Open access peer-reviewed chapter - ONLINE FIRST

A Review on Convective Boiling Heat Transfer of Refrigerants in Horizontal Microfin-Tubes: A Typical Example

By Thanh Nhan Phan and Van Hung Tran

Submitted: April 26th 2021Reviewed: August 20th 2021Published: September 29th 2021

DOI: 10.5772/intechopen.100024

Downloaded: 23

Abstract

Understanding the Heat transfer performance of refrigerant for convective boiling in horizontal microfin tube and smooth tube is place an importance role on the designing of evaporator, the main equipment on refrigeration system. Reviewing the general concept especially the theory of boiling in the tube, the formation of the flow pattern map, the calculating procedure for heat transfer coefficient and pressure drop during boiling process of refrigerant in microfin tube. Besides, a typical example will be presented more detail in step by step to define the heat transfer coefficient and pressure drop for one working condition to estimate the data results without doing experiments.

Keywords

  • convective boiling
  • microfin tube
  • flow pattern
  • heat transfer coefficient
  • pressure drop

1. Introduction

The boiling process of Refrigerant is very important on the designing of evaporator on the refrigeration system. The optimization of heat exchanger about the size, weight and heat transfer performance is the main problem. In order to solve this problem, microfin tube is the ones should pay attention.

To understand the boiling process, the pattern of flow should be known during the boiling of refrigerant. With the type of flow patterns and the general map of flow pattern for boiling in smooth tube is very clear it is concluded fully stratified, slug flow, stratified wavy flow, intermittent flow, annular flow, dryout and mist flow. While for microfin is still unclear especially for the newest refrigerant. With the method of Rollmann et al. [1], the pattern of boiling in microfin tube could be classify in such fully stratified flow, stratified wavy flow, the combination of slug and stratified wavy flow, helix flow, annular flow. In order to build this method, Rollmann et al. was updated the method of Wojtan et al. [2] which was introduced for smooth tube. Those method based on the mathematical model of two phase stratified the geometries of flow from [3] to determine the geometries of flow. Besides that, in recent years some new method to build the map for flow pattern are still updated from Zhuang et al. [4] and Yang et al. [5].

In case of internal flow, the main difficulty, concerning to the evaluation of the heat transfer coefficient and friction factor, is related to the flow regimes (distribution of liquid and vapor in a cross-section). As it is easily understood, the main heat transfer mechanism changes if, at the wall, there is liquid, vapor, both of them, droplet impingement, bubble formation and so on. Every flow regime requires a specific analytical description and appropriate criteria to state if it occurs or not. As quality, liquid mass flux and vapor mass flux change along a duct, several flow regime onsets along a duct in the presence of heat transfer. The criteria are usually represented in two-dimensional diagrams called flow pattern maps. The internal geometry of the enhanced tubes and the thermal properties of the fluid affect the distribution of the phases in the cross section.

It is obviously that the outstanding performance of heat transfer in microfin tubes for boiling is valuable to consider without introducing excessive penalization in the pressure drop. Those have been proven in so many experimental researches which are published in recent years and also presented in the paper of Phan et al. [6]. Besides, with the correlations for heat transfer of evaporation process on microfin tube are published would be introduced in this chapter are come from Thome et al. [7], Cavallini et al. [8], Yu et al. [9], Yun et al. [10], Chamra et al. [11], Wu et al. [12], Rollmann and Spindle [13].

Also for the pressure drop of two phase flow, some correlations were built for both evaporation and condensation Choi et al. [14], Goto et al. [15], the others used for separated purposed. Some particular pressure drop correlations could be mentioned for evaporation Rollmann and Spindler [13], Wongsa-Ngam et al. [16] and Kuo et al. [17].

About this problem, Phan Thanh Nhan [18] focused on the experimental test to determine flow pattern, heat transfer and pressure drop for both boiling and condensation in microfin tube for two kind of Refrigerants R134a and R1234ze.

