ǫǰǡǟVol. 2: )3125*Ą22ġ31ʯ˄Ĝʠૺ௾ཡࡉɅȤȫɥɺˋʺʣɺࣅ౫ൎᆔဖຣɅ࠲ȳɥॸ࢞Īൎ৐ᆔĆူ਄ᆔɅɢɥ྘ߏīࣉ࣮ࣞࢺᘧ⵨Ⓨჾ࡟࠾ࡅࡿ࢔ࣥࣔࢽ࢔ᙉไᑐὶἛ㦐࡟㛵ࡍࡿ◊✲㸨㸦ᑐྥὶ࣭୪⾜ὶ࡟ࡼࡿẚ㍑㸧
᭷㤿 ༤ྐ*1㸪ᑠᒣᖾᖹ*1㸪ụୖᗣஅ*1Experimental study on flow boiling in plate evaporators(Comparison of heat transfer characteristics between parallel- and counter-flow configurations)
Hirofumi ARIMA*1, Kohei KOYAMA*1 and Yasuyuki IKEGAMI*1*1
Institute of Ocean energy, Saga University
1-48, Hirao, Kubara-aza, Yamashiro-cho, Imari-shi, Saga, 849-4256, JapanAbstract
Ocean thermal energy conversion (OTEC) systems has been attracted attention as renewable and ocean energy. The OTEC
uses a plate heat exchanger as evaporator and condenser and ammonia or ammonia/water mixture as the working fluid
because the heat source temperature and temperature difference between the surface and deep seawater is very small. To
improve the power efficiency of OTEC, improving the heat transfer performance of the plate evaporator is important.
Therefore, some experimental studies about boiling characteristic of ammonia on a plate evaporator have been investigated.
However, almost studies are target for measurement of boiling heat transfer coefficient at different operation conditions withcounter-flow configuration as well as actual evaporator of OTEC. The author previously also investigated the measurement ofthat on a flat plate evaporator under only counter-flow; however, the influences of boiling ammonia heat transfer coefficienton different flow configuration have not yet been clarified. Therefore, in the present study, local boiling heat transfer
coefficient of ammonia were measured and compared at counter- and parallel flow configuration on a flat plate evaporator.
The local heat transfer coefficients were obtained at a range of mass fluxes (7.5–15 kg/m2s), heat fluxes (15–25 kW/m2),
pressures (0.7–0.9 MPa), and operating as parallel- and counter-flows. The results show that the averaged heat transfer
coefficient of parallel-flow was superior to counter-flow at low mass flax conditions. However, in case of high mass flux, thecounter-flow is slightly larger than parallel flow.

Key Words : Boiling and evaporation, Heat exchanger, Heat transfer coefficient, Ammonia, Counter flow, Parallel flow ⥴   ゝ⎔ቃ࡜࢚ࢿࣝࢠ࣮ၥ㢟ࡢゎỴࡢࡓࡵ㸪Ᏻ඲ᛶࡀ㧗ࡃ⏕ែ⣔࡟ඃࡋ࠸Ⓨ㟁ࢩࢫࢸ࣒ࡀồࡵࡽࢀ࡚࠸ࡿ㸬≉࡟㏆ᖺ࡛ࡣ㸪෌⏕ྍ⬟࢚ࢿࣝࢠ࣮ࢆ౑ࡗࡓⓎ㟁ࡢᐇ⏝໬ࡀᮇᚅࡉࢀ࡚࠸ࡿ㸬OTEC ࡢࡼ࠺࡞ᾏὒࡢ ᗘᕪⓎ㟁ࢆ⏝࠸ࡓᑠ ᗘᕪⓎ㟁ࡣ㸪CO2 ࡢⓎ⏕ࡶ࡞࠸ࡓࡵ⏕ែ⣔࡟ඃࡋ࠸ࢩࢫࢸ࣒࡛࠶ࡿ࡜⪃࠼ࡽࢀࡿ㸬࡜ࡇࢁ࡛ OTEC ࡟ࡣ⇕஺᥮ჾ࡜ࡋ࡚ࣉ࣮ࣞࢺᘧ⇕஺᥮ჾ(PHE)ࡀ౑⏝ࡉࢀ࡚࠸ࡿ㸬OTEC ࡀ౑⏝ࡍࡿ⇕※࡛࠶ࡿᾏὒࡢ⾲ᒙࡢ ᾏỈࡢ ᗘࡣ⣙ 25 ~ 30ºC㸪῝ᒙࡢ෭ᾏỈࡣ⣙ 5 ~ 10ºC ࡛࠶ࡾ㸪ࡑࡢ᭱኱ࡢ ᗘᕪ࡛࠶ࡿ 25Υ࡛࠶ࡿ㸬PHE ࡣ㸪⟶ᆺࡢ⇕஺᥮ჾ࡟ᑐࡋ࡚༢఩య✚ᙜࡓࡾࡢఏ⇕㠃✚ࡀ኱ࡁ࠸ࡇ࡜࡜ఏ⇕ᛶ⬟ࡀ㧗࠸ࡓࡵ㸪ᾏὒ࠿ࡽࡢపᐦᗘࡢ⇕ᅇ཰࡟᭱㐺࡛࠶ࡿ㸬୰㇂ (୰㇂, 1995)ࡣ㸪⟶ᆺࡢ⇕஺᥮ჾ࡟ᑐࡋ࡚ PHE ࡣ 1/3 ࠿ࡽ 1/4 ࡢ㔜㔞࡛࠿ࡘ෭፹ࡢ㔞ࢆ༙ศ࡟࡛ࡁ
ཎ✏ཷ௜ 2014 ᖺ 07 ᭶ 31 ᪥
బ㈡኱Ꮫᾏὒ࢚ࢿࣝࢠ࣮◊✲ࢭࣥࢱ࣮ 㸦ࠛ849-4256 ఀ୓㔛ᕷᒣ௦⏫ஂཎᏐᖹᑿ 1-48㸧
*1E-mail: arima@ioes.saga-u.ac.jp
**122

