Heat transfer for boiling on finned tube bundles

INT. OZIMM. HEAT MASS TRANSFER 0735-1933/85 $3.00 + .00 Vol. 12, pp. 355-368, 1985 ©PergatonPress Ltd. Printed intheUnitedStates

HEAT TRANSFER FOR BOILING

ON FINNED TUBE BUNDLES

R. Windlsch end E. Hahne Instltut for Thermodynemlk und WBrmetechnik Untverstt§t Stuttgart, D-7000 S t u t t g a r t 80, Fed.Rap. o f Germany Technteche H o c h s c h u l e

V. K i s s fQr KBltetechntk,

Leningrad,

USSR

(C~aL~micated by E. Hahne) ABSTRACT E x p e r i m e n t s were p e r f o r m e d f o r two d i f f e r e n t configuret i o n s o f f i n n e d t u b e s immersed i n R 11 e t s a t u r a t i o n c o n d i t i o n s (p = 1 b a r , ~ = 2 3 . 3 1 0 C ) . I t was o b s e r v e d t h a t the heat t r a n s f e r c o e f f i c i e n t i s a f f e c t e d by l a t e r a l f l o w s as ~ong e s c o n v e c t i v e i n f l u e n c e s d o m i n a t e p e r t o f an 1 B - t u b e s b u n d l e where • t w o - p h a s e onf l o w e x i s t s , the o v e r a l l heat t r a n s f e r c o e f f i c i e n t can be o b t a i n e d f r o m a s i m p l i f i e d 2-tubes configuration heated out of s i x - u t t h i n a f i x e d boundary c h a n n e l . Introduction A number o f both

single

made on p l a i n

single

ments on f i n n e d water /2/,

studies

a r e knoun f o r

t u b e s and t u b e b u n d l e s . tubes is

single

by G o r a n f l o

consisting /13/, ler

and S c h r o t h

17,

/h/.

by G O t t i n g e r

Heat t r a n s f e r

of finned

Jones / 1 4 / /16,

g i v e n by S l t p 6 e v i 6

and Bore r e c e n t l y ,

end Koycma / 1 1 / .

heat t r a n s f e r

on

/1/.

Measure-

t u b e s were p e r f o r m e d by H a l e y end West/3/

t u b e b u n d l e s was i n v e s t i g a t e d keJlma / 7 / ,

boiling

A survey of investigations

Heat t r a n s f e r /5/,

Wallner

by C o r n w e l l

et el.

results

boiling

for

/8,

18/ r e p o r t e d

In recent

times,

on such m e a s u r e m e n t s .

355

/6/,

Na-

9, 10/

on b u n d l e s

t u b e s a r e g i v e n by D a n t l o v e / 1 2 / ,

end Myers / 1 5 / .

from

Heimbach

Hahne and MOi-

356

R. Windisch and E. Hahne Experimental

ficlslly

results

enlarged

vi~ /19/,

Yilmez

Vol. 12, No. 4

of the b o i l i n g

surfaces" and Palen

performance

are p r e s e n t e d /20/,

Marto

of "arti-

by Stephen

and Mitro-

and H e r n a n d e z

/21/

and

others. It is found transfer 24/.

occur

in all

between

Geometric

array

single

vessel

/26/ and,

bubble

flow from lower Hahne

tubes

of the tubes

tainer

differences.

investigations

most

/25/,

and MOller

/17/

of h o r i z o n t a l l y

rents

induced b y them.

The lateral

tubes

upon

was found

each

2-dR.Forsuch transfer vels

other)

performance

in llne above

above

the other,

cient

of the upper

averaged Such

highly

termination

each

other)

tube c o r r e s p o n d s transfer

desiresble

behsviour

for another

- especially

experiments

uere

coefficients

and to learn

Test

For the tests, as in /17/. frigerant tubes

current.

ration

is cooled unit.

one

coeffito the bundle.

for an e x p e r i m e n t a l automatically

to obtain tube

de-

be

- tube distance.

in order

Thus,

heat arrange-

simplifications.

setup

and i n s t a l l a t i o n s is p r e s e n t e d

on h o r i z o n t a l l y These

by s t a b i l i z e d

is c o n d e n s e d tap water

water

vessel

finned

used

1. Retest

indirectly alternetlng

set for each tube

in the c o n d e n s e r

or water

temperature

and mixing

were

in Fig.

arranged

are heated

can be s e p a r a t e l y

either

The r e q u i r e d

tubes

inside)

power

by the use of a m i x i n g

in 6 le-

arranged

transfer

setup

The vapour

with

s =

the heat

(arranged

same

heater

The heating

by a t r a n s f o r m e r .

st s distance

of the entire

cannot

ef-

and the cur-

(of h o r i z o n t a l

of this

11 e v a p o r a t e s

these

Installations

in the e v a p o r a t o r .

