EVALUATION OF ARTICLE: HYDRAULIC RESISTANCE OF COLUMNS PACKED WITH A GRANULATED CATALYST

• Document Type: CREST
• Collection: General CIA Records
• Document Number (FOIA) /ESDN (CREST): CIA-RDP80-00926A001400040002-2
• Release Decision: RIPPUB
• Original Classification: R
• Document Page Count: 63
• Document Creation Date: December 14, 2016
• Document Release Date: December 18, 2001
• Sequence Number: 2
• Publication Date: September 12, 1949
• Content Type: REPORT

Approved F ASWROT 02j&y4jiG% P? '
0~? ffO040002-2
REPORT NO.
INFORMATION REPORT
CENTRAL INTELLIGENCE AGENCY
COUNTRY USSR
SUBJECT Evaluation of articles H ultc Resistance ?~f
Columns eked xjth , ,ranxulaa Catalyst
PLACE
ACQUIRED
DATE
ACQUIRED BY SOURCE
Summary 2 Papers
CD NO.
DATE DISTR.
NO. OF PAGES 1
NO. OF ENCLS.
(LISTED BELOW)
SUPPLEMENT TO
REPORT NO.
25X1A
~z Sep 1949
1. gzirau-U-c Resistance of C umns P eke with granulated Catalyst, BA Zakharoy and
AV Frost, Izvestiya Akademii Nauk, SSSR, Otdelenie Tekhnicheskikh Nauk, 1946, 421-39
constitutes a discussion of the Chilton-Colburn and Zhav'oronkov formulae used for the
determination of the hydraulic resistance of a tower packed with catalyst, and deriva-
tion of a third formula for the same purpose, which is held by the authors to be more
advantageous than the other two.
moral Evaluations
2. The type of operation and the catalysts referred to in this article are those frequently
employed in the refining industry, thus making the discussion pertinent. This iA a
mathematical discussion and only after a thorough study of the mathematics involved
and, perhaps also after verification of the experimental data given could an evaluation
of the importance of this contribution be made.
the work is well done.
25X1X 4.
Other Commentas
Ail Frost, the second of these authors He has previously
n.e must be regarded as a reliable research worker. 25X1A
published a considerable amount of good research on thermodynamics and related subjects
CLASSIFICATION REST
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Hg~rq%l v- Rosistaneq ~f E, to
The hydraulic resistance of catalytic co]ur.ms without the packing can be
calculated by the formula of d c Arcy
A 1j w2G
L\ P = W a
?d
where -6 p is the 163s of pressure in kg./sq.rn? /,; is the density of the
gas in kg. see. fd', %r is the average linear velocity of the gas in
m./sec, I is the length and d the diameter of the column in meters,
G the coefficient of resistance, depending upon the Reynolds number
Red =; , in which v is the coefficient of the kinematic viscosity
in sq. m./sec.
For a streamline flow (Red less than 2,320)
0 = /la/
Red
while for a turbulent flow (Rod more than 2,320) the coefficient of resist-
ance can be expressed, depending upon the Reynolds number, as follows:
At Red from 3,000 to 100, 000, according to the law of Blasius
G 0.3164
Red0.25
/I/
/2/
At Red from 105' to 3 x 106, the formula given by Nikurradze can be made
use of
G 0.0032 +
0.221
Reci0237
/3/
To determine the order of magnitude of the hydraulic resistance of a con-
tact column without a catalyst, comparative calculations were carried out
by the authors. Air served as the viscous medium and Its temperature was
15 and 500?. The column consisted of a single tuba or identical tubes
(for instance, 180 tubes per column). In one case the altitude of the coluum
was 1 m., diameter 0.1 m. In the second case the altitude was 2.544 r3., the
diameter 0.2 in. The rate of flow air by weight is connected with the
linear velocity by the relationship .:> = 3600 vos m where (J is the rate
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of flow in k./hr., vo linear velocity in m./sec., s? cross sectional
area of the tube in sq. m?, m number of tubes in the column, and r
specific gravity of the air for the given temperature. The rate of flow
so determined changed within 2.28 and 18 304 kg./hr. The physical pare
meters for air given by Kirpichev et al (1) were used. The results of the
calculations for an empty column are shown in Table 1 for given conditions
of performance of this column. This table shows that the resistance of
the column walls to the gas flow is quite small as compared to that exerted
by the surface of the catalyst grains.
Utdra ulie staence of Packed C lump
On the basis of analysis of experimental data, Chilton and Colburn suggested
(2) a formula for the calculation of the hydraulic resistance of columns
packed with granulated material. Ferry gives (3) this formula in the
metric system as follows:
6P =
202f?cvo2L
Dg
In this formula Z-Np is the pressure drop In kg./sq. m. due to the
hydraulic resistance] vo the linear velocity in m./see., through
/4/
the tube, L the thickness of the layer. of packing in motors,, D average
diameter of a grain of the packing in me., t? the resistance coefficient
depending upon the modified Reynolds number Res = D vo ~i / s 9 in which -r-
is the specific gravity of the gas in kg./cu. m.,a z is the coefficient
of viscosity in centipoises : z :. ~~.. g . Here IA is the coefficient of
viscosity in kg. sec./sq. rai., g acceleration due to gravity in M./see.
c a factor which is a function of the ratio tube 5 Dp is the
average diameter of the particle in meters, def d as a mean arithmetical
value of three sizes, while Dtuba is the diameter of the tube in meters.
A calculation of c and f? is quite difficult and inexact if attempted
graphically. For this reason mathematicaal expressions were derived by the
authors for the dependencies f? -- f(Re') and f( ~p based
on the graphs given by Perry. Dtube
Fig. 1 shows two curves characterizing the first of these dependencies.
Curve 1 refers to streamline conditions, while curve 2 refers to turbulent
conditions. The critical value of the Re' number is 44.1 The points on
the curves give values found from this graph, and the curves correspond to
the obtained equations. For the streamline flog (Rot less than 44.1)
912 f
/5/
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for turbulent flow (Re' more than 44,].)
0 30.2 /6/
f t '.-"-
Re+0.1
Figs 2 shows two curves for the dependence c- f (Dp/Tuba). The points
on the curve also indicate values graphically found and the curves
correspond to equations obtained. The curves for both conditions consist
of two parts described by different equations. The critical value, again
DP /Dtube, is 0.037. For streamline flow (curve 1) the following are
less than 0.037
valid: For Dp /D,tube
0.838
C
/7/
str D 0.03384
p
tube 1
and when this ratio is more than 08037
0.604
C
/8/
atr
D 0.3327
p
tub;5
For the turbulent flow (curve 2) the case of DP / Dtube less than 0.037 is
represented by equation
Ct
0.732
/9/
080578
D
P
tube'
while , when the value of DP / D tube is more than 0.037
at
0.424
D 0-22
p \\(tube.
/10/
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In 1944 Zhaavoronkov published (4) a study of the hydraulic resistance of scrubbers
packed with solid granulated material, which constitutes a part of his doctoral
dissertation (5). The experimental data are generalized as follows:
2f' Po'-11-
D 0 1- ree
where &P is the hydraulic resistance in kg./sq. m?; vo is linear velocity
in m./see., calculated for the complete cross section of the empty tubs;
H, altitude of the packed tube in motors; density of the air in kF,, sect/m,4;
f', coefficient of resistance which depends upon the Reynolds number
d vo
'3 of reo
y being the coefficient of kinematic viscosity in sq. m./aecr, de the equi-
valent diameter of the tube in motors, of o the free volume of the packing.
For streamline flow at values of the Reynolds number less than 40 to 50,
f d = 100/Re. For an unstable
to bulent flow within the Reynolds numbers
from 50 .. 5, 000, f 1 = 3.8 Ro?t'? and, finally, for a stable turbulent flow
at Reynolds numbers above 5,000,, ft will be independent of Re and aamoa nt
to Oa7
do
4 tube f%ve
stubs
where Vtuba is the volume of the packed tube in cubic meters, stube the
total surface which exerts the hydraulic resistance, square raters, i.a.,
a' + s". Here s' is the surface of the granules of the packing and
all the surface of the wall of the tube.
For a cylindrical tube
an
7 Dtub9H,
s a3za n - l vf'roe) tu3
V3
where n is the number of particles in the packing, s and v3 are the
average surface and the average volume of a granule of the packing, respec-
tively. For calculation of the hydraulic resistance of the packed contact
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column by the Zhavoro cov formula, it is necessary to determine experimentally
the values of n, s , V~f yes in addition to knowing the values of the
basic parsrnoters Of the co.uznn and of the gas stream.
By correlation of the values of the free volume experimentally determined by
Zhavoronkov and by the present authors for different granulated paackings.,
(Table 2',with the value of the average grain size, the dependence shown in
F'iC, 3 was estAbli.shed.
In Fig. 3 points on the curve correspond to experimentally determined values
of the free space of the catalyst bed and the average particle diameter, and
the curve is represented by
v'ree
?-- 0.222Dg0,252
Dependence of the Hydraulic Resistance
of a Column Upon the Average Diameter
of ttae C+t;san ,
It is quite important to find whether there is any interdependence between
the hydraulic resistance of the contact column and the average diameter of
the grain size. For this purpose calculations were carried out by the
authors, using the formulas of Chilton and Colburn and of Zhavoronktnr,,
respectival.y. A particular case was considered under the following con-
ditions: Diameter of the cola, 0.2 m; altitude, 2.544 m.; air tempera-
ture s 5000; linear velocity of the air in the streamline flow region,
0.068; that under turbulent conditions, 1 m./sec.; p __ 0.0459 kg. sec.2/m.4;
1j 8,0410- aq, m./sec,; V Y = 0.45 kg./cu. m.= 0.03617 centi-
poises; average grain diameter within 0.004 and 0.0127ri . 'he catalyst wa
shaped into cylinders.
The results are shown in Rig. 4, where the dots represent calculated values
and the curves mathematical expressions derived. Figs. 4 and 3 characterize
streamline flow corresponding to the formulas of Chilton and Colburn and of
Zhavoronkov. Curves 1 and 2 refer to turbulent flow tazsd the first of these
is based on the Chilton and Colburn formula,, the second on the Zhavoronkov
formula. For streamline flow the following expression corresponds to the
Chilton and Colburn formula:
DP 2.077-
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 TABLE l.- HYDmim. RESIST}Ip~041Qi3 TI flYA~YL1ANDClr1ADP80-0092
pp, pressure drop
Dimensions
In the empty
of the tube
column
^
Rate of flow
of the air
Cl?
A,
?~
a,
15
0,1
1
2,28
0,068
1
streamline
4,03.10-1
0,054
53,2
2 15
0,1
1
33,5
1
1
turbulent
0,019 1
35,2
219,2
3 500
0,2
2,544
3,46
0,068
1
streamline
1,09.10-6
0,07
1
67,6
4 500
0,2
2,544
3,46
0,0004
180
1
6,07.10-8
0,07
67,6
(0,000378)
11
5 500
0 2
2,544
-0,9
1-
1
turbulent .
.0,013
7,93
492,8
6 500
0,2
2,544
50,9
0,0055
180
streamline
0,004
0,01
985
7 500
0,2
2,544
18304
360
1
turbulent
446,4
3,09.105
1,96.10'
8 500
0,2
2,544
18304
2
180
0,044
4,85.10'
3,07.107
DP/Dtube in M.
FIG. 2. DEPENDENCE OF THE COEFFICIENT OF THE EFFECT
OF THE WALLS c UPON THE RATIO OF THE AVERAGE DI-
AMETER OF THE PARTICLES TO THE DIAATER OF THE TUBE
Dp/Dtu BY THE FORMUl A OF MILTON AND COLBM.
1 - for streamline flow; 2 - for turbulent flow
on
av. diameter of the particles, in.
FIG. 4. DEPENDENCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYST BED G) p UPON THE AVERAGE DIAMETER OF THE
CATALYST GRAINS, For turbulent flow: 1 - according to
Chilton and Colburn; 2 - according to Zhavoronkov.
For streamline flow: 3 - according to Zhavoronkov; 4 -
according to Chilton and Colburn.
Izv. (tekh,)
1946, .421 ff.
25-
Z
qj
turbulent flow
14 I.
fG A? Y
SD 6
Ret modified Reynolds number
streamline flow
FIG. 1. DEPENDENCE OF THE MODIFIED FRICTION
FACTOR TO UPON THE MODIFIED REYNOII)S NUMBER
Re' BY THE FORMULA OF CHILTON AND COIBURN,
1 - streamline flow; 2 - turbulent flow
0 0
o Zhavoronkov's data
? experimental data
p !0 20 J . !f0 50
av. diameter of the particle
FIG. 3. DEPENDENCE OF THE FREE VOLM-f] OF TILE
CATALYST BED UPON THE AVERAGE DIAMETIsTR OF
THE PARTICLES.
-Aluminosilicate
catalyst
Catalyst for con-
version of CO
Vanadium catalyst
Coke
Glass granules
Coke
a
Gravel
Coke
Andesite
Cylindrical
tablets
Tablets
n
Irregular
Pear-shaped
Irregular
Spherical
Irregular
Av. diam-
Dimensions of the
eter of
the grain
Free
grains, mm.
mm.
mace
5 X 5 X 8
6,0
0.35
9X9X4
7,3
0,35
11X11X6
9,3
0.38
11 X 11 X 6.5
9,5
0,43
29,6 X 25,8 X 18
24,5
0;532
20 X 20 X 37,5
25,8
0,500
35,6 X 28,8 X 18
27,5
0,535
47,6X41,5X33,4
40,8
0,545
56,8 X 40,8 X 29
42,2
0,570
52 X 40,3 X 35,5
42,6
0,560
56 X 43,7 X 32,6
44,1
0.565
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b
~
JJJ
turbulent
flow
AX
-
I
s
treamline
o
flow
Z
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The expression corresponding to the, Zhavoronkov formula /11/ is given by:
Psh 1.866 x 10`"5
DD 3.044
/14/
The interrelationship of these expressions for small values of the average
particle diameter, below 0.0065, is
P h = 3 LPc.c, m 100 /15/
e-chile for values above 0.0065 it is:
Ap~I, = 1.49LPc.c. '" 9 /16/
For turbulent flow the following obtain:
A 'zh = 0&:L6
P
The equations 17 and 18 can be combined as follows:
/17/
/18/
/19/
Dependence of the Hydraulic Resistance
of a Column Packed with Granulated
Catalan t,o t Rata r
lnasnuch as the basic equations under discussion show no clear connection
between the hydraulic resistance of the contact column and its diameter,,
this problem was also considered in the study under report. The conditions
and parameters of the principal hydrodynamic values were in the main the
same a+ for the expression L p = f(D ) discussed before. The difference
consists in the values of Dip and D P . The average grain diameter was
constant, 0.0073 motors. vfre wastta~ 0.359. Silica lumina catalyst was
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psh 0.0038 -P 1 *68
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used, shaped as cylindrical tablets, 9 x 9 x 4 mm. The diameter of the
catalyst column, consisting of a single tube, varied from 0.04 to 0.7
meters.
Fig. 5 shows the results of the calculation for particular cases, based on
the formulas of Chilton and Colburn /4/ and of Zhavoronkov /11/. The four
curves shown each consist of two branches corresponding to the mathematical
e re ;erns for the dependency o - f (Dtube) for tubes with small or
large diameters. The points represent values calculated by the formulas
/4/ and /11/.
The formula of Chilton and Colburn for streamline conditions to represented
by the curve 4. The critical value of the tube diameter is 0.162. At smeller
values
L r0,c,
2.363DO.1Q43
tub
/20/
For cases where the diameter exceeds 0,162
The curve 2 is valid for the regions of turbulent flow. At values of the
tube diameter below 0.2042
A Pc. c. -= 2663Dtu1
.1.992DO.035
tube
/22/
and for diameters exceeding 0,2042, the relationship
/- p'c.c.,
i28'' 'tubbe56g
/23/
Data pertaining to the hydraulic resistance of columns with granulated packing
as a function of the column, diameter obtained with the aid of the 7havoroulcov
formula, are represented by the curves 3 and 1. The first of these refers to
streamline conditions, the second to turbulent conditions. For tubes with a
small diameter, i.e.p below 0.074
pth - u .
Dtube
/24/
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 App
rove
d F
r
r?
mob;
A -0
49
=2
r-4
diameter of the tube in in.
G. 5. D3P_ *')Eh!CE CF THE HYDRAULIC RESISTANCE IN THE
CATALYTIC TO:P.;R Oc UPON ITS DIAMETER D
curves 1 and 3 were calculated accordin bjQ- The
and curves 2 and 4-according to Chilton and Co1bu Colburn.
FIG. 6. EXPERIMENTAL UNIT FOR THE STUDY OF THE
EFFECT OF THE LINEAR VELOCITY OF A STREAM OF GAS
UPON THY HYDRAULIC RESISTANCE OF A COIihpl WITH
SOLID GRANULATED CATALYST
TABLE 3. EFFECT OF THE AVERAGE, GRAIN SIZE OF THE CATALYST (D AND THE DIAMETER OF THE
CONTACT ('nTTV
,R, /?
.
__._
. . .. ___
> 470
470-77
77-25
25-12
12-2,3
< 2,3
>100
Interval of values of
Dp for known Dtube m
for Dtube = 0,7 M
< 0,0015-
1010015-01009
0,009-0,0028
0,9,028--0,0583
~-- T-?.004x
OAST 0, 017
> 0,017
for D b. = 0,07 Y
< 0,0073
(0,0005 -0,0073)
> .0,0073.
(0,0073-0,65)
for Dtube =0,04m
0,005-0, 015
Interval of values I
I. e,.) of 'tube for (From D of the
D P = 0.0073 m, !entire interval
> 3,43
3,43-0,562
0, E62-0,182
0,182-0,087
0,087-0,017
< 0,017
> 0,73
e The numerical value
~v
~ 2 y
D
Ie2
0
?
D
1
e!
?
I
?J
e7
m
'1
6
?
02
0
,2 4Y S 41 0, [ L'
linear velocity of the air, m./sea.
E
FEEDHECE O THE H
YDRAULIC RESISTANCE 4p OF
COIURE WITH GRANULATED CATALYST UPON THY LINEAR VELOCITY
OF THE GAS STREAM OBSERVYD IN THIS WORK. 1 - d p at the
air inlet to the column; 2 - op at the middle of the
column; 3 - average values of Gp; 4 - pp at the emit
from the column; 5 - Gp according to Zhavoronkovl 6 - sp
according to Chilton and Colburn; 7 - &p according to
Chilton and Colburn, assuming the average die eter.;of.the
particle, to be equal to the cubic root of three
dimensions.
3D p 0,085
2,11 D 0,03
P
pp 0,09
1
D p 0,I04
3,08 Dp 0,202
51,33 Dp 0 12
Dp 0,098
85,6 D P 0.373
Itctreme values Dtub
given for the
Values of K
interval
corresponding to them
(7; 4)
(2,64;
2,97) D 0,04
tube
1
(3; 0,8)
(2,22;
2,12)
Dtube 0,04
(0,5; 0,2)
L. ,0,04
(0,15; 0.09)
(1,05;
1,06) D o,ca
tube
(0.07; 0,018)
(3,2;
3,14) 10.
Dtube2lk
(0,017; 0,003)
(3; 0,R)
cube
(51,9; 49)
D tube 0.036
0,015-0,034 I 0;'822-0,0087 I 600 Dp 0,999 (0,03i 0,008)
of M,
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?,D tube0, 059
(85;89 1
tube 0.913
(165,2)? 1
D tub, .0 , 4211
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while those with a larger diameter
Aube
/25/
In the case of the turbulent flow (cum 1) the critical value of the diameter
of the cols for the conditions and parameters discussed is 0.138. For
smaller diameters of the coli.m n the equation
?zh = W-1 /26/
tube
was derived, while for diemotr.?rs exceeding 0.138, the equation
is valid.
/27/
The mathematical expressions 20 - 27 for the det?nnination of the effect of
the diameter of the col t on the hydraulic resistance, which were obtained
by using,g, the formulas of Chilton and Colburn and of Zhavoronov are mutually
related as follows (Fig.. 5). For streamline flow at diameters of the tube
smaller than 0.065
pah -1.1.0.7/.. Pc.c. + 256.5 /28/
and diameters larger than 0.065
Z-\ -32.3 + 128,4 /29/
For turbulent flow at diameters of the tube below 0.1.17
Pzh r-0.7164 c s cs. + 1324 /30/
and at diameters larger than this value, the relationship
A h = -0.2221:, Pc.c. + 817
/31/
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ai or the middle of the column (at the height of 0.5 ra. )
Pttaiddle = 1.01-vo ~9 01 /33/
xa'aich is represented by curve 2. The pressure drop at the exit from the
catalyst color n (hydraulic resistance of the layer l m.. thick) Is repre-
sented by the curve 4 based on the equation.
exit = 935.4-7.1-891
Curve 3 gives the average value of the hydraulic resistance
1373
Paver age = 984v0.
/34/
/35/
which is an average of the values -shown by the curves 1,, 2 and 4. It should
be noted that the scattering of the points observed for high air velocity
is connected with a certain degree of inexactness in the flow meter scale,,
which is built on extrapolated values. The curve 5 joins points calculated
by the formula /11/ of Zhavoronkov for the experimental conditions and para-
meters used In this sttIy and is described by two equations. The critical
value of 'the- rate of flow is 0.1122. For ptreamline conditions whom vo
is loss than 0.1122
Psh 1.58.5vo
/36/
The region of turbulent flow with v exceeding 0.U22 is characterisgd by
the equation 37. Forimla /4/ of Chilton and Colburn is represented by the
points of the curve 6 for the conditions used here. The critical value is
0.089 m../sec. The streamline section of the curve can be. expressed by the
equation 38.
4e~S P 2;h =
931.8.
/37/
pc.~a
52.5v0
/38/
The section of the curve describing the turbulent conditions., that is, where
vo exceeds 0.089, is described by the equation
ZL. .c. 359,7vv?8 /39/
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For the sake of comparison, the curve 7 was drawn f ro n data obtained by the
Chilton and Colburn formula for the case where the average grain diameter
is a cubic root of three dihiensi+^na,.
