Flow investigation of phase change material (PCM) slurry as a heat transfer fluid in a closed loop...

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INTERNATIONAL JOURNAL OF ENERGY RESEARCHInt. J. Energy Res. (2008)Published online in Wiley InterScience(www.interscience.wiley.com). DOI: 10.1002/er.1478

Flow investigation of phase change material (PCM) slurry as a heattransfer fluid in a closed loop system

L. Royon1,�,y, D. Jacquier2 and P. Mercier2

1Laboratory M.S.C., University Paris Est Marne la Vallee, France2C.E.A Grethe, Grenoble 38054, France

SUMMARY

Aqueous phase change material (PCM) particles are dispersed in an organic phase to constitute a slurry for using as acold heat transfer medium for district cooling in refrigeration and air conditioning industry. The PCM contains 90% ofwater stabilized by a three-dimensional network of polymer. The flow behaviour of the slurry is investigated in a small-scale loop circuit with transparent pipes to allow observation of flow patterns. Data show that pressure drop increaseswith velocity and decreases with temperature, which can be explained by heterogeneities in flow for temperature higherthan 01C and for Reynolds number (based on the properties of the liquid phase) lower than 7000. A homogeneousparticle field is observed for Reynolds number up to 7000, which guarantees a safe operation of the system without theoccurrence of clogging in ducts. For this range of flow, the flow rate and the pump consumption for the PCM slurrydecrease notably for the same heat transportation quantity compared with chilled water. Copyright r 2008 John Wiley& Sons, Ltd.

KEY WORDS: phase change material; rheological characteristics; slurry; pressure drop; flow properties

1. INTRODUCTION

Since Kyoto protocol regulating the emission of

greenhouses gases as hydrofluorocarbons, the

industry of refrigeration is accordingly now

demanding new practical solutions for the produc-

tion and distribution of cold. A promising concept

has been proposed for district cooling systems by

using a slurry of phase change material (PCM) for

the thermal energy distribution through a piping

network to multiple locations where cooling is

required. Such slurries present large apparent

specific heats during the phase change period,

which enhances heat transfer rate between the fluid

and the tube wall. This is a solution to significantly

decrease the mass flow requirements and the pump

consumption of the system.Among different slurries, ice–water slurry is one

of the first PCM suspension used in industrialapplications. The fluid consists of mixtures ofwater (or ethanol/water) and fine ice particles inwhich the size distribution (0.1–3mm) depends on

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45*Correspondence to: L. Royon, Laboratory M.S.C., University Paris Est Marne la Vallee, France.yE-mail: [email protected], [email protected]

Received 30 March 2007

Revised 22 September 2008

Accepted 22 September 2008Copyright r 2008 John Wiley & Sons, Ltd.

UNCORRECTED PROOF

different production methods and the storagemethod. Several studies have been shown thatheat capacity will be increased 2–4 times morethan a traditional monophasic fluid and the size ofthe district cooling machinery can be reducedaccordingly [1–3]. The major economical andtechnical drawback appear through the high costof icemaking equipment and its maintenance.Actually, new research is focused on fluidizedbed heat exchangers as an alternative solution toproduce low-cost ice slurry [4].

An alternative form of ice slurry is considered in

this paper, which consists of particles containing a

water concentration near close to 90% dispersed in

a carrier fluid. Water is introduced, by using a

chemical process, inside a three-dimensional

network of polymer to form PCM particles.

Compared with an ice–water slurry, several

advantages, specific to this slurry, appear in the

absence of an ice generator (a passage, thought to

be a heat exchanger, as evaporator is enough to

reload the slurry in ice), a more significant weight

fraction (420%) by the polydispersity of the

particles and a constant weight fraction in the

circulating pipe.Preliminary work has been made to check their

suitability for district cooling applications. Goodstability under repeated thermal cycling (with alow subcooling phenomenon) confirms thepossibility of using such a fluid as reversible coldstorage [5]. Thermal behaviour in an agitated tankduring a phase change process has been analysed

in a previous study showing that this slurrypresents a great potentiality to accumulate andtransport a high quantity of thermal energy [6].Mass fraction is limited in the range 0.15ofo0.30to allow both good efficiency of the cold storageand the transport of the fluid in a unit includingpumps.

