Epoxidation of Ethylene with Products of Thermal Gas-Phase Oxidation of n-Butane

Article abstract of DOI:10.1134/S096554412002005X

Abstract: Epoxidation of ethylene with the reactive products formed during thermal gas-phase oxidation of n-butane has been carried out under flow conditions with the separation of the zones of generation of radicals and their interaction with ethylene. Butane is oxidized in the first section of a two-section reactor, and ethylene is fed to the second section. It has been found that increasing the residence time of a butane–oxygen mixture in the first section of the reactor from 7 to 13 s increases the ethylene oxide accumulation rate. A further increase in the contact time leads to a decrease in the rate. Similarly, increasing the C₄H₁₀/O₂ ratio in the range of 0.05–0.25 leads to an increase in the rate of accumulation of ethylene oxide. A further increase in this ratio decreases the rate of epoxidation. It has also been found that the temperature dependences of the ethylene oxide accumulation rate in both sections of the reactor pass through a maximum. The obtained data give evidence for the occurrence of the ethylene epoxidation reaction initiated by the n-butane oxidation products under the conditions when ethylene itself is slightly oxidized.

Full text of DOI:10.1134/S096554412002005X

ISSN 0965-5441, Petroleum Chemistry, 2020, Vol. 60, No. 2, pp. 187–193. © Pleiades Publishing, Ltd., 2020.
Russian Text © The Author(s), 2020, published in Neftekhimiya, 2020, Vol. 60, No. 2, pp. 206–213.
Epoxidation of Ethylene with Products of Thermal Gas-Phase
Oxidation of n-Butane
R. R. Grigoryana and S. D. Arsenteva, *
aNalbandyan Institute of Chemical Physics, National Academy of Sciences of the Republic of Armenia, Yerevan, 0014 Armenia
*e-mail: arsentiev53@mail.ru
Received July 31, 2019; revised September 29, 2019; accepted October 14, 2019
Abstract—Epoxidation of ethylene with the reactive products formed during thermal gas-phase oxidation of
n-butane has been carried out under flow conditions with the separation of the zones of generation of radicals
and their interaction with ethylene. Butane is oxidized in the first section of a two-section reactor, and eth-
ylene is fed to the second section. It has been found that increasing the residence time of a butane–oxygen
mixture in the first section of the reactor from 7 to 13 s increases the ethylene oxide accumulation rate. A fur-
ther increase in the contact time leads to a decrease in the rate. Similarly, increasing the C4H10/O2 ratio in
the range of 0.05–0.25 leads to an increase in the rate of accumulation of ethylene oxide. A further increase
in this ratio decreases the rate of epoxidation. It has also been found that the temperature dependences of the
ethylene oxide accumulation rate in both sections of the reactor pass through a maximum. The obtained data
give evidence for the occurrence of the ethylene epoxidation reaction initiated by the n-butane oxidation
products under the conditions when ethylene itself is slightly oxidized.
Keywords: ethylene, epoxidation, ethylene oxide, butane
DOI: 10.1134/S096554412002005X
Olefin oxides are base petrochemical products with method is more efficient. However, the production of
the rapidly growing volume of consumption [1–3]. ethylene oxide using this process requires the use of
This is explained by the continuous growth in the chlorine and chlorine-resistant reactor materials and
industrial production of their derivatives [4, 5]. For is accompanied by the formation of a significant
example, ethylene glycol, which is the main derivative amount of chlorine-containing wastes polluting the
of ethylene oxide, is used as a reactant in the produc- environment.
tion of polyethylene terephthalate, a solvent and a
Catalytic oxidation of ethylene is much more envi-
plasticizer, as well as in the production of antifreezes
ronmentally friendly [14–17]. Currently, almost all
and monomers for the fabrication of synthetic fibers
ethylene oxide is catalytically obtained on industrial
[6]. Another derivative, diethylene glycol, is the feed-
scale. The most effective catalysts for the oxidation of
stock in the production of polyester resins and foamed
ethylene to its oxide are silver and its compounds [1, 5,
plastics, and dinitroethylene glycol is used as an alter-
18–20], which make it possible to obtain the target
native to nitroglycerin in the production of nonfreez-
product with the selectivity exceeding 70% [13, 19,
ing, impact-resistant dynamite. Nonionic surfactants
21]. At the same time, the use of silver in catalytic pro-
obtained on the basis of ethylene oxide are very effec-
cesses is fraught with a number of complex problems.