This chapter is demonstrated in convective boiling of refrigerant in horizontal microfin tube. Flow pattern map, heat transfer coefficient and pressure drop during boiling process would be presented with the published correlations and taken on working condition for boiling as an example to calculate step by step.

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2. Flow pattern map

In order to draw a map of flow mechanism, there needs to be a classification of different regimes of flow in microfin tube, which relies on flow patterns such as slug, fully stratified, stratified wavy, helix, annular and some regimes are the combination of two or three flow pattern simultaneously happened. To build the map, many parameters have been cleared about geometries of tube, heat flux, mass flux, thermo-physical and thermodynamics properties of fluid, local quality, quality change of boiling processes and define the void fraction, Martineli parameter or also estimate the shape of flow (about the liquid part and vapor part consisted on the position of tube).

Even many different group researches, they also classified the map into some main regimes: bubbly flow, plug flow, slug flow, intermittent flow, stratified flow, stratified wavy flow, annular flow, dry-out regime, mist flow or transition regime, other differences just only the difference name they called for the same regime. Flow patterns in horizontal flows are illustrated in Figure 1. Depend on every single group they have every different name for their classification regimes. Every regime can be described as below:

  • Bubbly flow: due to buoyancy force, gas bubbles focus on the upper part of tube, and normally take place at the high mass flow rate.

  • Plug flow: the individual small bubbles have coalesced to create long bubble, can call the name elongated bubble flow.

  • Slug flow: at high velocity, the wave amplitude is so large which increasing and touching to the top of the tube

  • Intermittent flow: could be defined instead of plug and slug flow

  • Fully stratified flow: at low velocity, liquid and vapor are completely separated, interface between them is smooth

  • Stratified wavy flow: the formation of wave in the interface between liquid and vapor of stratified flow when the velocity of gas rises up

  • Annular flow: when the liquid forms around perimeter of the tube, vapor flows in the core separate and make the annular shape of liquid flow.

  • Dry-out regime: at higher quality of vapor, thinner of annular liquid flow will be disappeared, at the top of tube becomes dry first, then gradually spread around tube to bottom

  • Mist flow: liquid will be entrained to the core of gas phase as small droplets

  • Transition regime: on the changing pattern regimes, it is not clear to define which pattern they are, so that the name transition regime is used.

Figure 1.

Flow regime for boiling from Collier and Thome 1994 [7].

For micro-fin tube, those the last few years, some other detailed regimes are called for flow patterns:

  • Helix flow: the formation of helix flow due to the helical structure of microfin where the liquid flow helically through out

  • Slug + helix flow: on the regime, slug and helix flow are spontaneously occurred

2.1 The flow pattern map of Rollmann and Spindler

Rollmann and Spindler [1] modified the procedure from Wojtan et al. [2] and introduced their method to build the flow pattern map for boiling in microfin tube as given in below (Figure 2):

Figure 2.

Flow pattern map of Rollmann and Spindle [1].

Void fraction ε: Rouhani-Axelsson correlation

ε=xρV1+0.121xxρV+1xρL+1.181xρLρV0.25GρL0.51E1

Stratified angle θstrat: Biberg correlation [19]

θstrat=2π2π1ε+3π21/3121ε+1ε13ε1312001εε121ε1+41ε2+ε2E2

Geometrical parameters for two phase flow in a circular tube are showed in Figure 3.

ALD=ALD2=A1εD2E3
AVD=AVD2=D2E4
hLD=0.51cos2πθstrat2E5
PiD=sin2πθstrat2E6

Figure 3.

Geometrical parameters of stratified flow in circular tube.