(with a r e s i s t a n c e

which

the

A sketch

and

the mutusl

tubes

of a different

possible

23,

cause

good a g r e e m e n t

smeller

necessary

in b u n d l e s

about

2.

with

coefficient

simplifications

of the bundle

tubes,

by only two tubes

further

ment

of 16 tubes

/22,

of the con-

to simulate

s = 2"dR. The heat

assumed

transfer

influence

in heat

convection

arranged

to be small

of a bundle

heat

upper

it uss p o s s i b l e

also uith

overall

geometry

investigated

and v e r t i c a l l y

distances,

bundles

enhanced

affecting

fects

differences

and tube

of all,

tubes

that

from a refrige-

can be kept

valve

as shown

constant in the

Vol. 12, No. 4

BOILING ON FI~qED ~33E BUNDLES

357

i thermostated

CeU

i

Mixing Ve~el

i

Mixin(

i i

Top-Water Storage

I

Thermo MainPump

i

/ Refrigeration Unit

i

FIG. 1 Sketch o f t h e E x p e r i m e n t a l sketch.

The r e f r i g e r a n t

heater at is

saturation

located

perature

inside

kept

x

600

to allow

x

is

370

s constant made o f

am.

available

had been used b e f o r e The t e s t

placed

of t h e l i q u i d

boiling

in

the

tubes

Fig.

2.

in

In order

• Wieland-Marka

in

the

size

tem-

of

The f i n n e d ,

in

two d i f f e r e n t

bundle,

17,

18/.

arrange-

glass plates

and t o were

S u r f a c e waves and s p l a s h glass plates additional

2. D-7900

they

/16,

to prevent retroflows

the lateral

Metallwerke,

loop

g l a s s windows

mechanisms.

side along the tubes.

AG,

a pre-

an a i r

* a r e made o f c o p p e r ;

by about 70 mm and i n s e r t Fig.

with

experiments reported

s larger

via

experimental

temperature.

steel

of the boiling

i n g was p r e v e n t e d by l e t t i n g ms shown i n

temperature cell

stainless

test

t h e Flow w i t h i n

on e i t h e r

the evaporator

The e n t i r e

t u b e s were i n s t a l l e d

ments as shown i n simulate

into

Three s i d e s a r e e q u i p p e d u i t h

the observation

commercially

rated

at the respective

The e v a p o r a t o r 680

is

temperature.

Setup

Ulm,

F.R.G.

stick

shorter

out plates

358

R. Windisch and E. Hahne

Vol. 12, No. 4

370

C Glass ~Plotes

i

9

"lhermocouple

i 70

- -

I

-T

Tube

N~

I

I

6

s I-~ ~3 :

600

t

,c:

5

~~00 3 2

2

1 P

"t

s = 1,6dR =30.2/, mm,

18-Tube Arrangement

6-1ube- Arrangement

FIG. 2 F i n n e d Tubes end P o s i t i o n uithin the Evepo?etor

of the

of Thermocouples

10~ W

¥

mZK

t

-

o eo

"

o o ol;

2

o o' ° e 12

1o3

NC;..-~=,-

r

~

""

"

.......

