Volume 05 Issue 01-2025
6
International Journal of Advance Scientific Research
(ISSN
–
2750-1396)
VOLUME
05
ISSUE
01
Pages:
6-13
OCLC
–
1368736135
A
BSTRACT
The article investigates the mass transfer process that occurs as a result of liquid droplets moving in a gas
flow. Additionally, the absorption of hydrogen fluoride from dusty gas into soda ash droplets was
examined. The study experimentally analyzed the influence of gas velocity and liquid flow on the mass
transfer coefficient and the purification efficiency of a rotary-filter gas cleaner, considering different types
of filters and liquid injection nozzles. To ensure the process is carried out effectively, optimal values for the
variable parameters, specifically liquid flow and gas velocity, were recommended.
K
EYWORDS
Population growth, food demand, mineral fertilizers, exhaust gases, environmental degradation, hydrogen
fluoride, gas purification, superphosphate production, rotor-filter apparatus, mass transfer process.
I
NTRODUCTION
As the global population continues to grow, the
demand for food, particularly agricultural
products, is increasing. Mineral fertilizers are
widely used to support agricultural production.
However, the processes and equipment used in
the production of these fertilizers are often
outdated and in need of modernization, leading to
the release of various exhaust gases into the
Journal
Website:
http://sciencebring.co
m/index.php/ijasr
Copyright:
Original
content from this work
may be used under the
terms of the creative
commons
attributes
4.0 licence.
Research Article
STUDY MASS TRANSFER PROCESS IN CAPTURING OF
HYDROGEN FLUORIDE GASES
Submission Date:
October 08,
2024,
Accepted Date:
December 20, 2024,
Published Date:
January 10, 2025
Crossref doi:
https://doi.org/10.37547/ijasr-05-01-02
Akmaljon Akhrorov
Associate professor (PhD), Fergana polytechnic institute, Fergana, Uzbekistan
Volume 05 Issue 01-2025
7
International Journal of Advance Scientific Research
(ISSN
–
2750-1396)
VOLUME
05
ISSUE
01
Pages:
6-13
OCLC
–
1368736135
atmosphere. These emissions contribute to
environmental degradation, including ozone
layer depletion and global warming. Therefore,
addressing the issue of exhaust gas purification
through the development of waste-free
technologies and the modernization of existing
machinery and equipment is a pressing concern.
The production of mineral fertilizers generates
various dusty gases, such as nitrogen,
phosphorus, and fluorine compounds. In
particular, hydrogen fluoride gas, emitted during
the production of dusty superphosphate, poses a
significant
environmental
threat.
This
necessitates the development of effective
methods and devices for gas purification. For
instance, Fergana Azot JSC operates a facility for
the production of superphosphate mineral
fertilizers, where hydrogen fluoride gas is
released into the atmosphere. The primary aim of
this study is to capture this gas, reintegrate it into
the technological process, and utilize it as a raw
material for other industrial applications.
M
ETHOD
This study investigates the mass transfer process
resulting from the interaction between liquid
droplets and gas within a device, aiming to
identify the optimal gas velocity and fluid
consumption for purifying secondary hydrogen
fluoride gas produced during superphosphate
fertilizer manufacturing. The effects of gas
velocity and fluid consumption on the mass
transfer coefficient were analyzed. Additionally,
the study experimentally examined the impact of
varying nozzle diameters, which influence the
perforation of the filter material and the spraying
of the absorption liquid onto the working surface.
The mass transfer process in the gas phase within
a rotor-filter apparatus exhibits complex
hydrodynamic and mass transfer characteristics,
making it challenging to comprehensively
describe the process and develop an accurate
mathematical model. To address this, mass
transfer processes in devices with similar
hydrodynamics and phase contact surfaces were
studied. Based on these findings, computational
equations for the gas-phase mass transfer process
in the experimental apparatus were proposed.
The effect of the consumption of absorption liquid
and gas streams on the process of substance
transfer in the experimental device is significant.
The following equations (1) and (2) are used to
calculate these factors influencing the process [1].
Liquid flow through injection nozzles is
determined by the next equation, m
3
/h;
2
3600
LIQ
Q
R
=
(1)
where, R- the diameter of the fluid nozzle hole ,
mm;
ω
-liquid velocity, m/s.
The sheber was installed in the gas inlet tube in
order to obtain different values of gas velocity.
According to the different gas velocities, flow of
gas is determined through the formula, m
3
/h;
2
3600
2000
G
D
Q
=
(2)
Volume 05 Issue 01-2025
8
International Journal of Advance Scientific Research
(ISSN
–
2750-1396)
VOLUME
05
ISSUE
01
Pages:
6-13
OCLC
–
1368736135
where,
D
–
tube diemeter for Pito-Prandtl, m.