tively used in oil producing and refining industry [7–
The catalyst fabrication technologies are complex and
9]. Liquid and waxy polymers used as plasticizers and
multistage. In the course of operation, catalysts lose
lubricants are obtained via the polymerization of eth-
the activity as a result of aging and poisoning [22] and
ylene oxide. Ethylene oxide itself, as well as com-
need to be periodically regenerated. The complicating
pounds on its basis, can be used as a fuel [10] and an
factors are special requirements to the purity of the
agent for sterilization of medical devices [11].
hydrocarbon feedstock. Sulfur compounds that are
In general, industrial-scale production of ethylene
natural concomitants of natural hydrocarbon feed-
oxide can be based on the following three processes:
stock, arsenic, and acetylene pose the greatest danger
catalytic oxidation of ethylene, noncatalytic oxidation
for silver catalysts. The presence of other hydrocar-
of ethylene, and preparation from ethylene chlorohy-
bons, hydrogen, and carbon oxides is also undesirable.
drin [12]. To date, only two processes, namely, the
oxidation of ethylene over silver catalysts and the alkali
Noncatalytic processes for producing ethylene
treatment on ethylene chlorohydrin, have found oxide are free from the above disadvantages. As
industrial application [13]. Of these, the chlorohydrin opposed to the catalytic processes, a number of valu-
187

188
GRIGORYAN, ARSENTEV
1
7
4
5
6
3
2
Fig. 1. Scheme of the reactor: (1) connector for feeding the butane–oxygen mixture, (2) first section of the reactor, (3) feeding
capillary for ethylene, (4) package of quartz tubes, (5) oven of the first section of the reactor, (6) oven of the second section of the
reactor, (7) sampling connector.
able products, such as ethylene oxide, formaldehyde, paraffin hydrocarbon from the epoxidation zone.
and organic acids, are formed in the case of homoge- The choice of the hydrocarbon that generates perox-
neous oxidation of ethylene with oxygen. Currently, ide radicals has been determined by the fact that
ethylene oxide synthesis methods via homogeneous alkyl peroxide radicals generated by the oxidation of
oxidation of ethylene in the gas phase are being devel- butane in a two-section reactor accumulate in the sec-
ond section at concentrations exceeding 10−9 mol/cm3
[33, 34].
oped [23, 24] because this process requires neither an
expensive catalyst nor chlorine. In addition, this eth-
ylene oxide production process does not require the
gases with purity as high as in the case of the catalytic
process. The disadvantage of the process is a wide vari-
ety of its products and low selectivity, which is
explained by the chain mechanism of occurring trans-
formations and high temperature. However, the devel-
opment of the theory of chain processes opens new
ways for improving gas-phase oxidation reactions of
ethylene.
In previous studies [25–29], it was shown that the
epoxidation of ethylene and propylene during their
thermal gas-phase oxidation involves the interaction
of peroxide radicals with the double bond of the olefin
according to the reaction
The aim of this work is to study the process of eth-
ylene epoxidation with reactive compounds generated
in the thermal gas-phase oxidation of butane in the
case of co-oxidation of ethylene and n-butane with the
separation of the zones of generation of radicals and
their interaction with ethylene.
EXPERIMENTAL
The scheme of the reaction unit for running the
ethylene coepoxidation process is presented in Fig. 1.
A two-section reactor was used which was a quartz
tube of a 20 cm length and a 2 cm diameter. The reac-
tor was divided into separate sections using a partition
consisting of a package of quartz tubes. The reactor
was heated with two independent electrical ovens,
which made it possible to set different temperatures in
the reactor sections. A mixture of n-butane with oxy-
gen was fed through a seal connector to the first sec-
tion of the reactor, where the oxidation of butane with
the formation of an active medium occurred. Ethylene
was fed to the second section of the reactor through a
capillary.
•R O + C H (C H ) →•R O + C H O C H O
(
)
2
2
4
3
6
2
4
3
6
and the rate constants of these reactions were mea-
sured. The analysis performed in [30] shows that in the
case of thermal gas-phase oxidation of ethylene, this
reaction plays the key role and other routes of epoxi-
dation including peroxide epoxidation (which plays
the key role in the case of liquid-phase epoxidation of
olefins) do not make a substantial contribution to this
process. It has also been found that in the process con-
ducted in a two-section reactor, the peroxide radicals
generated in the reaction of gas-phase thermal oxida-
tion of methane can effectively epoxidize ethylene
[31].