The values of the pressure drop in the air flow passing through the catalytic
column according to Zhavoronkov /36/ and /37/, and according to Chilton and
Colburn /38/ and /39/, are connected between themselves and with the average
values of the pressure drop established by the present authors /35/ as follows:
A Ph 2.6 ,LPe.co /40/
Pzh 0.9352 A Par,er. 21.6 All
%.c. 0.3697 /-\Pav ore /42/
The pressure drop at the inlet /32/ and at the exit /34/ from the contact
column is connected with the average value /35/ as follows:
/-\- Piniet 1,3 A Paver. /43/
?exit = 0.944 /.. Phver. /44/
The pressure drop of the air at the inlet /32/ into the column is expressed
according to Zhaavoronkov /36/ and /37/ as follows:
p'i.nlet -?= l x437 ' h - 6 A5/
bra; DisquBsion
.It is of interest to campare the values of hydraulic resistance of catalytic
coluns, empty as well as packed? and to appraise the effect of the number
of tubes in a collector contact column upon the hydraulic resistance. The
numerical values are given in Table 1. The hydraulic resistance of the empty
catalytic column) as dependent upon the Reynolds nutmber$ was calculated by
the formula of dArcy /i/ and /la/ for streamline conditions (cases 1, 4 and 6).
For turbulent conditions the law of Blasius /2/, (eases 2, 5 and 8) and the
formula of Tikuradzo /3/ (case 7) were m de use of. Considering that the
Zhaveronkov formula has two members which - describe,, respectivOyw, the
hydraulic resistance caused by the surface of the walls of the column and
the surface of the grains of the catalyst, the question can be answered whether
this formula permits a correct evaluation of the hydraulic resistance of the
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 Approved For Release 2002/01/11 : CIA-RDP80-00926AO01400040002-2
empty column. For this column the following is valid for streamline conditio;as:
.Pstr,
200 P r vOE
Dtub; vfree'
For the turbulent region the following obtains:
__ _
L~ Pt
%Ubel?2vfree
As follows from Table 1, the hydraulic resistance of the empty catalytic
tower calculated by the Zhavoronkov.formula has a considerably higher value
for all cases under consideration here (100 - 1,000 times), as compared with
the value obtained with the aid of hydrodynamic formulas widely employed in
practice. It is possible, therefore, to conclude that the hydrauli, resistance
of empty catalytic columns cannot be calculated from the Zhavoronkov formulas
For packed catalytic columns the hydraulic resistance,, as calculated from the
Zhavoronkov formula, is represented in the last column of Table 1. The cata-
lyst consisted of cylindrical tablets 9 x 9 x 4 mm., of average diameter
0.0173 m. and free volume 0.359. By correlating the valuesof the hydraulic
resistance in the empty and catalyst-packed columns, one observes that the
hydraulic resistance of the columns with the catalyst exceeds the resistance
of empty columns 100,000 times or more. Hence, the hydraulic resistance to the
gas flow exerted by the yells of the contact column is quite negligible.
In commercial practice catalytic columns are of a special value, made up of
a bundle of tubes of the same diameter. In streamline flow and at a constant
value of the weight rate of gas flow, a change in the number of tubes in a
uacked column of this type exerts no effect upon the resistance of the coiu r.
The linear velocity is used in the equation for hydraulic resistance in the
first degree; consequently for the cases 3 and 4 in Table 1, the following will
be valid:
P4 = mv4 : MV4 .~ 1
P3 V3 mv4
7.6 fT 0.x,.01"
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 Approved For Release 2002/01/11 : CIA-RDP80-00926AO01400040002-2
because v3 = -!,m (m is the number of tubes in the column). A totally
differ ant situation obtains in the regions of. turbulent 'low. Here the
linear velocity is used in the fornula in the degree of 1.8. Discussing
the cases numbers 8 and 7 of Table 1, it is seen that, inasmuch as the
height rate is constant, v7 - mv8 :
1.3
P8 mvg
1.8
L_\17 (mv )
The hydraulic resistance of a catalytic collector column decreases in pro-
portion to the number of tubes taken to the degree of C.$; consequently`
: f the technology of the process is connected with high rates of flow by
weight of the gas izn .the region of turbulent flow, and the value of the
hydraulic resistance exerted by the catalyst or the dinyions of the
column do not permit to realize these velocities in the column, consisting
of a single tube, then in order to rerove these hindrance a collector
catalytic column should be used with a number of tubes equal to the ratio
of the linear velocities for a.simple and a collector col: . (Thus, for
the cases 7 and 8 of Table 1, m V7 1C0) .
V8
~'he effect of the average grain diameter upon the hydraulic resistance is
described qualitatively by the Chilton and Colburn f oru~lr
s /4/ and that of
Zhavoronkov /11/ . The hydraulic resistance of the cataly tic power drops
a,rith increase of the grain size. The Chilton and Colburn foxiula gives for
both hydrodynamic conditions a lower drop of the hydraulic resistance of
the column with increase of the average grain size, as ca ipared to the
Zhavoronkov formula. An exception is presented by eerie cases in the stream-
line region, where Dtube/ D exceeds 30. Here a reverse situation obtains
and the Chilton and Colburn Formula shows a larger drop in the hydraulic
resistance, with increase of the grain size as compared to the data given by
the Zhavoronkov foe la. The connection between the two formulas with
:aspect to the dependence gyp f(D ) is a straight line for streamline
conditions (/15/ and /16/) and an ex nential for turbulent conditions (/19/) .
A very interesting result was obtained by the authors in the study of the
affect of the dS.sr )ter of the contact column upon the hyd aulic resistance.
According to equations /20/ through /277/ and Fig. 5, the two formulas show
contrasting effects of the diameter of the catalytic column upon the
S
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 Approved For Release 2002/01/11 : CIA-RDP80-00926AO01400040002-2
hydraulic resistance. With increase of the diameter of the catalytic column
the hydraulic resistance for both hydrodynai.c conditions increases, accord-
ing to Chilton and Colburn, but drops according to Zhavoronkovo The connec-
tion between the two formulas is etraightline in character, (equations /278/
through /31/).
Ly correlating the quantitative interpretation of the dependence of the
hydraulic resistance of the catalytic colunns with the granulated packing
upon the linear velocity of the gas strew, average grain size and diameter
of the column, as expressed by the Chilton and Colburn and Zhavoronkov
formulas, the following characteristic of the Chilton and Colburn formula is
obtained: In L`a, p w. f(vo) considerable lowering of the values of /gyp is
noted; for & p .? f (Di,) a considerable decrease of the value of L p and,
finally, in i p =- f(Dt bs) a totally abnormal character of the functional
dependence, as cozipaaed to conventional concepts is manifested
Additional calculations of the dependence of the hydraulic resistance of
columns packed with granulated catalyst upon average grain site of the packing
and diameter of the column, which were based on the Zhavoronkov formula, mada3
it possible to write a general formula embracing all principal factors which
determine the performance of catalytic towers. These factors characterize
the contact column (altitude II, diameter Dtubs), the granulated catalyst
(average grain diameter D) and the viscous medium N More N is the product
obtained by multiplying thie density t-.~, kinematic viscosity ^y and the lineaa,
velocity of the gas vo) :
MIN
Dm6D C
Ptube
The hydraulic condition of the performance of the catalytic column deter14ne.3
the exponent of the co:ponents of N. For stream ne conditions NYstr 0 ?
while for turbulent conditions N.t P y 0.Z rol? To establish the o
character of the hydraulic conditions prevailing in the catalytic column with
granulated packing, and considering that the criticaal value of the Reynolds
number corresponding to the transition frown the streamline to turbulent state
is 40 - 50, the Reynolds number should be determined from the expression
at In this equation the equivalent diameter of the column with
'urfr?e
the catalyst (de) was substituted by the average grain diameter DP , which
is valid when Dtnbe considerably exceeds the value of DP
.
In order to conpare the value of K in equation A6/ and the extoat of the
effect upon it of Dp and Dtue, additional calculations were peY%1oxmd.
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 Approved For Release 2002/01/11 : CIA-RDP80-00926AO01400040002-2
For this purpose into the Zhavoronkov formula /11/ int :. adiate values were
included, and it was connected with equation /46/. The values of and no
were taken from the corresponding particular expressions ..th cone oration
of the value of Dt be . For the streamline conditions Ino for DP was
P
en from equation /14/, n for Dty~~ from equations /24/ and /25/ for
the turbulent flow m0 from equation /18/ and no from equations /26/
and /27/.
Catalyst grains had uniformly the shape of a cylinder, with a ratio of the
diameter to the altitude D3 = 2h39 unlike the varying ratios a
D3/h3 when particular expressions for the dependencies !1 p . f Dp) and
L\,P - = f (Dtui.*) were to be found. In the determination of the effect upon
the coefficient K in the equation /46/ of the average grain diameter D ,
the latter was changed within 0.0005 to 0.05 ra. at Dtube values of p'
0.7 and 0.04 m. In the determination of the effect on YK of the diameter
of the cylindrical catalyst tower consisting of a single tubs,, the value of
Dtube was changed within 7 and 0.008 m., while the value of DP was kept
constant at 0.0073 m. The free volume of the catalyst bed for various value r3
of Dp was determined from equation /12/.
The results of the calculations are given in Table 3. The values obtained
for K =f(D) and K = f (Dtubs) shoald be introduced into equation /46/.
The equatioh
will finally be obtained. The numerical values of KO and those of the
exponents of DP and Dtube are shown in Table 4. o These values differ
and refer to a definite region of values of Dtubo/ Dp and to the prevailing
hydraulic conditions.
The value of Ko in equation /47/ is a physical factor of the order of
magnitude m , which has so far not yet been determined. For streamline
conditions it is close to l ; for turbulent conditions, of the order of 0.8.
Concerning the effect upon hydraulic resistance of the geometrical form of
the granulated catalyst, which will affect the coefficient KO in the
equation /47/, two groups of -eonetrical forms can be considered, within
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 Approved For Release 2002/01/11 : CIA-RDP80-00926AO01400040002-2
TALC 4. 5~?M?iIC? D 1TALM OF K~e AND Q, in L ND n TINT EQUATION /47/ FOR D F ` REN
IT`ERV t OF THE 'RATIO OF TIC BIA ETE', OF THE TUB To TIM, AVE k E DXAt TDR OF IME
No,
Interval of
Dtube/Dp
P?u rical'
value of
KO
Values of
in for DP
n for Dt,ft
1 turbulent . . . . . . . . 470
'~
3.00 2,030 0.040
2
. . . . ? . ? ? 470 - 77
2.11 2,086 0.040
3 ft . . . ? . . ? . 77 - 25
1.38 2.176 0,040
4 . ? ? ? ? . . . 25 - 12
1,16 2.225
0,040
5 ~a w . . 12 - 2.3
/
3.08 1.934 0.211.
6 2n3
8.50 1.487 01480
1 streamline . . , . . , . . x-100
51.33 2.924 0,056
2 ?' .
100
17,60 3.142 0.056
(}
3 8
? . . ? . ? ? . - 3
[
8
5.60 2,670 0.316
4 " . ? . ? w 3 - 1,2
/
165.20 2.205 0,742
which the ratio of the surface of the grain to its volume s. /v3 a,--d conse-
quently K. will be constant: I, ftuy nde s of a h3 = 005D &nd r a longer
cylinder of h -- 26 and
3 cylinder
(h3 = D3), a cu alas a ephane. Here h and D3 are, respectively, the
altitude and the diameter of the grain in meters,
For an appraisal of the effect of the dimensions of the grain D upon the
connedtion of K with the geometrical forri, the value of D pwas varied in
size 100 times in the calculations performed, keeping the p diameter of the
catalytic ooltamn constant at 0.7 m. The results are shown in Table 5. The
dimension of the grain DP does not markedly affect the relationship between
KO and the geometrical form of the grain. For the group II, lower values
of Igo were obtained, and for streamline conditions a more considerable drop
of KO is observed, 20 a as compared to 10;j' for turbulent flow. Thus,,
a more compact geometrical form of the grain, i.e., a reg-ilar cylinder, a
cube or a sphere, exert 9a smaller hydraulic resistance to a gas flow than a
longer form (group 1).
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 Approved For Release 2002/01/11 : CIA-RDP80-00926AO01400040002-2
TABLE 5
D p p MO
Turbulent
0.0005 1 0.005 1 0.05 1 0.0005 I 0,005
Conditions
Streamline
0.05
I`~o, I group . . . . . . 20.65 26.47 23.60 1.57 1.80 1.60
Ko, 11 " . . . . . . . 16.18' 20.98 x.8,77 1.40 10,61 1044
Ko, % . . . . . . . 21.6 20,7 20,4 U.1 10.7 10.6
The formulas of Chilton and Colburn /4/, of Zhavoronkov /:11/ and of the present
author /47/ describe the interdependencies as applied to a uniformly granulated
catalyst, i.e., to a catalyst consisting of granules of uniform dimensions,,
forming a narrow fraction of material by sieve analysis.
Hydraulic Resistance of Hon-
gn-ifprm Granulated I?Saterial
For the sake of completion, the hydraulic resistance of A catalyst column
or layer consisting of non-unifozma granulated material should be discussed,,
For the ca a of the gas flow through a layer of sand? L. S. Le"benson modified
(6) the formula of Slichter (7) for flow of waters and obtained the following
expression:
192Q i. Itm i
a(Irdsd
/48/
Here p1 and 2 are respectively the pressure at the inlet to the layer and
exit from i1 given in kg./sq. m,; p = -RT in absolute atmospheres
(1 kg./sq. cm.) Q .. consumption of gas in cum./sec.; coefficient of
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 Approved For Release 2002/01/11 : CIA-RDP80-00926AO01400040002-2
viscosity in kg. see,/sq. na; a and coefficients, the second of
which depends upon the relative porosity; 11 - thickness of the layer
in meters; # = specific gravity of the gas with respect to air; F = cross-
.sectional area of the layer in sq. Me; def average effective diameter
of a sand particle in m-.
2 - 1
def 100
where di is the diameter of the sand particles and 'f'i weight per cent
of individual fractions.
Using the experimental data of the Institute of !iineral Fuels pertaining to
the hydraulic resistance of a tube packed with sand, as reported by
Lelbenson, and the equations of the present authors, the following results
were obtained: For the average effective diameter of particles of fine
sand, the Letbenson formula gave 0.22 mm.; the Slichter curve, based on
weight units, gave 0.223. A similar value of def (0.225) can be directly
found if the average diameter of particles of the predominating fraction-of
the sand layer (over 50 per cent) is considered. The relative porosity of
the sand determined from specific gravity is 2.5 tines larger than the free
space in the layer calculated from equation /12/, considering that Dg = def.
It should be noted especially that the equation /46/ given by Le .benson was
verified only for streamline flow, Inasmuch as the experiments of the State
Institute of :inoral Fuels were performed at Reynolds number not exceeding
21 and the critical value of the Reynolds number was 50 - 60. Correlatirn
of experimental values of the hydraulic resistance of a sand layer with the
value calculated from equation /47/ gave:
Vo in
m./sec,
p1
P2
1 pexper.,
kg./sq. in.
Lip
according
to /47/
0.279
1.141 22180 1040 2.1 x 10'
940
0.8 x 104
3.3x10''
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 Approved For Release 2002/01/11 : CIA-RDP80-00926AO01400040002-2
These data show that the formula /47/ is applicable also for evaluation of
the hydraulic resistance of a column packed with a non-uniform catalyst.
In conclusion, it should be noted that instead of three experimentally
determined values characterizing the catalyst material (number of granules,
surface of the granules and free volume of the catalyst bed) which are
required for calculations by the Zhavoronkov formula, the formula derived by
the present authors requires only a single determination of the free volume
of the catalyst bed (from the volume of water or fine sand filling that
apace). The factor characterizing the catalyst packing according to this
formula, i.e., the average grain diameter, can be found from equation /12/.
Received at the Editorial Office
July 14, 1945
REFERENCES
1. T.. V. Kirpichev, Ti. A. Mikheev and L. S. Ei:genaon, Teploperedacha
(Heat Transfer), 1940.
2. T. Chilton and A. Colburn, Ind. Eng. Chem.,.Rb 913, 1931.
3. J. Perry, Chemical Engineers$ handbook, Vol. I, 1937 (Russian translation).
4. P'. M. Zhavoronkov Zhurnal khimicheakof promyshlennosti (Journal of the
Chemical Industry) 129, No. 1, 4.
5. N. M. Zhavoronkov, Doctoral Dissertation, Mendeleev Institute of Chemical
Technology, Moscow, 1942.
6. L. S. Leibenson, Neftyanoe khozyadstvo (Petroleum Industry) 181, No. 10,
497, 1929; Neftyanaya promyslovaya mekhanika (Oil Production Mechanics)
Fart 1, 1929.
7. 1. G. Es+man, Ueftyanaya gidravlika (Petroleum Hydraulics), 1932.
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 pp
ov
)r
25X1A
elease 2002/01/11: CIA-RDP80-00926A0d1 00040002 '
FIG. 5. DEP_NDENCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYTIC TOWER A o UPON ITS DIAMETER Dttub The
curves 1 and 3 were calculated according to ~havoronkov
and curves 2 and 4according to Chilton and Colburn.
FIG. 6. EXPERIMENTAL UNIT FOR THE STUDY OF THE
EFFECT OF THE LINEAR VELOCITY OF A STREAI4 OF GAS
UPON THE HYDRAULIC RESISTANCE OF A COLU}41 WITH
SOLID GRANULATED CATALYST
0,, Q2 Q3 4 MF 47
l (I
linear velocity of the air, m,/eeo.
FIG. 7. DEPENDENCE OF THE HYDRAULIC RESISTANCE pp Og"
COLUMN WITH GRANULATED CATALYST UPON THE LINEAR VELOCITT`
OF THE GAS STREAM OBSERVED IN THIS WORK. 1 - d p at the
air inlet to the column; 2 - Ap at the middle of the
column; 3 - average values of Gp; 4 - Ap at the exit
from the column; 5 - A p according to Zhavoronkov; 6 - Ap
according to Chilton and Colburn; 7 - Ap according to
Chilton and Colburn, assuming the average diamete.r:-of,the
particles to be equal to the cubic root of three
dimensions.
7t/l2
s
~e2
os
7
-.
{i ~
I
1 o ,
~
s
I
?
1
m,
6
TABLE 3. EFFECT OF THE AVERAGE GRAIN SIZE OF THE CATALYST (D ) AND THE DIAIUTER OF THE
CONTACT COLUMN (Dtube) ON THE VALUE OF K IN NUUATION P/46/
Interval of
values of
Dtube /D p
Interval of values of
Dp for known Dtube , m.
"in m.)of Dtube fox'
Dp = 0.0073 m,
for Dtube = 0,7 N
turbulent
> 470
< 0,0015 -
> 3,43
a
470-77
0,0015-0,009
3,43-0,662
77-25
0,009-0,0028
M162-0,02
25-12
r
0
0028-0
00583
0
182-0
087
o`r
,
x,
,
,
19,114 M
12
2
3
-
,
0,0033-0, 117
0,087-0,017
< 2,3
> 0,017
< 0,017
>100
-for D. be ? 0,07 M
> 0
73
< 0,0073
,
(0,0005 -0.0073)
Value of K
rom Dp of the
entire Interval
n ecuation /46/
Extreme values Dtub
given for the
interval
0
085
3D
,
p
(7; 4)
0,03
2
11 D
,
p
(3; 0,8)
1
8
,3
DP 0,08
(0,5; 0,2)
I
D p 0,102
(0,15; 0.09)
3,08 D p 0,202
(0.07; 0,018)
6
29
17
62 D
0
.
,
p
.
(0,017; 0,003)
51,33 Dp 012
(3; 0,R)
17
6
,
Dp 0,098
85,6 D p 0.873
Dp 0,830
(0,03; 01008)
numerical valucApproved.E1gr Rekealset200~/O1/'b1 CIA-RDP80-00926AO01400040002-2
>.O ' 0073.
(0,0073-0,03)
for Dtube =0,01 Y
0,005-0,015
Values of K
corresponding to them
(2,64; 2,97) Dtube 0,04
(2,22; 2,12)
D
tube
G X0,04
(1,05; 1,06) D 0.04
tube
(3,2; 3,14)
D tube 0.211
(8,5)* 1
Gubeo.26 "
(51,9; 49)
D tube 0,056
(16,6; 17,67);n tube0,056
(85,89'h tube 01313
(165,2)tube 0,426
 ~b
w
zo
~tA
5voo
-
M
l
i
f v
.
1
v
4
lease 2002/01/11: CIA-RDP80-00926A001400040002
diameter of the tube in in.
FIG. 5. DEP_"DENCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYTIC TOWER On UPON ITS DIAMETER Dtub The
curves 1 and 3 were calculated according to ~havoronkov
and curves 2 and 4 -according to Chilton and Colburn.
> .0. 0073
(0,0073-0,03)
forDtube =0,04 M
0,005-0,015
FIG. 6. EXPERIMENTAL UNIT FOR THE STUDY OF THE
EFFECT OF THE LINEAR VELOCITY OF A STREAM OF GAS
UPON THE HYDRAULIC RESISTANCE OF A COIXJHE WITH
SOLID GRANULATED CATALYST
TABLE 3. EFFECT OF THE AVERAGE GRAIN SIZE OF THE CATALYST (D) AND THE DIANLTTER OF THE
CONTACT COLIJNN (Dtube) ON THE VALUE OF K IN EQUATION P/46/
Interval of
values of
Dtbe/Dp
Interval of values of
DP for known Dtube ? m?
> 470
0,0015
470-77
0,0015-0,009
77-25
0,009-0,0028
25-12
0
0028-0
0583
,
,,0
g
fo
,4?a-~rpT V 0 4 r
12
2
3
-
,
0,0033-0,017
X2,3
> 0,017
? 0,07 Y
-for Dtub
>100
e
< 0,0073
(0, 0005 - 0, 0073)
Interval of values
?Z
~
I
ff
?v
as
I
7
?7
-4
1o
! y
I&
m
i
I
I
linear velocity of the air, m,1550.
FIG. 7. DEPEADEUCE OF THE HYDRAULIC RESISTANCE pp OF;4.
COMM WITH GRANULATED CATALYST UPON THE LINEAR VELOCITY
OF THE GAS STRE.!N OBSERVED IN THIS WORK. 1 - 4 p at the
air inlet to the column; 2 - np at the middle of the
column; 3 - average values of Op; 4 - .4p at the exit
from the column; 5 - op according to Zhavoronkovl 6 - ep
according to Chilton and Colburn; 7 - A p according to
Chilton and Colburn, assuming the average diemeter,:orY.the
particles to be equal to the cubic root of three
dimensions.