23

ᄵ༣གષ -!ழટড়ိ -!ද௫য়་

ࡿࡇ࡜ࢆ㏙࡭࡚࠸ࡿ㸬ࡼࡗ࡚㸪PHE ࢆ౑ࡗࡓⓎ㟁ࢩࢫࢸ࣒ࡢሙྜ㸪ᚑ᮶ࡢタィࡼࡾᘓタࢥࢫࢺࡀୗࡆࡽࢀࡿࡇ࡜ࡀᮇᚅࡉࢀ࡚࠸ࡿ㸬୍᪉㸪OTEC ࡛ࡣ⇕※ࡢ ᗘࡀ㠀ᖖ࡟ప࠸ࡓࡵ㸪సືὶయ࡜ࡋ࡚పἛⅬࡢ࢔ࣥࣔࢽ࢔ࡲࡓࡣ࢔ࣥࣔࢽ࢔㸭Ỉࡀ౑⏝ࡉࢀ࡚࠸ࡿ㸬ࡲࡓ㸪࢔ࣥࣔࢽ࢔ࡢ⵨Ⓨ₯⇕ࡣỈࢆ㝖ࡃ୍⯡ⓗ࡞෭፹࡟ẚ࡭࡚㠀ᖖ࡟㧗࠸ࡇ࡜ࡶࡑࡢ⌮⏤ࡢ୍ࡘ࡛࠶ࡿ㸬࡜ࡇࢁ࡛㸪ᐇᾏỈࢆ⏝࠸ࡓ OTEC ࣉࣛࣥࢺࡣ㸪⌧ᅾࡢ࡜ࡇࢁ 2103 ᖺ 3 ᭶࡟᏶ᡂࡋࡓἈ⦖┴ஂ⡿ᓥࡢ 50kW ᐇドᐇ㦂⏝ࣉࣛࣥࢺ(ụୖ㸪ྂሀ, 2013)ࡢࡳ࡛࠶ࡿ㸬୍᪉㸪⡿ᅜࡢࣁ࣡࢖࡛ࡶ OTEC ࡢᐇ⏝໬࡟ྥࡅࡓ◊✲࣭㛤Ⓨ(Lockheed Marcin, 2013, OTEC International LLC, 2012) ࡀ㐍⾜୰࡛࠶ࡿࡀ㸪ࡇࢀࡽࡶᐇ⏝ࣉࣛࣥࢺ࡛ࡣ࡞࠸㸬ᑗ᮶ⓗ࡞ OTEC ࡢᐇ⏝໬࡟ࡣ㸪ࢥࢫࢺࡢపୗ࡜ᛶ⬟ྥୖࡀᚲせ࡛࠶ࡾ㸪≉࡟ຠ⋡ࡢྥୖ࡟ࡣ⵨Ⓨჾࡢఏ⇕ᛶ⬟ࡢྥୖࡀ㔜せ࡛࠶ࡿ࡜⪃࠼ࡽࢀࡿ㸬ࡋ࠿ࡋ㸪ఏ⇕ᛶ⬟ࡢྥୖ࡟ᚲせ࡞࢔ࣥࣔࢽ࢔ࡸ࢔ࣥࣔࢽ࢔㸭Ỉࢆ⏝࠸ࡓ OTEC ࡢ PHEࡢ◊✲ࡣ㠀ᖖ࡟ᑡ࡞࠸㸬᷸㒊ࡽ (᷸㒊௚, 2005, 2006) ࡣၟ⏝ࡢࣉ࣮ࣞࢺᘧ⵨Ⓨჾࢆ⏝࠸ࡓ࢔ࣥࣔࢽ࢔ࡲࡓࡣ࢔ࣥࣔࢽ࢔㸭Ỉࡢᖹᆒ⇕ఏ㐩⋡ࡢ ᐃ࡟㛵ࡍࡿ◊✲ࢆ⾜ࡗ࡚࠸ࡿ㸬ࡲࡓ㸪᭷㤿ࡽ (᭷㤿௚, 2010, 2011) ࡜ᒸᮏࡽ (ᒸᮏ௚, 2011)ࡣ PHE ࢆ᝿ᐃࡋࡓࣉ࣮ࣞࢺ⵨Ⓨჾࡢ◊✲ࢆ⾜ࡗ࡚࠸ࡿ㸬ࡇࢀࡽࡢ◊✲࡛ࡣ㸪ࣉ࣮ࣞࢺᘧ⵨Ⓨჾࡢᖹᆒࡲࡓࡣᒁᡤ⇕ఏ㐩ࡢ࢔ࣥࣔࢽ࢔ࡲࡓࡣ࢔ࣥࣔࢽ࢔㸭ỈࡢἛ㦐⇕ఏ㐩⋡࡟ࡘ࠸࡚ሗ࿌ࡉࢀ࡚࠸ࡿ㸬୍᪉㸪᭷㤿ࡽ (᭷㤿௚, 2010) ࡣஂ⡿ᓥ OTEC ࡟ࡶ᥇⏝ࡉࢀ࡚࠸ࡿᚤᑠพฝ㠃ࢆᣢࡘࣉ࣮ࣞࢺᘧ⵨Ⓨჾࡢఏ⇕ಁ㐍࡟㛵ࡍࡿ◊✲ࡶ⾜ࡗ࡚࠸ࡿ㸬ࡇࡢ◊✲࡛ࡣ㸪ࣉ࣮ࣞࢺఏ⇕㠃࡟ᚤᑠพฝࢆ᪋ࡍࡇ࡜࡛ᖹᯈ࡟ᑐࡋ࡚ 40%ࡢఏ⇕ᛶ⬟ࡢྥୖࡀሗ࿌ࡉࢀ࡚࠸ࡿ㸬࡜ࡇࢁ࡛㸪OTEC ⏝ࡢ PHE ࡢタィ࡟ࡇࢀࡽࡢ⇕ఏ㐩⋡ࢆ᥇⏝ࡍࡿࡓࡵ࡟ࡣ㸪ᚑ᮶ࡢࣉ࣮ࣞࢺᘧ⇕஺᥮ჾࡢ◊✲࡛ࡣసືὶయ࡜⇕※ࡢὶࢀ᪉ྥ࡜ࡋ࡚ᑐྥὶࡢࡳࡋ࠿⾜ࢃࢀ࡚࠸࡞࠸ࡓࡵ㸪⇕※ࡢὶࢀ᪉ྥ࡟ࡼࡿᙳ㡪ࡶྵࡵࡓࡼࡾヲ⣽࡞ゎᯒࡀᚲせ࡛࠶ࡿ࡜⪃࠼ࡿ㸬Djordjevic ࡽ (Djordjevic and Kabelac, 2008) ࡣ㸪ࣉ࣮ࣞࢺᘧ⇕஺᥮ჾ࡟࠾࠸࡚ᑐྥὶ࡜୪⾜ὶ࡛⇕ఏ㐩⋡ࡢẚ㍑ࢆ⾜࠸㸪᮲௳࡟ࡼࡗ࡚ࡣ୪⾜ὶࡢ᪉ࡀࡼ࠸ሙྜࡀ࠶ࡿࡇ࡜ࢆ♧ࡋࡓ㸬ࡇࡢ⤖ᯝࡼࡾ㸪ὶయࡢὶࢀ᪉ྥࡣࣉ࣮ࣞࢺᘧ⵨Ⓨჾࡢᛶ⬟ホ౯࡟㔜せ࡞ࣃ࣓࣮ࣛࢱ࣮࡛࠶ࡿࡇ࡜ࡀศ࠿ࡿ㸬ࡼࡗ࡚㸪ᮏ◊✲࡛ࡣ㸪ࣉ࣮ࣞࢺᘧ⵨Ⓨჾࡢᑐྥὶ࡜୪⾜ὶ࡟࠾ࡅࡿἛ㦐⇕ఏ㐩⋡ࡢ ᐃ࡜ẚ㍑ࢆ⾜ࡗࡓ㸬 グ   ྕA㸸 ఏ⇕㠃✚ [m2]T㸸G

