SCIENTIFIC ABSTRACT BORISHANSKIY, V. M. - BORISIKHINA, V. I.

• Document Type: CREST
• Collection: Scientific Abstracts
• Document Number (FOIA) /ESDN (CREST): CIA-RDP86-00513R000206320017-0
• Release Decision: RIF
• Original Classification: S
• Document Page Count: 100
• Document Creation Date: November 2, 2016
• Document Release Date: June 9, 2000
• Sequence Number: 17
• Publication Date: December 31, 1967
• Content Type: SCIENCEAB

KUTATELADZE, Samson Semenovich. Prinimali uchastiye: LEONTIYEIT,
A.I.; BORISHANSKIY,.V.M.;_ZYSINA) L.M., doktor tekhn. naak,
rets~n_zent; GORDOV, A.N.., kand. fiz.-mat. nauk, red.;
ONISHCHENKOY R.N., red. izd-va; MITARCHUK, G.A., red. izd-va;
SHCHET321ITIA, L.V.J. tekhn. red.
[Fundamentals of the heat transfer theory] Osnovy teorii teplo-
obmena. I~d.2., dop. i perer. Moskva) Masbgiz, 1962. 455
WRA 15-4*
(Heat-Transmission)

----------
S/86;~/6Z/002/000/006/029
-Uiermodynamic analog A059/A126
Critical loads in boiling and the
where X 'is the value of the charzLCUristic at the measuring pressure p* and
f (p/pcrr,the,ordinate of the. curve- for a given P/Por- The equation
q
:'P
T2 F (10),
Clar. p*. 1. or Per Per
~is derived, where qor.- 'p and qer. an thecritical thermal loads at the
current pressure p and at'the measurdng pressure p*,, respectively. The critical
loads can,be determined also fromthe-formulas
or. p ,q, J,
q F, (P/Pcr)
or. p*
..-:where,F is the ordinate:of the'.generalizing curve for, the given relative pnes-
sure and
qer., po/f P0/Pcr)J9
qcr. Pi
where qcr. po Is the critical loid-atrandom pressure p0, and f (PC,/Pcr) the
ordinate of the curve for the-relative pressure PO,/Pcr. -V.G. Morozov, S.M. Lu-
komakiy, M.A. Styrikovich-J, and G.M. Folyakov are mentioned. There are 3 figures.
ASSOCIATION: TzKTI im. Polzunova (TsXTI imeni Polzunov)
.,Card 3/3

S/4862/62/002/000/014/029
A0591,1125
AUTHORS:
Porlsh,.=kiy, V. N. ,Maslichenko., P.A., rokin, B.S.
TITLE: Some data 'on the mecha*nism of film boiling in a large volume of
liquid
SOURCE: Teplo- i massoperenos. t. 2: Teplo- i massoperenos pri fazovykh i
khimiolie3kikh prevrashcheniyakh. Ed. by A.V. Ly1cov and B.M. Smol'~
skiy. Minsk, lzd-vo.AN BSSA, 1962. 128 131
TZKT: 'Theoretical formulas ~&r the calculation of the coefficient of heat
transfer developed by V.M. Borishanskiy,.L.A. Bromley, and S.S. Kutateladze were
derived on the assumption of.continuous laminar flow of the vapor layer near!the
surface. The formula for the mean-coefficient of heatexchange on boiling 'at
the vertical heated'surface is:,
7~7. 0 1 1
r
7~7c q const,
jL" qL
where L'is the vertical size of the heated surface, q the thermal stress of.the
card 1/4

