )f f f c c c v v f f c c vm h h m h h W h h kS T m h m h Wh
Overall mass balance
Mass balance of solid
Enthalpy balance
What is important (at least for exam)HP8
.hhu 454 2
.hhu 313 2
1
5
2
Thermocompressor
Recompression of vapours by thermo-compressor (that is driven by Laval nozzle)
Laval nozzle
Mixing chamber
Laval nozzle
Diffuser
Speed of sound
Motive steam
Suction
1
1
1 1 1
2.
1m S p
13
1
0.53 for air=0.58 for steam
2
1
p
p
Supersonic flow for pressure ratio
Mass flowrate is independent of outlet pressure at supersonic flow
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