The next step in the project is effective

implementation shown in Figure 1, which runs

with the new secondary fluid. In such a system,

cold energy is generated in a primary cycle and

then transferred to a secondary cooling cycle with a

heat exchanger. The slurry distribute thermal

energy through a piping network to multiple

locations where cooling is required. The optimum

design of the system requires a good knowledge of

flow and heat transfer characteristics of two-phase

slurry, in order to reduce the capital cost, system

size and energy consumption. For such a system, it

appears necessary to know how particles circulate

continuously through a heat transfer flow system

as in a real application. Nevertheless, the

knowledge of the hydrodynamic conditions of

slurries is often difficult mainly for two reasons.

Firstly, rheology is usually complex due to the

presence of sedimentation or creaming phenomena

and interactions of solid and liquid phases. A

suitable flow pattern should be found to obtain

both optimal hydrodynamic conditions and heat

transfer performance. Previous studies on ice

slurries show that turbulent flow is often

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Figure 1. Schematic representation of primary and secondary cooling cycles.

ColoronlineB&W

inprint

L. ROYON, D. JACQUIER AND P. MERCIER2

Copyright r 2008 John Wiley & Sons, Ltd. Int. J. Energy Res. (2008)

DOI: 10.1002/er

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necessary for having a good heat exchange

efficiency [7] and to avoid sedimentation (or

creaming) of particles [8,9]. Secondly, standard

commercial instruments and techniques developed

for liquids are not always suitable for

characterizing the rheology of real slurries,

principally because of settling phenomena and the

size particles [10,11]. Measurements of pressure

drops in a pipe for different average speed of the

mixture appear the best experimental approach to

examine flow stratification for some flow rate range

and to evaluate the pressure drops.

Mooney–Rabinovitch method cannot be applied

because of turbulent flow used for obtaining a

homogenous mixture.

The purpose of this study is to experimentally

investigate the flow properties of the slurry in a

horizontal pipe. A small-scale loop circuit is built

for studying the fluid with in steady isothermal

conditions. A transparent test section is included

to allow observation of different patterns, covering

both laminar (Rebo2100) and turbulent flow

(2200oRebo4000) with 25% by weight particle.

Results of pressure drop with velocity and

temperature are presented. The effects of

repeated use of PCM particles upon melting and

solidifying are investigated through the analysis of

the size of particles.

2. PRESENTATION OF THE SLURRY

The making of the particles of the slurry [12] is

based on a process of mass polymerization. The

obtained particles contain a water concentration

close to 90% and have the consistency of a

viscoelastic gel for a temperature above 01C. The

phase change element is thus retained in the

network both because of interfacial stress and

chemical bonds and no exit of water occurs during

the phase change cycle (Figure 2). A very small

quantity of antifreeze protein is introduced in the

mother solution in order, for the final particle, to

inhibit agglomeration of particles containing ice.

Same additives are used for ice slurry [13,14].The final material remains a well-shape-defined

sample, requiring no coating. It appears whiteand hard when frozen as opposed to transparentand elastic when unfrozen. Particles are thendispersed in a carrier fluid, which must beselected very carefully because it constitutes thegreater fraction of the circulating material andserves as intermediary for heat transfer between thedispersed phase and the heat exchanger surfaces.Syltherm HF manufactured by Dow ChemicalCompany is chosen as a suspending phase. A solidfraction of 25% is chosen for this study.

The specific enthalpy and the phase changetemperature of the PCM particles measured bythe technique of DSC are 292kJkg�1 and01C, respectively. Their measured specific heatcapacity is 3.9kJkg�1K�1 at 101C. The specificheat of the Syltherm HF is 1.65kJkg�1K�1 at 101C.