㸸 ㉁㔞ὶ᮰ [kg/m2s]x㸸 ⇕ᖹ⾮஝ࡁᗘ [-]h㸸 ⇕ఏ㐩⋡ [W/m2K]z㸸 ࣉ࣮ࣞࢺᒁᡤࡢᗙᶆ [m]i㸸 ẚ࢚ࣥࢱࣝࣆ࣮ [J/kg]

ῧ࠼Ꮠifg㸸 ⵨Ⓨ₯⇕ [J/kg]

avek㸸 ⇕ఏᑟ⋡ [W/mK]eva㸸 ⵨Ⓨჾm㸸 ㉁㔞ὶ㔞 [kg/s]g㸸 Ẽ┦P㸸 ᅽຊ [Pa]hw㸸q㸸 ⇕ὶ᮰ [W/m ]l㸸 ᾮ┦Q㸸 ⇕஺᥮㔞 [W]sat㸸 㣬࿴

Q’㸸 ྛࢭࢢ࣓ࣥࢺ࡟࠾ࡅࡿ⇕஺᥮㔞 [W]wf㸸 సືὶయ2ᗘ [Υ]㸸 ᖹᆒỈ ᐇ   㦂࣭ ᐇ㦂⿦⨨
Fig. 1 ࡟ᐇ㦂⿦⨨ᴫ␎ᅗࢆ♧ࡍ㸬ᐇ㦂⿦⨨ࡣసືὶయ⣔㸪 Ỉ⣔㸪෭Ỉ⣔ࡢ 3 ࡘࡢᚠ⎔⣔࡛ᵓᡂࡉࢀࡿ㸬సືὶయᚠ⎔⣔ࡣ⵨Ⓨჾ (ࢸࢫࢺࢭࢡࢩࣙࣥ)㸪จ⦰ჾ㸪࢔ࣇࢱ࣮ࢥࣥࢹࣥࢧ࣮㸪సືὶయࢱࣥࢡ㸪సືὶయ࣏ࣥࣉ㸪ࢧࣈࢡ࣮࣮ࣛ㸪ࣉࣞࣄ࣮ࢱ࣮࡛ᵓᡂࡉࢀࡿ㸬ࡓࡔࡋ㸪ᮏ◊✲࡛ࡣᐇ㦂᮲௳ࡢ㒔ྜୖࣉࣞࣄ࣮ࢱ࣮ࡣ౑⏝ࡋ࡞࠸㸬Ỉᚠ⎔⣔ࡣࡉࡽ࡟ 2 ࡘࡢᚠ⎔⣔ (I, II) ࡛ᵓᡂࡉࢀࡿ㸬 Ỉᚠ⎔⣔ I ࡣ㸪 Ỉࢱࣥࢡ࡜࣏ࣥࣉ㸪࢞ࢫ࣎࢖࣮ࣛ (୕ᾆᕤᴗ♫〇, UT-200HP-S, ᭱኱ฟຊ: 1,400 kW)㸪 Ỉᚠ⎔⣔ II ࡣᑠᆺ Ỉࢱࣥࢡ㸪࣏ࣥࣉ࠾ࡼࡧᢞࡆ㎸ࡳᘧࣄ࣮ࢱ࣮ (ඵග㟁ᶵ〇㸪SWB3230㸪3kW) ࡛ࡑࢀࡒࢀᵓᡂࡉࢀ࡚࠸ࡿ㸬ࡲࡓ㸪෭Ỉᚠ⎔⣔ࡣ㸪෭෾ᶵ (ᮾⰪ〇㸪74 kW,ʯ˄Ĝʠૺ௾ཡࡉɅȤȫɥɺˋʺʣɺࣅ౫ൎᆔဖຣɅ࠲ȳɥॸ࢞Īൎ৐ᆔĆူ਄ᆔɅɢɥ྘ߏī

Eva:
DV
Hot water
circuit I

T

VMH

T

Counterflow

Parallelflow

HP1

Working fluid
circuitT

Cold water
circuit

Cond.

Eva.

P

T
P

HT1

AC
T
T

PH

Hot water
circuit II

T

T

ST

P

MF
㻴㻼㻞T

HT2

P

WP

CP

T

P

SC

RV

CT

Cond.:
PH:
AC:
ST:
SC:
HT1:
HT2:
BL:
CT:
RE:
WP:
HP1:
HP2:
CP:
MF:
VMH:

VMC

P

T

BL

P

T

RE

VMC:
DV:
RV:

24

Test plate(Evaporator)
Condenser
Pre-heater
After condenser
Working fluidstorage tank
Sub cooler
Hot water tank I
Hot water tank IIBoiler
Cold water tank
Refrigerator
Working fluid pump
Hot water pump I
Hot water pump II
Cold water pump
Mass flow meter
Volumetric flow
meter for hot water
Volumetric flow
meter for cold water
Degassed valve
Release valve