Value of x in equation /46/
in m.) of Dtube foxFrom D of the
D? : 0.0073 m, entire interval
> 3,43
3,43-0,562
0, E62-0,182
0,182-0,087
0,087-0,017
< 0,017
> 0,73
3D p 0,085
2,11 D 0,08
1,38
3,08 DP 0,202
17,62 Dp 0.5.'20
51,33 Dp 012
17,6
p.p 0,098
83,6 D p 0.8n
Extreme values Dtu Values of K
given for the corresponding to them
interval
(7; 4)
(3; 0, 8)
(0,5; 0,2)
(0,15; 0.09)
(0,07; 0,018)
(0,017; 0,003)
(3; 0,9)
Dp 0.839 (0,03; 0,008)
numerical va1uA 7pxo edDFq- Releseta0Q??/Q i/1D' CIA-RDP80-00926A001400040002-2
2
64
2
97
,
(
;
,
) D 0,05
tuba
(2
22
2
12
,
;
,
) D 0,04
tube
1
(1,05;
1,06)D 0.04
to
(3-2: R-14) -
cube 20 S
'D tube 01050
(85;89
tube 0,313
(165,2)
Dtube 0,425
 PP
ov
r
.Aw
1
l
diameter of the tube in m.
FIG. 5. DE1E2'DENCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYTIC TOWER A n UPON ITS DIAMETER Dttub . The
curves 1 and 3 were calculated according #o ~havoronkov
and curves 2 and 4 -according to Chilton and Colburn.
FIG. 6. EXPERILO ITAL UNIT FOR THE STUDY OF THE
EFFECT OF THE LINEAR VELOCITY OF A STREAM OF GAS
UPON THE HYDRAULIC RESISTANCE OF A COLUMN WITH
SOLID GRANULATED CATALYST
ev
of
I
e7
1z
1
?
l
l
FIG. 7. DEPEEDHECE OF THE HYDRAULIC RESISTANCE pp Cg;
COLUMN WITH GRANULATED CATALYST UPON THE LINEAR VELOCITT`
OF THE GAS STREAI4 OBSERVED IN THIS WORK. 1 - d p at the
air inlet to the columm; 2 - Ap at the middle of the
column; 3 - average values of Ap; 4 - Ap at the eadt
from the column; 5 - A p according to Zhavoronkovj 6 - sp
according to Chilton and Colburn; 7 - A p according to
Chilton and Colburn, assuming the average diameter,:of,the
particles to be equal to the cubic root of three
dimensions.
TABLE 3. EFFECT OF THE AVERAGE GRAIN SIZE OF THE CATALYST (D ) AND THE DIAI4;TER OF THE
CONTACT COLUMN (Dtube) ON THE VALUE OF K IN EQUATION P/46/
Interval of
values of
Dtube/p
Interval of values of
DP for known Dtube ? m?
for Dtabe = 0,7 M
11-
0711-1-1
r r
Interval of values
(in m.) of Dtube #or - From D of the
Dp - 0,0073 m. lentire nnterval
turbulent
> 470
> 3
43
< 0,0015
,
H
470-77
0,0015-0,009
3,43-0,562
77-25
0,009-0, 0028
0, 562-0,182
25-12
0 028-0,0583
0
182-0
087
fo1, ru604 M
,
,
12
2
3
-
,
0,087-0,017
< 2,3
> 0,017
< 0,017
>100
for Dtube - 0.07 M
> 0
73
< 0,0073
,
(0, 0005 - 0, 0073)
> .0,0073
(0,0073-0,03)
for Dtube = 0,01 M
0,005-0,015
Extreme values Dtub Values of K
given for the
interval corresponding to them
3D
0
085
,
P
(7; 4)
2,11 D p 0,03
(3; 0,8)
I
1,38
D p 0,09
(0,5; 0,2)
1
DP 0,10?
(0,15; 0.09)
3,08 DP 0,202
(0.07; 0,018)
17,62 DP 0,629
(0,017; 0,003)
51,33 DP 0 19
(3; 0,6)
Dp 0,098
85,6 D p 0.893
DP 0,839
(0,03; 0,008)
numerical ValuA9 proeedDjup- Rele,alset20@2 /0.$/1Dj CIA-RDP80-00926AO01400040002-2
elease 2002/01/11 : CIA-RDP80-00926A001400040002- 25X1A
MW
(2,64; 2,97) D 10,04
tube
Dtube0,04
(1,35; 1,33)
L _0 0.04
(1,05; 1,06) D O,o4
tube
(3,2; 3,14) D tube 0,211
(8,5)?
~ube0,20 s
(51,9; 49) D O,o-O
tube
(16,6; 17,67)D 0,050
tube
(85;891 )
tube 0,813
(I65,2)?
Dtube 0,420
 PP
ov
~r
26
Gfi
~A
4
1 a
z
9
i
a 4
4F 4
diameter of the tube in m.
FIG. 5. DEPE.NDLENCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYTIC TONER &p UPON ITS DIAMETER Dttub The
curves 1 and 3 were calculated according to ~havoronkov
and curves 2 and 4'according to Chilton and Colburn,
FIG. 6. EXPERIMENTAL UNIT FOR THE STUDY OF THE
EFFECT OF THE LINEAR VELOCITY OF A STREAI4 OF GAS
UPON THE HYDRAULIC RESISTANCE OF A COLUIhPT WITH
SOLID GRANULATED CATALYST
linear velocity of the air, n./eeo,
FIG. 7. DEPEEDETCE OF THE HYDRAULIC RESISTANCE pp OF. .
COLUMN WITH GRANULATED CATALYST UPON THE LINEAR VELOCITT
OF THE GAS STREAK OBSERVED IN THIS WORK. 1 - 4 p at the
air inlet to the colorm; 2 - pp at the middle of the
column; 3 - average values of Gp; 4 - &p at the exit
from the column; 5 - Ap according to Zhavoronkov) 6 - ep
according to Chilton and Colburn; 7 - A p according to
Chilton and Colburn, assuming the average diameter: of, the
particles to be equal to the cubic root of three
dimensions.
TABLE 3. EFFECT OF THE AVERAGE GRAIN SIZE OF THE CATALYST (D ) AND THE DI/RETER OF THE
CONTACT COLUMN (Dtubs) OPN THE VALUE OF K IN EQUATION P/46/
Interval of
values of
Dtube /Dp
Interval of values of
DP for known Dtube I '-
Interval of values
in m.) of Dtube for.
Dp - 0.0073 M.
for Dtube = 0,7 IY
turbulent
> 470
> 3
43
< 0,0015
,
s
470-77
0,0015-0,009
3,43-0,562
C
77-25
0,009-0,0028
0,01-0,182
25-12
0 0028-0,0583
0,182-0,087
=b0 04 u
12
2
3
-
,
0,087-0,017
< 2;3
> 0,017
< 0,017
>100
for Dtube = 0,07 K
> 0,7.3
< 0,0073
(0,0005 - 0,0073)
> .0,0073.
< 0,73
(0,0073-0,03)
for Dtube = 0,01 Y
0,005-0,015
0,058-0,222
0;'622-0,0087
Value of K in equation /46/
I
(From D of the
(entire Fnterval
I
2
i
I
E
!I
~
-r
-
I
a ~o;
s
m i
6
(
e
I
3D P 0,085
(2,64; 2,97) Dtuba0104
from D
Extreme values Itub Values of K
given for the
interval corresponding to them
(7; 4)
2,11 Dp 0,03
(3; 0,8)
1,38
(0,5; 0
2)
Dp0,06
,
D P 0,IOd
(0,15; 0.09)
3,08 DP 0,202
(0,07; 0,018)
17,62 DP 0.829
(0,017; 0,003)
51,33 DP 012
(3; 0,4)
17,6
7; 0
(0
06)
pp 0,098
,
,
85,6 D P 0.33
(0,05; 0,02)
D P 0,839
(0,03; 01008)
* The numerical valuA provedDF - Redeaset20( /QNlDl CIA-RDP80-00926AO01400040002-2
Dtube0,04
1
(1,35; 1,33)
G J? 0,04
(1,05; 1,06)D 0104
tube
(3,2; 3,14) 1
D a' u
tube
(8 , 5)i
,uUO.26 8
(51,9; 49) 0 056
D tube
(16,6; 17,67), 0,056
tube
(85;891
tube 0,313
(165,2)D* tube
01423
 Appr
ove
)r
u
izi
.
Q
-11
I
diameter of the tube in in,
FIG. 5. DNP SrDDNCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYTIC TO'dER On UPON ITS DIAMETER Dtub2? The
curves 1 and 3 were calculated according to havoronkov
and curves 2 and Q -according to Chilton and Colburn.
FIG. 6. EXPERIMENTAL UNIT FOR THE STUDY OF THE
EFFECT OF THE LINEAR VELOCITY OF A STREAM OF GAS
UPON THE HYDRAULIC RESISTANCE OF A COTIJNI WITH
SOLID GRANULATED CATALYST
O0
I
.2
m3
?V
of
~ j
~
?7
1
/A
linear velocity of the air, m./seo.
FIG. 7. DEPERDE2?CE OF THE HYDRAULIC RESISTANCE Ap OF :, ,
COLUI~IC1 WITH GRANULATED CATALYST UPON THE LINEAR VELOCITY
OF THE GAS STREAM OBSERVED IN THIS WORK. 1 - d p at the
air inlet to the column; 2 - op at the middle of the
column; 3 - average values of Gp; 4 - Op at the exit
from the column; 5 - Ap according to Zhavoronkor; 6 - sp
according to Chilton and Colburn; 7 - .6p according to
Chilton and Colburn, assuming the average diametez::-of,the
particles to be equal to the cubic root of three
dimensions.
TABLE 3. EF?ECT OF THE AVERAGE GRAIN SIZE OF THE CATALYST (D ) AND THE DIAI?TER OF THE
CONTACT COLUMN (Dtube) ON THE VALUE OF K IN EQUATION P/46/
Interval of
values of
Dtube/Dp
Interval of values of
DP for known Dtube , I.
Interval of values f
in m.) of Dtube fol
Dp = 0.0073 m.
b
4
0
tur
ulent
7
>
0,0015
> 3,43
a
470-77
0,0015-0,009
3,43-0.562
A
77-25
0,009-0,0028
0,.'62-0,182
25-12
f 0 0028-0 , 00~583
or ?rv00,04 M
0,182-0,087
12-2,3
0,0033-0,017
0,087-0,017
< 2;3
>0,017
= 0,07 M
for Dt
b
< 0,017
> 100
u
e
-
> 0,73
< 0,0073
(0,0005 -0,0073)
> .0,0073
(0,0073-0,03)
for Dtube =0,04 M
0,005-0,015
From D of the
entire ~nterval
Value of K in ecuation /46/
3D p 0,085
from Dt"be
Extreme values Dtub
given for the
interval
(7; 4)
0,03
2
11 D
p
,
(3; 0,8)
Dp 0,06
(0,5; 0,2)
I
D 0, tOa
(0,15; 0.09)
3,08 DP 0,202
(0.07; 0,018)
17,62 Dp 0.620
(0,017; 0,003)
51,33 DP 0 11
(3; 0,R)
17,6 1
Dp 0,028
85,6 D p 0,673
DP 0,839
(0,03; 0,008)
0 The numerical valuAPplaovedrf, - Fled a t2OQ /O il1D1t CIA-RDP80-00926A001400040002-2
elease 2002/01/11 : CIA-RDP80-00926A001400040002
Values of K
corresponding to them
2
64
1010
2
9
(
,
;
,
7) D
4
tube
2
22
2
12
(
,
;
,
) Dtube0,04
1
35
1
(
,
;
,33) G
0,04
(1
05
1
06
,
;
,
)D tube
0104
3
2
3
(
,
;
,14)
D tube 0,211
(8.5)?
cube? "
-,- 'D tube 0,050
(85;89
tube 0,313
(165,2)D tube 0,425
 25X1A
lease 2002/01/11 : CIA-RDP80-00926AO01400040002-2
B00
ARY
FIG. 5, D-?
PEgDENc OF THE HYDRAULIC RESISTANCE IN THE
TJI~R &,, UPON ITS
ubLh The
curves 1C and 3 were calculated Dac ingDto avOronkov
and ctu`ves 2 and 4 -according to Chilton and Colburn.
FIG. 6. EXPERIMENTAL UNIT FOR THE STUDY OF THE
EFFECT OF THE LINEAR VELOCITY OF A STREAM OF GAS
UPON THE HYDRAULIC RESISTANCE OF A COLUMN WITH
SOLID GRANULATED CATALYST
TABLE 3. EFFECT OF THE AVERAGE GRAIN SIZE OF THE CATALYST (D_) AND THE DIAMETER OF THE
COSITACT CnTrremt r? I ,... -.__ ----
pp
ove
F
or
X
Y
y
i+7
i ~~
~ b al
QJ Q1
1
y
Interval of
Flow values of
Dtuberop
(0,0073-0,05)
for Dtube = 0,04 Y
I
turbulent
> 470
for Dtube = 0.7 H
> 3,43
3D p 0,085
2
470-77 0,0015-0,009 3,43-0,562
03
2,11 D 0
3
,
p
77-25 0,009-0
0028
02
0
1
,
,
-0,182
1.38
D.p 0,00
25-12
0 0028-0
0583
I
,
0,182-0,087
fo
r
1
16
Tvb~
49 Dip=.0,04 K
.
D p 0, t0A
a 12-2
3
,
0, 0033-0, 017 0,087-0,017
3,08 Dp 0,202
0,017 < 0,017
0,6,29
17,62 D
or Dube = 0,07 N
>100
p
< 0,0073 > 0,73
51,33 D
o 13
(0,0003-0,007,3)
p
? .I < 100 I > .0,0073.
Value of K in equation /G6/
in m.) of Dtube for' ram D of the
DP = 0.0073 m, entire interval
1.100 I
~
I 2 y
1200
S
!00
I.2
m3
1000
~ J
?6
e7
I i
~
I I
~
Aff
a ~?, e
m I6
300
LB
?
X00
-
O
kz
aaq
js
FIG. 7. DEPHEDH?CE OF THE HYDRAULIC RESISTANCE pp OF".
COLUMN WITH GRANULATED CATALYST UPON THE LINEAR VELGCIT!
OF THE GAS STRE?a. OBSERVED IN THIS WORK. 1 - d p at the
air inlet to the column; 2 - pp at the middle of the
colwwx; 3 - average values of
from the Gp; 4 - pp at the exit
column. 5 - op according to Zhavoronkovt 6 - ep
according to Chilton and Colburn; 7 - A p according to
Chilton and Colburn , assuming the average diametez;af,the
particles to be equal to the cubic root of three
dimensions.
17,6 1
D 0.088
P
85,6 Dp 0,ats
cube0' 20 8
I 3-1,2 I 0,015-0,034 I 0;922-0,0087 I
600 Dp 0,e39 (0,03; 0,008)
numerical value ?fA 04'bVe6Fbvr? eatse i 0@2/04 1 : CIA-RDP80-00926A0 1400040002-
Extreme values Dtut
given for the
Values of K
interval corresponding to them
(7; 4)
(2,64;
2,97) D 0,04
tube
(3; 0,8)
(2,22;
2,12) a
tube
(0,5;
0
2)
35;
(1
1
33
,
,
,
) G 0,04
(0,15;
0.09)
(1,05;
I,06)10,04
tube
(0,07;
0,018)
(3,2;
3,14)
D tube 0 211
(0,017;
0,003)
(3; 0,4)
(16,6; 17,67),D 0,06,6,
tube
1
($5;891
0,x13
tube
(165,2)+ 1
D tube 0,420
 ppr
ove
d F
r R
h
fl
4.6
-
-
vv
r
--j
r
-~
r-4
r---~ P
25X1A
lease 2002/01/11 : CIA-RDP80-00926A001400040002-
.
D
O
FIG. 5. DEIEEW)ENCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYTIC TOWER An UPON ITS DIAMETER D
curves 1 and 3 ,,sere calculated according d~ub The
and curves 2 and 4'according to Chilton and Colvb ov
urn.
FIG. 6. EXPERIIHITAL UNIT FOR THE STUDY OF THE
EFFECT OF THE LINEAR VELOCITY OF A STREAM OF GAS
UPON THE HYDRAULIC RESISTANCE OF A 0010, DT SOLID GRANULATED CATALYST
TABLE 3. EFFECT OF THE AVERAGE GRAIN
SIZE OF THE CATALYST (D) AND THE DIAMETER OF THE
CONTACT nnrmar it ...,
Interval of
values of Interval of values of
Dtbe/Dp Dp for known Dtube m?
in m.) of Dtube f of
Dp = 0.0073 m.
turbulent
> 470
for Dtube = 0.7 N
3,43
v
470-77 0,0015-0,009 3,43-0,562
77-25 0,009-0,0028 0,562-0,182
25-12 f 0,023-0,0583 0,182-0
087
,
T?r Tube-
-.0,04 w
12-2,3 0,087-0,017
0,0033-0,017
< 2;3 > 0,017 < 0,017
or Dtube - 0,07 Y
>100
< MOM- > 0,73
(0-0005 -0,0073)
> 0,0073
(0,0073-0,03)
For Dtube = 0,04 Y
rom D of the
entire ?nterval
.. I
I 1Y
o!
let
03
i
eY
of
I
'6
e7
_
1
'
I
~~ I
~
a
o, s
o ; I
16
I
FIG. 7. DEPJCEDE'CE OF THE HYDRAULIC RESISTANCE pp Og;
COLTJNN WITH GRANULATED CATALYST UPON THE LINEAR VELOC
OF THE GAS STREAtd OBSERVED IN THIS WORK. 1 - TTY`
air inlet to the column; 2 - d p at the
col eP the middle of the
3 - average values of Ap; 4 - pp at the eo~tt
fromtmin; the column; 5 - Ap according to Zhavoronkov; 6 - ap
according to Chilton and Colburn; 7 - op according to
Chilton and Colburn, assuming the average diameteE-aP.the
particles to be equal to the cubic root of three
dimensions,
3D p 0,065
2,11 Dp 0,03
Dp 0,I01)
3,08 D p 0,202
17,62 Dp 0,e29
51,39 Dp 01I
17,6
p
D 0,039
85, 6 D p 0, 73
of K in equation /46/
ISctreme values D
given for the tub
11 s o f K
7V
-
interval
responding to them
-
-
(7; 4)
(2,64;
2,97) D 0,04
tube
8)
(3; 0
(2
22
2
12
,
,
;
,
) D,04
tube
1
(0,5; 0,2)
(1,35;
1,33)
#OA4
(0,15; 0.09)
(0,07; 0,018)
(3,2;
3,14) I
D tube 0,211
(0,017; 0,003)
(8,5)* 1'
GubeO' n
(3; 0,9)
(51,9; 49)
D tube 11,036
(0,7; 0,06)
(16,6; 17,67);D o,oso
tube
(0,05; 0,02)
(85;89 0
tube 1 ,31;
(0,03; 0,008)
(165,2)* 1
1400040002-2
Dtube 0,42b
0,015-0,034 I 0;'922-0,0087 I 600 Dp 0,939
numerical value qiA pfP6\PedeF6r edease 2 X 2i0Q 1 : CIA-RDP80-00926A0
 1
I
I
!
ove
d
r
u
ZA
ci
W
a
a
~ a
s
a ,
v -a
R
f 4
7
lease 2002/01/11: CIA-RDP80-00926A00140004000 25X1A M
diameter of the tube in m.
FIG. 5. DEPiG7JN ?CE OF THE HYDRAULIC RESISTANCE IN THE
CATALYTIC TO'P R n UPON ITS DIAMETER Dtub~, The
curves 1 and 3 were calculated according to havoronkov
and curves 2 and 4-according to Chilton and Colb 'n.
FIG. 6. EXPERIIFITAL UNIT FOR THE STUDY OF THE
EFFECT OF THE LINEAR VELOCITY OF A STREAM OF GAS
UPON TIP HYDRAULIC RESISTANCE OF A COLUMN WITH
SOLID GRANULATED CATALYST
f
z
I
e2
m3
i .
4
e 7
~
_
o
j
e
a
f
e
?
linear velocity of the air, m./seo.
FIG. 7. DEPEFDINCE OF THE HYDRAULIC RESISTANCE a p COLUHE WITH GRANULATED CATALYST UPON THE LINEAR VELOCITY!`
OF THE GAS STREAK OBSERVED IN THIS WORK. 1 - d pat the
air inlet to the column; 2 - pp at the middle of the
column; 3 - average values of Op; 4 - Ap at the exit
from the column; 5 - np according to Zhavoronkovl 6 - sp
according to Chilton and Colburn; 7 - A p according to
Chilton and Colburn , assuming the average diameter,: of, the
particles to be equal to the cubic root of three
dimensions.
TABL
E 3. EFFECT OF THE AVERAGE
CONTACT COLUMN (Dtube) ON
GRAIN SIZE OF THE C
TIE VALUE OF K IN
ATALYST (D ) AND THE DIAMNTER OF THE
3EUATION p/46/
Value of K in equation /46/
Interval of
...__
~ .._. f
_...,.,._...,~,
values of
D
/D
Interval of values of
D
for known D
Interval of values
in m.) of Dtube foi
frrom D of the
rom D
ISrtreme values Dtub
tube
p
P
tube m?
DP = 0,0073 m,
entire ~nterval
iv for terv
l the
Igin
Values of R
corresponding to them
a
turbulent > 470
for Dtube - 0,7 24
> 3
43
0
085
3D
< 0,0015
,
,
p
(7; 4)
(2,64; 2,97) D 0
04
N 470-77
0,0015-0, 009
3,43-0,562
0,09
2
11 D
,
tube
,
P
(3; 0,8)
(2,22; 2,12) D 0
0
77-25
0
009-0
0028
6
1
,
tube
,
,
0, X
2-0,182
1,38
p
0
08
(0,5; 0,2)
-'
25-12
0,028-0, 0583
0,182-0
087
P
,
I
G 0,04
Grp .0,04 'I
,
DP 0,108
(0,15; 0.09)
(1,05; 1,06)D 0,04
tube
12-2,3
0,087-0,017
0,202
08 D
3
P
,
(0.07; 0,018)
(3,2; 3,14) D 0
211
< 2,3
> 0,017
< 0,017
0
6
29
17
62 D
,
tube
,
.
,
P
(0,017; 0,003)
(8,5)*
= 0,07 14
-for D
b
cube0' 208
>100
l
,
>0,73
012
51,33 D
< 0,0073
P
(3; 0,R)
(51,9; 49)
(0,0005 - 0,0073)
D tube 0,036
>.0,0073
.
0
- ' -
(16
6
I7
67
(
,0073-0,63)
0,098
D
,
;
,
);D 0
0
8
for D tube = 0,01
P
,
5
tube
6 D 0.8'13
85
1
,
(85;89b
tube 0.911
0,839
600 D
(0
03; 0
008)
2
P
,
,
)
(165,
0
8
value ,gpproare jEpriRe sea209
2Lk1/Islj CIA-
RDP80-00926A0014
,42
tube
00040002-2
 V
rul
Zr
a
aw-
1
B
Ql
QZ
.1
y
diameter of the tube in m.