The density of the continuous phase oscillates

between 906 kgm�3 (at 201C) and 912 kgm�3 (at

�201C). The density of the particle is, respectively,

1047 kgm�3 for T401C and 920 kgm�3 for

To01C. According to the temperature and the

weight fraction considered, the slurry is thus

presented in the form of a quasi-homogeneous

fluid when To01C. For T401C, the slurry is

non-homogeneous because of phenomenon of

sedimentation. A separation between the phases

can be observed when the flow is stopped.

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47Figure 2. Schematic representation of a spherical PCM particle.

FLOW INVESTIGATION OF PCM 3


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3. EXPERIMENTAL METHOD

Figure 3 shows a schematic diagram of theexperimental device, which consists of a hydro-dynamic test section, a section of visualization anda heat transfer section. The hydrodynamic testsection consists of a circular smooth stainless steeltube, 1.6m length with an internal diameter of23.7mm. This section, covered with 25mm thickfoam insulation, present two pressure measuringpoints. Sixty diameters of straight pipe with thesame diameter were provided upstream and down-stream of the test section in such a way that theslurry flow structure in this section is not affectedby bends and other source of flow disturbance.A 0.5m long Plexiglas observation section ismounted after the hydrodynamic test section andbefore the pump. The heat section, placed after thepump, is a coiled double tube heat exchanger. Theslurry circulating on one side of the heat exchangerand ethylene glycol circulating on the other side.

Pressure drops are measured using differential

pressure transducers with a precision of 5%. They

were calibrated within 0.5% of true gauge

pressures within a range of 0–320mbars. These

sensors appeared to be reliable and stable in all

conditions that occurred in the circuit during the

tests. A Coriolis flow sensor (Micro rotation

R100S) is used to measure the mean mixture

velocity. The instrument has a maximum error of

71%. Temperature is measured using K-type

thermocouples (type K) inserted into the slurry

flow. This sensor was calibrated using a constant

temperature bath and electronic thermometer with

an accuracy of 70.51C. Hence, the calibration

accuracy is within 70.11C between �10 and 251C.

During the experiments, the inlet and outlet

temperature difference of the test section and the

inlet fluid temperature fluctuation were less than

0.21C.A centrifuge pump (Salmson GET-C E131-2)

connected to a speed variator set the flow insidethe loop. Suspending liquid of the slurry iscirculated before to check the overall accuracy ofmeasurements. It was observed that flow ratecould be maintained constant to an accuracy of10%. Experiments are obtained for mass flow rateQ between 1 and 5m3 h�1.

The adopted procedure was to set the flowconditions for the rig and allow the slurry tocirculate in quasi-steady isothermal conditions. It

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47Figure 3. Schematic representation of the experimental loop.



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was assumed in our case that there is no variationof the concentration distribution in the downstreamdirection. This can be satisfied by assumption thatthe horizontal pipe is long enough to have a fullydeveloped flow, and that there is no influence of theheat transfer or pressure drop along the pipe on theconcentration profile. Video acquisitions of the flowpattern are made through a transparent circularpipe of the visualization section. Clean water is usedas a liquid of known behaviour to test theapparatus and for comparison with slurry.

4. EXPERIMENTAL RESULTS

4.1. Size of particles and mechanical stability underextended cycling

Repetitive cycles of freezing and thawing areinvestigated to examine the useful life of PCMparticles and its mechanical degradation due topumping, flowing and phase change state of water.

To analyse evolution of the size distribution,

numerous photographs have been taken and

statically evaluated. Figure 4 shows the particle

size distribution before cycling and after 80 cycles.

One can observe that particle size distributions

have changed due to an increased proportion of

fine particles. Mean diameter is around 1100 mmfor new particle and around 750 mm for used

particle. For more cycles than 80, particles size is

found to be constant, which confirm a mechanical

stability. Degradation observed is probably due to

the passage through the pump.

4.2. Pressure drop

Flow tests were conducted with the carrier fluidand 25% particle slurry at flow rate Qs between 1and 5m3 h�1. Temperature in the test section ismaintained constant at 231C and then at �71C,respectively. In order to validate the reliability ofthe loop and the results, experimental runs wereperformed using at first the suspending phase.Experimental runs were then performed with theslurry at different flow rates.