Fig. 1 Schematic diagram of the experimental apparatus.
RAW-100UC) ࡜෭Ỉࢱࣥࢡ㸪෭Ỉ࣏ࣥࣉ࡛ᵓᡂࡉࢀ࡚࠸ࡿ㸬సືὶయࡣసືὶయᚠ⎔⣔࡟࠾࠸࡚ᅗ 1 ࡢᐇ⥺࡟ἢࡗ࡚▮༳ࡢྥࡁ࡟ᚠ⎔ࡋ࡚࠸ࡿ㸬ࡲࡎ㸪సືὶయ࣏ࣥࣉ࡟ࡼࡾసືὶయࢱࣥࢡࡼࡾ㏦ࡾฟࡉࢀࡓసືὶయࡣ㸪ࢧࣈࢡ࣮࣮࡛ࣛ㐣෭ᗘࢆㄪᩚࡉࢀ⵨Ⓨჾ࡟ὶධࡍࡿ㸬ḟ࡟㸪⵨Ⓨჾ࡛ Ỉ࡟ࡼࡗ࡚ຍ⇕ࡉࢀࡓసືὶయࡣ஧┦≧ែ࡜࡞ࡾ⵨Ⓨჾ࠿ࡽὶฟࡋ㸪จ⦰ჾ࠾ࡼࡧ࢔ࣇࢱ࣮ࢥࣥࢹࣥࢧ࣮࡟࠾࠸࡚෭Ỉ࡛෭༷ࡉࢀࡿ㸬จ⦰ᚋࡢసືὶయࡣసືὶయࢱࣥࢡ࡟ᡠࡾ෌ࡧᚠ⎔ࡍࡿ㸬࣭ ィ ⿦⨨ᐇ㦂࡛ࡣ㸪඲࡚ࡢ≧ែⅬ࡟ࡘ࠸࡚ࢭࣥࢧ࣮࡟ࡼࡿ ᐃࢆ⾜ࡗࡓ㸬సືὶయࡢ㉁㔞ὶ㔞ࡣࢥࣜ࢜ࣜᘧ㉁㔞ὶ㔞ィ(Endress+Hauser ♫〇: PROMASS 80A ⢭ᗘ ±1% of F.S.) ࡟࡚ ᐃࡋࡓ㸬 Ỉ࠾ࡼࡧ෭Ỉࡢయ✚ὶ㔞ࡣ㟁☢ᘧὶ㔞ィ(ᮾⰪ〇, LF410, ⢭ᗘ ±0.5% of F.S.)㸪ᅽຊࡣ 6 ᮏࡢࢤ࣮ࢪᅽຊኚ᥮ჾ (ᮾⰪ〇, 3051CG, ࣞࣥࢪ 0 - 2,070 kPa, ⢭ᗘ ±0.25% of F.S.) ࢆ౑⏝ࡋࡓ㸬 ᗘࡣ 10 ᮏࡢ᢬ᢠయ (ᯘ㟁ᕤ♫〇, ER6, JIS A-class, ⢭ᗘ ±0.15°C) ࢆ౑⏝ࡋࡓ㸬ࡍ࡭࡚ࡢࢭࣥࢧ࣮࡟ࡘ࠸࡚ࡣ PC ࡟᥋⥆ࡉࢀࡓ PLC (୕⳻㟁ᶵ〇: MELSEC Q) ࡟୍࡚᪦཰㞟ࡉࢀ㸪VB6 ࣉࣟࢢ࣒࡛ࣛಖᏑࢆ⾜ࡗࡓ㸬࣭ ࢸࢫࢺࣉ࣮ࣞࢺᅗ 2 ࡟⵨Ⓨჾࡢᵓᡂࢆ♧ࡍ㸬⵨Ⓨჾࡣࣉ࣮ࣞࢺᮏయ㸪ᢲ࠼ᯈ 2 ᯛࡢィ 3 ᯛࡢ SUS304 〇ࡢࣉ࣮ࣞࢺ࡛ᵓᡂࡉࢀ
࡚࠸ࡿ㸬ᅗ 2 ࡟♧ࡍࡼ࠺࡟㸪඲࡚ࡢࣉ࣮ࣞࢺࡢᖜࡣ 380mm㸪㧗ࡉ 850mm ࡛㸪ࣉ࣮ࣞࢺᮏయࡢཌࡉࡣ 40mm, ᢲ࠼ᯈࡢཌࡉࡣ 30mm ࡛࠶ࡿ㸬ࡲࡓ㸪ᅗ 3 ࡟♧ࡍࡼ࠺࡟㸪సືὶయ࠾ࡼࡧ Ỉࡢὶ㊰ࡣఏ⇕㠃ࢆᣢࡘࣉ࣮ࣞࢺᮏయ࡜ᢲ࠼ᯈ㸪ࡑࡢ㛫࡟ᣳࡲࢀࡓࢫ࣮࣌ࢧ࣮࡛ᵓᡂࡉࢀ࡚࠸ࡿ㸬సືὶయഃࡢࢫ࣮࣌ࢧ࣮ࡣཌࡉ 2mm ࡢࢸࣇࣟࣥ〇㸪Ỉഃࡣཌࡉ 10mm ࡢࢦ࣒〇࡛࠶ࡿ㸬࡞࠾㸪ఏ⇕㠃ࡢᑍἲࡣ 250 mm×650 mm ࡛⾲㠃ࡣ 2000 ␒ࡢ࢚࣓࣮ࣜ⣬࡛◊☻ࡋࡓࡶࡢࢆ౑⏝ࡋࡓ㸬ࡲࡓࣉ࣮ࣞࢺᮏయࡢ ᗘ ᐃࡢࡓࡵ㸪ᅗ 2(b)࡟♧ࡍࡼ࠺࡟ ᐃ⏝ࡢ✰ࢆ㧗ࡉ᪉ྥ࡟ 6 ࠿ᡤ㸪100mm 㛫㝸࡛タ⨨ࡋࡓ㸬ࡇࢀࡽࡢ✰࡟ࡣ㸪ᅗ 4 ࡟♧ࡍࡼ࠺࡟┤ᚄ 3mm㸪㛗ࡉ 38mm ࡢ࢘ࣞࢱࣥ〇ࡢࢳ࣮ࣗࣈ࡟┤ᚄ0.1mmࡢK ᆺ⇕㟁ᑐࡢ⣲⥺2ᮏࢆᤄධࡋࡓ㸬
ィ12Ⅼࡢ⇕㟁ᑐࡢࢹ࣮ࢱࡣ40chࡢ࣐ࣝࢳ࣓࣮ࢱ࣮ (Keithley♫〇 2701 ᆺ) ࡟୍᪦㞟ࡵࡽࢀ㸪PC ୖࡢ LabVIEW ࣉࣟࢢ࣒ࣛ࡟࡚ㄞࡳྲྀࡾ㸪ಖᏑࢆ⾜ࡗࡓ㸬࡞࠾㸪⇕㟁ᑐࡣணࡵᜏ ᵴ᳨࡛ᐃࢆ⾜࠸㸪⢭ᗘ±0.1°C ࡢࡶࡢࢆ౑⏝ࡋࡓ㸬

25ᄵ༣གષ -!ழટড়ိ -!ද௫য়་

30

40

㻞

Working fluid side frame

100

㻝㻜

Plate

Plate

SpacerWarm heat source side frame
Warm heat source

100

T.C. wells

100

Fig. 3 Cross sectional view of test plate(A-A’ on Fig. 2)

Hot Water channel

100

100

850Warm heat source side frame

A䇻A

Working fluid
Working fluidside frame

CounterorParallel

Measuringpoints

30

Working fluid channel

380

Spacer102(a) Top view(b) Side viewFig. 2 Assembly of test plate.

Fig. 4 Local position of thermocouples inside the plate.