The separation and determination of the concen-
trations of the gaseous products was performed on an
LKhM-8MD chromatograph. Methanol, ethanol,
acetaldehyde, and ethylene oxide were separated on a
column packed with the polymer sorbent Polisorb-1
(l = 3 m, d = 3 mm, Tcol = 378 K, Q = 30 cm3/min, and
helium as the carrier gas). C1–C4 hydrocarbons were
separated on a column packed with Silipor-600 (l = 3 m,
d = 3 mm, Tcol = 363 K, Q = 24 cm3/min, and helium
as the carrier gas). Hydrogen, oxygen, methane, and
CO were separated on a column packed with molecu-
lar sieves 5 Å (l = 2 m, d = 3 m, Tcol = 363 K, Q =
Earlier, epoxidation of ethylene was also studied
using co-oxidation of ethylene and butane. It was
shown that in this case, the epoxidation of ethylene
proceeds at low temperatures, at which ethylene itself
is not oxidized [33]. At the same time, the introduc-
tion of ethylene into the reaction mixture from the
very beginning of the process leads to its untenable
consumption for undesired products. Because of this,
it was decided to separate the zone of generation of 24 cm3/min, and argon as the carrier gas). In all the
reactive particles formed during the oxidation of the cases, a thermal conductivity detector was used.
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EPOXIDATION OF ETHYLENE WITH PRODUCTS
189
Table 1. Concentrations of the main products obtained for different contact times in the first and second sections of the
reactor. T1 = 673 K, T2 = 613 K, n-C4H10 : O2 = 0.117, and P = 86.7 kPa
Partial pressure of the reaction products, kPa
Q1, cm3/s
Q2, cm3/s
No.
CH3OH
CH3CHO
C2H4O
HCHO
CO
1
2
3
4
5
6
7
8
9
0.51
0.63
0.76
0.83
1.03
1.28
1.34
1.45
1.52
1.59
1.92
0.92
1.14
1.37
1.49
1.85
2.30
2.41
2.61
2.73
2.86
3.45
0.459
0.441
0.433
0.412
0.354
0.305
0.281
0.134
0.106
0.096
0.083
0.526
0.542
0.561
0.583
0.592
0.588
0.467
0.372
0.296
0.254
0.186
1.396
1.449
1.437
1.354
1.318
1.211
1.234
1.103
0.982
0.723
0.292
0.502
0.509
0.521
0.532
0.532
0.518
0.474
0.368
0.271
0.218
0.153
2.14
2.13
2.12
2.03
1.95
1.63
1.23
0.91
0.45
0.23
0.09
10
11
The flow rates of feeding the mixture to the first and second sections of the reactor (Q and Q ) were selected in such a way that the con-
1
2
centration of ethylene was the same in all the experiments.
The concentration of formaldehyde was measured
Since the concentration of ethylene oxide at the
using chromotropic acid on a KFK-2 photoelectric outlet from the reactor is determined by the difference
colorimeter. For formaldehyde determination, the between its formation and consumption and depends
effluent reaction gases were bubbled through distilled on the concentration gradients of the epoxidizing
water for a certain time. To increase the contact sur- active particles, we can speak with confidence only
face of the gases with the solvent, the bubbler was filled about the experimentally measured average rate of
with fine glass cullet. The concentration of formalde- ethylene oxide accumulation in the second section of
hyde in the reactor was calculated by the formula C = the reactor. This quantity was calculated from the data
CbVTamb/QtbTr, where C is the concentration in the of Table 1 according to the formula
reactor, mol/cm3; Cb is the concentration in the solu-
WC H O = РC H O t2 ,
tion from the bubbler, mol/cm3; V is the volume of
water in the bubbler, cm3; Q is the volumetric flow rate
of the reactants fed to the reactor, cm3/s; tb is the dura-
tion of bubbling, s; and Tamb and Tr are the ambient
and reactor temperatures, respectively.
2
4
2
4
where
tion rate, kPa/s;
is the average ethylene oxide accumula-
W
C2H4O
is the partial pressure of eth-
Р
C2H4O
ylene oxide at the reactor outlet, kPa; and t2 is the res-
idence time of the reaction mixture in the second sec-
tion of the reactor, s. Figure 2 presents the dependence
of the average rate of ethylene oxide accumulation on
the residence time of the butane–oxygen mixture in
the first section of the reactor.
As is seen from Fig. 2, the average rate of accumu-
lation of ethylene oxide is maximum at the residence
time of ~13 s for the butane–oxygen mixture in the
first section of the reactor. In the case of a decrease or
increase in the contact time, the rate of accumulation
of ethylene oxide sharply decreases. Obviously, its
decrease is due to the fact that the oxidation of butane
is a degenerate branched process, as a result of which
the rate of the process and concentrations of active
species depend on the contact time. Since the rate of
accumulation of ethylene oxide is associated with the
concentration of active particles that come from the
If needed, the concentration of formaldehyde was
recalculated to the partial pressure according to the
formula P = PstCNATr/TstNL, where P is the partial
pressure, kPa; Tst is the standard temperature, 298 K;
Pst is the standard pressure, 101.308 kPa; NA is the
Avogadro number; and NL is the Loschmidt number.