Transition between stratified flow and stratified wavy flow:

Gstrat=4μLgρLρVρVε1ϵS2x21x1/3+C5;S2=0.02844;C5=22.9kg/sm2.E7

Transition between slug flow and stratified wavy flow:

Gslug=16AV3˜gDρLρVx2π212HL˜12C624π2S12HL˜2FrWeL+10.5+C7;FrWeL=σgD2ρL;S1=5.889;C6=1.015;C7=53.35kg/sm2,E8

where HL is liquid height, HL˜=HL/Dand AV is gas phase area, AV˜=AV/D.

Transition between stratified wavy flow and helix flow:

GSW=16AV3˜gDρLρVx2π212HL˜12C620.5+C7,forx0.3;C6=0.8441;C7=0kg/sm2.E9

For x ≥ 0.3 the transition curve in Eq. (3) was applied. With x < 0.3 the linear equation With the lope of transition curve from x ≥ 0.3.

Transition between slug/helix flow and helix flow:

GSlughelix=16AV3˜gDρLρVx2π212HL˜12C620.5+C7;C6=1.754;C7=84.79kg/sm2.E10

Transition between helix flow and annular flow:

Gslug=16AV3˜gDρLρVx2π212HL˜12C624π2S12HL˜2FrWeL+10.5+C7;S1=57.71;C6=1.772;C7=25.39kg/sm2.E11

The classification of the regimes on the map:

ConditionsRegime
G < GstratStratified flow
G > Gslug and G < GswStratified wavy flow
G < Gslug and G < GswStratified wavy/slug flow or slug flow
G < Gslug-helixSlug/helix flow
G < GhelixHelix flow
G > GhelixAnnular flow

2.2 The flow pattern map of Zhuang et al.

The flow pattern map of Zhuang et al. [4] in Figure 4 was form from the model of Kim et al. combine with their experimental data for R170 with working range of saturation pressures from 1.5 MPa to 2.5 MPa on mass flux from 100 kg/m2s to 250 kg/m2s. The map was built in the terms of dimensionless weber number We and Mattinelli parameter Xtt.

Figure 4.

Flow pattern map of Zhuang et al. [4].

Four transition curves were presented to draw the transition line to separate five different zones, each zone is named as smooth annular, wavy annular, transition, slug, plug.

Marttinelli number: Xtt

Xtt=1xx0.9ρGρL0.5μlμG0.1E12

Determine Weber number (We) based on the Reynold range of liquid flow:

ReL=G1xDμLE13

With ReL1250

We=2.45ReG0.64SuG0.31+1.09Xtt0.0390.4E14

With ReL>1250

We=0.85ReG0.79Xtt0.157SuG0.31+1.09Xtt0.0390.4μGμL2ρLρG0.084E15
SuG=ρGσDμG2E16

The transition line between patterns:

Smooth-annular to wavy-annular flow:

We=29.25Xtt0.27E17

Wavy-annular to transition flow:

We=18.91Xtt0.33E18

Transition to slug flow:

We=9.62Xtt0.35E19

Slug to plug flow:

We=4.38Xtt0.45E20

2.3 The flow pattern map of Yang et al.

The map of Yang et al. [5] introduced two maps in Figure 5, one map is presented for plug flow, slug flow, other is separate between slug flow and annular flow. Two transitions line on two difference maps as a function of Martinelli parameter Xtt, the transition lines based on three dimensionless numbers K1, K2, K3 which depended on the inertia force, surface tension force, shear force, gravity force and evaporation momentum force.

Figure 5.

Flow pattern map of Yang et al. [5].