FIG. 5. DEP u.'DINCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYTIC TOWER On UPUN ITS DIAMETER Dt~tub The
curves 1 and 3 were calculated according to 2havoronkov
and curves 2 and. 4 -according to Chilton and Colburn.
FIG. 6. EKPERIHY3TAL UNIT FOR THE STUDY OF THE
EFFECT OF THE LINEAR VELOCITY OF A STREAM OF GAS
UPON THE HYDRAULIC RESISTANCE OF A COLULIPI WITH
SOLID GRANULATED CATALYST
Interval of
values of
Dtube /Dp
TABLE 3. EFFECT OF THY AV!-:RAGE GRAIN SIZE OF THE CATALYST (D) AND THE DIAWTER OF THE
CONTACT COLUMN (Dtube) OH THE VALUE OF K IN EQUATION P/46/
> 470
470-77
77-25
25-12
12-2,3
< 2;3
>100
Interval of values of
DP for known Dtube m?
0,0015
0,0015-0,009
0,009-0,0028
0 0028-0,0583
f ov b -r ube- r
n n- V
~?vP -- ,
0,0033-0,017
> 0,017
for Dtube - 0,07 N
< 0,0073
(0,01005-0,0073)
.0,0073
(0,0073-0,05)
for Dtube - 0,04
0,005-0,015
Interval of values !
in m.)of Dtu;e fog. frrom D of the
DP . 0.0073 M. entire ~nterval
> 3,43
3,43-0,562
0,E62-0,182
0,182-0,087
0,087-0,017
< 0,017
> 0,7.3
8
p 0 . 1 0 . 2 Q3 QV 0,5 6 0.7 t u
linear velocity of the air, m./eeo
FIG. 7. DEPEEDNUCE OF THE HYDRAULIC RESISTANCE pp OF..,
COLURE WITH GRANULATED CATALYST UPON THE LINEAR VELOCITY`
OF THE GAS STREA1-! OBSERVED IN THIS WORK. 1 - A p at the
air inlet to the column; 2 - ap at the middle of the
column; 3 - average values of Op; 1 - Ap at the exit
from the column; 5 - ap according to Zhavoronkov; 6 - ep
according to Chilton and Colburn; 7 - Ap according to
Chilton and Colburn, assuming the average diametar.:of.the
particles to be equal to the cubic root of three
dimensions.
3D P 0,085
from Dtube
D p 0,104
3,08 DP 0,202
17,62 DP 0,629
51,33 DP o fl
p 0,098
P
Extreme values Dtub
given for the
interval
(7; 4)
(3; 0,8)
(0,5; 0,2)
(0,15; 0.09)
(0.07; 0,018)
(0,017; 0,003)
(3; 0,R)
0,058-0,222 85,6 DP 0,373 (0,05; 0,02)
I 3-1,2 I 0,015-0,034 I 0; 22-0,0087 I 600 DP 0,939 I (0,03; 0,008)
valyd4 pfo gdD gr R e et2002/Qx1/b CIA-RDP80-00926A001400040002-2
P Ube
25X1A
Release 2002/01/11 : CIA-RDP80-00926A0014000400
~ I
I
2
I
.2
I
m3
.a
of
?6
~
i
I
_ r
?
1
~o; e
I
r
~
Q
1:
t
6
-
I
Values of K
corresponding to them
(2,64; 2,97) Dtube 1 0,04
DtubeO,o4
(1,35;
1,33)
_,
0 ,04
05
1
0
(
,
;
1,
6) D
tube
o,cw
(3,2;
3,14) D tube o,111
(8,5)? yllbeo,28 n
(51,9; 49) ,~ 058
D tube
(16,6; 17'67),Dtube0,058
1
(85;891
tube 0,913
(165,2)D 0,420
tube
 ICU rUF
7,f
Y
r
4
q
L
(
1J
42
.1
q
4
diameter of the tube in m.
FIG, 5, DEPEEDENCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYTIC TOWER Gu ONCE ITS DIAMETER Dub The
curves 1 and 3 were calculated according o &avoronkov
and curves 2 and 4-according to Chilton and Colburn,
Interval of
values of
Dtube/D
linear velocity of the air, m./seo~
FIG. 6. EXPERD4ENTAL UNIT FOR THE STUDY OF THE
EFFECT OF THE LINEAR VELOCITY OF A STREAM OF GAS
UPON THE HYDRAULIC RESISTANCE OF A COLUMN WITH
SOLID GRANULATED CATALYST
TABLE 3. EFFECT OF THE AVERAGE GRAIN SIZE OF THE CATALYST (D) AND THE DIAMETER OF THE
CONTACT COLUMN (Dtube) ON TIES VALUE OF K IN EQUATION '/46/
Interval of values of
D P for known Dtube ? m,
for Dtube = 0,7 M
turbulent
> 470
> 3,43
< 0,0015
470-77
0,0015-0,009
3,43-0,562
77-25
0,009-0,0028
0,562-0,182
25-12
0 0028-0
0583
182-0
087
0
,
for
,
,
=.0,04 M
01
087
0
0
12-2,3
7
-
,
,
< 2;3
>0,017
= 0,07 1[
for Dt
b
< 0,017
>100
u
e
> 0,73
0,0073
(0,0005 -0,0073)
>, 0. 0073
< 0,73
(0,0073-0,05)
for Dtube - 0,01 1l
0,005-0, 015
Interval of values 1
in m.) of Dtube fox frrom D of the
Dp . 0.0073 m, entire lpnterval
0,058-0,222
0,-022-0.0087
/ I
7 Y
e2
03
eq
_
I
aS
e7
7
s
~s
0
t
?
3
fi
0
FIG. 7. DEPENDENCE OF THE HYDRAULIC RESISTANCE 46p O.
F
COLUMN WITH GRANULATED CATALYST UPON THE LINEAR VELOCITY`
OF THE GAS STREAM OBSERVED IN THIS WORK. 1 - d p at the
air inlet to the column; 2 - Gp at the middle of the
column; 3 - average values of gyp; 4 - Ap at the exit
from the column; 5 - Ap according to Zhavoronkov; 6 ?- dp
according to Chilton and Colburn; 7 - A p according to
Chilton and Colburn, assuming the average diameter:of,the
particles to be equal to the cubic root of three
dimensions.
Lies Dtub
from D
j
3D p 0,085
(7; 4)
2,11 D P 0,03
(3; 0,8)
1,38
(0,5; 0,2)
D.p 0,00
pp 0,rok
(0,15; 0.09)
3,08 D p 0,202
(0,07; 0,018)
17,62 Dp 0.829
(0,017; 0,003)
51,33 Dp 012
(3; 0,8)
1
6
7,
D 0,098
(0,7; 0,06)
p
83,6 D p 0?
(0,05; 0,02)
600 DP 0,330
(0,03; 0,008)
numerical vauAppr;to ,d 1J Q0 F &e OOD2/(Ud1 fi CIA-RDP80-00926A001400040002-2
Values of K
corresponding to them
(2,64; 2,97) Dtube 0,04
(2,22; 2'12) D 0,04
tube
(1,35; 1,33)
L e 0,04
(1,05; 1,06) D tube 0104
D tube 011-111
(8, 5)' cube0.2(t e
(51,9; 49)D 0,050
tube
(16,6; 17,67),Dtube0,058
1
(85;89 0,913
tube
 R
LW
B
R!
QZ
d
,q
Q
1.
diameter of the tube in in.
FIG, 5. DEl'COJO,NCE THE HYDRAULIC RESISTANCE IN THE
CATALYTIC TOWER On UPON ITS DIAMETER Dtub . The `.'
curve" 1 and 3 were calculated according to ~havoronkov
end curves 2 and 4according to Chilton and Colburn.
FIG. 6. EXPERIMENTAL UNIT FOR THE STUDY OF THE
EFFECT OF THE LINEAR VELOCITY OF A STREAM OF GAS
UPON THE HYDRAULIC RESISTANCE OF A CODJIIN WITH
SOLID GRANULATED CATALYST
TABLE 3. EFFECT OF THE AVERAGE GRAIN SIZE OF THE CATALYST (D ) AND THE DIAFFTER OF THE
CONTACT COLUMN (Dtube) ON THE VALUE OF K IN E7UATION P/46/
Value of K in equation /46/
Interval of
values of
Dtube/Dp
> 470
470-77
77-25
25-12
12-2,3
< 2;3
>100
Interval of values of
DP for known Dtube a m.
for Dtube = 0,7 i1
0,0015
0,0015-0,009
0,009-0,0028
elease 2002/01/11 : CIA-RDP80-00926A001400040 M
>0,017
for Dtube 0,01 M
< 0,0073
(0,0005 -0,0073)
>0,0073,
(0,0073-0,03)
for Dtnbe = 0,01: Y
Interval of values 1
in rn.) of Dtube for jFrom D of the
DP . 0.0073 in. (entire interval
> 3,43
3,43-0,562
0, 562-0,182
0,182-0,087
0,087-0,017
< 0,017
> 0,73
3D P 0,085
2,11 D p 0,03
1,38
1
D .p 0,06
1
DP 0,108
3,08 D P 0,202
17,62 Dp 0,629
51,33 DP o 17
< 0,73
~ I
I
Z
I
?Z
m3
os
_
!
I
I
_ r
r
I ~' ?
I
?
?
0
6
FIG. 7. DEPENDENCE OF THE HYDRAULIC RESISTANCE &p o?.;.
COLUMN WITH GRANULATED CATALYST UPON THE LINEAR VELOCITY -
OF THE GAS STREAM OBSERVED IN THIS WORK. 1 - d p at the
air inlet to the column; 2 - Ap at the middle of the
column; 3 - average values of Ap; 4 - Qp at the exit
from the column; 5 - Ap according to Zhavoronkov; 6 ep
according to Chilton and Colburn; 7 - A p according to
Chilton and Colburn, assuming the average dismeter:of,the
particles to be equal to the cubic root of three
dimensions.
17,6 1
D o,o?e
P
85,6 D 0,573
he
(7; 4)
(3; 0,8)
(0,5; 0,2)
(0,15; 0.09)
(0,07; 0,018)
(0,017; 0,003)
(3; 0.)
3-1,2 I' 0,015-0,034 1 0;'022-0,0087 I 600 Dp 0,939 I (0,03; 0,008)
numerical valu4 RP 0Yd5 r For ,el a ~0Q2/Q4/1D' CIA-RDP80-00926A001400040002-2
Values of K
corresponding to them
(2,64; 2,97) 5 tube 10,08
(2,22; 2,12)5tube0,04 1
(1,35; 1,33) G 0,09
(1,05; 1,06)
0.04
5 tube
(3,2; 3,14)
D tube o.z;;
(8,5)*
cube0.'l9 ti
(16,6; 17,67);5tube 0,056
(85;89 tube 0,31;
(165,2)'
Dtube 0,921
g
g
~
 ep
,-~
lease 2002/01/11 : CIA-RDP80-00926A001400040002-
q 900
U
700
607
P,
diameter of the tube in is.
FIG. 5. DEP NDENUD OF THE HYDRAULIC RESISTANCE IN THE
CATALYTIC TOHER a n UPON ITS DIAIlETER Dtub The
curves 1 and 3 were calculated according to 2havoronkov
and curves 2 and 4'according to Chilton and Colburn,
FIG. 6. EXPERIMENTAL UNIT FOR THE STUDY OF THE
EFFECT OF THE LINEAR VELOCITY OF A STREAM OF GAS
UPON THE HYDRAULIC RESI3TANCE OF A COLUPIIN WITH
SOLID GRANULATED CATALYST
4500
_I_I _ i ? e
?
o ?
1
-.
m. s
?
0 0.1 0.2 0,3 4y S
linear velocity of the air, m./Sea.
FIG. 7. DEPE?DI27CE OF THE HYDRAULIC RESISTANCE Qp (Qr'4,
COLUMN WITH GRANULATED CATALYST UPON THE LINEAR VE,oCITr`
OF THE GAS STRELtl-I OBSERVES IN THIS WORK, 1 - AP at the
air inlet to the column; 2 - pp at the middle of the
column; 3 - average values of Gp; 4 - Ap at the exit
from the column; 5 - AP according to Zhavoronkov; 6 - ep
according to Chilton and Colburn; 7 - &p according to
Chilton and Colburn, assuming the average diameter;of',the
particles to be equal to the cubic root of three
dimensions.
TABLE 3. EFFECT OF THE AVERAGE GRAIN SIZE OF THE CATALYST (D ) AND THE DIAMETER OF THE
CONTACT COMM (Dtube) ON THE VALUE OF K IN EQUATION P/46/
turbulent
Interval of
values of
Dtube /Dp
470
Interval of values of
DP for known Dtube ? m?
for Dtube = 0.7 U
< 0,0015
Interval of values
in m.) of Dtube for rom D of the
DP = 0.0073 M. entire ~nterval
> 3,43
470-77
0,0015-0,009
3,43-0,562
77-25
0,009-0,0028
0,662-0,182
25-12
0.182-0,087
1
or 'T~$,04 x
2-2,3
0,087-0,017
< 2,3
> 0,017
< 0,017
>100
- for Dtube - 0,07 M
-
> 0
7
3
< 0,0073
,
.
(0,0005 -0,0073)
> .0,0073
(0,0073-0,03)
for Dtube =0,0I Y
0,005-0,015
Values of K
corresponding to them
(2,64; 2,97) D 1 0.04
tube
(2,22; 2,12) D,04
tube
(1,35; 1,33) -
L 0,04
(1,05; 1,06)D o,oa
tube
(3,2; 3,14) D 0,211
tube
(8,5)?
cube0.28 b
(51,9; 49)
s
D tubeo,o5
(16,6; 17,67)Dtube?'0
(85;89) 1
tube ?'91;
I
, . , I 1 - p I v,vvv"
The numerical value, pr y edt, griRe easee2092/ i1/i CIA-RDP80-00926A001400040002-2
3Dp0,065
2,11 Dp 0,03
3,08 DP 0,202
17,62 Dp 0,029
51,33 DP 0 17
17,6
Dp0.098
85,6 D p 0.8?3
i
I
2y
I
m3
,f
?6
7
K in equation /46/
from D~
Ebctreme values Dtub
given for the
interval
(7; 4)
(3; 0,8)
(0,5; 0,2)
(0,15; 0.09)
(0,07; 0.018)
(0,017; 0,003)
(3; 0,4)
 Q
I Q
2 ,
1 .
4
lease 2002/01/11 : CIA-RDP80-00926A001400040002
diameter of the tube in m.
FIG, 5, DE1E3m PILE OF THE HYDRAULIC RESISTANCE IN THE
CATALYTIC TOWER 41) UPON ITS DIAI9ETER Dub The
curves 1 and 3 were calculated according o 2havoronkov
and curves 2 and 4-according to Chilton and Colbarn.
FIG. 6. EXPERIMENTAL UNIT FOR THE STUDY OF THE
EFFECT OF THE LINEAR VELOCITY OF A STREAM OF GAS
UPON TILE HYDRAULIC RESISTANCE OF A COLU?fiI WITH
SOLID GRANULATED CATALYST
I
I
2 4
/300
J200
S
100
OJ
e2
J000
I
m3
?4
? J
--,
'
900
?7
0
1
60,7
1
~ o
s
S00
m
~
s
raa
300
200
100
A
ll O.J 0.
2 0
3
4 S
J
0
linear velocity of the air, m,/aeo;
FIG. 7. DEPENDO'CE OF THE HYDRAULIC RESISTANCE pp OF;; ,
COLUMN WITH GRANULATED CATALYST UPON THE LINEAR VELOCITY
OF THE GAS STREAM OBSERVED ON THIS WORK. 1 - d p at the
air inlet to the column; 2 - pp at the middle of the
column; 3 - average values of Gp; 4 - pp at the exit
from the column; 5 - op according to Zhavoronkovj 6 - ep
according to Chilton and Colburn; 7 - op according to
Chilton and Colburn, assuming the average diameter:ef.the
particles to be equal to the cubic root of three
dimensions.
TABLE
3. EFFECT OF THE AVERAGE
CONTACT COLDER (Dtube) ON
GRAIN SIZE OF SHE CA
THE VALUE OF K IN
TALYST (D ) AND THE DIAMETER OF THE
EQUATION P/46/
Value of x in equation /46/
Interval of
values of
I
Interval of values
from D
Dtbe/Dp
nterval of values of
DP for known Dtube m?
in m.) of Dtube fox
Dp . 0.0073 m,
From D of the
entire nterval
Extreme values Dtub
given for the
interval
Values of K
corresponding to them
for Dtube = 0,7 M
> 470
> 3
43
0
085
3D
< 0,0015
,
,
p
(7; 4)
(2,64; 2,97) D 10104
tube
470-77
0,0015-0,009
3,43-0.562
0,03
2
11 D
,
p
(3; 0,8)
77-25
0
009-0
0028
0
162-0
182
1
,
,
,
,
(0,5; 0
2)
D .P 0,08
,
G e 0,04
25-12
0028
00
0
1
Q .
c
-
,
583
0,182-0,087
1
16
(0
15
0
09
(1
05
1
06
,
, r
UU 0,04 U
,
DP 0,10a
,
;
.
)
,
;
,
) D o,cw
tube
12
2
3
-
,
0
0033-0
017
0,087-0,017
0,202
08 D
3
0
018
(0
07
(3
2
3
1
,
,
p
,
,
.
;
)
,
;
,
4)
D tube 0,211
0,017
< 0,017
17
62 D
0.820
017
0
003
0
8
*
- 0,07 K
for Dt
b
,
p
(
,
;
,
)
(
,5)
cube0, 28 a
>100
u
e
> 0
73
0
< 0,0073
,
11
51,33 DP
(3; 0,R)
(0,0005-0,0073)
> .0,0073
(0,0073-0,03)
for Dtube = 0,01 N
D p 0,098
(16.6; 17'67);D tube 0,050
1
0
005-0
015
0.579
85,6 D
(85
89
,
,
p
;
1 0,811
tub
e
p
0,530
(0
03
008
0
p
,
.
)
;
(165,2)
0
926
D
The numerical valu pw oved1E r aele"et20e
/ M/14 CIA-R
DP80-00926A0014
.
tube
00040002-2
 pp
ov
r
M B
I
1
(
U Q
Z
J
4
lease 2002/01/11 : CIA-RDP80-00926A001400040002-
diameter of the tube in in.
FIG. 5. DEP11'DENCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYTIC TOWER 6 n UPON ITS DIAMETER Dttub The
curves 1 and 3 were calculated according to ~havoronkov
and curves 2 and 4'aceording to Chilton and Colburn.
z~
s
ez
(D 3
0s
6
1
7
1
~o
s
.
~
s
~
?
I
rt
FIG. 6. EXPERIMENTAL UNIT FOR THE STUDY OF THE
EFFECT OF THE LINEAR VELOCITY OF A STREAM OF GAS
UPON THE HYDRAULIC RESISTANCE OF A COMM WITH
SOLID GRANULATED CATALYST
FIG. 7. DEPENDENCE OF THE HYDRAULIC RESISTANCE Ap MA
COLUMN WITH GRANULATED CATALYST UPON THE LINEAR VELOCITY
OF THE GAS STREAM? ODSERVED IU THIS WORK. 1 - d p at the
air inlet to the column; 2 - Ap at the middle of the
column; 3 - average values of Ap; 4 - Ap at the exit
from the column; 5 - 4p according to Zhavoronkov; 6 - Ap
according to Chilton and Colburn; 7 - Ap according to
Chilton and Colburn, assuming the average diameter::of.the
particles to be equal to the cubic root of three
dimensions.
TABLE 3. EFFECT OF THE AVERAGE GRAIN SIZE OF THE CATALYST (D ) AND THE DIAMETER OF THE
CONTACT COLUN (Dtbe) ON THE VALUE OF K IN EQUATION p/46/
Interval of
values of
Dtube/Dp
Interval of values of
Dp for known Dtube , m.
Interval of values I
In m.) of Dtube fox ' From D of the
Dp c 0.0073 m. entire interval
for Dtube = 0,7 N
> 470
< 0,0015
> 3,43
470-77
0,0015-0,009
3,43-0,562
77-25
0,009-0,0028
0,.162-0,182
25-12
0,182-0.087
12-2,3
0,087-0,017
< 2,3
> 0,017
< 0,017
>100
for Dtube = 0,01 x
> 0
73
< 0,0073
,
(0,0005 -0,0073)
> 0,0073
(0,0073-0,05)
for Dtube =0,01 14
0,005-0,015
Value of K in equation /46/
ISctreme values Dtub
given for the
interval
Values of K
corresponding to them
0
085
3D
,
p
(7; 4)
0,03
2
11 D
,
p
(3; 0,8)
1
D p 0,0?
(0,5; 0,2)
1
DP 0,104
(0,15; 0.09)
3,08 D p 0,202
(0.07; 0,018)
17,62 Dp 0.629
(0,017; 0,003)
51,38 Dp 012
(3; 0,R)
D p 0,098
85,6 D p 0,573
DP 0,639
(0,03; 0,008)
valugpcpplrovecbf{gr Releaset206~/Q, /b1 CIA-RDP80-00926A001400040002-2
64
2
2
9
1
;
,
(
,
0,04
7) D tube
(2
22
1
2
12
,
;
,
)D 0
,04
tube
(1
35
1
33
,
;
,
) G e o,04
(1
05
1
06
,
;
,
) D 0,04
tube
3
2
3
1
(
,
;
,14)
D o,zu
tube
(8,5)e ,ube0,26 8
(51,9; 49)
D tube 0'030
(16,6; I7,67),D 0,054
tube
(85;89
tube 0,313
(165,2)
Dtube_0,420
 App
rov
ea
or
AF
{
{
B !
U Q
Z .
1 .
w
diameter of the tube in in.
FIG. 5. DEPFDENCE OF THE HYDRAULIC RESISTANCE IN THE
1'~9
CATALYTIC TOifL'R Ap UPON ITS DIAMETER D
The
ub ,
curves 1 and 3 were calculated according Eo ~havoronkov
and curves 2 and 4'according to Chilton and Colburn,
f~l
FIG. 6. EXPERIMENTAL UNIT FOR THE STUDY OF THE
EFFECT OF THE LINEAR VELOCITY OF A STREAI4 OF GAS
UPON THE HYDRAULIC RESISTANCE OF A COLUMN WITH
SOLID GRANULATED CATALYST
Zr
L
1
e1
eZ
~
e4
of
_
~ j
e7
m
(
6
611
FIG. 7. DEPENDEECE OF THE HYDRAULIC RESISTANCE pp OF;~
COLUMN WITH GRANULATED CATALYST UPON THE LINEAR VELOCITY
OF THE GAS STREit4 OBSERVED IN THIS WORK. 1 - A p at the
air inlet to the column; 2 - Ap at the middle of the
column; 3 - average values of Ap; 4 - Ap at the exit
from the column; 5 - Ap according to Zhavoronkov; 6 - Ap
according to Chilton and Colburn; 7 - A p according to
Chilton and Colburn, assuming the average diametex.or,the
particles to be equal to the cubic root of three
dimensions.