࣭ ࢹ࣮ࢱᩚ⌮ᒁᡤࡢ⇕ὶ᮰ q㸪⇕ఏ㐩⋡ h㸪஝ࡁᗘ x ࡣ௨ୗࡢ᪉ἲ࡛ồࡵࡓ㸬ᒁᡤࡢ⇕ὶ᮰ࡣ 1 ḟඖᐃᖖ⇕ఏᑟࢆ᝿ᐃࡋ࡚㸪ᅗ 4 ࡟♧ࡍ ᗘ T1㸪T2㸪⇕㟁ᑐ㛫㝸 l1 ࢆ⏝࠸࡚㸪ḟᘧ࡛ồࡵࡓ㸬qkT1  T2l1(1)ࡇࡇ࡛㸪k ࡣ SUS304 ࡢ⇕ఏᑟ⋡ࢆ⏝࠸ࡓ㸬ḟ࡟ᒁᡤࡢ⇕ఏ㐩⋡ h ࡣ㸪⇕ὶ᮰ q㸪㣬࿴ ᗘ Tsat㸪సືὶయഃࡢቨ㠃 ᗘ Twall ࢆ⏝࠸࡚ḟᘧ࡛ồࡵࡓ㸬hq
Twall  Tsat(2)ࡇࡇ࡛㸪Tsat ࡣ⵨Ⓨჾධཱྀᅽຊࢆ㣬࿴ᅽຊ Psat ࡜ࡋ࡚⨨ࡁ㸪≀ᛶ್ィ⟬ࣛ࢖ࣈ࣮࡛ࣛࣜ࠶ࡿ PROPATH (PropathGroup, 2002) ࢆ౑ࡗ࡚ồࡵࡓ㸬ࡲࡓ㸪ቨ㠃 ᗘ Twall ࡣᘧ(1)ࢆእᤄࡋࡓᘧ(3)࡛ồࡵࡓ㸬TwallT2 ql2k(3)⵨Ⓨჾࡢ㧗ࡉ᪉ྥ࡟ἢࡗࡓ 6 ࠿ᡤࡢྛ ᐃⅬ࡟࠾ࡅࡿᒁᡤ஝ࡁᗘ x ࡣᒁᡤẚ࢚ࣥࢱࣝࣆ࣮i ࢆ⏝࠸࡚㸪ḟᘧ࡛ồࡵࡓ㸬xi  isat,li fg(4)ʯ˄Ĝʠૺ௾ཡࡉɅȤȫɥɺˋʺʣɺࣅ౫ൎᆔဖຣɅ࠲ȳɥॸ࢞Īൎ৐ᆔĆူ਄ᆔɅɢɥ྘ߏī26

ࡇࡇ࡛㸪isat,l ࡣ㣬࿴ᾮࡢẚ࢚ࣥࢱࣝࣆ࣮㸪ifg ࡣ⵨Ⓨ₯⇕࡛࠶ࡿ㸬࡞࠾㸪ᘧ(4)࡟୚࠼ࡓᒁᡤẚ࢚ࣥࢱࣝࣆ࣮i ࡣḟࡢ᪉ἲ࡛ồࡵࡓ㸬ࡲࡎ㸪⵨Ⓨჾࢆᅗ 5 ࡟♧ࡍࡼ࠺࡟㧗ࡉ᪉ྥ࡟ἢࡗ࡚ྛ ᐃⅬࢆ୰ᚰ࡜ࡍࡿ 6 ࠿ᡤࡢࢭࢢ࣓ࣥࢺ࡟ศ๭ࡋ㸪⇕ὶ᮰ qj㸪ఏ⇕㠃✚ Aj ࠾ࡼࡧ⇕஺᥮㔞 Q’j ࢆ୚࠼ࡓ㸬ḟ࡟㸪⵨Ⓨჾධཱྀࡢẚ࢚ࣥࢱࣝࣆ࣮ieva,in ࢆồࡵ㸪ྛࢭࢢ࣓ࣥࢺ࡛ᚓࡽࢀࡿẚ࢚ࣥࢱࣝࣆ࣮ࡢቑศ'i ࢆධཱྀ࠿ࡽ㡰࡟ຍ⟬ࡍࡿࡇ࡜࡛㸪ḟᘧࢆ⏝࠸࡚ᒁᡤࡢ್ࢆᚓ࡚
࠸ࡿ㸬
ninieva ,in  ¦ 'i j(5)j 1࡞࠾㸪⵨Ⓨჾධཱྀࡢẚ࢚ࣥࢱࣝࣆ࣮ieva,in ࡣ㸪࢔ࣥࣔࢽ࢔ᾮࡀ⵨Ⓨჾ࡟㐣෭ᾮ࡛౪⤥ࡉࢀࡿࡇ࡜࠿ࡽ㸪ࡑࡢධཱྀ࡟࠾ࡅࡿ ᗘཬࡧ㣬࿴ᅽຊࢆ⏝࠸࡚ PROPATH (Propath Group, 2002)࡛ồࡵࡓ㸬ࡲࡓ㸪ྛࢭࢢ࣓ࣥࢺࡢẚ࢚ࣥࢱࣝࣆ࣮ࡢቑศ'i ࡣḟᘧ࡛ồࡵࡓ㸬

'i jQ cj / m(6)

y6=1252 ~ 6)

qav,610075­Q '1 q1 A1 / 2®
¯Q ' j ( q j 1 A j 1  q j A j ) / 2 ( jQ7T. C. wells
Heattransferarea

100y5=100qav,5Q5100

y4=100qav,4Q4100

y3=100qav,3Q3100

y2=100qav,2Q2
y1=125qav,175

650

Q8Q1125w = 250

Fig. 5 Separation of each heat exchange areas.

27ᄵ༣གષ -!ழટড়ိ -!ද௫য়་

 ᐇ㦂᮲௳ᐇ㦂᮲௳ࢆ⾲ 1 ࡟♧ࡍ㸬ᐇ㦂᮲௳࡜ࡋ࡚㸪ὶࢀ᪉ྥࡣᑐྥὶ㸪୪⾜ὶࡢ 2 ᮲௳㸪㉁㔞ὶ᮰ࢆ 3 ᮲௳㸪ᖹᆒ⇕ὶ᮰࡜ࡋ࡚ 3 ᮲௳㸪᧯సᅽຊ࡜ࡋ࡚ 3 ᮲௳ࢆ୚࠼ࡓ㸬ྛ᮲௳ࡣᐃᖖ≧ែ࡟࡚ 1 ⛊ࡈ࡜࡟ 5 ศ㛫グ㘓ࢆ⾜ࡗࡓ㸬Table 1 Experimental conditions.
Flow configuration

Counter/ Parallel

Mass flux G [kg/m2s]

7.5, 10, 15
2

Averaged heat flux q [kW/m ]15, 20, 25

Saturation pressure P [MPa]0.7,0.8,0.9

Saturation temperature Tsat [ºC]