As a result of the movement of the droplets
formed in the rotor-filter apparatus in the gas
phase, a mass transfer is observed, the hydrogen
fluoride component in the gas mixture is
absorbed into the liquid droplet. To calculate this
mass transfer process, it is important to
determine the diameter of the drop surface and
the volume that varies during the process. When
the nozzle diameter varied, the volume of the
liquid droplet and the average diameter at which
the surface was retained were determined
according to the following equation, μm [2,3];
3
32
2
Х
С
d
d
d
=
(3)
бунда
, d
х–
the diameter of the droplet forming
the main part of the fraction
i
, m;
d
с–
is the surface diameter of the drop, m;
The velocity of the gas passing through the hole
in the drum-coated filter material is determined
according to the following equation, m / s [4];
аpp
hol
hol
w
w
F
=
(4)
where
, w
app
–
gas velocity in experimental
apparatus, m/s;
Σ
F
hol
–
surface of filter’s holes,
m
2
;
The mode of motion of the gas passing through
the filter holes is determined by the following
equation;
Re
hol
D
G
G
w
d
=
(5)
where, w
hol
–
velocity of gas passing through the
hole, m/s;
ν
G
- kinematic viscosity coefficient of
the gas, m
2
/s; d
D
–
drop diameter,
μ
m.
The dependence of the rate of component
transition in the gas phase on the
physicochemical properties of the phases and the
process parameters is expressed in the form of
criterion equations. The criteria equation
proposed by Fresling was chosen to calculate the
process of mass transfer in the gas phase in a
rotor-filter apparatus. This equation was
confirmed on the basis of tests conducted on the
mass transfer between a liquid drop and a gas [2].
0,5
0,33
2 0,552 Re
Pr
G
G
G
Nu
= +
(6)
where,
Re
G
–
fluid motion regime of passed gas
through the filter;
Pr
–
quantity of Prandtl for gas phase.
Mass transfer coefficient in absorption of
hydrogen fluoride component into the liquid
drops is calculated by the following equation,
m/s [5,7];
G
G
G
D
Nu
D
d
=
(7)
where,
Nu
G
–
Nusslet’s quantity for gas phase
;
D
G
–
diffusion coefficient in absorption of hydrogen
fluoride component into the fluid drops, m
2
/s.
Volume 05 Issue 01-2025
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International Journal of Advance Scientific Research
(ISSN
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2750-1396)
VOLUME
05
ISSUE
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Pages:
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OCLC
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1368736135
In the mass transfer process is occurred between
hydrogen fluoride component of gas mixture and
fluid drops, the transport number and
purification efficiency of apparatus are
calculated by the following formula, [4,5,6,7];
1
ln
1
G
K
G
F
n
G
=
=
−
(8)
F
К
–
contacting surface of phases, m
2
;
G
G
–
gas
flow, m
3
/h
; η–
purification efficiency, %.
R
ESULTS
The experiment in order to determine the mass
transfer coefficient was carried out following two
stages, firstly measuring gas and fluid flows,
secondly impact of that flows to the mass transfer
and cleaning efficiency of apparatus.
In the first stage of experiment, in order to
measure the gas velocity ВА06
-TROTEC
measurement with the 1,1-30 m/s working range
and 0,3% inaccuracy was used. Different gas
velocities were obtained having installed the
sheber into the gas input tube. Sheber forms the
0
0
, 30
0
, 45
0
, 60
0
, 90
0
angels in the input tube after
fan [1].
The gas flow rate to the apparatus was increased
by 5m/s and the speed change interval was set at
5 ÷ 30m/s.
Absorption liquid was selected according to the
GOST-3846-10 and supplied through the nozzle
with diameters
d
ш
=1mm;
d
ш
=2mm;
d
ш
=3mm;
Also, according to GOST-13045-81, the flow rate
of the absorption fluid passing through the
rotometer RS-5 with a scale of 0-100 was
measured for each nozzle in a volumetric
manner for the beaker. According to him, when
the diameter of the nozzle hole
d
ш
= 1mm, a
change in fluid flow according to rotameter
readings in the range
Q
сую
=0,068÷0,160 m
3
/h
was observed. According to the rotameter, when
the diameter of the nozzle hole
d
ш
=2mm, the
liquid flow rate in the range
Q
сую
=0,071÷0,168
m
3
/h and when the diameter
d
ш
=3mm, the fluid
flow rate
Q
сую
=0,072÷0,178 m
3
/h [2].
In the second stage of the experiment, it was
analyzed that the liquid droplets formed as a
result of disintegration of the liquid film and
secondary decomposition of the liquid falling into
the drum through the filter holes of the hydrogen-
fluoride component gas move in the gas flow and
occur. At this stage of the experiment, the rate of
hydrogen-fluoride component gas mixture with
the diameter of the hole of the filter material
d
Ф
=2;3;4mm and the consumption of the
absorbing liquid Na2CO3 sprayed into the
apparatus through the nozzle
d
ш
=1;2;3mm were
studied. The results obtained are illustrated in the
form of diagrams given in Figures 1; 2; 3 below
[3,4,5,6-17].