TABLE 3. EFFECT OF THE AVERAGE GRAIN SIZE OF THE CATALYST (D ) AND THE DIAMETER OF THE
CONTACT COLUMN (Dtube) ON THE VALUE OF K IN DEUAT.ICN P/46/
Interval of
Interval of values I
from Dt
values of
Dtubs/Dp
Interval of values of
Dp for known Dtube , m,
in m.) of Dtube fat '
Dp = 0,0073 m.
'rom D of the
entire ~nterval
Extreme values Dtub
given for the
interval
Values of K
corresponding to them
for Dtube = 0,7 u
> 470
> 3
43
0
085
3D
2
2
9
64
< 0,0015
,
,
p
(7; 4)
(
,
,
7)
;
D 0,04
tube
470-77
0
0015-0
009
43-0
3
562
0
03
2
11 D
,
,
,
,
,
,
p
I
(3; 0,8)
Dtube0,04
77-25
0,009-0,0028
0,162-0,182
D p 0,09
(0,5; 0,2)
(1,35; 1,33) G ~e 0,04
1
25-12
0,Q023-0,0583
or T vbG
0,182-0,087
D0,t0?
(0,15; 0.09)
(1,05; 1,06) D t
be 01c4
-0,04 M
u
1
2
3
2-
,
0,087-0,017
3,08 Dp 0,202
(0,07; 0,018)
? ' D tube 0.211
3
0
017
< 0
017
17
62 D
0
620
17
00
#
8 5
P
,
= 0,07 M
for Dtub
,
,
p
.
; 0,
(0,0
3)
)
(
sube0 28 8
>100
e
7
> 0
3
0 19
51,33 D
< 0,0073
.
,
p
(3; 0,R)
0,058
? ? -'D
(0,C005-0,0073)
tube
> 0
0073
1
6 1
,
.
(0,0073-0,03)
for Dtube = 0,01 M
7,
Dp 0,098
(16,6; 17,67), tubeo.0so
373
6 D 0
85
0,005-0,015
.
,
(85;89 tube 0,311
0;,022-0
0087
600 D
0
939
?
,
I
p
,
I
(0,03; 0,008)
(165,2)
0,425
Bt
numerical va
luA1prOVe
dDFuOJ BeI etaOG
2/Qilif14,CIA-R
DP80-00926A0014
00040002-2
ube
 APP
ov
or
u
g Or
-2
a
~ a
z
a
y
a
FIG. 5. DEPi'lPUDNCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYTIC TONER On UPON ITS DIAIRETER Dttub The
curves 1 and 3 were calculated according to ~havoronkov
and curves 2 and 4'according to Chilton and Colburn.
FIG. 6. EXPERIRENTAL UNIT FOR THE STUDY OF THE
EFFECT OF THE LINEAR VELOCITY OF A STREAM OF GAS
UPON TILE HYDRAULIC RESISTANCE OF A COLUU WITH
SOLID GRANULATED CATALYST
V
of
e7
_ _
I
,
im,
l
linear velocity of the air, m./seo.
FIG. 7. DEPENDENCE OF THE HYDRAULIC RESISTANCE pp O? 4
COLUMN WITH GRANULATED CATALYST UPON THE LINEAR VIIOCIT!`
OF THE GAS STREAM OBSERVED IN THIS WORK. 1 - d p_at the
air inlet to the columm; 2 - pp at the middle of the
column; 3 - average values of Gp; 4 - .gyp at the exit
from the column; 5 - d p according to Zhavoronkov; 6 -,&p
according to Chilton and Colburn; 7 - &p according to
Chilton and Colburn, assuming the average diameteaN of. the
particles to be equal to the cubic root of three
dimensions.
TABLE 3. EFFECT OF THE AVERAGE GRAIN SIZE OF THE CATALYST (D) AND THE DIAN,ETER OF THE
CONTACT COLUMN (Dtbe) ON THE VALUE OF K IN EQUATION P/46/
Interval of
values of
Dtube/D
Interval of values of
Dp for known Dtube , '-
Interval of values
In m) of Dtube for
DP . 0.0073 m,
for Dtube = 0.7 M
turbulent
> 470
> 3
43
< 0,0015
,
u
470-77
0,0015-0,609
3, 43-0,562
S
77-25
0,009-0,0028
0,562-0,182
25-12
0,0028-0583
0,182-0,087
T
T =.0,04 K
12-2,3
0,087-0,017
< 2;3
> 0,017
- 0,07 M
for D t
b
-
< 0,017
>100
u
.
e
> 0,73
< 0,0073
(0.0005-0,0073)
> -0,0013
< 0,73
(0,0073-0,03)
for Dtube =0,04 Y
0
058
0,005-0,015
,
-0,222
0;022-0,0087
Value of K in equation /46/
_-
from D
rom D of the I
entire Lnterval
Fxtreme values Dtub
given for the
interval
Values of K
corresponding to them
0
065
3D
2
2
64
9
,
P
(7; 4)
,
(
,
;
7)
D o,oa
tube
03
11 D 0
2
2
1
,
,
(3; 0,8)
(
,22; 2,
2)D 0,04
tube
1,38
D .p 0.00
(0,5; 0,2)
(1,35; 1,33) G e0 04
1
1,
6
DP 0- 10A
(0,15; 0.09)
(1,05; 1,06) D tube 01o4
0
202
3
08 D
3
3
2
,
,
P
(0.07; 0.018)
,14)
(
,
;
D tube 0,211
629
0
17
62 D
1
?
,
,
P
7; 0,003)
(0,0
(8 , 5)
cubeo, 23 n
0 a
51,33 D
5
P
(3; 0,S)
(
1,9; 49)
D tube0,050
17,6
(0,7; 0,06)
P
D 0,099
tube 01050
873
6 D 0
85
1
8
.
,
(0,05; 0,02)
(85;
9) tube o,s-;
939
D 0
,
(0,03; 01008)
The numerical valuApplROVaddj Fil 0,20 2/Q1114CIA-RDP80-00926A001400040002-2
 As
pp
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o
1
of i
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?Z
o3
?f/
oS
?7
1
I
I
_
r
elease 2002/01/11 : CIA-RDP80-00926A00140004000
diameter of the tube in m.
FIG. 5, DEPIUI.'JINCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYTIC TOW R ap UPON ITS DIANETER Dub The
curves 1 and 3 were calculated according o g avoronkov
and curves 2 and 4-according to Chilton and Colburn.
FIG, 6. EXPEIIIHYSITAL UNIT FOR THE STUDY OF THE
EFFECT OF THE LINEAR VELOCITY OF A STREAM OF GAS
UPON TIIE HYDRAULIC RESISTANCE OF A COMIN WITH
SOLID GRANULATED CATALYST
FIG, 7. DEPENDEIICE OF THE HYDRAULIC RESISTANCE pp OF .' .
COLUMN WITH GRMrULATED CATALYST UPON THE LINEAR VELOOIT!`
OF THE GAS STREAM OBSERVED IN THIS WORK. 1 - d p at the
air inlet to the column; 2 - pp at the middle of the
column; 3 - average values of Gp; 4 - Ap at the exit
from the column; 5 - 41) according to Zhavoronkov; 6 - sp
according to Chilton and Colburn; 7 - p according to
Chilton and Colburn, assuming the average diametelE of, the
particles to be equal to the cubic root of three
dimensions.
TABLE 3. EFFECT OF THE AVERAGE GRAIN SIZE OF THE CATALYST (D ) AND THE DI4 ETER OF THE
CONTACT COLUI?IN (Dtube) ON TEE VALUE OF K IN EQUATION P/46/
Interval of
values of
Dtube/Dp
Interval of values of
Dp for known Dtube , a.
in rn,) of Dtube for
Dp .0,0073 m,
for Dtube = 0,7 M
turbulent
> 470
43
> 3
< 0,0015
,
u
470-77
0,0015-0,009
3,43-0.562
77-25
0,009-0,0028
0,L62-0,182
25-12
0&028-0
0583
182-0
0
087
,
fCor
d
,
,
=
0~S4 it
12-2,3
0,0033-0,017
0,087-0,017
< 2;3
> 0,017
< 0,017
>100
-for Dtube = 0,07 M
-
> 0,7.3
< 0,0073
(0,0005 -0,0073)
>. 0. 0073
470
470-77
77-25
25-12
12-2,3
2;3
>100
Interval of values of
DP for known Dtube , '-
< 0,0015
12,747
1199
Interval of values I
in m.) of Dtube fox frrom D of the
Dp . 0,0073 m, entire Fnterval
> 3,43
0,0015-0,609
3,43-0,562
0,009-0,0028
0,562-0,182
f 0028-0 , 0583
o--
0,182-0,087
=.0,04x
0,0033-0,017
0,087-0,017
> 0,017
for Dtube - 0,07 Y
< 0,0073
(0,0003-0,007,3)
> -0,0073
(0,0073-0,03)
< 0,017
> 0,73
< 0,73
for Dtube = 0,04 x
0
058
0
0,005-0,015
,
-
,222
0;,e22-0.0087
1
eo2
I
m0
?t
oS
-:
6
7
~
?
'e
T
?
m
J
?
0 0/ 02 12 RV 0,s o, a7
linear velocity of the air, m,/seo;
FIG. 7. DEPENDENCE OF THE HYDRAULIC RESISTANCE Ap CF.*
COLUEIN WITH GRANULATED CATALYST UPON THE LINEAR VELOCITY
OF THE GAS STREAEI OBSERVED IN THIS WORK, 1 - 4 p at the
air inlet to the column; 2 - Ap at the middle of the
column; 3 - average values of Op; 4 - Gp at the exit
from the column; 5 - Ap according to Zhavoronkov; 6 6p
according to Chilton and Colburn; 7 - p according to
Chilton and Colburn, assuming the average diameter.;of,the
particles to be equal to the cubic root of three
dimensions.
Value of K in equation /46/
1 from D
J Extreme values Dtub
given for the
__ interval
3D p 0,085
2,11 D P 0,03
3,08 D P 0,202
17,62 DP 0,6.29
51,33 D P 0 13
17,6
D.p 0,098
85,6 D P 0,673
600 Dp
(7; 4)
(9; 0,8)
(0,5; 0,2)
(0,15; 0.09)
(0,07; 0,018)
(0,017; 0,003)
(3; 0,R)
(0,7; 0,06)
(0,05; 0,02)
(0,03; 0,008)
The numerical we lueApp~-o ~ecb bgr I eIe S8t,20g2/f1 /it1, CIA-RDP80-00926A001400040002-2
Values of K
corresponding to them
2
4
2
1
(
,6
;
,97)
0,04
D tube
2
1
(
,22;
2,
2)
D,04
tube
(1,35;
1,33)
f_, 0,04
05
1
1
0
(
,
;
,
6)
D
0104
b
tu
e
(3
2;
3
14
)
,
,
D tube 01,111
(8,5)*
Gllbe~. 29 b
(51,9; 49)L;
O,OaO
tube
(16,6; 17,67),D tube 0,050
(85;89 '
tube 0,31;
(165,2)D? tube 0,428
 or.
p
ro
a
or
R
a
Ih
4
B Q
! 4
2
.1
4
diameter of the tube in m.
IG. 5, DEP 1?DETCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYTIC TOWER &T) UPON ITS DIAMETER Dttu The
curves 1 and 3 were calculated according tobEhavoronkov
and curves 2 and 4according to Chilton and Colburn.
FIG. 6, EXPERIMENTAL UNIT FOR THE STUDY OF THE
EFFECT OF THE LINEAR VELOCITY OF A STREAM OF GAS
UPON THE HYDRAULIC RESISTANCE OF A COUJMN WITH
SOLID GRANULATED CATALYST
TABLE 3. EFFECT OF Tiff AVERAGE GRAIN SIZE OF THE CATALYST (D ) AND THE DIA1,1FTER OF THE
CONTACT COLUtfN (Dtube) ON THE VALUE OF K IN FEUATION P/46/
(0,0005 -0,0073)
Interval of
values of
Dtube/Dp
Interval of values of
Dp for known Dtube , '-
for Dtube = 0,7 N
> 470
< 0,0015
470-77
0,0015-0,009
77-25
0,009-0,0028
25-12
Lo 1, 0:6028-0,0383
-rvk
all =f,,04 x
12-2,3
< 213
> 0,017
for Dtube - 0.07 K
>100
< 0,0073
>-0,0073
.
(0,0073-0,03)
for Dtube = 0,04 K
i.9
Interval of values
in m.) of Dtube fox F'rom D of the
D_ .0,0073 m, entire interval
Value of K in equation /46/
from D
> 3,43
3D p 0,085
3,43-0.562
2,11 D p 0,03
0
02-0
182
__ I
,
,
pp 0,06
1
0,182-0,087
DP 0,10
0,087-0,017
3,08 DP 0,203
< 0,017
17,62 DP 0,629
> 0, 7.3
51,33 DP 9 n
D 0,098
I
?Z
?p
of
I
j
I
to
-
?
?
,
.
m
f
?
B 0.1 0.2 93 QV 95 0, 97 91 fiff ZB IF U
linear velocity of the air, m,/seo.
FIG. 7. DEPEEDE'CE OF THE HYDRAULIC RESISTANCE pp 0?. ,
COLUMN WITH GRAIu LAMED CATALYST UPON THE LINEAR VELOCITf
OF THE GAS STREAK OBSERVED IN THIS WORK. 1 - d p at the
air inlet to the column; 2 - op at the middle of the
column; 3 - average values of Ap; 4 - Ap at the exit
from the column; 5 - op according to Zhavoronkov; 6 - sp
according to Chilton and Colburn; 7 - &p according to
Chilton and Colburn, assuming the average diameteiE of. the
particles to be equal to the cubic root of three
dimensions.
p
85,6 D p 0.873
Extreme values Dtub
Values of K
given for the
interval
corresponding to them
(7; 4)
Dtube0,04
(3; 0,8)
D tubs 0,04
1
35
(0,5; 0,2)
(
,
; 1,33) L 0 .04
I
1
05
(0,15; 0.09)
(
,
;
,06)D o
ca
,
tube
1
(0.07; 0,018)
(3,2; 3,14) D
ztt
o
,
tube
'
(0,017; 0,003)
(8, 5)
,ubeo.26 s
5
9
(3; 0,4)
(
1,
; 49) D 0,056
tube
(16,6; I7.67),
D tube 01050
0,-922-0,0087 600 DP 0,980 I (0,03; 01008)
The numerical valueAppu-Qv:ec>b c r J e et,20g2/ /1t1 CIA-RDP80-00926A001400040002-2 ubb
elease 2002/01/11 : CIA-RDP80-00926A0014000
(85;89~
tube o,s-I
(165,2)D? tube
0. 426
9
 M-
riN
1u
Gu
VI
80 Xf-
Aw-
i1~ q ~I
w ~,-oiwl
tl
4 4
1 4
2
.1
r
4
4
diameter of the tube in m,
FIG. 5. DEPSEDENCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYTIC T0'.'ER On UPON ITS DIAMETER Dub . The
curves 1 and 3 were calculated according o ~havoronkov
and curves 2 and 4'accoxding to Chilton and Colburn.
FIG. 6. EXPERII4ENTAL UNIT FOR THE STUDY OF THE
EFFECT OF THE LIPIEAR VELOCITY OF A STREAM OF GAS
UPON THE HYDRAULIC RESISTANCE OF A COMM WITH
SOLID GRANULATED CATALYST
woo
I
1
'900
(200
I
.2
('00
m9
?r
0 5
/l(00
?S
?7
900
AN
700
i-~-
609
~ ? s
sa~7
roc
--
90D
290
100
3
1
a
.?
v
A
f A
S
M
1
4
linear velocity of the air, m./see..
FIG. 7. DEPENDR'.CE OF THE HYDRAULIC RESISTANCE pp OF.,
COMM WITH GRANULATED CATALYST UPON THE LINEAR VELOCITY
OF THE GAS STREAAS OBSERVED IN THIS WORK. 1 - d p at the
air inlet to the column; 2 - op at the middle of the
column; 3 - average values of Op; 4 - 4p at the exit
from the column; 5 - Ap according to Zhavoronkov; 6 - AP
according to Chilton and Colburn; 7 - &p according to
Chilton and Colburn, assuming the average diameter..: of, the
particles to be equal to the cubic root of three
dimensions.
TABLE 3. EFFECT OF THE AVERAGE GRAIN SIZE OF THE CATALYST (D) AND THE DIAI+IE;TER OF THE
CONTACT COLUED (Dtube) ON THE VALUE OF K IN EQUATION P/46/
Interval of
values of
Dtube /Dp
Interval of values of
Dp for known Dtube , m?
Interval of values I
in m.) of Dtube fox'tFrom D of the
Dp . 0,0073 m, entire ?nterval
Value of K in equation /46/
1 from D.
Extreme values Dtub~ Values of K
given for the corresponding to them
interval
for Dtube - 0,7 K
0
085
l
turbulent
> 470
< 0,0015
> 3,43
,
3D p
(7; 4)
0'08
(2,64; 2,97) D
tube
0
03
- 1
1
2
470-77
0,0015-0,009
3,43-0,562
,
2,11 Dp
(3; 0,8)
,22; 2,
2)D
(
1
tube
77-25
0,009-0,0028
0,M-0,182
1,38
2)
(0
5; 0
(1,35; 1,33) -
D .p 0,08
,
,
G ~, 0.04
1
25-12
0,9
028--0,0583
0,182-0,087
(0
15; 0.09)
(1,05; 1,06)
,
i T
p0,10k
,
D tube 0 .04
u0', 04 w
0
202
12-2,3
0,087-0,017
,
3,08Dp
(0.07; 0,018)
(3,2; 3,14) D tube 0,211
0
01
0
629
6
D
0
G 2,3
> 0,017
,
7
.
17,
p
2
(0,017; 0,003)
(8,5)
axbe0.26 5
for Dtnbe - 0,07 H
73
0
012
33 D
1
>100
0
0073
>
,
p
,
5
(3; 0,4)
(51,9; 49) 0.036
D
,
(0,0005 -0,0073)
tube
>.0.0073
17,6 1
7; 0
(0
06)
(16
6; 17
67)
,
(0,0073-0,03)
for Dtube =0,04 11
p
D 0,068
,
,
,
;
,
D tubeO 0
1
0,005-0,015
85,6 D p 0,$73
(0,05; 0,02)
(85;89 tube 0,31;
4
0
0
'62
0
00
7
0
I
a I
3-1,2
34
0,015-0,
;
,
8
2-
600 Dp
?930
(0,03; 0,008)
(165,2)Dtube 0.420
? The numerical vlnpP1 d FtAr Fe sie &OOD2 /Q1d19t CIA-RDP80-00926A001400040002-2
 T A U . L L ' i
1 4 - HYDRAULI
C R D S T MC W C{/
KMMAW@W
YET ~x180-00
Ap, pressure drop
Dimensions
In the empty
of the tube
column
M.
Rate of flout
of the air
m
g
.p
+~
ills W
0
$:
14
41 0
`y<
15 a
a b W
A
oU t,
o
'
-,
1 15
0,1
1
2,28
0,068
1
streamline
4,03.10-4
0,054
53,2
Z 15
0,1
1
33,5
1
1
turbulent
0,019
35,2
219,2
3 500
0,2
2,544
3,46
0,068
1
streamline
1,09.10-6
-0,07
67,6
4 500
0,2
2,544
3,46
0,0004
180
a
6,07.10-8
0,07
67,6
(0,000378)
5 500
0,2
2,544
E0,9
1-
1
turbulent .
0,013
7,93
492,8
6 500
0,2
2,544
50,9
0,0055
180
streamline
0,004
0,01
985
7 500
0,2
2,544
18304
360
1
turbulent 1
446,4
3,09.101
1,96.107
8 500
0,2
2,544
18304
2
180 1
a
0,044
4,85.10'
3,07.107
.,uu
4
r
f
47
W
FIG. 2. DEPENDENCE OF THE COEFFICIENT OF THE EFFECT
OF THE WALLS a UPON THE RATIO OF THE AVERAGE DI-
APETER OF THE PARTICLES TO THE DIAMETER OF THE TUBE
DP/Dtube BY THE FORMULA OF CHILTON AND COLBURN.
1 - for streamline flow; 2 - for turbulent flow
41/f/M ~f(Mzs RIM
av. diameter of the particles, m.
FIG. 4. DEPENDENCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYST BED 4 p UPON THE AVERAGE DIAMETER OF THE
CATALYST GRAINS. For turbulent flow: 1 - according to
Chilton and Colburn; 2 - according to Zhavoronkov.
For streamline flow: 3 - according to ~Lhavoroukov; 4 -
according to Chilton and Colburn.
No.
1*
2*
Izv. (tekh.)
2, .421 if.
?w
ZGiNl
Y/
b'00
ZGm
turbulent
flow
,
streaml.ine - ,~
flow
Z
(
9#
0
0 /0 ZO W SO
av. diameter of the particle
FIG. 3. DEPENDENCE OF THE FREE VOIUPL? OF THE
CATALYST BED UPON THE AVERAGE DIAILHT R OF
THE PARTICLES.
IBhrbulent flow
9 16, M X +wa
Re', modified Reynolds number
streamline flow
FIG, 1. DEPENDENCE OF THE MODIFIED FRICTION
FACTOR f0 UPON THE 1N10DIFIED REYNOLDS NUMBER
Rev BY THE FORMULA OF CHILTON AND COLBURN.
1 - streamline flow; 2 - turbulent flow
0 0
1
o Zhavoronkov's data
? experimental data
INTERD PEPIDEUCE BETA THY. FREE SPACE OF THE PACKING AND THE AVERAGE
DIAMETER OF THE GRAIN
-Aluminosilicate
catalyst
Catalyst for con-
version of CO
Vanadium catalyst
Coke
Glass granules
Coke
n
Gravel
Coke
Andesite
Dimensions of the
grains, mm.