13.9

17.9

21.6


 ᐇ㦂⤖ᯝ࠾ࡼࡧ⪃ᐹ࣭ ⾲㠃 ᗘ࠾ࡼࡧᒁᡤ⇕ὶ᮰
ᅗ 6 ࡟⵨Ⓨჾࡢసືὶయഃࡢὶࢀ᪉ྥ(⵨Ⓨჾ㧗ࡉ᪉ྥ)࡟ἢࡗࡓᒁᡤࡢసືὶయഃ Twf, wall ࡜ Ỉഃࡢቨ㠃 ᗘThw, wall ࡢศᕸ࡟ࡘ࠸࡚␗࡞ࡿ㉁㔞ὶ᮰㸪ᅽຊ㸪ᖹᆒ⇕ὶ᮰᮲௳࡟࠾ࡅࡿ⤖ᯝࢆ♧ࡍ㸬ࡲࡓᅗ 6 ࡟ࡣྠ୍᮲௳࡟࠾ࡅࡿᑐྥὶ㸪୪⾜ὶࡢ⤖ᯝ࡟ࡘ࠸࡚ࡢẚ㍑ࡶ♧ࡍ㸬࠸ࡎࢀࡢ᮲௳࡛ࡶ㸪ᑐྥὶ࡛ࡣ Ỉഃࡢቨ㠃 ᗘࡢῶᑡ࡟క࠸సືὶయഃࡢቨ㠃 ᗘࡀῶᑡࡋ࡚࠸ࡿࡢ࡟ᑐࡋ࡚㸪୪⾜ὶ࡛ࡣ Ỉࡢ ᗘࡢῶᑡ࡟క࠸సືὶయഃ࡟ࡘ࠸࡚ࡣᗘࡀୖ᪼ࡋ࡚࠸ࡿࡇ࡜ࡀศ࠿ࡿ㸬ࡲࡓ㸪㉁㔞ὶ᮰ࡀ G = 7.5 kg/m2s ࡢሙྜ㸪సືὶయഃࡢቨ㠃 ᗘࡣᑐྥὶࡼࡾ୪⾜ὶࡢ᪉ࡀ㧗࠸ࡇ࡜ࡀศ࠿ࡿ㸬ࡋ࠿ࡋ㸪㉁㔞ὶ᮰ࡀ G = 15 kg/m2s ࡜㧗࠸ሙྜ㸪ᑐྥὶࡢቨ㠃 ᗘࡣ୪⾜ὶࡼࡾࢃࡎ࠿࡟㧗࠸㸬ࡑࡢ⤖ᯝ㸪୪⾜ὶࡢቨ㠃㐣⇕ᗘ࡟ࡘ࠸࡚ẚ㍑ࢆ⾜࠺࡜㸪ᑐྥὶ࡟ᑐࡋ࡚ G = 7.5 kg/m2s ࡢሙྜ࡛ࡣࡼࡾపࡃ㸪G = 15 kg/m2s ࡢሙྜ࡟ࡘ࠸࡚ࡣࡼࡾ㧗ࡃ࡞ࡿࡇ࡜ࡀ᫂ࡽ࠿࡟࡞ࡗࡓ㸬ᅗ 7 ࡣᅗ 6 ࡜ྠ୍ࡢ᮲௳࡟࠾ࡅࡿ⵨Ⓨჾࡢὶࢀ᪉ྥ࡟ἢࡗࡓᒁᡤ⇕ὶ᮰ࡢศᕸ࡟ࡘ࠸࡚㸪୪ὶ࠾ࡼࡧᑐྥὶࡢ
⤖ᯝࡢẚ㍑࡜ඹ࡟♧ࡍ㸬ᒁᡤࡢ⇕ὶ᮰ࡣᅗ 6 ࡛♧ࡋࡓ Ỉഃቨ㠃 ᗘࡢῶᑡ࡟క࠸పୗࡋ࡚࠸ࡿࡇ࡜ࡀศ࠿ࡿ㸬࡜ࡇࢁ࡛㸪ᮏ◊✲࡛ࡣᖹᆒࡢ⇕ὶ᮰ࢆ⏝࠸࡚ࢹ࣮ࢱࡢᩚ⌮ࢆ⾜ࡗ࡚࠸ࡿࡀ㸪ᅗ 6 ࡟♧ࡍࡼ࠺࡟ᒁᡤࡢ⇕ὶ᮰ࡢࡤࡽࡘࡁࡀഹ࠿࡞ࡀࡽᏑᅾࡋ㸪ࡑࡢ┦ᑐㄗᕪࡣᖹᆒ⇕ὶ᮰࡟ᑐࡋ࡚ P = 0.7MPa ࡛ࡣ ± 4 %㸪P = 0.8MPa ࡛ࡣ ± 5 %㸪P = 0.9MPa ࡛ࡣ ± 7.5% ௨ୗ࡛࠶ࡗࡓ㸬ᒁᡤࡢ⇕ὶ᮰ࡀసືὶయ࡟ἢࡗ࡚ቑຍࡋࡓ⌮⏤࡜ࡋ࡚㸪ᅗ 6 ࡟♧ࡍࡼ࠺࡟సືὶయഃࡢቨ㠃 ᗘࡀࡑࡢὶࢀ࡟ἢࡗ࡚పୗࡋ࡚࠸ࡿࡇ࡜ࡀᣲࡆࡽࢀࡿ㸬

22G = 7.5 kg/m s,2qave = 20 kW/m , Psat = 0.8 MPa

ParallelCounterThw, wall

Thw, wall

80

7070

flow direction

60
0100200

300

400

500

0600

Twf, wall

ParallelCounter

21

flow direction

100200

300

400

500

600

ParallelCounter25

flow direction

200ParallelCounter

26

22
Twf, wallG = 7.5 kg/m s,
280 qave = 20 kW/m , Psat = 0.9 MPa

100200flow direction

300 400z [mm]

500600(a) G = 7.5 kg/m2s, qave = 20 kW/m2, Psat = 0.8 MPa

240100200300 400z [mm]500600(b) G = 7.5 kg/m2s, qave = 20 kW/m2, Psat = 0.9 MPa

Fig. 6-1 Surface temperatures distributions on working fluid and hot water side.

ʯ˄Ĝʠૺ௾ཡࡉɅȤȫɥɺˋʺʣɺࣅ౫ൎᆔဖຣɅ࠲ȳɥॸ࢞Īൎ৐ᆔĆူ਄ᆔɅɢɥ྘ߏī90

2

G = 15 kg/m s
qave = 20 kW/m2, Psat = 0.8 MPa

ParallelCounterThw, wall

Thw, wall

80

70
flow direction

60
0100

200

300

400

2

G = 15 kg/m s
qave = 25 kW/m2, Psat = 0.7 MPa

ParallelCounter80
flow direction

500

70
0600

22100

200

300

400

500

600

19
ParallelCounterTwf, wallTwf, wall

28

21

ParallelCounterflow direction

18

flow direction

200100200300 400z [mm]500

170600(c) G = 15 kg/m2s, qave = 20 kW/m2, Psat = 0.8 MPa

100200300 400
z [mm]

500600(d) G = 15 kg/m2s, qave = 25 kW/m2, Psat = 0.7 MPa

Fig. 6-2 Surface temperatures distributions on working fluid and hot water side.

22000

2

G = 7.5 kg/m s
qave = 20 kW/m2, Psat = 0.8 MPa

G = 7.5 kg/m2s,
2qave = 20 kW/m , Psat = 0.9 MPa

21000

20000
19000

20000
19000
flow direction

flow direction

18000
0100

200300 400
z [mm]

500

22000

G = 15 kg/m2s2
qave = 20 kW/m , Psat = 0.8 MPa

100200300 400z [mm]500600(b) G = 7.5 kg/m2s, qave = 20 kW/m2, Psat = 0.9 MPa
27000

ParallelCounter2

G = 15 kg/m s,qave = 25 kW/m2, Psat = 0.7 MPa

26000

ParallelCounter22qave [W/m ]

21000

18000
0600(a) G = 7.5 kg/m2s, qave = 20 kW/m2, Psat = 0.8 MPaqave [W/m ]ParallelCounter2

qave [W/m ]21000

ParallelCounter2

qave [W/m ]

22000

20000

25000
24000

19000

flow direction

flow direction

18000
0100200300 400z [mm]500

600(c) G = 15 kg/m2s, qave = 20 kW/m2, Psat = 0.8 MPa

23000
0100200300 400z [mm]500600(d) G = 15 kg/m2s, qave = 25 kW/m2, Psat = 0.7 MPa

Fig. 7 Comparison of local heat flux distributions between parallel and counter flow.