8 6

-

102 10z

O

sepQrately

A

S

3

2

~

6 810 2 & 6 810~ heat flow density tin =

2

4 W/m z 10s

FIG. 3

Heat T r e n e f e r

Coeffiotent v s . Heat F l o u D e n s i t y Heated Tubes i n s B u n d l e

for

Separately

Vol. 12, NO. 4

BOILING ON F ~

3. Ex~ertmen, t e l

TUBE BL~DLES

359

Pro(sOurs

T e m p e r a t u r e s were measured w i t h

0 . 5 mm N i C r - N l

metal-coated

thermocouples ( P h i l l p s ) . With the thermocouples in ducts w i t h i n the Finned tubes, the tube inner temperatures uere obtained at s i x d i f f e r e n t points along the length and the circumference. The outside mean

wall

The heat

with

wall

temperatures

~ was averaged From the six t e m p e r a t u r e s . w coefficient was calculated from

~s b e i n g t h e s a t u r a t i o n

space above t h e l i q u i d . held constant Aa i s

in

all

t e m p e r a t u r e measured i n

At s p r e s s u r e

experiments,

was a l s o c o n s t a n t

t a k e n as t h e e n t i r e

the respective

~s = 23"310C" surface

indication

wattmeter, In order

from Q t o

class

with

saturation

tem-

The h e a t e j e c t i n g

ares

ares of the Finned tube.

1.5 b a r ) ;

pressure

the heating

gauge ( c l a s s

power by s

0.1.

to obtain

good r e p r o d u c i b i l i t y

t u b e s were F l u s h e d r e p e a t e d l y rator

the vapour

o f p = 1.0 b a r which was

The p r e s s u r e was measured by s p r e c i s i o n 0.1;

end an effective

temperature transfer

perature

were c a l c u l a t e d

of results,

i n R 11.

l o o p were c l e a n e d s e v e r a l

times,

the test

E v a p o r a t o r end r e f r i g e e v a c u a t e d end f l u s h e d

R 11.

Before the

e x p e r i m e n t s were s t a r t e d ,

t e d F o r 50 hours with a heat

t h e t u b e s had been hea-

flow density

Q/A a = q >

GOOD0

~/m 2

end a t a p r e s s u r e o f p = 1.3 b a r .

4. &.l

Bundle w i t h

~.1.1

Experimental Results

18 t u b e s

Separately_heated middle tubes As i n

The r e s u l t the various suring

/17/, is

o n l y the middle tube of e e a h

presented in Fig.

tubes is

uncertainty.

Ferences e x i s t

3. The s c a t t e r

approximately Thus,

it

is

within

assumed t h a t

among t h e t u b e - s p e c i f i c

the heat transfer

coefficient.

the

row was h e a t e d . of r e s u l t s limits

For

o f mea-

no d i s t i n c t

dif-

parameters influencing

360

R. Windisch and E. Hahne

4.1.2

Two heated Results

pared

of these

to former

arrangement results heated

range

The heat

are in full

upper

heated

ratio

4.1.3

b V the

Middle

tubes

Results shown

flow differ

coefficient crease

(no.

and entire that

increases

is e s p e c i a l l y

each

ments

a tube d i s t a n c e

In Fig. the middle

6, the heat

tubes,

Compared

higher

for t h e case

with

that

of lateral

exists

ficients, regions

the results

flow d e n s i t i e s

e remarkable

increase

e s p e c i s l l V for the upper

of 5 < 7 0 0

~/m 2 and

transfer row.

This in-

region

and

transfer

coef-

tubes

as m e a s u r e d

that

all

in Fig.

of 700 W/m 2 to

tubes

on

18 tubes 5 it can

is r e l a t i v e l V high.

in the heat

~ > 10000

coeffinatural

to the former m e a s u r e -

coefficients,

From c o m p a r i s o n

there

the heat

are

altogether.

are heated.

the effect

are heated

transfer

of s = 2"dR, the heat

are p r e s e n t e d

of heat

tubes

to the t o p

be o b s e r v e d

In the region

heated

the t w o - p h a s e

other:

transfer

in the

can be ex-

in the c o n v e c t i o n

boiling.

here at s = 1.6.dRare

coefficients

higher,

the heat

from the bottom

of incipient

ulth

all middle

pronounced

the region

ficients

bundle

2 to G) uithln

among

for the lower,

used here /25/.

5. It can be seen that

of the tubes

convection

ratio

two-tube

transfer

somewhat

4. Com-

the f o l l o w i n g

W/m 2. This effect

aspect

heated

2.0),

Heat

are here

for the case

in Fig.

cients

smaller

s/dR=

coefficients

agreement.

tube

in Fig.