Av. diam-
eter of
the grain
mm. I
Free
space
5X5X8
6,0
0
35
Cylindrical
tablets
9X9X4
7,3
,
0.35
Tablets
11X11X6
9,3
0,38
if
11X11X6.5
9,5
0,43
Irregular
29,6 X 25,8 X 18
24,5
0,532
Pear-shaped
20 X 20 X 37,5
25,8
0,500
Irregular
35,6 X 28,8 X 18
27,5
0
535
47,6 X 41.5 X 33,4
40
8
,
545
0
Spherical
Irregular
56,8 X 40,8 X 29
52 X 40,3 X 35,5
,
42,2
42,6
,
0,570
0,00
56 X 43,7 X 32,6
44,1
0.565
Approved For Release 2002/0'F/9+~(a~4l26A001400040002-2
926A'0
Z
 TABLE 1 HYDRAUI c REST Q2vp~ACZ~'c ~'C9~W?11 1@w ;W QA JAT? 1r'I AIZR'3! 80-00926
T gyp
pressure drop
,
Dimensions
In the empty
of the tube
colimm
Rate of flaw
of the air
H
g
~
~,
~
~
m
5
g
ro
ppp
~
g
q
q
N
l 15
0,1
1
2,28
0,068
1
streamline
4,03.10-4
0,054
Z 15
0,1
1
33,5
1
1
turbulent
0,019
35,2
219,2
3 500
0,2
2,544
3,46
0,068
1
streamline
1,09.10-5
0,07
67,6
4 500
0,2
2,544
3,46
0,0004
180
6,07.10-8
0,07
67,6
(0,000378)
5 500
0,,2
2,544
50,9
1-
1
turbulent
0,013
7,93
492,8
5 500
0,2
2,544
50,9
0,0055
180
streamline
0,004
0,01
985
7 500
0,2
2,544
18304
360
1
turbulent
446,4
3,09.10'
1,96.10'
B 500
0,2
2,544
18304
2
180
0,014
4,85.10'
3,07.107
auu
a o
n -
a
aP
FIG. 2. DEPENDENCE OF THE COEFFICIENT OF THE EFFECT
OF THE WALLS a UPON THE RATIO OF THE AVERAGE DI-
METER OF THE PARTICLES TO THE DIAMLTFR OF THE TUBE
Dp/Dtube BY THE FORMULA OF CHILTON AND COLBURN.
1 - for streamline flow; 2 - for turbulent flow
?"
$G071
aa7
~~oa
ZLi1
r
turbulent
flow
SQ7
-
s reemlin?
flow
0
L
av. diameter of the particles, m,
FIG. 4. DEPENDENCE OF TIM HYDRAULIC RESISTANCE IN
CATALYST BED . p UPON THE AVERAGE DIAIYM;TER OF THE
CATALYST GRAINS. For turbulent flow: 1 - according to
Chilton and Colburn; 2 - according to Zvoronkov.
For streamline flow: 3 - according to Zhavoronkov; 4 -
according to Chilton and Colburn.
/0 20 V so
av, diameter of the particle
FIG. 3. DEPENDENCE OF THE FREE VOIUNa' OF TIIE
CATALYST BED UPON THE AVERAGE DIAMETER OF
THE PARTICLES.
TABLE 2. INTERDEPENDENCE BETWEEN THE FREE, SPACE OF THE PACKING AND TIWE AVERAGE
DIAMETER OF THE GRAIN
No. Type of packing
1*
2*
Izv. (tekh.)
,421 if.
?Aluminosilicate
catalyst
Catalyst for con-
version of CO
Vanadium catalyst
Coke
Glass granules
Coke
1,
Gravel
Coke
Andosite
Cylindrical
tablets
Tablets
Irregular
Pear-shaped
Irregular
H
Spherical
Irregular
Dimensions of the
grains, mm.
5X5X8
9X9X4
11X11X6
11X11X6,5
29,6X25,8X18
20 X 20 X 37,5
35,6 X 28,8 X 18
47,6 X 41,5 X 33,4
56,8 X 40,8 X 29
52 X 40,3 X 35,5
56 X 43,7 X 32,6
Approved For Release 2002/0't/1J4t R80400NA001400040002-2
'streamline flow
FIG. 1, DEPENDENCE OF THE MODIFIED FRICTION
FACTOR f0 UPON7 THE MODIFIED REYNOLDS NUMBER
Re' BY THE FORMULA OF CHILTON AND COIBURN,
1 - streamline flow; 2 - turbulent flow
0 0
O
o Zhavoronkov's data
? experimental data
r 21
w
2
lS
G
,
'Bhrrblent flow
1'! 0
i J00 aM
60
D
Av. diam-
eter of
the grain Free
nmi. 1 space
6,0
7,3
9,3
9,5
24,5
25,8
27,5
40,8
42,2
42,6
44,1
0,35
0.35
0,38
0,43
0,532
0,500
0555
0,545
0,570
0,560
0,565
0
 TABLE 1 HYDRAULIC REST Qdvl ASY C "RRdL"*%j2T`Y'ItE iA1.1r jg&.I DP80-00926
pp, pressure drop
Dimensions
In the empty
of the tube
column
m.
Rate of flow
of the air
'1,
04
~,
m
wN
y{
7 m
z
? ~~
Ya q
ci~a
4
aps
0~
A 1001
t I
.
+
l 15
0,1
1
2,28
0,068
1
streamline
4,03.10-4
0,054
53,2
Z 15
0,1
1
33,5
1
1
turbulent
0,019
35,2
219,2
3 500
0,2
2,544
3,46
0,068
1
streamline
1,09.10-5-
0,07
67,6
4 500
0,2
2,544
3,46
0,0004
180
6,07.10-8
0, 07
67,6
(0,000378)
1
5 500
0;2
2,544
i0,9
1-
1
turbulent
0,013
7,93
492,8.
6 500
0,2
2,544
50,9
0,0055
180
streamline
0,004
0,01
985
7 500
0,2
2,544
18304
360
1
turbulent
446,4
3,09.105
1,96.107
B 500
0,2
2,544
18304
2
180
n
0,044
4,85.10'
3,07.107
47
A
V 4
91- 1
N
FIG. 2. DEPENDENCE OF THE COEFFICIENT OF THE EFFECT
OF THE WALLS c UPON THE RATIO OF THE AVERAGE DI-
AMET'ER OF THE PARTICLES TO THE DIAMETER OF THE TUBE
DpIDtube BY THE FORMULA OF CHILTON AND COLBURN.
1 - for streamline flow; 2 - for turbulent flow
ruu
.,'i~'1
180
2
law-
turbulent
flow
is
- SQ7
s
reemline
'
flow
0
0
050 2Df7S 0
&7
FIG. 4. DEPENDENCE OF THE HYDRAULIC RESICCTANCE IN THE
CATALYST BED 4 p UPON THE AVERAGE DIAMETER OF THE
CATALYST GRAINS. For turbulent flow: 1 - according to
Chilton and Colburn; 2 - according to Z~avoronlcov.
For streamline flow: 3 - according to Zhavoronkov; 4 -
according to Chilton and Colburn.
Izv, (tekh.)
1946,.421 ff.
0 !0 20 MG 31
av. diameter of the particle
FIG. 3. DEPENDENCE Or THE FREE VOLUME" OF THE
CATALYST BED UPON THE AVERAGE DIAMiET R OF
THE PARTICLES.
TABLE 2. INTERDEPENDENCE BETWEEN T;U; FREE SPACE OF THE PACKING AND THE AVERAGE
DIAMETER OF THE GRAIN
No.
1?
2*
3
4
5
6*
?A1uainosilicate
catalyst
Catalyst for con-
version of CO
Vanadium catalyst
Coke
Glass granules
Coke
Gravel
Coke
Andesite
Cylindrical
tablets
Tablets
n
Irregular
Pear-shaped
Irregular
Spherical
Irregular
11 X 11 X 6.5
29,6 X 25,8 X 18
20 X 20 X 37,5
35,6 X 28,8 X 18
47,6 X 41,5 X 33,4
56,8 X 40,8 X 29
52 X 40,3 X 35,5
56 X 43,7 X 32,6
Approved For Release 2002/0'hr1 AtRBP 0926A001400040002-2
23
w
Z
s
Bhrbulent flow
fI 15
G .NIO 9.
f0 60
0
streamline flow
FIG. 1. DEPENDENCE OF TEE MODIFIED FRICTION
FACTOR f0 UPON THE MODIFIED REYNOLDS NUMBER
Ret BY THE FORMULA OF CHILTON AND COIBURN.
1 - streamline flow; 2 - turbulent flow
0 0
?
0 Zhavoronkov's data
? experimental data
Dimensions of the
grains, are.
5X5X8
9X9X4
11X11X6
Av. diam-
eter of
the grain Free
mm. space
6,0
7,3
9,3
9,5
24,5
25,8
27,5
40,8
42,2
42,6
44,1
0,35
0.35
0,38
0,43
0,532
0,500
0,535
0,545
0,570
0,500
0,565
Z
 11
TABLE it HYDRAUIJC RESI61WW"M T 'Y1STFi(1bT'rffl*' ATL~JT:AIAf ,%-&Y"1' 80-00926
Dimensions
of the tube
In the empty
column
M.
Rate of flow
of the air
us
r
.q
A
"54
E WA
.,s 42
15
0,1
2,28
0,068
4,03.10-4
0,054
53,2
15
0,1
33,5
1
0,019
35,2
219,2
500
0,2
2,544
3,46
0,068
1,09.10-5
0,07
67,6
500
0,2
2,544
3,46
0,0004
180
6,07.10-1
0,07
67,6
(0,000378
500
0,2
2,544
`0,9
1-
turbulent
A,013
7,93
492,8 .
500
0,2
2,544
50,9
0,0055
180
streamline
0,004
0,01
985
500
0,2
2,544
18304
360
turbulent
446,4
3,09.10'.
1,96.107
500
0,2
2,544
18304
2
180
4,85.10'
3,07.107
cw
07
-
25
W
2
IS
411
NGrbulent flow
1! IS
O 700 Y4
a 60
0
Re', modified Reynold o
s number 'streamline flow
FIG. 1, DEPENDENCE OF THE MODIFIED FRICTION
FACTOR f0 UPON THE MODIFIED REYNOLDS NUfNNBER
Res BY THE FORMULA OF CHILTON AND COIBURN,
1 - streamline flow; 2 - turbulent flow
0 0
0
o Zhavoronkov's data
? experimental data
Z
0 I
O 2
0
4
0 5
Dp/Dtube in m.
FIG. 2. DEPENDENCE OF THE COEFFICIENT OF THE EFFECT
OF THE WAILS c UPON THE RATIO OF THE AVERAGE DI-
AMETER OF THE PARTICLES TO THE DIAMETER OF THE TUBE
Dp/Dtube BY THE FORMULA OF CHILTON AND COLBURN.
1 - for streamline flow; 2 - for turbulent flow
W b`00
o~aU
2W !AV-
turbulent
flow
/
streamline
''
flow
0 0.
OSO 200%5
L 7
FIG. 4. DEPENDENCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYST BED 4p UPON THE AVERAGE DIAMETER OF THE
CATALYST GRAINS, For turbulent flow: 1 - according to
Chilton and Colburn; 2 - according to Z~avoronkov.
For streamline flow: 3 - according to Zhavoronkov; 4 -
according to Chilton and Colburn.
0
av. diameter of the particle
FIG. 3. DEPENDENCE OF THE FREE VCIXJ ' OF THE
CATALYST BED UPON THE AVERAGE DIAMETER OF
THE PARTICLES.
TABLE 2, INTERDEPENDENCE BETWEEN TIM; FREE SPACE OF THE PACKING AND THEE AVERAGE
DIAMETER OF THE GRAIN
No. Type of packing
Izv. (tekh,)
22 6,,421 ff.
-Aluminosilicate
catalyst
Catalyst for con-
version of CO
Vanadium catalyst
Coke
Glass granules
Coke
Gravel
Coke
Andosite
Cylindrical
tablets
Tablets
n
Irregular
Pear-shaped
Irregular
Spherical
Irregular
n
Dimensions of the
grains, mm.
5X5X8
9X9X4
11X11X6
11X11X6.5
29,6 X 25,8 X 18
20 X 20 X 37,5
35,6 X 28,8 X 18
47,6 X 41.5 X 33,4
56,8 X 40,8 X 29
52 X 40,3 X 35,5
56 X 43,7 X 32.6
Approved For Release 2002/01111 . IA DP80 9 A001400040002-2
Av. diam-
eter of
the grain Free
mm. mace
6,0
7,3
9,3
9,5
24,5
25,8
27,5
40,8
42,2
42,6
44,1
0,35
0,35
0,38
0,43
0;532
0,500
0,535
0,545
0,570
0,5b0
0,565
0
ADO
0
S
 FABLE 1 HYDRAULIC REISTYMr& hF-Rr 2C@ oC~'TH &41 11 ANHl44`STP80-00926
pp, pressure drop
Dimensions
In the empty
of the tube
column
M.
Rate of flow
f th air
g
4'
+
~
~ &
H
$
m
pro
m
qp
~
1
Q
':.
?`
4
~I
.fib q
~~
'Z ++
U
nl i?
W ki
~.~k
N v am
.~
H
~
,
1 15
0,1
1
2,28
0,068
1
streamline
4,03.10-6
0,054
53,2
2 15
0,1
1
33,5
1
1
turbulent
0,019
35,2
219,2
3 500
0,2
2,544
3,46
0,068
1
streamline
1,09.10-6
-0,07
67,6
4 500
0,2
2,544
3,46
0,0004
180
6,07.10-6
0,07
67,6
(0,000378)
5 500
0}2
2,544
X0,9
1-
1
turbulent ,
,0,013
7,93
492,8
6 500
0,2
2,544
50,9
0,0055
180
streamline
0,004
0,01
985
7 500
0,2
2,544
18304
360
1
turbulent 1
446,4
3,09.105
1,96.107
8 500
0,2
2,544
18304
2
180
0,044
4,85.10'
3,07.107
0 407 /~4m Qa 48A
DP/Dtube in m.
FIG. 2. DEPENDENCE OF THE COEFFICIENT OF THE EFFECT
OF THE WAILS a UPON THE RATIO OP THE AVERAGE DI-
AI4ETER OF THE PARTICLES TO THE DII4I TER OF THE TUBE
Dp/Dtube BY THE FOENU A OF CHILTON AND CCLBURN.
1 - for streamline flow; 2 - for turbulent flow
w
75
R
FIG. 4. DEPENDENCE OF THE HYDRAULIC RESISTANCE IN
CATALYST BED !J p UPON THE AVERAGE DIAMETER OF. THE
CATALYST GRAINS. For turbulent flow: 1 - according to
Chilton and Colburn; 2 - according to Zhavoronkov.
For streamline flow: 3 - according to havoronkov; 4 -
according to Chilton and Colburn.
Izv. (tekh.)
1946,,421 if,
Retr modified Reynolds number
- 'streamline flow
FIG. 1. DEPENDENCE OF THE MODIFIED FRICTION
FACTOR fO UPON THE MODIFIED REYNOLDS NUMBER
Ret BY THE FOiiMILA OF CHILTON AND COIBURN.
1 - streamline flow; 2 - turbulent flow
O C
O
o Zhavoronkov's data
? experimental data
F
10
20 J
a0 J
O
_
'av. diameter of the particle
FIG. 3. DEPENDENCE OF THE FREE VOI]R?O OF TILE
CATALYST BED UPON THE AVERAGE DIAIRCTSR OF
THE PARTICLES.
No.
Dimensions of the
grains, M.
Av. diam-
eter of
the grain Free
mm. space
1'
5 X 5 X 8
6
0
0
35
2?
-Aluminosilicate
Cylindrical
,
,
catalyst
tablets
9X9X4
7,3
0,35
3
Catalyst for con-
version of CO
Tablets
11X11 x6
9,3
0,38
4
Vanadium catalyst
n
11 X 11 X6.5
9,5
0,43
5
Coke
Irregular
29,6 X 25
8 X 18
24
5
0
532
6*
Glass granules
Coke
Peas-shaped
Irregular
,
20 X 20 X 37,5
.
25,8
,
0,500
n
35,6 X 28,8 X 18
27,5
0,535
47,6 X 41,5 X 33,4
40
8
545
0
Gravel
Spherical
56,8 X 40,8 X 29
,
42
2
,
0
570
Coke
Andosite
Irregular
n
52 X 40,3 >< 35,5
56 X 43,7 X 32,6
,
42,6
44,1
,
0,560
0,565
Approved For Release 2002/0111laIaMAIRDP&Ot009,2&A001400040002-2
b~00
turbulent
flow
SQ7
-
s
treamline
flow
1
25
w
2
s
4ftrbulent flow
. M
l; JIIO a
yy BO
D
Z
 TABLE 1 HYDRAULIC RESI Pr%vaA liR Tow@am '?HE/,RjLjjT'AQl&T!I RP80-00926
pp, pressure drop
Dimensions
In the empty
of the tube
column
Rate of flow
of the air
g
+
a
I
q.
4
Ys q
o
O4"
N?.iaks
?8ali
?c~?...o.
I 15
0,1
1
2,28
0,068
1
streamline
4,03.10-4b
0,054
53,2
2 15
0,1
1
33,5
1
1
turbulent
0,019
35,2
219,2
3 500
0,2
2,544
3,46
0,068
1
streamline
1,09.10-5
0,07
67,6
4 500
0,2
2,544
3,46
0,0004
180
6,07.10-8
0, 07
67,6
(0,000378)
'
5 500
0?,2
2,544
'0,9
1-
1
turbulent
.0,013
7,93
492,8
6 500
0,2
2,544
50,9
0,0055
180
streamline
0,004
0,01
985
7 500
0,2
2,544
18304
360
1
turbulent
446,4
3,09.105
1,96
8 500
0,2
2,544
18304
2
180
1
0,044
4,85.107
3,07
SW
1
W1
4
1 4
W40
FIG. 2. DEPENDENCE OF THE COEFFICIENT OF THE EFFECT
as
~' av
OF THE WALLS a UPON THE RATIO OF THE AVERAGE DI-
AMETER OF THE PARTICLES TO THE DIAMETER OF THE TUBE
o 19
Dp/Dtube BY THE FORMULA OF CHILTON AND COLBURN.
m
1 - for streamline flow; 2 - for turbulent flow
~,1/
ISOa
ZGm
I
turbulent
flow
I
I
SAf
--
s
treamline
flow
0
0.
0
a BOYS
B7
av, diameter of the partioles, m.
FIG. 4. DEPENDENCE OF THE HYDRAULIC RESISTANCE IN
CATALYST BED Q p UPON THE AVERAGE DIAMETER OF THE
CATALYST GRAINS. For turbulent flow: 1 - according to
Chilton and Colburn; 2 - according to Zhavoronkov.
For streamline flow: 3 - according to Ghavoronkov; 4 -
according to Chilton and Colburn.
Izv. (tekh.)
1946,421 ff.
25
All
2
13hrbulent flow
+'v ,
. ,Inv ;
f sa
v
streamline flow
FIG. 1. DEPENDENCE OF THE MODIFIED FRICTION
FACTOR #0 UPON THE MODIFIED REYNOLDS NUMBER
Re' BY THE FORMULA OF CHILTON AND COIBURN.
1 - streamline flow; 2 - turbulent flow
O O
O
O
o Zhavoronkov'a data
? experimental data
0
la
0 j
b~ N
G S
a
av. diameter of the particle
FIG. 3. DEPENDENCE OF THE FREE VOINM% OF THE
CATALYST BED UPON THE AVERAGE DIAMIETER OF
THE PARTICLES.
TABLE 2. INTERDEPENDENCE BETWEEN THE FREE SPACE OF THE PACKING AND TIrE AVERAGE
DIAMETER OF THE GRAM
(
Shape
Dimensions of the
grains, mm.
Av. diam-
eter of
the grain
M.
Free
space
5X5X8
6,0
0,35
?Almatnosilicate
catalyst
Cylindrical
tablets
9X9X4
7,3
0,35
Catalyst for con-
Tablets
11X11X6
9,3
0,38
version of CO
Vanadium catalyst
11 X 11 X 6.5
9,5
0,43
Coke
Irregular
29,6 X 25,8 X 18
24,5
0,532
Glass granules
Pear-shaped
20 X 20 X 37,5
25,8
0,500
Coke
u
Irregular
35,6 X 28,8 X 18
47,6 X 41.5 X 33,4
27,5
40
8
0535
545
0
Gravel
Spherical
56,8 X 40,8 X 29
,
42
2
,
0
570
Coke
Irregular
52 X 40,3 X 35,5
,
42,6
,
0
5ii0
Andosite
56 X 43,7 X 32,6
44,1
,
0,565
Approved For Release 2002/0111 gatiaC#A?RLW&OtOO9,2 4001400040002-2
 . Approved For Release 2002/01/11 : CIA-RDP80-00926AO01400040002-2
TABLE 2,- HYDRAULIC RESISTANCE OF C TALYTIC TOWERS WMIO THE CATALYST AND WITH IT
Ap, Pressure drop
Dimensions
In the empty
of the tube
coltmm
M.
Rate of flow
of the r
N
0
4
o
8
z f
ca
1 15
0,1
1
2,28
0,068
1
streamline ``
4,03.10 4
0,054
53.2
2 15
0,1
1
33,5
1
1
turbulent
I
0,019
35,2
219,2
3 500
0,2
2,544
3,46
0,068
1
streamline
1,09.10-5
0,07
67,6
4 500
0,2
2,544
3,46
0,0004
180
6,07.10-'t
0,07
67,6
(0.000378)
'
5 500
0;2
2,544
E0,9
1'
1
turbulent .
0,013
7,93
492,8.
6 500
0,2
2,544
50,9
0,0055
180
streamline
0,004
0,01
985
7 500
0,2
2,544
18304
360
1
turbulent
446,4
3,09.105
1,96.107
8 500
0,2
2,544
18304
2
180
0,014
4,85- 10'
3,07
J
9.
?/A
0
FIG. 2. DEPENDENCE OF THE COEFFICIENT OF THE EFFECT
M
OF THE WALLS o UPON THE RATIO OF THE AVERAGE DI-
AtE'TER OF THE PARTICLES TO TBE DIATETBR OF THE TUBE
D_/Dtube BY THE FORANLA OF CHILTON AND COLBURN.
1 - for streamline flow; 2 - for turbulent flow
2fr~711
IGOJ
turbulent
flow
SLC
~
- -
s
I
reamline
flow
3
FIG. 4. DEPENDENCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYST BED a p UPON THE AVERAGE DIAMETER OF THE
CATALYST GRAINS. For turbulent flow: 1 - according to
Chilton and Colburn; 2 - according to Z avoronkov.
For streamline flow: 3 - according to Zhavoronkov; 4 -
according to Chilton and Colburn.