Figure 5 shows the variation of the pressure losswith the velocity along the test section for twotemperatures, 23 and �71C, respectively. For thesingle-phase and the two-phase mixture, one canobserve that the pressure drop increases withvelocity and decreases with temperature. Thismeasured pressure drop represents the results ofa single quasi-steady test.

Experimental data, presented in logarithmiccoordinates, show that, for the carrier fluid, thepressure drop increases as V 1,75. This AQ1result isfound in accordance with classical formula ofBlasius form for turbulent flow. The maximumdeviation of the measured pressure drop from thepredicted values of the Blasius equation was 2%.Therefore, the experimental system can beconsidered reliable.

For the slurry, on note that (i) pressure dropsare, for low velocity, always higher than pressure

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47Figure 4. Particle size distribution before cycling and after 80 cycles.



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drops of the carrier fluid and (ii) pressure loss ofthe particles flow at liquid state 1231C is greaterthan pressure loss at solid state at �71C. At highvelocity (41m s�1), pressure drop of the slurrytends to the same slope of the curve of singlephase, which is characteristic of a symmetricsuspension flow pattern. This effect is betterobserved for T5�71C than for T5 231C,because of particle density, which is closer tocarrier fluid density at T5�71C. At intermediatevelocity (o1m s�1), the divergence of the slurrycurves from the suspending fluid increases withdecreasing flow rate, which reflects an asymmetricsuspension flow pattern.

The measurement of the viscosity of the slurry

by standard commercial instruments is not

conceivable as mentioned in the section

‘Introduction’. The use of mathematical models

as Thomas equation [15] is often used in the

literature as a solution to evaluate viscosity of the

slurry for homogenous distribution of the particles

in the carrier liquid. For the case of heterogeneous

suspension as we observe when the velocity

iso1m s�1, it appears difficult to define a mean

viscosity (and therefore a Reynolds number)

because the unequal repartition of particles.The following analysis considers a Reynolds

number based on the properties of the carrier fluid.

Previous data are fitted by empirical expression ofthe form: DP/L5 a Ren with a and n two constantsparameters. Results of this analysis for the carrierfluid and 25% concentrated slurry are presented inTable I.

One can observe that, for the carrier fluid,DPl=L is proportional to Reynolds number to the–1.75 as predicted by Blasius equation for asmooth duct. For the slurry, pressure drops areless dependent on Reynolds number. Expressionsof Table I give the opportunity to comparepressure drop DPs=L of the slurry and singleliquid pressure drop DPl=L by introducing arelative pressure drop DPr defined as

DPr ¼DPs

L

�DPl

Lð1Þ

Figure 6 presents the variation of relative pressuredrop DPr as a function of number Reynolds Re forT5 231C and �71C. This AQ2figure shows clearly the

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Figure 5. Pressure drops versus velocity at T5 123 and �71C.

Table I. Correlation between pressure drop andReynolds number for T5 23 and�71C.

Temperature (1C)DPl of thecarrier fluid

DPs of theslurry

23 8� 10�5Re1.75 0.42Re1.04

�7 3� 10�4Re1.75 0.033Re1.41



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UNCORRECTED PROOFeffect of the presence of particles on the pressure

drop. One can note:

� an important difference between DPl=L andDPs=L for Reynolds number less than 7000; thiscan be explained by heterogeneous flow. In thehigh velocity region (Re47000), a homogenousflow is observed; the best repartition of particlesin the flow can explain the decrease in thepressure drop ratio as well for T5�7 and 231C.

� An important difference between relative pres-sure drop DPr at �7 and 231C can be explainedby the change of density of particles. Thepressure of PCM slurry is between 5 and 10times more important than pressure drop of thecarrier fluid.