(on a similar

transfer

6 = 3000 W/m 2 to 20000

plained

other are shown

from /17/

with a distance

tube

each

experiments

results

appear:

for the

tubes T above

Vol. 12, No. 4

10000 W/m 2,

transfer

in the bundle.

coefIn the

W/m 2 no e n h a n c e m e n t s

can

be observed. The heat uell

with

transfer that

No r e m a r k a b l e is purelv

coefficients

of the upper differences

liquid.

on the tube no.

tube

occur

of s t w o - t u b e for tube no.l,

2 corresponds arrangement. where

the onflow

Vol. 12, NO. 4

BOTT.TNG ON FINNI~ TUBE BI.II~DLES

/

10~ W

)

i mZK ff

O

2

0 •

'4.--

103

Rll,

8

~

/

/

/ >,/ /

/

/

/

/ /

/

1

p= : 1 b a r

/2r/

s : 1,6 dR=30,2&mm

O

/

/

O

ao 6 o eo 5 Oa O 4 ° eeOo 23 O

-"

i~_

361

.P

/

t,,beNo.

/

6

/

/

l-

v

6

<> rn

3

O

2

N

1

P

,4,--

"B ~J .-1-

I0210z

2

&

6 8 103 2 4 6 8 10¢ heat Flow densif y cl.

W/m2 I0 s

2

FIG. 4

Heat T r a n s f e r C o e f f i c i e n t vs. Heat Flow D e n s i t y f o r Two Heated Tubes Above Each Other i n m Bundle (~5 = ~6 )

Io

a

o

6

Iooo o ~,,

III

I

toO, Pll 6

..-

- • O

~eoted tube u n h e o t e d tube

"

I'

I I"

10

2

~

I/I

I

IA / I ~ / I I

/171 II

YI

~ I ~Y /"

I"

~

l' J / ""'" / ~" -

/.iF/ / "

I"

I

J/J"

Y""

I"

I

~ ~----

t u b e NO.6

HahnelM/Jller

2

Heat T r a n s f e r

6 8103 2 & 6 810 ~ 2 4 Wire z 105 heat How density q s = q 6 - - - - Fir,. 5 Coefficient v s . Heat Flow D e n s i t y f o r e l l M i d d l e Tubes

Heated

(~I 1

=

q2

. . . . .

tin)

362

R. Windisch and E. Hahne

For creeses

the tubes towards

ate boiiing

overaiI

bundie

this

with

being

tubes

flow of bubbies

W/m2),

heat

is an effect positioned

resuitlng

cient.

It shouId

be posslbie

the flow between

4.2 Six-tube

configuration

for the entire no.

5. Thus, of

of the upper

in /17/.

of the d l s t a n c e / d i a m e t e r together,

in s higher

ratio:

a sidewise

current

heat

to simulate fixed

nucIe-

coefficient

by that

end a vertlcei

is enhanced

of the heat

increase.

of tube

transfer

in-

we have

deveIoped

coefficient

as found

cioser

is hampered

over most fuiiy

to that

be r e p r e s e n t e d

arrangement

no.2,

is a smalIer

the heat

tubes

channeiing

there

coefficient

to tube

with

transfer

here,

cannot

of e two-tube

Obviousiy,

Oniy

spproximeteiy

in the c o n f i g u r a t i o n

tube

transfer

for the top tube(no.G)

corresponds

the tube

heat

compared

investigated.

(~ > 20000

The averaged bundie

to 6 the

the top rows;

s 100 % increase flow densities

no.3

Vol. 12, No. 4

off-

between

transfer

the

coeffi-

such an effect

by

boundaries.

i n channeled

flow

S i x heated t u b e s

4.2.1

The vertically glass ~/2

plated - a

parallel

directed

to the vertical

= 1 . 3 g . ~ apart.

In the region there

upwards

The results

flow is simulated tube ere

row.

shown

The plates in Fig.

of fully

developed

nucleate

boiling

is no difference

to former

results.

A distinct

in heat

transfer

can be observed,

however,

both

tion r e g i o n end f o r i n c i p i e n t b o i l i n g (competed

by two ere

7.