Dimensionless number K1 is a ratio of evaporation momentum force with inertia force:

K1=evaporation momentum forceinertia force=qhlv21ρvG2ρl=qhlv2ρlρvE21

Dimensionless number K2 is a ratio of evaporation momentum force with surface tension force:

K2=evaporation momentum forcesurface tension force=qhlv21ρvσD=qhlv2DσρvE22

Dimensionless number K3 is a ratio of shear force with gravity force:

K3=shear forcegravity force=μlρlGDρlρvgD=μlGρlρvρlgD2E23

The transition line from plug to slug and slug to annular based on function of Xtt:

Plug to slug:

K=KPS=K10.8385K21.1388K30.3993=14.87Xtt1.269E24

Slug to annular:

K=KSA=K10.2963K20.3620K30.1941=0.3044Xtt0.5671E25
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3. Two phases heat transfer coefficient in boiling

Due to the changing phase during the convective boiling, the proportion of liquid and vapor is also changed, which affected the mechanism of boiling. In order to indicate the boiling heat transfer coefficient, the nucleate boiling and convective boiling are considered. More detailed about the methodology, the boiling number and some other factors are presented in the method of each group authors as below:

3.1 The correlation of Han et al.

Base on the basic form of boiling heat transfer coefficient, Han et al. [20] was established their correlation from the updating their experimental result. The experimental data results were done on the working range of mass flux G = [100; 250] kg/m2s, heat flux q = [11.76; 52.94] kW/m2, temperature T = [−5, 8]°C with fluid R161 for microfin tube with 6.34 mm average inside diameter, 15° helix angle, 30° fin angle, 0.1 mm fin height, 65 number of fins.

Heat transfer coefficient of two-phase flow:

hr,tp=Fhr,l+Shr,nbE26

Convective heat transfer with convective fin factor:

hr,l=ERBhlE27
hl=0.023Rel0.8Frl0.4kldiE28
ERB=1+2.64Rel0.036edi0.212pdi0.21β90o0.29PrL0.02471/7E29
Rerl=G1xdiμlE30

Heat transfer of nuclear boiling

hr,nb=55Pr0.12log10Pr0.55M0.5q0.67E31

The new function of F and S

F=1+aBo1.16+b1Xtt0.86E32
S=11+cFdRel1.17E33

In which a = 7196.741; b = 1.5135; c = 2.703; d = 1.94,

where e: microfin height; p: axial pitch from fin to fin; β: helix angle; N: number of fin; Pr: reduced pressure.

3.2 The correlation of Rollmann and Spindler

The model of Rollmann and Spindler [13] for heat transfer coefficient was derived with total 1614 data points experiment for refrigerant R407C on microfin tube at 8.95 mm fin root diameter, 0.24 mm fin height, 15° Helix angle, 25° Apex angle and 55 fins. Heat flux q = [1000; 20000] W/m2, mass flux G = [25; 300] kg/m2s, saturation temperature Tsat = [−30; 10]°C,

The model defined by Nuselt number:

NuxBoRePr=C4C1Pr2+C2Re2/3lnBo+C3xC1Pr2+C2E34

where

C1=3.7; C2=0.71; C3=12.17; C4=1.2

Bo=qGhv; Re=GDFRηL; Pr=ηLCp,LλL; Nu=hDFRλL

DFR: diameter at fin root

Working range: Bo >5.1837.10−6; Pr > 2.2828

3.3 Correlation for boiling model of Chamra and Mago

The semi empirical model of Chamra and Mago [11] was derived based on 380 collected data points from available literature.

Working range of collected databaseThe range of microfin tube on database
Fluid: R134A, R12, R22, R123,
Ts = [0.6; 15]°C
q = [0; 64.3] kW/m2
x = [0.05; 1]
G = [25; 410] kg/m2s
di = [7.92; 15.88] mm (inner tube diameter)
nf = [21; 100] number of microfin per unit length
e = [0.12; 0.38] mm (fin height)
β = [10; 90]° (apex angle)
γ = [3; 30]° (helix angle)
L = [0.3-4.88] m
th = [0.28-0.51] mm (tube wall thickness)

Developed on the basic of Cavallini model

htp=hpb1.5160Xtt1.1610F11.7640+hlΦRx2.6220BonwFrV0.2158F20.5927F30.0582E35
hpb=55PR0.12log10PR0.55M0.5q0.67E36
q=G.ifg.xE37
Xtt=1xx0.9ρvρl0.5μlμv0.1IfXtt>1thenXtt=1E38
F1=0.01di1E39
hl=0.023kldiRel0.8Prl0.4E40
Φ=1x+2.63xρlρv120.8E41
Rx=2enf1sinβ/2πdicosβ/2+11cosγE42
Bonw=gρLdi8σnfE43
FrV=G2ρv2gdiE44
F2=0.01di1E45
F3=100G1E46

3.4 The correlation of Yun et al.

Using the database with 749 data points of five different refrigerants to create a generalized correlation for boiling heat transfer in horizontal microfin tubes.