4.3. Comparison with conventional chilled water—feasibility discussions

The previous pressure drop gives the opportunityto analyse transportation cost (i.e. transport coldheat energy versus the pump consumption) and tocompare the use of the PCM slurry instead ofconventional chilled water.

Let us consider the following comparisonbetween chilled water and 25wt% PCM slurryfor air conditioning application where it isassumed that the working temperature range is0–121C. With a mass fraction for 25%, theequivalent specific heat of the slurry forthe range 0–121C is 8.3 kJ kg�1K�1 (includingthe latent heat) while water specific heat is

4.2 kJ kg�1K�1. For a given cold heattransportation quantity, the mass flow rate ofPCM slurry to the water is

vqms

qmw¼

q

CpsDTq

CpwDT

¼Cpw

Cps¼

4:2

8:3¼ 0:5 ð2Þ

The mass flow rate can be reduced in this way by afactor 2 with a 25% PCM slurry.

In the case of the same pump efficiency (Z) andthe same duct, the pump consumption ratio of thePCM slurry to the chilled water is given by

Ns

Nw¼

QsDPs

ZQwDPw

Z

¼VsDPs

VwDPwð3Þ

The pressure drop of chilled water DPw can becalculated by the classical Darcy Weisbach [16] fora circular smooth tube of 1.6m length with aninternal diameter of 23.7mm. The value of thefriction factor is obtained by the Colebrookequation [16].

Figure 7 shows the relationship of the pumpconsumption and the heat transportation rate Ffor the PCM slurry and the chilled water. Thiscurve reveals that for the same heat transportationrate the pump consumption of water is more thanof PCM slurry when the heat transportation rate ismore than 12.8 kW. Taking the transportation rateF5 20 kW, for example, the pump consumptionfor the 25wt% PCM slurry can reduce around30% of that for water. This reduction is due to

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0

5

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15

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25

30

0 2000 4000 6000 8000 10000 12000 14000

Re

∆Pr 23 °C

-7 °C

Figure 6. Relative pressure drop DPr as a function of Reynolds number Re.



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UNCORRECTED PROOF

high cooling capacity obtained by the presence ofPCM particles. In light of this analysis, the newPCM slurry shows good potentiality and appearswell adapted for a wide variety of scheme wherethe production involves low-temperature intervals,such as refrigeration or air conditioning industry.

5. CONCLUSIONS

A prototype of slurry is presented and studied for

a concentration of 25wt% as a potential working

fluid for district cooling and air conditioning

process. This double phase fluid consists of

particles of a gel containing water concentration

close to 90%, dispersed in a carrier fluid with

adjusted density and viscosity. Pressure drop

measurements are investigated and results show

that the pressure drops of the slurry increased over

the whole range of measured flow rate, while

remaining in suitable values for a practical use.

A homogeneous particle field is observed for

Reynolds number up to 7000, which guarantees a

safe operation of the system without the occur-

rence of clogging in ducts. A comparison with

chilled water shows that flow rate and pump

consumption of the 25wt% PCM slurry decrease

notably for the same heat transportation quantity

due to phase change. The PCM slurry has good

application feasibility in practice and its use offers

attractive opportunities for advanced cooling

storage system including heat exchanger.

NOMENCLATURE

a 5 parameter (Pam�1)Cp 5 specific heat (kJ kg�1K�1)D 5 diameter (m)L 5 length (m)N 5 pump consumption (W)P 5 pressure (Pa)Q 5mass flow rate (kg s�1)Re 5Reynolds numberT 5Temperature (1C)V 5 velocity (m s�1)

Greek symbols

Z 5 pump efficiencym 5 viscosity (Pas)r 5 density (kgm�3)f 5 volume fractionF 5 heat transportation rate (W)

Subscripts

l 5 liquid phasep 5 particler 5 relatives 5 slurryw 5water

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0.1

0

0.2

0.3

0.4

0.5

0.6

0.7

0.8

0.9

1.0

0 5000 1000 1500 2000 2500Φ (W)

N(W

)

Chilled water

yPCM slurr

Figure 7. Pump consumptions N as function of the heat transportation rate F.



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