Izv. (tekh.)
1946, ,421 ff.
0 0
?
1
0 Zhavoronkov's data
? experimental data
av, diameter of the particle
FIG. 3. DEPENDENCE OF THE FREE VODE-IL OF THE
CATALYST BED UPON THU AVERAGE DIALP;TER OF
THE PARTICLES.
DIAMETER OF THE GRAIN _ _
Rat, modified Reynolds number
streamline flow
FIG. 1. DEPENDENCE OF THE MODIFIED FRICTION
FACTOR fO UPON THE MODIFIED REYNOLDS NUMBER
Re' BY THE FORMULA OF CHILTON AND COIBURN.
1 -.streamline flow; 2 - turbulent flow
Dimensions of the
grains, mm.
Av, diam-
eter of
the grain Free
--, I space
10
i
5X5X8
6,0
0,35
2*
?Aluminosilieate
Cylindrical
catalyst
tablets
9(9X4
7,3
0.35
3
Catalyst for con-
version of CC
Tablets
IIXIIX6
9,3
0.38
4
Vanadium catalyst
it
11X11X6.5
9,5
0,43
5
Coke
Irregular
29,6 X 25,8 X 18
24,5
0;532
6*
7
Glass granules
Coke
Pear-shaped
Irregular
20 X 20 X 37,5
35,6 X 28',8 X 18
25,tt
27,5
0,500
0,535
8
47,6X41.5)(33,4
40,8
0,545
9
Gravel
Spherical
56,8 X 40,8 X 29
42,2
570
0
10
11
Coke
Andosite
Irregular
a
52 X 40,3 X 35,5
56 X 43,7 X 32,6
42,6
44,1
,
0,540
0.565
* Catalyst tested in this work
Approved For Release 2002/01/11 : CIA-RDP80-00926AO01400040002-2
2S
~1
.
1
X
turbulent flow
II /
SG .70D C.
4D f0
0
 Approved For Release 2002/01/11: CIA-RDP80-0092630AO01400040002-2
TABLE 1. HYDRAULIC RESISTANCE OF CATALYTIC TOWERS WITHOUT THE OATAI.YST AND WITH IT
&p, pressure drop
Dimensions
In the empty
of the tub
columi
M.
e
of flaw
of th
air
`~
o
P0
8 ?0 4'
o d
a
a~ c~ rn
a
a
9
w
tA~
l
8
n
z l
n
s!
C)
o -? aI
a"
. .
15
0,1
1
2,28
0,068
1
streamline
4,03-10-4
V, 054
53,2
2 15
0,1
1
33,5
1
1
turbulent
0,019
135,2
219,2
3 500
0,2
2,544
3,46
0,068
1
streamline
1,09.10-5
'0,07
67,6
4 500
0,2
2,544
3,46
0,0004
180
>
6,07.10-e
0,07
67,6
(0,000378)
1
5 500
0,2
2,544
50,9
1-
1
turbulent
0,013
7,93
492,8.
6 500
0,2
2,544
50,9
0,0055
180
streamline
0,004
0,01
985
7 500
0,2
2,544
18304
360
1
turbulent
446,4
3,09105
1,96.10,
8 500
0,2
2,544
18304
2
180
0,044
4,85.101
3,07.107
as
flow
I 0 O.OOZS 0050 3 0075 D OJ7s
av. diameter of the particles, is.
.r~
FIG. 4. DEPENDENCE OF TILE HYDRAULIC RESISTANCE IN THE
CATALYST BED Q p UPON THE AVERAGE DIAMETER OF THE
CATALYST GRAINS. For turbulent flow: 1 - according to
Chilton and Colburn; 2 - according to Z}}l~avoronkov.
For streamline flow: 3 - according to Zhavorankov; 4 -
according to Chilton and Colburn.
Izv. (tekh.)
1946,.421 ff.
25
,
Z
m
s
%rbulent flow
I
!
V
"
S61 to
o
'streamline flow
FIG, 1. DEPENDENCE OF THE MODIFIED FRICTION
FACTOR 20 UPON THE MODIFIED REYNOLDS NUMBER
Re' BY THE FOIP-ILA OF CHILTON AND COIBURN.
1 - streamline flow; 2 - turbulent flow
0 0
o Zhavoronkov's data
? experimental data
0
(0 20
c
0 5
0
av, diameter of the particle
FIG. 3. DEPENDENCE OF THE FREE VOIJEN OF THE
CATALYST BED UPON TIM AVERAGE DIAENT R OF
THE PARTICLES.
INTERDEPENDENCE BETWEEN TIIi:: FRET; SPACE OF THE PACKING AND N-IN AVERAGE
DIAMETER OF TILE GRAIN
Av. Siam-I
eter of
No.
Shape
Dimensions of the
grains, mm.
the grain
mm.
Free
since
1*~
5X5x8
2*
-Altmjinoeilicate
Cylindrical
catalyst
tablets
9X9X4
7,3
0,35
3
Catalyst for con-
Tablets
1IX11X6
9,3
0,38
4
version of CO
Vanadium catalyst
v
11 X 11 X 6,5
9,5
0,43
5
Coke
Irregular
29,6 X 25,8 X 18
24,5
0;532
6*
Glass granules
Pear-shaped
20 X 20 X 37,5
25,8
0,500
Coke
n
Irregular
17
35,6 X 28,8 X 18
27,5
0,535
47,6 X 41,5 X 33,4
40,8
0,545
Gravel
Spherical
56.8 X 40,8 X 29
42,2
570
0
Coke
Irregular
52 X 40,3 X 35,5
42,6
,
0,5ti0
Andosite
56X 43,7 X 32,6
44,1
0,565
* Catalyst tested in this work
Approved For Release 2002/01/11 : CIA-RDP80-00926A001400040002-2
tube in m.
FIG. 2, DEPENDENCE OF THE COEFFICIENT OF THE EFFECT
OF TIM WALLS a UPON THE RATIO OF THE AVERAGE DI-
P14ETFSi OF THE PARTICLES TO THE DIAMETER OF TEE TUBE
Dp/Dtube BY THE FORMULA OF CHILTON AND COLBURN.
1 - for streamline flow; 2 - for turbulent flow
turbulent
flow
SRS
J
Z
 Approved For Release 2002/01/1.1 : CIA-RDP80-00926AO01400040002-2
.30
TABLE I.- HYDRAUIIC RESISTANCE OF CATALYTIC TOWERS WITHOUT THE CATALYST AND WITH IT
&p, pressure drop
Dimensions
In the empty
of the tube
oolimm
m,
Rate of f1aW
of the r
pp
y
vp~~
pp
o
cz
~d
~?
Ys q
~+Fi
o`dw
~,a~az
? ?rn
f
1 15
0,1
1
2,28
0,068
1
streamline
4,03.10-4
0,054
53,2
2 15
0,1
1
33,5
1
1
turbulent
0,019
35,2
219,2
3 500
0,2
2,544
3,46
0,068
1
streamline
1,09.10-6
.0,07
1
67,6
4 500
0,2
2,544
3,46
0,0004
180
a
6,07.10-8
0,07
1
67,6
(0,000378)
1
5 500
012
2,544
1-0,9
1-
1
turbulent
,0,013
7,93
492,8 .
6 500
0,2
2,544
50,9
0,0055
180
streamline
0,004
0,01
985
7 500
0,2
2,544
18301
360
1
turbulent
446,4
3,09- 105
1,96.107
8 500
0,2
2,544
18304
2
180
0,014
4,85.10'
3,07.107
vu
1
--r- -
Q
FIG. 2. DEPENDENCE OF THE COEFFICIENT OF THE EFFECT
OF TIM WALLS c UPON THE RATIO OF THE AVERAGE DI-
P14ETER OF THE PARTICLES TO TEE DIAMETER OF THE TUBE
Dp/Dtube BY THE FORMULA OF CHILTON AND COLBURN.
1 - for streamline flow; 2 - for turbulent flow
26.81!
IS00
-Mv
turbulent
.flow
SQ1
-
~.
s
treamline
'
flow
FIG. 4. DEPENDENCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYST BED 46 p UPON THE AVERAGE DIAMETER OF THE
CATAIYST GRAINS, For turbulent flow: 1 - according to
Chilton and Colburn; 2 - according to Zpavoronkov.
For streamline flow: 3 - according to Zhavoronkov; 4 -
according to Chilton and Colburn.
Izv. (tekh.)
1a, .421 #f .
2S
a
Z
tjhrbulent flow
VI /
SG .77g Y
SO 60
0
Re', modified Reynolds number
streamline flow
FIG. 1, DEPENDENCE OF THE MODIFIED FRICTION
FACTOR f0 UPON THE MODIFIED REYNOLDS MM4BER
Re' BY THE FORMULA OF CHILTON AND COIBURN.
1 - streamline flow; 2 - turbulent flow
0 0
0 Zhavoronkov' a data
? experimental data
0 IO 20 . V0 SO
av, diameter of the particle
FIG. 3. DEPENDENCE OF THE FRAN VOTIJEL OF TfD;
CATALYST BED UPON THE AVERAGE DINJTEP. OF
THE PARTICLES.
1?I
2'
-Aliminosilicate
catalyst
Cylindrical
tablets
3
Catalyst for con-
version of CO
Tablets
4
Vanadium catalyst
II
5
Coke
Irregular
6'
Glass granules
Coke
Gravel
Coke
Andesits
Pear-shaped
Irregular
R
Spherical
Irregular
Dimensions of the
grains, mm.
Av. diam- I
eter of
the grain
mm,
Free
suaoe
5X5X8
6,0
0,35
9X9X4
7,3
0,35
11X1IX6
9,3
0.38
11 X 11 X 6.5
9,5
0,43
29,6 X 25,8 X 18
24,5
0,532
20 >( 20 X 37,5
25,8
0,500
35,6 X 28,8 X 18
27,5
0,535
47,6 X 41.5 X 33,4
40.8
0,545
56,8 X 40,8 X 29
42,2
0,570
52 X 40,3 X 35,5
42,6
0560
56 X 43,7 X 32,6
44,1
0.565
* Catalyst tested in this work
Approved For Release 2002/01/11 : CIA-RDP80-00926AO01400040002-2
 0,068
1
0,068
0,0004
(0,000378)
1-
0,0055
360
2
turbulent 10,013
streamline 0,004
turbulent 446,4
SW
Q1
Q
FIG. 2. DEPENDENCE OF THE COEFFICIENT OF THE EFFECT
OF THE WALLS o UPON THE RATIO OF THE AVERAGE DI-
A14ETER OF THE PARTICLES TO THE DIAMETER OF THE TUBE
Dp/Dtube BY THE FORMULA OF CHILTON AND COLBURII.
1 - for streamline flow; 2 - for turbulent flow
N
av. diameter of the particles, m.
FIG. 4, DEPENDENCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYST BED 4 p UPON THE AVERAGE DIAMETER OF THE
CATALYST GRAINS. For turbulent flow: 1 - according to
Chilton and Colburn; 2 - according to Z~aavoronkov.
For streamline flow: 3 - according to Zhavoronkov; 4 -
according to Chilton and Colburn.
Izv. (tekh.)
.1946p421 ff.
b'0
av i
turbulent
flow
J JX'
-
streamline
flow
3
7 25
7
a.
'~+
2
I f5
c3
4Grbulent flow
1'I I5
7, 0!0 y5
0 60
0
streamline flaw
FIG. 1. DEPENDENCE OF THE 140DIFIED FRICTION
FACTOR f0 UPON THE MODIFIED REYNOLDS MOONED
Re' BY THE FORMULA OF CHILTON AND COIBURN.
1 - streamline flow; 2 - turbulent flaw
O O
00
O
?
0 Zhavoronkov's data
? experimental data
0 JO 20 J _ 40 50
av, diameter of the particle
FIG. 3. DEPENDENCE OFF THE FREE VOIDIU, OF THE
CATALYST BED UPON TIIE AVERAGE DIA1fETS;R OF
THE PARTICLES.
TABLE 2. INTERDEP1 DENCE BLTWEN TIIY: FRT SPACE OF THE PACKING AND TIlE AVERAGE
DIAMETER OF THE GRAIK__,
No, Type of packing
1*
2*
-Aluminosilicate
catalyst
Catalyst for con-
version of CO
Vanadium catalyst
Coke
Glass granules
Coke
n
Gravel
Coke
Andosite
Sha
Pe
Dimensions of the
grains, mm.
Av. diam-
eter of
the grain
mm.
Free
space
5X5X8
6
0
0
35
Cylindrical
tablets
9X9X4
,
7,3
,
0,35
Tablets
11 X11 X6
9,3
0,38
11X11 X6.5
9,5
0,43
Irregular
29,6 X 25,8 x 18
24,5
0
532
Pear-shaped
20 X 20 X 37,5
25,8
;
0,500
Irregular
35,6 X 28,8 X 18
27,5
0
535
Spherical
Irregular
47,6 X 41,5 X 33,4
56,8 X 40,8 X 29
52 X 40,3 X 35,5
40,8
42,2
42,6
,
0,545
0,570
0
5p0
56 X 43,7 X 32,6
44,1
,
0,565
Approved For Release 2002/0191t4' a+ t RDP&o oo 26AO01400040002-2
 TABLE l .1, HMDEMISC REST f~i~1lur- Mg p1 .,.5j ,-Vk~P80-00926
T w n
ressure d-
p
0 op
Dimensions
In the empty
of the tube
t
column
M.
Ra
e of flow
air
of th
o
0)
W
A
~
M.
o

517
3
flow
streamline
flow
2
759 Ifl /77T
m
m
ga
av. diameter of
the particles, m.
0 IO 20 J V SO
av. diameter of the particle
FIG. 3, DEPENDENCE OF THE FREE VOLUI?L: OF -,TIE
CATALYST BED UPON THE AVERAGE DIATHT2R OF
THE PARTICLES.
TABLE 2. INTERDEPEMETICE BETWEEN THE FREE SPACE OF THE PACKING AND THE AVERAGE
DIAMETER OF THE GRAIN
No. Type
of packing Shape
of the
grains, mm._
Av. diam-
eter of
the grain
mm.
Free
1 space
1?
2?
-Aluminosilicate
catal
t
Cylindrical
t
bl
t
5X5X8
6,0
0,35
3
ys
a
e
s
9X9X4
7,3
0,35
Catalyst for con-
version of CO
Tablets
11X11X6
9,3
0,38
Vanadium catalyst
Coke
II
Irregular
11 X 11 X6.5
9,5
0,43
29,6 X 25,8 X 18
24,5
0
532
Glass granules
Coke
Pear-shaped
Irregular
20)20X37,5
25,8
,
0,500
e
35,6 X 28,8 X 18
27,5
0
535
Gravel
Spherical
47,6 X 41,5 X 33,4
40,8
,
0,545
Coke
Irregular
56,8 X 40,8 X 29
42,2
0,570
Andesite
52 X 40,3X35,5
42,6
0,500
56 X 43,7 X 32,6
44,1
0,565
FIG. 4, DEPENDENCE OF TILE HYDRAULIC RESISTANCE IN THE
CATALYST BED A D UPON THE AVERAGE DIAMETER OF THE
CATALYST GRAINS. For turbulent flow: 1 - according to
Chilton and Colburn; 2 - according to Zp]iavoronkov.
For streamline flow: 3 - according to Zhavoronkov; 4 -
according to Chilton and Colburn,
Izv. (tekh.)
1946,,421 ff.
Approved For Release 2002/019filY8C - P8 6A001400040002-2
7 25-
9
W
Z
Uhrbullent flow
aI /5
6 800 'ti
n 800
streamline flow
FIG. 1. DEPENDENCE OF THE MODIFIED FRICTION
FACTOR f0 UPON THE MODIFIED REYNOLDS NUMBER
Re? BY THE FORMULA OF CHILTON AND COIBURN.
1 - streamline flow; 2 - turbulent flow
0 0
o Zhavoronkov's data
? experimental data
 rJWL 1 HYDRA I,T RESI IiID
101L17
X11 5~ f~t~B' I'2 U-UL
L p, pressure drop
Dimensions
In the empty
of the tube
column
m.
Rate of flow
of th air
+,
U
N
m -
PP
I
MV
a,
15
0,1
1
2,28
0,068
1
streamline
4,03.10-41
0,054
53,2
2 15
0,1
1
33,5
1
1
turbulent
0,019
35,2
219,2
3 500
0,2
2,544
3,46
0,068
1
streamline
1,09.10-5
0,07
67,6
4 500
0,2
2,544
3,46
0,0004
180
6,07.10-8
0,07
67,6
(0,000378)
1
5 500
0,2
2,544
'0,9
1-
1
turbulent .
0,013
7,93
492,8 .
6 500
0,2
2,544
50,9
0,0055
180
streamline
0,004
0,01
985
7 500
0,2
2,544
18304
360
1
turbulent
446,4
3,09- 105
1,96- 107
8 500
0,2
2,544
18304
2
180
a
0,044
4,85.10'
3,07.107
trw
07
0
:
L
O
48
37aff
1 P
1 25
o
A
Z
Bhrbulent flow
A JS
G J00 ?A
7 6Y/
0
streamline flow
FIG. 1. DEPENDENCE OF THE MODIFIED FRICTION
FACTOR f0 UPON THE MODIFIED REYNOLDS ITUIIBER
Re' BY THE FORMULA OF CHILTON AND COIBURN.
1 - streamline flow; 2 - turbulent flow
0 0
?
e Zhavoronkov's data
i
2
? experimental data
FIG. 2. DEPENDENCE OF THE COEFFICIENT OF THE EFFECT
OF THE WALLS o UPON THE RATIO OF THE AVERAGE DI-
AMETER OF THE PARTICLES TO THE DIMMER OF THE TUBE
Dp/Dtube BY THE FORMULA OF CHILTON AND COLBURN.
1 - for streamline flow; 2 - for turbulent flow
av. diameter of the particles, M.
FIG. 4. DEPENDENCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYST BED L.1 p UPON THE AVERAGE DIAIER OF THE
CATALYST GRAINS. For turbulent flow: 1 - according to
Chilton and Colburn; 2 - according to Z~avoronkov.
For streamline flow: 3 - according to Zhavoronkov; 4
according to Chilton and Colburn,
Izv. (tekh.)
1946, ,421 if.
2G9I/
Ar
1
turbulent
flow
J
SW
streamline
~
flow
1
I
O
/0 20 NO SO
av. diameter of the particle
FIG. 3. DEPENDENCE OF THE FREE VOEMT-] OF THEM
CATALYST BED UPON TIM AVERAGE DIAbff;TER OF
THE PARTICLES.
TABLE 2. INTERDEPENDENCE B TWEEN TIC'. FREE SPACE OF THE PACKING AND TAE AVERAGE
DIAMETER OF TEE GRAIN
_ __
Av. diam-
eter of
Dimensions of the
the grain
Free
No. Type of packing
grains, mm.
mm. I
space
1?
2*
-Aluminosilieate
Cylindrical
5X5X8
6,0
0.35
catalyst
tablets
9X9X4
7
3
0
35
3
Catalyst for con-
Tablets
11X11X6
,
9,3
,
0
38
4
version of CO
Vanadium catalyst
II
11 X 11 X6.5
9,5
,
0,43
5
~ Coke
Irregular
6*
29,6X25,8x 18
24,5
0532
Glass granules
Pear-shaped
20 X 20 X 37,5
25,8
0,500
7
Coke
Irregular
11
35,6 X 28,8 X 18
27
5
0
535
8
9
Gravel
Spherical
47,6 X 41,5 X 33,4
,
40,8
,
0,545
10
Coke
Irregular
56,8 X 40,8 X 29
42,2
0,570
52 X 40,3X35
5
42
6
0
I1
Andesite
,
56 X 43,7 X 32,6
,
44,1
0,565
Approved For Release 2002/0`1Phle GIAgRD 0NP6A001400040002-2
 TABLE 1 IlYDRAUIaC REST 4?*;0 Ajj j8j P80-00926
A p
pressure drop
0
Dimensions
In the
empty
of the tube
,
0017MMM
M.
Rate of flow
Of the air
+a .~
H
m ..
H
ca
m
41
~p}
1 15
0,1
1
2,28
0,068
1
streamline
4,03.10-4
0,054
53,2
Z 15
0,1
1
33,5
1
1
turbulent
0,019
35,2
219,2
3 500
0,2
2,544
3,46
0,068
1
streamline
1,09.10-6
0,07
67,6
1 500
0,2
2,544
3,46
0,0004
180
>
6,07.10-8
0,07
67,6
(0,000378)
5 500
0,,2
2,544
-0,9
1-
1
turbulent .
0,013
7,93
492,8.
5 500
0,2
2,544
50,9
0,0055
180
streamline
0,004
0,01
985
7 500
0,2
2,544
18304
360
1
turbulent
446,4
3,09105
1,9610'
8 500
0,2
2,544
18304
2
180
0,044
4,85.10'
3,07.107
cw
4
0
tube in m.
FIG. 2. DEPENDENCE OF THE COEFFICIENT OF THE EFFECT
OF TILE WALLS c UPON THE RATIO OP THE AVERAGE DI-
AMETER OF THE PARTICLES TO THE DIAMETER OF THE TUBE
Dp/Dtube BY THE FORINLA OF CHILTON AND COLBURN.
1 - for streamline flow; 2 - for turbulent flow
7G47
4'pp
2V
I
turbulent
flow
J
SW
- --
streamline
flow
D
av. diameter of the particles, M.
FIG. 4. DEPENDENCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYST BED LS D UPON THE AVERAGE DIAMETER OF THE
CATALYST GRAINS. For turbulent flow: 1 - according to
Chilton and Colburn; 2 - according to Zhavoronkov.
For streamline flow: 3 - according to Zhavoronkov; 4 -
according to Chilton and Colburn.
Izv. (tekh.)
x,.421 ff,
J7 -- d , 4w Sp
av. diameter of the particle
FIG. 3. DEPENDENCE OF THE FRED VOIUIE; OF THE
CATALYST BED UPON THE AVERAGE DIAMETER OF
THE PARTICLES.
TABLE 2. INTERDEPENDENCE BETWEEN LID:: FREE SPACE OF THE PACKING AND THE AVERAGE
DIAMETER OF THE GRAIN_ _- _
Av. diam-I
eter of
No., Typ Shape Dimensions of the the grain Free
a of pa
grains, mm. mm. 1 space
1*
2*
3
4
5
6*
?Aluminosilicate
catalyst
Catalyst for con-
version of CO
Vanadium catalyst
Coke
Glass granules
Coke
?