29ᄵ༣གષ -!ழટড়ိ -!ද௫য়་

ᅗ 8 ࡣᅗ 6㸪7 ࡜ྠ୍ࡢ᮲௳࡟࠾ࡅࡿὶࢀ᪉ྥ࡟ᑐࡍࡿᒁᡤ⇕ᖹ⾮஝ࡁᗘࡢศᕸࢆᑐྥὶ㸪୪⾜ὶࡢ⤖ᯝࡢẚ㍑
࡜ඹ࡟♧ࡍ㸬࠸ࡎࢀࡢὶࢀ᪉ྥࡢ᮲௳࡟ࡘ࠸࡚ࡶ㸪⇕ᖹ⾮஝ࡁᗘࡣὶࢀ᪉ྥ࡟ᑐࡋ࡚┤⥺ⓗ࡟ቑຍࡋ࡚࠸ࡿࡇ࡜ࡀศ࠿ࡿ㸬ࡑࢀࡣ㸪ᒁᡤ⇕ὶ᮰ࡢ್ࡀ࡯ࡰ୍ᐃ࡛࠶ࡾ㸪ᘧ(4)࠿ࡽ(6)ࡢ㛵ಀ࡛஝ࡁᗘࢆ୚࠼ࡿࡇ࡜࠿ࡽ㸪ྛࠎࡢ
ᐃⅬ࡟࠾ࡅࡿ⇕ᖹ⾮஝ࡁᗘࡢ㛫㝸ࡀ࡯ࡰ୍ᐃ࡟࡞ࡿࡓࡵ࡛࠶ࡿ㸬୍᪉㸪Djordjevic (Djordjevic and Kabelac, 2008) ࡣၟ⏝ࡢ PHE ࢆ⏝࠸㸪R134a ࡜࢔ࣥࣔࢽ࢔ࢆసືὶయ࡜ࡋ࡚ᑐྥὶ࠾ࡼࡧ୪⾜ὶࡢ᮲௳ୗ࡛ᒁᡤࡢἛ㦐⇕ఏ㐩⋡ࡢẚ㍑ࢆ⾜ࡗ࡚࠸ࡿ㸬ࡑࡢ୰࡛㸪⵨Ⓨჾὶࢀ᪉ྥ࡟ἢࡗࡓᒁᡤ⇕ᖹ⾮஝ࡁᗘࡢศᕸ࡟ࡘ࠸࡚୪⾜ὶ࡜ᑐྥὶࡢ⤖ᯝࢆሗ࿌ࡋ࡚࠸ࡿࡀ㸪ὶࢀ᪉ྥ࡟ᑐࡍࡿ஝ࡁᗘศᕸࡣ㸪୪⾜ὶ࡛ୖ࡟ฝ㸪ᑐྥὶ࡛ୗ࡟ฝ࡜࡞ࡿࡇ࡜ࢆ♧ࡋ࡚࠾ࡾ㸪ᮏ◊✲࡜ࡣ␗࡞ࡿ⤖ᯝࡀᚓࡽࢀ࡚࠸ࡿ㸬
0.80.5
Parallel flow
Counter flow

0.60.3x [-]x [-]Parallel flow
Counter flow

0.40.40.2
20.2002G = 7.5 kg/m s 2
qave = 20 kW/m
Psat = 0.8 MPa

100200300 400
z [mm]

500

G = 15 kg/m s 2
qave = 25 kW/m
Psat = 0.7 MPa

0.100600(a) G = 7.5 kg/m2s, qave = 20 kW/m2, Psat = 0.8 MPa

100200300 400z [mm]500600(b) G = 15 kg/m2s, qave = 25 kW/m2, Psat = 0.7 MPa

Fig. 8 Local vapor quality along the plate.
࣭ ᒁᡤ⇕ఏ㐩⋡
ᅗ 9 ࡟ᒁᡤࡢ⇕ఏ㐩⋡ࡢศᕸ࡟ࡘ࠸࡚㸪୪⾜ὶ࡜ᑐྥὶࡢ⤖ᯝࡢẚ㍑࡜ඹ࡟♧ࡍ㸬G = 7.5 kg/m2s ࡟࠾ࡅࡿ୪⾜ὶࡢᒁᡤࡢ⇕ఏ㐩⋡ࡣ㸪ᑐྥὶࡢሙྜ࡟ẚ࡭࡚ 5 ~ 12%⛬ᗘ኱ࡁ࠸ࡇ࡜ࡀศ࠿ࡿ㸬୍᪉㸪G = 15 kg/m2s ࡛ࡣ㏫ࡢ
8000

8000
Parallel flow
Counter flow

7000

6000

h [W/m2 K]

h [W/m2 K]

Parallel flow
Counter flow

2

7000

6000

2

G = 7.5 kg/m s 2
qave = 20 kW/m
Psat = 0.8 MPa

5000
00.2

0.4

0.60.8

G = 7.5 kg/m s 2
qave = 20 kW/m
Psat = 0.9 MPa

5000
010.20.4x(a) G = 7.5 kg/m2s, qave = 20 kW/m2, Psat = 0.8 MPa

0.81(b) G = 7.5 kg/m2s, qave = 20 kW/m2, Psat = 0.9 MPa

8000

8000
Parallel flow
Counter flow

Parallel flow
Counter flowh [W/m K]

7000

7000

22h [W/m K]

0.6x

6000

5000
0

G = 15 kg/m 2s
2qave = 20 kW/m
Psat = 0.8 MPa

0.1

0.2
x

0.3

0.4

6000

5000
0

G = 15 kg/m 2s
2qave = 25 kW/m
Psat = 0.7 MPa

0.1

0.2x

0.3

0.4

(c) G = 15 kg/m2s, qave = 20 kW/m2, Psat = 0.8 MPa(d) G = 15 kg/m2s, qave = 25 kW/m2, Psat = 0.7 MPa
Fig. 9 Comparison of local heat transfer coefficient distributions between parallel and counter flow.