Heat transfer coefficient of two-phase flow:

htp/hl=C1BoC2PsatdiσC3+C41XttC5GfμlC6RelC7PrlC8δfC9E47
Bo=qGhlvE48
hl=0.023Rel0.8Frl0.4kldiE49
Rel=G1xdiμlE50
δ=dr1ε4E51
ε=xρG1+0.121xxρG+1xρL+1.181xρLρG0.25GρL0.51E52
Xtt=1xx0.9ρvρl0.5μlμv0.1E53
Coefficients of correlationThe range of database
C1 = 0.009622
C2 = 0.1106
C3 = 0.3814
C4 = 7.6850
C5 = 0.5100
C6 = −0.7360
C7 = 0.2045
C8 = 0.7452
C9 = −0.1302
di: maximum inside diameter of a microfin tube
dr: diameter of a microfin tube at fin root
d = [8.82; 14.66] mm (inner diameter)
f = [0.12; 0.381] mm (fin height)
spiral angle = [16; 30]°
G = [50; 637] kg/m2s
q = [5; 39.5] kW/m2
Ts = [−15; 70]°C
R22, R113, R123, R134A, R410A

3.5 The correlation of Cavallini et al.

The correlation of Cavallini et al. [8] produced for not only microfin tube but also for cross groves tubes with 643 data points collected from available literatures.

Heat transfer coefficient of two phase flow:

α=αnb+αcvE54

Nucleate boiling component:

αnb=αcooperS.F1di=55PR0.12log10PR0.55M0.5q0.67S.F1diE55
S=A.XttB=A.1xx0.9ρGρL0.5μLμG0.1BIfXtt>1thenXtt=1E56

F1(di): function of fin tip tube diameter

F1di=dodiCE57

Convective term:

αcv=λLdi.Nucv,smooth tube.RxS.Bo.FrT.F2di.F3GE58
Nucv,smooth tube=NuLOΦ=0.023GdiμL0.8PrL1/31x+2.63xρLρG1/20.8E59
Rx=2hng1sinγ/2πdicosγ/2+11cosβE60
Bo=gρLdi8σngE61
Fr=uGO2gdiE62
F2di=dodiVE63
F3G=GoGZE64

uGO: velocity of gas phase with total flow rate

ABCSTVZdoGo
G < 500 kg/m2s1.360.360.382.14−0.150.590.360.01100
G ≥ 500 kg/m2s1.360.360.382.14−0.210.590.360.01100

Working range:

Geometry of tubes:
di = [3; 14.3] mm (minimum inside tube diameter)
ng = [30; 112] (number of grooves)
h = [0.1; 0.35] mm (fin height)
γ = [20; 120]° (apex angle)
β = [4; 30]° (spiral angle)
L = [0.2; 3.67] m
Experimental Data bank: 643
Fluid: R134A, R12, R22, R123, R125, R32
Ts = [−6.6; 48]°C
q = [3; 82] kW/m2
x = [0.05; 0.9]
G = [90; 600] kg/m2s

PropertyUnitValuePropertyUnitValue
Tsat[°C]5Psat[MPa]0.2593
ρL[kg/m3]1225.5λL[W/m-K]8.14E-02
ρV[kg/m3]13.9λV[W/m-K]1.20E-02
νL[m3/kg]8.16E-04μL[Pa-s]2.53E-04
νv[m3/kg]7.18E-02μV[Pa-s]1.14E-05
hLV[kJ/kg]181PrL[−]4.102
CpL[kJ/kg-K]1.319PrV[−]0.86
CpV[kJ/kg-K]0.898σ[N/m]1.15E-02

Table 1.