LIM,

-3/852/62/002/00-0/014/029
Some d at aon the nephanism of film boiling in~ .... A059/A126.
for L were examined'. 'The experiments were performed in the tube shown In Figure
Dy the Moving-pAture films, -it was shown that vapor flow and va-por-film
shape in boiling at horizontal and vertical',surfaces are very different from
each other. In the.former case,,laminar flow occurs at the small-diameter sur-
face, with large, flat bubbles entering the volume and horizontal wave-11ke os-
cillattons of the interface
;_when the thermal stress~is lowered, the film thick-
nezs decreaSb3and so does the frequency of bubble separation, but the size of
the bubbles remains unchanged.. 'The vapor film at a vertical surface represents
an assembly of large vapor bubbles of various shapes near to pear-shape, separat-
ed by short section Isof a very thinvapor film; at great enlargements, a strong
tuxbulent notion of the vapor is observed. With increasing thermal stress, the
)aorizontal dimension-of the vapor bubbles and their rate of ascent are increased.
Average data on the Vapor thickness of various boiling liquids at a vertical
Ourface in time and along the operating section were obtained by measuring the
area of theYapor film With a planimeter., From the measured data, the mean film
ihickness iw time: It was shown by,thes'e cal-
..red of the vapor was calculated.
culations that the film thicknesses obtained this way are 10 to 15 times greater
than those calculeted.from equation (1), and also %"ed is about 20 times great-
r
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s/B62/62/602/000/014/029
Some data on the mechanism of film boiling in .... A059/A126
er than X", which'indicates the turbulent. nature of vapor flow in thefilm.
Heat-transfer was experimentally shown,to be independent of the length of the,
heat-transmitting surface in a ver.tioal position. There are 3 figures and I ta-
ble.
ASSOCIATION: Leningradskly politeldmicheskiy institut im. M.I. Kalinina (Lenin-.
grad Polytechnic Institute imeni 14.1. Kalinin)
Figure 2: JELperimental tube with a stoam ~collector at the working position:
I.,.-:working section; 2~.--.. 42
al - working tube
c
c ector; 3 40 0~
1 X 18 H9 T (iKhi8ii9T),- 4
-out.
voltaic lead
A X;~4
A
*1 25
card 4/4'

s/ll4/62/ooo/0O8/0b`z/oo6
E194/E:45'5
C'2 0 0
AUTHORS: Bo~~y_,_V_K,, Doctor of.Techni.cal~Sciences,
--M-itskevich, A.I., Candidate of.Technical,.Sciences
I
TITLE: Criterial working-out of complicated cases"'O'f"'
convective heat-transfer
PERIODICAL: Energomashinostroyeniye, no.8, 1962, 18-20
TEXT: In the general case of convective heat-transfer, the
temperature is not luniform over the surface and the heat-transfer
coefficient accordingly varies from place to peace on'the'surface.
Complicated temperaiure distributions arise in ribbed"c*oblIng
surfaces. Here thd,criterial heat-transfer relation~ship should
include, in addition~jto the usual criteria, complexes'obtained
for the heat balanc4i.~,condltions on the boundary of separation
between the surface and the heat-transfer medium i.e.
ATLve
Nu fl Res Pr, A " ) (1)
XMLT
or 5 Re, Pr, ?'TLM (2)
t f2
Card 14~

Cvltevlal wovk�ng-out ...
s/114/62/ooo/6o8/Oo2/006
E194/E455
where Nu = (qd~~)/( 6tXT); d9 - a typical mean dimension of the
system; XT and XM - thermal conductivity.coefficients of the
heat-transfer medium and surface material; LT and L~f - typical
linear dimensions that govern motion of the heat-transfer medium
and the surface geometry at the place of flow. To simplify the
calculations an experimental relationship must be found between the
parameters by specially working up the experimental data.. In
engineering practice, the final criterial formulae can often be
considerably simplified by obtaining a combination criteria and
solving the equations of heat distribution for an element- of
surface geometry, assuming a heat-transfer law. Two examples
show that test results are best worked out in the form
St = f (Remoast Prmeas) where Remeas = 'Re(XT/XM)P and
Prmeas ' Pr?1',-../XM)q. The cases examined are the most typical
elements of heat-transfer surfaceel a.rod and a circular rib with
uniform ooolihg over the perimetore The following *xpres alon is
obtained for a rod . I Ll + L2 L
Stav = f[Remeass Prmeas' - I 1 (11)
f Lfl
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s/ii4/62/000/008/002/oo6
Criterial working-out ... E194/E455
where Ll is the length of rod over which heat transfer takes
place and L2 the remaining length of the rod. A corresponding
expression is obtained for a circular rib cooled by an axial: flow
of heat-transfer medium. The method of working out the
experimental data described-here in recommended for other cases of
complex heat-transfer, for instance for transverse flowover tubes
or longitudinal flow over closely-packed bundles of tubes when the
heat transfer coefficient is not constant over the tube perimeter.
However, the use of these analytical relationships for unfamiliar
arrangements requir4 experimental verification.
There are 2 figures.-,
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43351
S/170/62/005/012/001/008
B104/B186
AUTHORS: Borishanskiy.,_Y. 1k., Kozyrev, A. P.
TITLE: Generalization of experimental data on heat transfer in
nucleate boiling on the basis of thermodynamic similarity
PERIODICAL: Inzhenerno-fizicheskiy zhurnal, v- 5, no. 12, 1962, 3 - 8
TEXTs In a previous paper (V. M. Borishanskiy, Voproey teplooidachi i
gidravliki dvukhfaznykh sred - Problems of heat transfer and hydraulics
of two-phase media, Gosenergoizdat, 1961, p. 18) the formula
a* - a* 1(p/pcr) was derived for the case of nucleate boiling where
p p
a* = a/q', a is the heat transfer coefficientt q the thermal load of the
heating surface. This formula makes it ~oasible to allow for the pressure
effect on the heat transfer of a medium over strongly varying physical
properties in a wide range of pressures. Formula
A,
a=B P q'19F3 (5)
(.9
-M 7,,Ip Pow'
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S/170/62/005/012/001/008
Generalization of experimental ... B104 B186
(Pkp - criticaII pressure, Tkp - critical temperature) is derived with the
aid of thermodynamic similarity (I. I. Novikov, Voprosy teplootdachi i
gidravliki dvukhfaznykh sred - Problems of heat transfer and hydraulics
of two-phase media, Gosenergoizdat, 1961, P. 7 and 14), allowing for the
experimentally proved fact that the heat transfer coefficient a is a
function of the thermal load q and of the physical parameters of the
medium when a nucleate boiling occurs with free convection. The function.
F3(p/pkp ) is universal .for thermodynamically similar substances and
characterizes the effect of reduced pressure on the heat transfer. The
shape of this curve is determined graphically by a method due to
Borishanskiy. Formulas
a 600 P qIs 0,37 +3,15 -L-) npil 0,2; (6)
'I~M'1- PKP PKP
TK
P-'118 p 1,85 ( P - 0,2 npit -E- > 0.2.
600 -F,/-
kP.MV. q'Is ex PHP PKP
are given for practcal application. Only p , T and M of the medium
or or
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3/170/62/005/012/001 /006
Generalization of experimental B104/B186
need to be known in order to calculate the heat transfor coefficient at
increased pressure and with free convection. The results obtained with
these formulas agree with the experimental data given in,a large number
of papers within � 30 %. There are 2 figures and 2 tables.
ASSOCIATION& Tsentrallnyy kotloturbinnyy institut imeni 1. 1. Polzunova,
g. Leningrad (Cential Boiler and Turbine Institute imeni
I. I. Polzunov, Leningrad)
SUBMITTED: February 26, 1962
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BORISIIANSKIY V.M.- AUDREUVSKIY, A.A.; ZHINXINA, V.B,
- p
Heat transfer to a staggered bank of tubes in transverse flow
of molten sodium. Atom. energ. 13 no.3:269-271 S 162.
(MIRA 15:9)
(Heat-Transmission) (Sodium)