ʯ˄Ĝʠૺ௾ཡࡉɅȤȫɥɺˋʺʣɺࣅ౫ൎᆔဖຣɅ࠲ȳɥॸ࢞Īൎ৐ᆔĆူ਄ᆔɅɢɥ྘ߏī

2:ഴྥࡀほᐹࡉࢀ㸪ᑐྥὶࡢ᪉ࡀ 0 ~ 7 %኱ࡁ࠸ࡇ࡜ࡀศ࠿ࡿ㸬ࡋ࠿ࡋ㸪G = 7.5 kg/m2s ࡢሙྜ࡜ẚ㍑ࡋ࡚ࡑࡢቑ
ຍࡣᑡ࡞࠸㸬
Djordjevic ࡽ (Djordjevic and Kabelac, 2008) ࡣࡲࡓ㸪R134a ࡢ඲࡚ࡢ㉁㔞ὶ᮰࡟࠾ࡅࡿ୪⾜ὶ࡜⪏ᚋὶࡢ⇕ఏ㐩⋡ࡢẚ㍑࡛ࡣ㸪୪⾜ὶࡢ᪉ࡀ኱ࡁࡃ࡞ࡿࡇ࡜ࢆሗ࿌ࡋ࡚࠸ࡿ㸬ࡇࡢࡇ࡜ࡣ㸪ᮏ◊✲ࡢഴྥ࡜ࡣ␗࡞ࡗ࡚࠸ࡿࡇ࡜
ࡀศ࠿ࡿ㸬ࡓࡔࡋ㸪ᙼࡽ◊✲࡛ࡣᮏ◊✲ࡼࡾ኱ࡁ࡞㉁㔞ὶ᮰ࡢ᮲௳࡛⾜ࢃࢀ࡚࠸ࡿࡇ࡜ࢆ௜ࡅຍ࠼࡚࠾ࡃ㸬࣭ ᖹᆒ⇕ఏ㐩⋡ᅗ 10 ࡟୪⾜ὶ㸪ᑐྥὶᐇ㦂࡟࠾ࡅࡿᖹᆒ⇕ఏ㐩⋡ࡢ⤖ᯝࡢẚ㍑ࢆ♧ࡍ㸬ࡇࡇ࡛⏝࠸ࡓᖹᆒ⇕ఏ㐩⋡ࡣᒁᡤ⇕ఏ㐩⋡ࡢ್ࢆ⟬⾡ᖹᆒࡋࡓ್࡛࠶ࡿ㸬඲࡚ࡢᐇ㦂᮲௳࡟࠾࠸࡚ᖹᆒ⇕ఏ㐩⋡ࡣ㉁㔞ὶ᮰ G ࡢቑຍ࡟క࠸పୗࡋ࡚࠸ࡿࡇ࡜ࡀศ࠿ࡿ㸬୍᪉㸪ὶࢀ᪉ྥ࡟ࡼࡿᖹᆒ⇕ఏ㐩⋡ࡢẚ㍑࡛ࡣ㸪G = 7.5 ࡜ 10 kg/m2s ࡢሙྜࡣ㸪୪⾜ὶࡢ᪉ࡀ1 ~ 9%⛬ᗘ㧗࠸್ࢆ♧ࡋࡓ㸬୍᪉㸪G = 15 kg/m2s ࡛ࡣᑐྥὶࡢ᪉ࡀ㏫࡟ 3 ~ 5%⛬ᗘ㧗࠸್ࢆ♧ࡋࡓ㸬ࡑࡢ⌮⏤࡜ࡋ࡚㸪ప㉁㔞ὶ᮰࡛ࡣ⵨Ⓨჾὶࢀ᪉ྥ࡟ᑐࡋ࡚ᒁᡤࡢ⇕ὶ᮰࡜ቨ㠃㐣⇕ᗘࡀྠ᫬࡟ῶᑡࡋ࡚࠸ࡿࡇ࡜࡟ᑐࡋ࡚㸪
㧗㉁㔞ὶ᮰࡛ࡣ㸪ప㉁㔞ὶ᮰ࡢሙྜ࡜㢮ఝࡋࡓ ᗘศᕸࢆ♧ࡍࡢ࡟࠿࠿ࢃࡽࡎ㸪ᑐྥὶࡢ᪉ࡀ㧗࠸ᖹᆒ⇕ఏ㐩⋡ࢆ♧ࡋ࡚࠸ࡿ㸬ࡲࡓ㸪ᅗ 6(c)ཬࡧ(d)ࡢ G = 15 kg/m2s ࡢ⤖ᯝ࡛ぢࡽࢀࡓࡼ࠺࡟㸪ᑐྥὶࡢ᪉ࡢቨ㠃㐣⇕ᗘࡀഹ࠿࡟ప࠸ࡇ࡜ࡶ⌮⏤࡜ࡋ࡚ᣲࡆࡽࢀࡿ㸬

8000

8000

have [W/m K]

qave=20 25kW/m
ParallelCounter2

P = 0.8 MPa22have [W/m K]

P = 0.7MPa

7000
qave=20 25kW/m
ParallelCounter

6000
02

10
G [kg/m2s]

2070006000
0(a) Psat = 0.7 MPa

10G [kg/m2s]

20(b) Psat = 0.8 MPa

Fig. 10 Comparison of averaged heat transfer coefficient distributions between parallel and counter flow.
 ⤖   ゝࣉ࣮ࣞࢺᘧ⵨Ⓨჾ࡟࠾ࡅࡿ࢔ࣥࣔࢽ࢔ࡢఏ⇕ᛶ⬟࡟ࡘ࠸࡚ᑐྥὶ࡜୪⾜ὶ࡟ࡼࡿẚ㍑ࢆ⾜࠺ࡓࡵ㸪ྛࠎࡢὶࢀ᮲௳࡟࠾ࡅࡿᒁᡤࡢἛ㦐⇕ఏ㐩⋡ࡢ ᐃࢆ⾜ࡗࡓ㸬୪⾜ὶ࡟࠾ࡅࡿసືὶయࡢὶࢀ᪉ྥ࡟ἢࡗࡓᒁᡤ⇕ఏ㐩⋡ࡢศᕸࡣᑐྥὶ࡜ࡣ㏫ࡢഴྥࢆ♧ࡋࡓ㸬୍᪉㸪ప㉁㔞ὶ᮰࡛ࡣసືὶయഃቨ㠃 ᗘࡢศᕸࡣ୧᪉ࡢὶࢀ᪉ྥ࡟࠾࠸࡚࡯ࡰྠᵝ࡛࠶ࡗࡓࡀ㸪୪⾜ὶࡢᒁᡤ࠾ࡼࡧᖹᆒࡢ⇕ఏ㐩⋡ࡣᑐྥὶࡢሙྜ࡜ẚ㍑ࡋ࡚㸪1 ~ 9%኱ࡁࡃ࡞ࡿࡇ࡜
ࡀศ࠿ࡗࡓ㸬ࡲࡓ㧗㉁㔞ὶ᮰࡛ࡣ㏫ࡢഴྥࡀほᐹࡉࢀࡓ㸬ㅰ   ㎡ᮏ◊✲ࡣ㸪⤒㈝ࡢ୍㒊ࢆ 21 ୡ⣖ COE ࣉࣟࢢ࣒ࣛ(ᾏὒ࢚ࢿࣝࢠ࣮ࡢඛᑟⓗ฼⏝⛉Ꮫᢏ⾡ࡢᵓ⠏)࠿ࡽཷࡅࡓ㸬ࡇࡇ࡟グࡋ࡚ឤㅰࡍࡿ㸬

31ᄵ༣གષ -!ழટড়ိ -!ද௫য়་ᩥ   ⊩
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