Properties of R1234ze.

3.6 The correlation of Thome et al.

The model was derived to predict the microfin with the test data for R134a, R123, mass flux G = [100; 500] kg/m2s, quality x = [0.15; 0.85] and heat flux q = [2; 47] kW/m2

h=Emfhnb3+ERBhcv31/3E65
hnb=55PR0.12log10PR0.55M0.5q0.67E66
hcv=0.0133Rel0.69Prl0.4λl/δE67
Relfilm=4G1xδ1εμlE68
δ=dr1ε/4E69
ε=xρG1+0.121xxρG+1xρL+1.181xρLρG0.25GρL0.51E70
Emf=1.89GGref23.7GGref+3.02E71
ERB=1+2.64ReD0.036edr0.212pdr0.21β90o0.29PrL0.02471/7E72
ReD=G1xdrμlE73
p=πdr/NtanβE74
Gref=500kg/m2sE75

where e: microfin height; p: axial pitch from fin to fin; β: helix angle; N: number of fins; dr: root diameter

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4. Pressure drop

4.1 The correlation of Choi et al.

The model form of Choi et al. [14] was carryout from Pierre 1964 model with 831 data pointed collected from NIST database with 626 data point for boiling and 205 data points for condensation for some different fluids R134a, R22, R125, R32, R407C, R410A and R32/R134a. Those data points derived with test section has 8.92 mm root diameter, 9.52 mm outside diameter, 18° helix angle.

Total pressure drop:

pL=pfL+pmL=G2fvtp,out+vtp,indh+vtp,outvtp,inLE76

Twophasefriction factor:

f=0.00506Reh,LO0.0951Kf0.1554E77
Reh,LO=Gdh/μlE78

Hydraulic diameter:

dh=4Accosβ/n.SpE79

Two phase number:

Kf=x.hlvgLE80

“Specific volumes of the two-phase fluid, vtp,out and vtp,in, are quality-weighted sums of the vapor and liquid specific volumes at either the outlet or inlet of the tube”

4.2 The correlation of Goto et al.

Model of Goto et al. [15] derived from experiment of R41A and R22 for both boiling and condensation at mass flux G = [200; 340] kg/m2s inside spiral groove tube 7.3 mm mean inside diameter and herring-born groove tube 7.24 mm mean inside diameter.

Frictional pressure gradient:

dPdzf=Φv2dPdzv=Φv22fe,v,GoGx2/ρvdeE81
Φv=1+1.64Xtt0.79E82

Or could be compute based on the liquid phase form

dPdzf=Φl2dPdzl=Φl22fe,l,LoG1x2/ρldeE83
Φl=1+7.61Xtt1.7E84
Ree,v=Gxde/μvDiameter of inner tubedeE85
Xtt=1xx0.9ρvρl0.5μlμv0.1E86
Ree,v2000;=>fe,v,Go=16/Ree,vE87
2000Ree,v2600;=>fe,v,Go=0.000147Ree,v0.53E88
2600Ree,v6500;=>fe,v,Go=0.046Ree,v0.2E89
6500Ree,v12700;=>fe,v,Go=0.00123Ree,v0.21E90
12700Ree,v;=>fe,v,Go=0.0092E91

4.3 The correlation of Wongsa et al.

The correlation for boiling with high mass flux was proposed by Wongsa et al. [16]. Derived from their experimental results for R134a on microfin tube with 8.92 mm inner diameter, saturation temperature Tsat = [10; 20]°C, mass flux G = [400; 800] kg/m2s.