Volume 05 Issue 01-2025
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International Journal of Advance Scientific Research
(ISSN
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VOLUME
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d
Sh
=1 mm and Q
liq
=0,068÷0,160 m
3
/h;
Figure 1. Changing of the mass transfer coefficient depends on the gas velocity,
d
F
=2 mm-
const.
2
0, 0001
0, 013
0,1116 ²
0, 9919
y
x
x
R
= −
+
+
=
(9)
2
0, 0001
0, 0143
0,1571 ²
0, 9757
y
x
x
R
= −
+
+
=
(10)
2
0, 0002
0, 0197
0, 2404 ²
0, 9423
y
x
x
R
= −
+
+
=
(11)
2
0, 0002
0, 025
0, 261 ²
0, 9779
y
x
x
R
= −
+
+
=
(12)
2
0, 0005
0, 0373
0, 2339 ²
0, 9963
y
x
x
R
= −
+
+
=
(13)
d
Sh
=2 mm and Q
liq
=0,071÷0,168 m
3
/h;
Figure 2. Changing of the mass transfer coefficient depends on the gas velocity,
d
F
=2 mm-const.
0.1
0.3
0.5
0.7
0.9
1.1
5
10
15
20
25
30
Mas
s
transf
er
coe
ff
ic
ie
nt,
β
Г
,
m
ol
/m
2
*
s
Gas velocity, υ
г
m/s
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2
0, 0002
0, 0157
0,1127 ²
0, 9813
y
x
x
R
= −
+
+
=
(14)
2
0, 0003
0, 02
0,1315 ²
0, 9753
y
x
x
R
= −
+
+
=
(15)
2
0, 0004
0, 0298
0, 2033 ²
0, 9827
y
x
x
R
= −
+
+
=
(16)
2
0, 0004
0, 0324
0, 2447 ²
0, 9542
y
x
x
R
= −
+
+
=
(17)
2
0, 0005
0, 0365
0, 2828 ²
0, 9357
y
x
x
R
= −
+
+
=
(18)
d
sh
=3 mm and Q
liq
=0,072÷0,178 m
3
/h;
Figure 3. Changing of the mass transfer coefficient depends on the gas velocity,
d
F
=2 mm-
const.
2
0, 0002
0, 016
0,1134 ²
0, 9859
y
x
x
R
= −
+
+
=
(19)
2
0, 0003
0, 0208
0,1338 ²
0, 9812
y
x
x
R
= −
+
+
=
(20)
2
0, 0004
0, 0289
0, 2245 ²
0, 9781
y
x
x
R
= −
+
+
=
(21)
2
0, 0004
0, 0313
0, 2627 ²
0, 9711
y
x
x
R
= −
+
+
=
(22)
2
0, 0003
0, 0347
0, 3168 ²
0, 9966
y
x
x
R
= −
+
+
=
(23)
Figures 1; 2; 3 show that the diameter of the hole
of the filter paronite material is
d
F
= 2mm, the
diameter of the nozzle hole is
d
ш
= 1mm and the
value of the mass transfer coefficient
β
G
= 0.170 ÷
0.399mol/m
2
·s change in interval was observed.
It was also observed that when the maximum
velocity of the purified gas flow is 30 m/s, the
value of the mass transfer coefficient is in the
range
β
G
= 0.382 ÷ 0.927 mol/m
2
·s. When the
diameter of the nozzle hole is
d
Sh
=2мм
and the
minimum velocity of the purified gas flow is
Volume 05 Issue 01-2025
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International Journal of Advance Scientific Research
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5m/sec, the value of the substance transfer
coefficient
β
G
= 0.184 ÷ 0.443mol/m
2
·s is
observed to change.
It was also observed that
when the maximum velocity of the purified gas
flow is 30 m/s, the value of the substance
transfer coefficient increases to
β
G
= 0.395 ÷
0.995mol/m
2
·s. When the diameter of the nozzle
hole
d
ш
= 3mm and the minimum velocity of the
purified gas flow was 5m/s, the value of the
substance transfer coefficient
β
G
= 0.184 ÷
0.471mol/m
2
·s was observed to change. When
the maximum velocity of the purified gas flow
was 30 m / s, the value of the substance transfer
coefficient increased to
β
G
= 0.402 ÷ 1.09mol/m
2
·s
[7,8,9,10,11,12,13,14,15,16,17].
C
ONCLUSION
In conclusion, As a result of theoretical analysis
and values obtained in experiments, the following
conclusions were given:
-given above 1; 2; and 3 figures show that, in
nozzle diameter dSh=3 мм and gas velocity υG
=30m/s, also filtering material hole diameter is
dF=2mm the value of mass transfer coefficient is
achieved βG =1,09mol/m2·s. It was also found
that the minimum value of the mass transfer
coefficient is βG = 0.143mol/m2·s when the
diameter of the filter material (paronite) hole is
dF = 4mm and the diameter of the nozzle hole is
dSh = 1mm and the velocity of the purified gas
flow is υG = 5m/s. It can be seen that an increase
in the velocity of the gas leads to an increase in the
mass transfer coefficient;
R
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