Gravel
Coke
Andosite
Cylindrical
tablets
Tablets
n
Irregular
Pear-shaped
Irregular
Spherical
Irregular
5X5X8
X9X
11 X 11 X46
11 X 11 X6.5
29,6 X 25,8 X 18
20 X 20 X 37,5
35,6 X 28,8 X 18
47,6 X 41,5 X 33,4
56,8 X 40,8 X 29
52 X 40,3 X 35,5
56 X 43,7 X 32,6
6,0
7,3
9,3
9,5
24,5
25,8
27,5
40,8
42,2
42,6
44,1
0,35
0,35
0.38
0,43
0,532
0,500
0,535
0,545
0,570
0,560
0.565
Approved For Release 2002/DIM GI - POiO0026AO01400040002-2
streamline flow
FIG. 1. DEPENDENCE OF THE MODIFIED FRICTION
FACTOR f0 UPON THE MODIFIED REYNOLDS IHIhIBER
Re' BY THE FOHEULA OF CHILTON AND COIBURN.
1 - streamline flow; 2 - turbulent flaw
0 0
00
?
o Zhavoronkov'a data
1
Z
? experimental data
F
25
W
Z
IS
~
La JS
%r bulent flow
G ,?p0 c.
7 Ep
p
S
 TABLE 1 HYDRAUIIC RESIST IBB' g~Y IQrT047ERS 1~i~U 01aIIx1 AiH I-FtPP80-00926A
AP, pressure drop
Dimensions
In the empty
of the tube
column
M.
Rate of flow of the air
~''
ti
ro ~
.? ci
s.
ti
N
?
p-~
B
m
? H
a
a
o-~
q
g
~
A
0
cA rn
WE
z
1
I 15
0,1
1
2,28
0,068
1
streamline
4,03.10-4
0,054
53,2
Z 15
0,1
1
33,5
1
1
turbulent
0,019
35,2
219,2
3 500
0,2
2,544
3,46
0,068
1
streamline
1,09.10-6
0,07
67,6
4 500
0,2
2,544
3,46
0,0004
180
>
6,07.10-8
0,07
67,6
(0,000378)
5 500
0,2
2,544
X0,9
1-
1
turbulent
0,013
7,93
492,8
6 500
0,2
2,544
50,9
0,0055
180
streamline
0,004
0,01
985
7 500
0,2
2,544
18304
360
1
turbulent
446,4
3,09.106
1,96.10'
8 500
0,2
2,544
18304
2
180
a
0,044
4,85.10'
3,07.107
FIG. 4. DEPENDENCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYST BED 4 p UPON THE AVERAGE DIAMETER OF THE
CATALYST GRAINS. For turbulent flow: 1 - according to
Chilton and Colburn; 2 - according to Zjlavoronkov.
For streamline flow: 3 - according to Zhavoronkov; 4 -
according to Chilton and Colburn.
Izv. (tekh.)
1946, .421 if.
No.
25
W
Z
'
@hrbulent flow
1c IS
L J00 41
M 60
0
Re', modified Reynolds number
streamline flow
FIG. 1. DEPENDENCE OF THE MODIFIED FRICTION
FACTOR f0 UPON THE MODIFIED REYNOLDS NUMBER
Re' BY THE FORMULA OF CHILTON AND COIBURN.
1 - streamline flow; 2 - turbulent flow
0 0
?
45
0.0
?
OJ
o Zhavoronkov'a data
? experimental data
O.Z
0.~
0 1
0
20 J
O V
0 5
0
av. diameter of the particle
FIG. 3. DEPENDENCE OF THE FREE VOIAIr; OP THE
CATALYST BED UPON TIE AVERAGE DIAIETER OF
TEE PARTICLES.
INTERDEPENDENCE BETWEEN TlL FREE SPACE OF THE PACKING AND TTTE AVERAGE
DIAMETER OF THE GRAIN_
Dimensions of the
grains, M.
Av. diam-
eter of
the grain Free
mm. space
?Alimiinosilicate
Cylindrical
5X5X8
6,0
0,35
catalyst
tablets
9X9X4
7,3
0,36
Catalyst for con-
version of CO
Tablets
11X11X6
9,3
0,38
Vanadium catalyst
Coke
Irregular
11 X 11 X 6,5
9,5
0,43
29,6 X 25,8 X 18
24,5
0,532
Glass granules
Coke
Pear-shaped
Irregular
20 X 20 X 37,5
25,8
0,500
35,6 X 28,8 X 18
27,5
0,535
47,6 X 41,5 X 33,4
40
8
545
0
Gravel
Spherical
56,8 X 40,8 X 29
,
42,2
,
0
570
Coke
A
d
it
Irregular
It
52 X 40,3 X 35,5
42,6
,
0,500
n
es
e
56 X 43,7 X 32,6
44,1
0.565
Approved For Release 2002/01/9ata: lai P,80M09k6A001400040002-2
uu
FIG. 2. DEPENDENCE OF THE COEFFICIENT OF THE EFFECT
OF THE WALLS o UPON THE RATIO OF THE AVERAGE DI-
A14ETER OF THE PARTICLES TO THE DIATTER OF TIE TUBE
Dp/Dtube BY THE FORMULA OF CHILTON AND COLBURN.
1 - for streamline flow; 2 - for turbulent flow
turbulent
flow
-
I
s
treamline
s
flow
 LE
I - HYDRAUII
C RESIS
rrdu R tr12
n4A ~T1 ~F P80-0
Ap, pressure drop
Dimensions
In the empty
of the tube
column
M.
Bate of flout
of th air
g
w
+
cc~~
~~yy
yg
O
ti
49
.0
ii
q
itl'
'
pp
Yb
M h
40
U
.m H I
..
'~
?
-
q
.
U
i?.,F6 Ct..
N
.14
F4 i,
1 15
0,1
1
2,28
0,068
1
streamline
4,03.10-'
0,054
53,2
2 15
0,1
1
33,5
1
1
turbulent
0,019
35,2
219,2
3 500
0,2
2,544
3,46
0,068
1
streamline
1,09.10-6
0,07
67,6
4 500
0,2
2,544
3,46
0,0004
180
a
6,07.10-8
0,07
67,6
(0,000378)
5 500
0,2
2,544
X0,9
1-
1
turbulent
0,013
7,93
492,8 .
6 500
0,2
2,544
50,9
0,0055
180
streamline
0,004
0,01
985
7 500
0,2
2,544
18304
360
1
turbulent
446,4
3,09.10'
1,96107
8 500
0,2
2,544
18304
2
180
>
0,044
4,85.10'
3,07.107
cuu
Q
0
a
w to-,
FIG. 2. DEPENDENCE OF THE COEFFICIENT OF THE EFFECT
OF THE WALLS c UPON THE RATIO OF THE AVERAGE DI-
AI4JTR OF THE PARTICLES TO THE DIM PER OF THE TUBE
Do/Dtube BY THE FORMULA OF CHILTON AND COLBURN.
1 - for streamline flow; 2 - for turbulent flow
0 !0 20 w f47
av, diameter of the particle
FIG. 3. DEPENDENCE OF THE FREE VOIULIE OF THE
CATALYST BED UPON THE AVERAGE DIAIEr;T R OF
THE PARTICLES.
TABLE 2. INTERDEPENDENCE BTTI,= TIG:: FREE SPACE OF THE PACKING AND TEE AVERAGE
i
Av. diam-
eter of
Dimensions of the
the grain
Free
Type of packing
Shape
grains, mm.
mm. 1
suace
5X5X8
6,0
0
35
-AlunLinosilicate
catalyst
Cylindrical
tablets
9X9X4
7,3
,
0,35
Catalyst for con-
Tablets
I1X11X6
9,3
0,38
version of CO
Vanadium catalyst
n
11 X 11 X 6.5
9,5
0,43
hCoke
Irregular
29,6 X 25,8 X 18
24,5
0,532
Glass granules
Pear-shaped
20 X 20 X 37,5
25,8
0,500
Coke
Irregular
35,6 X 28,8 X 18
27,5
0,535
47,6 X 41,5 X 33
4
40
8
545
0
Gravel
Spherical
,
56,8 X 40,8 X 29
,
42
2
,
0
570
Coke
Irregular
52 X 40,3 X 35,5
,
42,6
,
0
560
Andesite
56 X 43,7 X 32,6
44,1
,
0.565
av. diameter of the particles, in.
FIG. 4. DEPENDENCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYST BED l.1 p UPON THE AVERAGE DIAMETER OF THE
CATALYST GRAINS. For turbulent flow: 1 - according to
Chilton and Colburn; 2 - according to Ziavoronkov.
For streamline flow: 3 - according to Zhavoronkov; 4 -
according to Chilton and Colburn.
Izv, (tekh,)
x,,421 ff,
.~A7
IS00
2LYJ
!
turbulent
flow
f
SR7
s
treamline
flow
2
0
Q
Approved For Release 2002/01F4 v M ..RDP88W026AO01400040002-2
0926Y
W
11
0>3
~
my f
I
q
.. w flow
4'I 14 300 vS0 1017
Re-, modifi d Reynolds number - streamline flow
FIG. 1, DEPENDENCE OF THE MODIFIED FRICTION
FACTOR f0 UPON THE MODIFIED REYNOLDS NUHEER
Re' BY THE FORMULA OF CHILTON AND COIBURN,
1 - streamline flow; 2 - turbulent flow
0 0
0
?
i
0 Zhavoronkovts data
? experimental data
w
2S
Z
f
 Approved For Release 2002/01/11 : CIA-RDP80-00926AO01400040002-2
1-ABLE 1.HYDRAUISC RESISTANCE CF C TALYTIC TOMS WITHOUT THE CATALYST AND WITH IT
pp, pressure drop
Dimensions
In the empty
of the tube
column
M.
Rate of flow
of the air
q
H,qm
m~
'a
fa m+'
y
.i
o
py~U m
g,
1 15
0,1
1
2,28
0,068
1
streamline
14,03.10-4
0,054
53,2
2 15
0,1
1
33,5
1
1
turbulent
0,019
135,2
219,2
3 500
0,2
2,544
3,46
0,068
1
streamline
1,09.10-?
10,07
67,6
4 500
0,2
2,544
3,46
0,0004
180
6,07.10-0
0,07
67,6
(0,000378)
5 500
0,2
2,544
`0,9
1-
1
turbulent
0,013
7,93
492,8.
6 500
0,2
2,544
50,9
0,0055
180
streamline
0,004
0,01
985
7 500
0,2
2,544
18304
360
1
turbulent
1446,4
3,09.105
1,96.107
8 500
0,2
2,544
18304
2
180
>
j0,044
4,85.10'
3,07.107
47
,
0
Q
YP
DP/D tube in m.
FIG. 2. DEPENDENCE OF THE COEFFICIENT OF THE EFFECT
OF TIM WALLS a UPON THE RATIO OF THE AVERAGE DI-
AIIETER OF THE PARTICLES TO TIIE DIAMETER OF THE TUBE
Dp'Dtube BY THE FORIULA OF CHILTON AND COLBURN.
1 - for streamline flow; 2 - for turbulent flow
IS00
T
1
turbulent
flow
s
treamline
flow
2
-
J
o.
oNO ao75 QDTOD M
91
av. diameter of the particles, in.
FIG. 4. DEPENDENCE OF THE HYDRAULIC RESISTANCE IN
CATALYST BED .6 p UPON THE AVERAGE DIMMER OF THE
CATALYST GRAINS. For turbulent flow: 1 - according to
Chilton and Colburn; 2 - according to Zjjttaavoronkov.
For streamline flow: 3 - according to 'Lhavoronkov; 4 -
according to Chilton and Colburn.
0 !0 za 4a SD
av. diameter of the particle
FIG. 3. DEPENDENCE OF THE FREE VOLUIM OF TILE
CATALYST BED UPON THE AVERAGE DIAIlTER OF
THE PARTICLES.
2S
O
w
2
T?
-hrbulent flow
so
Ret, modified Reynolds number,
streamline flow
FIG. 1. DEPENDENCE OF THE MODIFIED FRICTION
FACTOR f0 UPON THE MODIFIED REYNOLDS IDE-lER
Re' BY THE FORMULA OF CHILTON AND COEBURN.
1 - streamline flow; 2 - turbulent flow
0 0
0
o Zhavoronkov's data
? experimental data
TABLE 2. INTERDEPENDENCE BETWEEN THE, FREE SPACE OF THE PACKING AND TOE AVERAGE
No.
1s
2*
3
Izv. (tekh.)
1946, .421 ff.
DIAMETER OF THE GRAIN
_
Dimensions of the
grains, mm,
Av. diam-
eter of
the grain
mm. 1
Free
space
5X5X8
6,0
0.35
-Alurdnosilicate
catalyst
Cylindrical
tablets
9X9X4
7,3
0,35
Catalyst for con-
Tablets
11X11 X6
9,3
0,38
version of CO
Vanadium catalyst
it
11 X 11 X6.5
9,5
0,43
Coke
Irregular
29,6 X 25,8 X 18
24,5
0;532
Glass granules
Pear-shaped
20 X 20 X 37,5
25,8
0,500
Coke
Irregular
35,6 X 28,8 X 18
27,5
0,535
47,6 X 41,5 X 33,4
40,8
0,545
Gravel
Spherical
56,8X40,8X29
42,2
570
0
Coke
Irregular
52 X 40,3 X 35
5
42,6
,
0
500
Andosite
n
,
56 X 43,7 X 32,6
44,1
,
0.565
* Catalyst tested in this work
Approved For Release 2002/01/11 : CIA-RDP80-00926AO01400040002-2
 ++'+
T
nLtGHUl
U I ubi
I
o
/ 1,~ ,,I P80-00
&p, pressure drop
Dimensions
In the empty
of the tube
Rate
f fl
coltmn
M.
o
ow
of the air
+,
1 15
0,1
1
2,28
0,068
1
streamline
4,03.10-6
0,054
53,2
15
0,1
1
33,5
1
1
turbulent
0,019
35,2
219,2
3 500
0,2
2,544
3,46
0,068
1
streamline
1,09.10-6
0,07
67,6
500
0,2
2,544
3,46
0,0004
180
>
6,07.10-8
0,07
67,6
(0,000378)
,
500
0,2
2,544
-0,9
1-
1
turbulent ;
0,013
7,93
492,8.
500
0,2
2,544
50,9
0,0055
180
streamline
0,004
0,01
985
500
0,2
2,544
18301
360
1
turbulent
446,4
3,09.105
1,96 10'
500
0,2
2,544
18304
2
180
0,044
4,85.10'
3,07
R75
0
0
ou
926
FIG. 2. DEPENDENCE OF THE COEFFICIENT OF THE EFFECT
OFF THE WALLS c UPON THE RATIO OF TILE AVERAGE DI-
AMETER OF THE PARTICLES TO THE DIA UBTER OF TILE TUBE
Dp/Dtube BY THE FORMULA OF CHILTON AND COLBURN.
1 - for streamline flow; 2 - for turbulent flow
'"`
2li00
WF''
IS00
2
!
turbulent
flow
I
-SW
streamline
'
flow
0 !0 20 ., _ NO SO
av, diameter of the particle
FIG. 3. DEPENDENCE or THE FREE VOIAIC; OF TILE
CATALYST BED UPON THE AVERAGE DlAIMT 'R OF
THE PARTICLES.
TABLE 2. INTERDEPENDENCE BE4JEEhI TID: FREE SPACE OF THE PACKING AND TI:E AVERAGE
DIAMETER OF THE RAIN
No.
A av. diameter of the particles, m.
FIG. 4. DEPENDENCE OF THE HYDRAULIC RESISTANCE IN
CATALYST BED G1 T) UPON THE AVERAGE DIAI4EIER OF THE
CATALYST GRAINS. For turbulent flow: 1 - according to
Chilton and Colburn; 2 - according to Z ~avoronkov,
For streamline flow: 3 - according to Zhavoronkov; 4 -
according to Chilton and Colburn.
Izv. (tekh.)
126, ,421 ff.
T
Type of packing Shape
Dimensions of the
grains, mm.
Av. diam-
eter of
the grain
mm.
Free
1 space
-Aluminosilicate
catalyst
Cylindrical
tablets
5X5X8
6,0
0,35
9X9X4
7
3
0
35
Catalyst for con-
version of CO
Tablets
11X11X6
,
9,3
,
0,38
Vanadium catalyst
Coke
Irregular
11 X 11 X6.5
9,5
0,43
29,6 X 25,8 X 18
24,5
0532
Glass granules
Coke
Pear-shaped
Irregular
20 X 20 X 37,5
25,8
0,500
ro
35,6 X 28,8 X 18
27,5
0
535
Gravel
Spherical
47,6 X 41,5 X 33,4
40,8
,
0,545
Coke
Irregular
56,8 X 40,8 X 29
42,2
0
570
Andesite
H
52 X 40,3 X 35,5
42,6
,
0500
56 X 43,7 X 32,6
44,1
0,565
Approved For Release 2002/019'+ '? tR?P89aOO&26AO01400040002-2
9 25
0
I
L
_
_
rbulent flow
fI /S
G TDO f w
600
streamline flow
FIG. 1. DEPENDENCE OF THE MODIFIED FRICTION
FACTOR fO UPON THE MODIFIED REYNOLDS WUIMER
Re' BY THE FORMULA OF CHILTOH MID COIBURN.
1 - streamline flow; 2 - turbulent flow
0
00
?
0
?
0 Zhavoronkov's data
? experimental data
Z
 TABLE 1 vRAUI.IC REST re d o t / 4Ajjr A9I jkPP P 8 0 -0 0 9 2 6
T n_ pressure r7ro
p
Dimensions
in the empty
of the tube
column
M.
Rate of flow
of th0 air
84N
U
RO
1 15
0,1
1
2,28
0,068
1
streamline
4,03.10-4
0,054
53,2
1 15
0,1
1
33,5
1
1
turbulent
0,019
35,2
219,2
3 500
0,2
2,544
3,46
0,068
1
streamline
I,09.10-5
0,07
67,6
4 500
0,2
2,544
3,46
0,0004
180
a
6,07.10-8
0,07
67,6
(0,000378)
5 500
0,,2
2,544
0,9
1-
1
turbulent
0,013
7,93
492,8.
3 500
0,2
2,544
50,9
0,0055
180
streamline
0,004
0,01
985
500
0,2
2,544
18304
360
1
turbulent 1
446,4
3,09.105
1,96.107
3 500
0,2
2,544
18304
2
180
a
0,044
4,85.10'
3,07.107
cuu
47
-.
Q
tube in m.
FIG. 2. DEPENDENCE OF THE COEFFICIENT OF THE EFFECT
OF THE WALLS c UPON THE RATIO OF THE AVERAGE DI-
l TER OF THE PARTICLES TO THE DIAMETER OF THE TUBE
Dp/Dtube BY THE FORMULA OF CHILTON AND COLBURN.
1 - for streamline flow; 2 - for turbulent flow
"O ZG
~3/ b'DD
}}per
b
q
2 ~
turbulent
flow
streamline
flow
av. diameter of the particles, m.
FIG. 4. DEPENDENCE OF THE HYDRAULIC RESISTANCE IN THE
CATALYST BED a p UPON THE AVERAGE DIAMETER OF THE
CATALYST GRAINS. For turbulent flow: 1 - according to
Chilton and Colburn; 2 - according to Zvoronkov.
For streamline flow: 3 - according to havoronkov; 4 -
according to Chilton and Colburn.
26--
H
.
iv
qi
@hrbulent flow
?1 15
G D00 ',?
w 600
'streamline flow
FIG, 1, DEPENDENCE OF THE MODIFIED FRICTION
FACTOR f0 UPON THE MODIFIED REYNOLDS NUMUER
Re' BY THE FORMULA OF CHILTON AND COIBURN,
1 - streamline flow; 2 - turbulent flow
0 0
00
0
c
?
z
_
o Zhavoronkov's data
? experimental data
0 10 20 NO SO
av. diameter of the particle
FIG. 3. DEPENDENCE OF THE FREE VOIUIC OF THE
CATALYST BED UPON THE AVERAGE DIARET R OF
THE PARTICLES.
TABLE 2, INTERD'PENDEPJCE BETIIEEN TII FREE SPACE OF THE PACKING AND THE AVERAGE
DIAMETER OF TILE GRAIN
Izv, (tekh.)
22,.421 ff,
Type of packing Sha
pe
-Alwninosilicate
catalyst
Catalyst for con-
version of CO
Vanadium catalyst
Coke
Glass granules
Coke
Gravel
Coke
Andosite
Cylindrical
tablets
Tablets
n
Irregular
Pear-shaped
Irregular
Spherical
Irregular
Av, diam-
Dimensions of the
eter of
the grain
Free
grains, mm,
mm. I
space
5X5X8
6,0
0,35
9X9X4
7,3
0.35
IIX11X6
9,3
0,38
11 X 11 X6.5
9,5
0,43
29,6 X 25,8 X 18
24,5
0;532
20 X 20 X 37,5
25,11
0,500
35,6 X 28,8 X 18
27,5
0
535
47,6 X 41,5 X 33,4
40,8
,
0,545
56,8 X 40,8 X 29
42,2
0
570
52 X 40,3 X 35,5
42,6
,
0
5ti0
56 X 43,7 X 32,6
44,1
,
0,565
Approved For Release 2002/01F4t':yClAuRDP8a 00026A001400040002-2
 d
o
E
1 15
2 15
3 500
4 500
500
500
500
500
0,1
0,1
0,2
0,2
0,2
0,2
0,2
0,2
2,544
2,544
2,544
2,544
2,544
2,544
2,28
33,5
3,46
3,46
`0,9
50,9
18304
18304
0,068
1
0,068
0,0004
(0,000378)
dL r Ralew*oPpg I J11t :AQIA QP80-00926
180
180
turbulent
streamline
turbulent
streamline
turbulent
pp, pressure drop
In the empty
coltmm
4,03.10-10,054
0,019
1,09.10-5
6,07.10-e
0,013
0,004
446,4
0,044
D 4w
40 - #.x 0,15' QTP
Dp/Dtube in m.
FIG. 2. DEPENDENCE OF THE COEFFICIENT OF THE EFFECT
OF THE WALLS c UPON THE RATIO OF THE AVERAGE DI-
AMETER OF THE PARTICLES TO THE DIAMETER OF THE TUBE
Dp/Dtube BY THE FORMULA OF CHILTON AND COLBURN.
1 - for streamline flow; 2 - for turbulent flow
35,2
0,07
0,07
7,93
0,01
3,09
4,85.101
0 !0 20 0 J.,
av, diameter of the particle
FIG. 3. DEPENDENCE OF THE FREE VOLUIt;' OF THE
CATALYST BED UPON THE AVERAGE DIMMER or
THE PARTICLES.
TABLE 2. INTERDEPEI