Two phase friction pressure drop

dPdzf=ΦVO2dPdzh,VO=ΦVO22fh,VOG2/ρvdhE92
4fh,VO=1.325lnRxh3.7+5.74Reh,VO0.92E93
Reh,VO=GdhμvE94
Rxh=0.3e/dh0.1+cosβE95
ΦVO2=2.32631.8043XttGgdhρvρlρv0.50.0802E96

4.4 The correlation of Kou and Wang

The correlation of Kou and Wang 1996 [17] was analyzed from their own experimental data results for boiling of R22 and R407C in a 9.52 mm diameter micro-fin tube and a smooth tube at two different evaporation temperatures (6°C and 10°C). The mass flux was between 100 and 300 kg/m2s and the heat fluxes 6 and 14 kW/m2.

dPdzf=0.0254G2xvv+1xvldfrE97
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5. Example

Determine the heat transfer coefficient and pressure drop of refrigerant R1234ze during boiling process inside horizontal microfin tube at 5°C and heat flux 8,62 kW/m2, mass flux 222 kg/m2s. The geometry of microfin tube is 60 number of fins, the inner surface diameter is 8.96 mm, fin height is 0.2 mm, the helix angle and apex angle are 18° and 40°, respectively.

Solve:

At saturation temperature tsat = 5°C of refrigerant R1234ze, thermal properties could be taken in Table 1.

Refrigerant: R1234ze, molar mass: M = 114 g/mol, pcritical = 3.64 MPa

Reduce pressure: pr = psat/pcritical = 0.2593/3.64 = 0.07124

Heat flux: q = 8.62 kW/m2

Mass flux: G = 222 kg/m2s

Microfin tube: N = 60 number of fins, dr = 8.96 mm, e = 0.2 mm, β = 18o; γ = 40°

5.1 Flow pattern map

Apply the flow pattern map of Rollmann and Spindler [1] to present in here. At first, calculate the transition lines between one regime to another as a function of quality x and use the classification of the regimes on the map:

ConditionsRegime
G < GstratStratified flow
G > Gslug and G < GswStratified wavy flow
G < Gslug and G < GswStratified wavy/slug flow or slug flow
G < Gslug-helixSlug/helix flow
G < GhelixHelix flow
G > GhelixAnnular flow

x [−]h [W/m2s]dP/dz. [Pa/m]
0.012807.278.0
0.053640.1248.5
0.104712.6532.1
0.155561.5811.6
0.206234.61115.3
0.256789.21441.7
0.307265.01789.0
0.357689.42155.5
0.408082.12539.5
0.458458.32939.1
0.508831.03352.5
0.559212.83777.6
0.609617.14212.3
0.6510060.34653.8
0.7010564.85099.2
0.7511164.65544.6
0.8011917.85984.8
0.8512938.26412.2
0.9014500.76814.0
0.9517596.57162.5
0.9927601.37331.9

Table 2.

Heat transfer coefficient and pressure drop during the boiling process.

In this case, the flow pattern map for boiling of R1234ze in microfin tube was built at 5 °C saturation temperature, heat flux q = 8.62 kW/m2, with the fixed mass flux G = 222 kg/m2s.

The result map shown in Figure 6, when the mass flux lower than 50 kg/m2s, the flow boiling during the changing phase just only occur at the fully stratified flow. But if working condition at mass flux 200 kg/m2s, at the beginning of boiling process, the quality is still low, the boiling occur at slug/helix flow until the quality reach to 0.15, the helix flow happen, and keep boiling with the helix flow until quality is 0.25, it moves to the annular flow boiling to the rest of changing phase.

Figure 6.

Flow pattern map on microfin tube.

5.2 Heat transfer coefficients

Could take quality x = 0.5 as an example to present the procedure to calculate heat transfer coefficient and pressure drop of boiling refrigerant inside horizontal microfin tube, with the data point of quality x from 0 to 1 can be determined with the same method.