BORISHANSKI _V.~,
X,. '... red.; KUTATELADZE) S.S., red.; LELICHUK, V.L.,
red.; NOVIKOV, I.I., red.; ROMMOVA, L.A., red.; MAZELI,
Ye.I.., tekhn. red.
[Liquid-metals] Zhidkie metally; sbornik stalei. Moskvap
Gosatomizdat, 1963. 326 p. WERA 16:12)
(Liquid metals-Thermal properties)

ACCESSTON'Z~M: AT4013171 8/3059/63/000/000,10005/0026-
AUTHOR: BorishansIdy, V. M.; Ivashchenko, N. I.; Zabl6tskaya, T. V.
.TITLE: Calculation-.of heat t --nsfer into liquid metals in 1)tarbulent flow when q is
constant
SOURCE: ZhidldycmetaRy*. Sbornikstatey. Moscow, Gosatomizdat. 1963., 5-26
TOPIC TAGS: liquid metal, turbulent flow, hydraulics, molecular heat exchange, heat I
exchange, heat transmission
ABSTRACT: When calculating turbulent flow in pipes, heat exchange is considered either
in two layers (Prandtl, Taylor) or in three layers (von Karman, Shvab). This investigation
further develops the three-layer thermal flow theory proposed by V. M. BorishansIdy
(Vtoroye soveshchaniye po teoreticheskoy i prikladnoy magnitnoy gidrodinamike. Riga,
Izd-vo tW Latv. SSR, 1962.) Flow is divided into three layers: a thermal sub-layer where,
heat is distributed by molecular transfer; an intermidiate, thermal core where heat is trans-
ferred both- by molecules and by turbulent flow, and a turbulent thermal core where heat is
transferr6d'only by turbulent flow. The investigation clearly shows that in the general case.
tho laws of turbulent transfer for low Prandtl figures are the same as for liquids when
Pr >, 1. The calculation of heat loss and temperature fields according to the proposed
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ACCESSION NIL AT4013171
scheme allows one to find the specific importance of heat transfer and momentum depending
on the Reynolds and Prandtl numbers. Comparative calculations We been made of tem-
porature fields and exchange rates by the three-layer flow theory for Pr. 3, 000). a simple formula is proposed.
"'7.5 + 0.005 Pe
for an interval where 200