(~>20000

W/m2),

increase

for the convecto r e s u l t s in

Fig. 6). There i s ,

however, p r o b a b l y en e f f e c t of channel w i d t h : i n the

bundle c o n f i g u r a t i o n the " f r e e " width (between the tubes) i s sj s*

= 0.39 dR, w h i l e i n the channeled f l o w t h i s i s o n l y = 0.19 dR. This could e x p l a i n the increase of heat t r a n s -

Fer from the bottom tube ( n o . q ) , as e consequence of increased onflow.

VOI. 12, NO. 4

Bo'n',TNG ON ~

TUBE BUNDLES

10~

/ m2K

t

ie •

.

•

,:o

• •

////

/

/

/

s

,°oO

2-

/

/

6

/

363

t

o.•

2

¢-

o

8

Z/Z'<<~/,/~/

s,1.6 dR:30,2/+mm

6

--

/

V

• heated tube

Z~

5

0

3 2

t-

P

tube N~6

y, n-

02

2

Heat

CIn - - ~

FIG. 6 Coefficient v s . Heat Flow D e n s i t y f o r H e a t e d (01 = 02 . . . . = 0n)

Transfer

104 W

++ Wlm ~ 10s

2

heat flow density

I

-

all

Tubas

/

7

m2K -

•

l

~-

2

0

6

6

/

:o s

•

• ,

4

"

3

•

1

h~qted tube

/

•

/

¢-

V L~

tube No 6 5

O 0

3 2 1

10210z " 2

Heat

4

6 81(l z 2 4 6 810 ~' heat flow density c l n ~ FIG. 7 Transfer Coefftclent v s . Heat Flow D e n s l t y H e a t e d 2n C h a n n e l e d Flow (~1 = ~2 . . . .

4. W/m 2 10 5

f o r 6 Tubas ~n )

364

R. Windisch and E. Hahne

It is observed

that

of the full V heated being

not

heat

transfer where

heat

18-tubes-bundle(not

in t w o - p h a s e

ment

the overall

Vol. 12, No. 4

onflow)

coefficient

onl V the

upper

for heat

flow

can

well

of the top two tubes

transfer

included

coefficient

tube

no.

be a p p r o x i m a t e d

tube are

(no.

I as

b V the

6) in an arrange-

heated

in a 6-tubes

channel. This

holds

overall (no.

heat

transfer

6) in the

agreement i.e.

exists

for almost

bundle,

it can be observed

that

of tube

of the top tube

no.

nucleate

to the top tube 5 and 6 heated,

only

5 >

10000

heat

no.

then

transfer

only little

tubes

W/m 2,

are compared,

overall

2 to 6 differs

6) when

this

boiling.

flow a r r a n g e m e n t s

the averaged

no.

(no.

is compared

flow densities

developed

channeled

~ > 2000 W/m 2. When

with tube

for heat

fully

If only 6-tubes

coefficient

coefficient

18-tube

only

densities

from that

5 and 6 are hea-

ted.

4.2.2

Two h e a t e d Results

heated in

are

Fig.

4,

of

with

shown i n

Fig.

transfer

heat

region

of

channeled

No d i f f e r e n c e increased tubes,

experiments

the

controlled" er

tubes

again

and maybe

heat

in the

transfer

might

tubes

tionally, is

in Fig. are

to

the

results

in

the

"convection-

densities

"boiling

from the

are

shown

distinctly

controlled"

lower

of the

itself,

the

Comparison

of results

high-

(no.5) smeller

which

region.

The

of the two channel

produces

width

a more

uni-

of

Results

from the previous

chapters

is

9.

18-tubes-

heated

presented.

tubes

flow.

A comparison

all

two upper

coefficients

be an effect

5.

Compared

the

Im c o m p a r i s o n flow

of the c h a n n e l i n g

directional

presented

8.

only

flow.

occurs

heat

with

or

and 6 - t u b e s

with

mean c u r v e

only of

tube

the

arrangements no.

with

5 and 6 h e a t e d .

separately

hested

either Addi-

middle

tubes

VOl. 12, NO. 4

BOTT.TNG ON FII~IED TUBE BUNDLES

10~

W

T

_

~

• •

2

/

/

/

/

6 5

o o

/

3 2

/

Rll, ps=l b~r

/ #q;/

,/~,%.?