5.2.1 Applied the correlation of Thome et al.

Apply equation from (65) to (75) to calculate heat transfer coefficients as below:

Void fraction

ε=xρG1+0.121xxρG+1xρL+1.181xρLρG0.25GρL0.51
ε=0.513.91+0.1210.50.513.9+10.51225.5+1.1810.59.81x0.01151225.513.90.25222x1225.50.51
ε=0.9266
δ=dr1ε4=8.96.10310.92664=0.00016m
Rel=4G1xδ1εμl=4x222x10.5x0.0001610.9266x0.000253=3931.067
hcv=0.0133Rel0.69Prl0.4λlδ=0.01333931.0670.694.1020.40.08140.00016=3497.97
hnb=55PR0.12log10PR0.55M0.5q0.67=55x0.071240.12log100.071240.551140.586200.67=1507.309
Gref=500kg/m2s
Emf=1.89GGref23.7GGref+3.02=1.8922250023.7222500+3.02=1.75
ReD=G1xdrμl=22210.50.008960.000253=3931.07
p=πdr/Ntanβ=πx0.00896/60tan18o=0.001444
ERB=1+2.64ReD0.036edr0.212pdr0.21β90o0.29PrL0.02471/7=1.43
ERB=1+2.643931.070.0360.00020.008960.2120.0014440.008960.2118o90o0.294.1020.02471/7
ERB=1.43
h=Emfhnb3+ERBhcv31/3=1.751507.3093+1.43x3497.9731/3=8831.04Wm2K

5.3 Pressure drop

5.3.1 The correlation of Goto et al.

Apply equation from (81) to (91) to calculate pressure drop as below:

Frictional pressure gradient:

dPdzf=Φv2dPdzv=Φv22fe,v,GoGx2/ρvde
Xtt=1xx0.9ρvρl0.5μlμv0.1=10.50.50.913.91225.50.50.0002530.00001140.1=0.1452
Φv=1+1.64Xtt0.79=1+1.640x14520.79=1.3571
Ree,v=G.x.deμv=222x0.5x0.008960.0000114=87242.11

Compare Ree,vto get fe,v,Go

Ree,v2000;=>fe,v,Go=16/Ree,v
2000Ree,v2600;=>fe,v,Go=0.000147Ree,v0.53
2600Ree,v6500;=>fe,v,Go=0.046Ree,v0.2
6500Ree,v12700;=>fe,v,Go=0.00123Ree,v0.21
12700Ree,v;=>fe,v,Go=0.0092

With 12700Ree,v=87242.11;=>fe,v,Go=0.0092

dPdzf=Φv2dPdzv=Φv22fe,v,GoGx2ρvde=1.35712x2x0.0092222x0.5213.9x0.00896=3352.52Pam

Apply the same procedure at each data point of quality x of refrigerant from 0.1 to 0.99 to determine heat transfer and pressure drop during the convective boiling. Data results are obtained in Table 2.

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6. Conclusions

This chapter is presented the boiling process of refrigerant in horizontal microfin tube. Those are related to the understanding of flow patterns and the procedure to build some flow pattern maps. Some of new correlations to calculate heat transfer coefficient and pressure drop of refrigerant during boiling process have been presented. Detailed step by step to calculate heat transfer performance for typical example is also introduced. However, this is still not enough for this topic, with the new structure of microfin tubes, new refrigerants, this just only the general method to estimate the value, it should be confirmed by experimental method and create the new correlation to extend the wide range of application working conditions.

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Acknowledgments

We would like to thank Ho Chi Minh City University of Technology (HCMUT), VNU-HCM for the support of time and facilities for this study.

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Thanh Nhan Phan and Van Hung Tran (September 29th 2021). A Review on Convective Boiling Heat Transfer of Refrigerants in Horizontal Microfin-Tubes: A Typical Example [Online First], IntechOpen, DOI: 10.5772/intechopen.100024. Available from:

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