$ = 1.6dR=30,2&mm -- • heated tube 0 unheated tube

0

,// //,/ "//

/

m2K

365

~ /

/Z~,~ ~ r / / * *

~//

/~ /

/

/

,,t.be.o~

I

ZI tube No.5

/

•

V) r" (3

/ / "r// /

.ww-

2

//

~

~U "1-

10z

2

~

6 810 ] 2 ~ 6 810 ~ 2 heat flow density q s = c]6 -"'"

FIG. 8 Coefficients vs. Heat Flow Denaity H e a t e d i n C h a n n e l e d Flow

Hemt T r a n s f e r

~ Wire 210 s

for

2 TubeB

10~ °.°°o,1°o, 5 /(~O

- -

~0,~

m2K

~o ~0 4

I0

~o~11

t

-; 0o -

o%! nO,~ n

0

-0-

2

t.;

10~.

"-

8

o

6

••

e-

-O

-3-

•

i°

o ~

o_e

-O-

-..-- " ~ -

ff

,O,0,.

~ o -0

O

Io

,-

0

T

lo

: : ' -~,>

R11, p:lbar, s=1,6dR=1,6.18,9mm O unheated tube E) separntety heated tube • heated tube

,%~/] ~,~/'~d3~ ~/'~f L~)

/!

/

.~

/,'ooX Y o o ~.. /

/

/

_

/

¢-

•

2

0

10102z

2

/+

6 810 s

2

/~

6 810 ~

heat flow density FIG.

Comparison

of Results

for

Averaged

in Different

2

/, Wlm2 10s

q n --"

9

Heat

Transfer

Arrangements

Coefficients

366

tion

R. Windisch and E. Hahne

Altogether,

the

region

700 W/m 2) and

(~ <

vection-controiied These

deviations

and fiow tube which

region are

is increased.

the

For

heat

isted have

iikes

by inserting • different

here

in the convec-

part

of the con-

700 <

~ <

between

a weii

than

from the

tubes

the verticai

effect

is smaii,

in those

cannot

be properiy

or at Ieast with

such

higher

tubes

fiow exists,

and thus

bundIe

W/m 2.

the verticai

of bubbies,

Such

2000

to the

two-phase

fiow density

is smaii

walIs;

distance

tubes:

off-fiow

in a tube rigid

iower i.e.

directed

wali.

fiow density

the fIow c o n d i t i o n s

the

the heat

s iaterai

occur

to be due to onflow

upwards

when

fiow acts

in the

of boiiing,

between

a vertlcaliy

is increased

deviations

supposed

distribution

rows,

two-phase when

largest

Vol. 12, No. 4

regions

waIis heat

simushouid

fiow den-

sities.

6. C o n c l u s i o n s The heat is affected for ~ < ment,

2000

the

cularily here,

but

transfer

by lateral W/m 2 with

effect

flows.

of a bundie

In order

a simplified

of laterally

considered. shell

coefficient

to

tub-tube

positioned

Such c o n s i d e r a t i o n s

be subject

of further

of finned

obtain

valid

simulation

tubes

tubes results arrange-

has to be perti-

are not carried

investigation.

out

VOI. 12, NO.

BOILING ON FI~qiD ~JBE BL~IDLES

4

367

Nomenclature A

surfsce

dR

diameter

P

pressure

q

heat f l o w heat f l o w

s

distance

(finned

tube)

density of tubes

Greek symbols c~

heat t r a n s f e r

coefficient

temperature Indices e

outside

n

t u b e number

S

saturation

W

wall References

I•

8• S l I p E e v t E ,

2.

½•W• H s l e y and J•M• Westweter, B o i l i n g heat t r a n s f e r from s i n g l e f i n s , Proc• 3rd I n t . H e a t T r e n e f • C o n f . , v o l • 3, 245 (1966)

3.

D• G o r e n f l o , Zum M§rmeDbergeng bet der Bleaenverdempfung an R t p p e n r o h r e n , D i e s • TH K a r l s r u h e (1966) H.H• S c h r o t h ,

5.

.

½1tme-K§lte-Techntk

Luft-

und ½ § l t e t e c h n t k

~,

212 (1966)

M• G O t t i n g e r , Der W~rmeUbergeng b e t der Verdazpfung des ½ R l t e m i t t e l a R 11 an h o r t z o n t e l e n Rohren, D t s s . U n t v e r stt§t Stuttgart (1970) R• W e l l n e r , Der k ~ l t e m t t t e l s e t t l g e W§rmeDbergeng i n g b e r fluteten RohrbDndelverdempfern, Dies• UnivereIt§t Stuttg a r t (1972)

7.

½• NaketJams and K• Morimoto, (3speneee)

8•

L•S•

9•

K• CornwelZ end R•B• S c h D l l e r , v o l • 25, 683 (1982)

10.

1-5, 186 (1973)

Leong end K• C o r n w e l l ,

Refrigeration

~_.~, 3 (1969)

Chem. Eng. 3~3, Int•J•Hest

219 (1979)

Mess T r a n s l .

½• C o r n w a l l , N•W• D u f f t n and R•8. S c h D l l e r , An e x p e r I l e n t e l s t u d y o f t h e e f f e c t s o f f l u i d f l o w on b o i l i n g w i t h i n s k e t t l e r e b a t l e r tube b u n d l e , ASME paper no• 80-HT-45 (1980)

368

R. Windisch and E. Hahne

Vol. 12, No. 4

11.

Y. Moyome and H. Hashizuma, Boiling heat transfer on outside of horizontal tube bundles, 1Gth Int. Contr. of Refri@eration, Com. B1, Paris (1983)

12.

G.N. Danilowa and V.A. Dyndin, Research, ~, 48 ( 1 9 7 2 )

13.

P. Heimbach, Linde, Berichte s c h e f t 2 9 , 33 ( 1 9 7 1 )

I1+.

W. 3ones,

15.

3 . E . Myers and D . L . (1952)

16.

E. Hahne and 3. HOller, Boiling tubs bundles, Nat. Heat Transl.

17.

E. Hahne and 3. (1983)

18.

E. Hahne and 3. MOiler, Boiling from finned tube bundles - the effect of enhanced convection, 16th Int. Congr. of J ~ , Paris, vol. 81, 469 (1983)

Ig.

M. Stephan and 3. M i t r o v i E , Heat T r a n s f e r i n N a t u r a i Convective BolIing of Refrigerants and R e f r i g e r a t i o n Oil-Mixtures i n 8undle~ at T-Shaped F i n n e d Tubes i n R . L . Webb: Advances i n Enhanced Heat T r a n s f e r ( 1 9 8 1 )

20.

S. Yllmaz, 3.W. Palen and J. Tabsvell, Enhanced B o i l l n g Surfaces as single Tubes and Tube Bundles i n R . L . Webb: Advances i n Enhanced Heat T r a n s f e r ( 1 9 8 1 )

21.

P . J . M a r t o and B. H e r n a n d e z , N u c l e a t e Pool B o i l i n g Characteristics o f a Gewa-T S u r f a c e i n Freon 113, AIChE Symposium S e r i e s , v o I . 2 9 , n = . 2 2 5 , 1 ( 1 9 8 3 )

22.

Refrigeration

VDI-W§rmeatlas, (1984)

MOiler,

4th BQ.,

aus Technik

Engng.

Katz,

Heat Transfer,

Soviet

und Wissen-

4~9, 413 ( 1 9 4 1 )

Refrigeration

Engng.6_~O, 56

heat transfer in finned Conf., Minsk (1980)

Int.J.Heat

chapter

Mass T r a n s f .

Ha, V D I - V e r l a g ,

2._66, 849

DQeael-

dorf

23.

D. G o r e n f l o , Stand d e r 8 e r e c h n u n g s m e t h o d e n zum W§rmeObergang b e i d e r Verdampfung von ½ § l t e m i t t e l n in freier ½onv e k t i o n , D M V - T a g u n g e b a r t c h t , 9, 213, Eesen ( 1 9 8 2 )

24.

B. Sllp~eviE end F. Zimmermann, W§rmeDbergsngskoefflzlenten ten balm Blesensleden van Hslogen-M§itsmitteln an Rohrb O n d e l n , D M V - T a o u n o a b e r i c h t 9, 287, Essen ( 1 9 8 2 )

25.

N.M. P o v o l o t s k a y a ,

26.

E. Hahne, W§rme- u.

Cholod.

Techn.

4_~5, 20 ( 1 9 6 8 )

StoffObertragung

l Z,

155 ( 1 9 8 3 )