RESULTS AND DISCUSSION
The experiments showed that the main products of
the process were carbon monoxide, ethylene oxide,
acetaldehyde, methanol, and formaldehyde. Ethanol,
methane, and carbon dioxide were also detected, but
they were in insignificant amounts.
Table 1 presents the concentrations of the main first section and the concentration of ethylene was
products measured at different flow rates of feeding of maintained the same in all the experiments (see
the butane–oxygen mixture to the first section of the Table 1), the nonmonotonic dependence of the rate of
reactor.
the process and concentration of the active particles
PETROLEUM CHEMISTRY Vol. 60 No. 2 2020

190
WC H O, kPa/s
GRIGORYAN, ARSENTEV
When the flow rate of the butane–oxygen mixture
2
4
fed to the first section of the reactor was Q1
=
0.35
0.30
0.25
0.20
0.15
0.10
0.05
0
1.92 cm3/s (Table 1, no. 11), the selectivity of conver-
sion of ethylene to ethylene oxide was ~96%. The
selectivity was calculated by the formula
S = C H O Δ C H ,
[
]
[
]
2
4
2
4
where S is the selectivity, [C2H4O] is the concentration
of ethylene oxide at the outlet of the reactor, and
Δ[C2H4] is the consumption of ethylene.
According to published data [27], the maximum
selectivity for ethylene oxide in the case of ethylene
oxidation under standard conditions cannot exceed
67%. Such a limit of selectivity is associated with the
fact that some ethylene is consumed for the formation
of peroxide radicals. Under the conditions of our
experiments in the two-section reactor, the generation
of the active particles occurs in the process of oxida-
tion of butane in the first section, while ethylene in the
second section is mainly consumed in the epoxidation
reaction. As a result, the selectivity of conversion of
ethylene to its oxide increases.
10
15
20
25
30
5
τ1, s
Fig. 2. Dependence of the average rate of accumulation of
ethylene oxide on the contact time in the first section of
the reactor. T = 673 K, T = 613 K, C H : O = 0.117,
1
2
4
10
2
and P = 86.7 kPa. The dashed line presents the results
obtained using argon instead of butane.
Obviously, the rate of oxidation of hydrocarbons
and concentrations of radicals during the process
depend on the composition of the reaction mixture. In
this connection, the influence of the composition of
the mixture in the first section of the reactor on the
epoxidation process was investigated. Table 2 presents
the concentrations of the main products obtained
upon varying the butane/oxygen ratio in the mixture
fed to the first section of the reactor.
arriving from the first section of the reactor on the
contact time leads to the appearance of a maximum in
the plot of
versus the residence time of the
W
C2H4O
butane–oxygen mixture (/1) in the first section.
For comparison, the dashed line in this same figure
presents a similar dependence obtained under the
same process conditions but with the replacement of
butane by argon in the mixture fed to the first section
of the reactor. The experiments showed that the rate of
accumulation of ethylene oxide is significantly lower
The data of Table 2 were used to plot in Fig. 3 the
dependence of the average rate of accumulation of
ethylene oxide on the butane/oxygen ratio in the mix-
ture fed to the first section of the reactor.
in this case. For example,
decreases more than
WC H O
2
30-fold for τ1 ~ 12–14 s. This r4esult suggests that eth-
ylene is very slowly oxidized under these conditions
and the presence of butane sharply increases the gen-
eration of particles that epoxidize the olefin.
As is seen from Fig. 3, increasing the n-C4H10/O2
ratio in the range from 0.05 to 0.25 leads to a 1.8-fold
increase in the average rate of accumulation of eth-
Table 2. Concentrations of the main products obtained for various compositions of the butane–oxygen mixture fed to the
first section of the reactor. T1 = 673 K, T2 = 613 K, Q1 = 1.30 cm3/s, Q2 = 2.30 cm3/s, and P = 86.7 kPa
Partial pressure of reaction products, kPa
C4H10 : O2
No.
CH3OH
CH3CHO
C2H4O
HCHO
CO
1
2
3
4
5
6
7
8
9
0.05
0.07
0.13
0.21
0.25
0.35
0.50
0.79
0.85
0.475
0.509
0.563
0.562
0.527
0.512
0.504
0.499
0.483
0.227
0.365
0.485
0.531
0.493
0.434
0.421
0.393
0.348
1.055
1.907
1.722
1.818
1.901
1.556
1.436
0.870
0.888
0.231
0.284
0.424
0.448
0.465
0.432
0.396
0.372
0.353
2.10
1.95
1.82
1.79
1.78
1.81
1.81
1.79
1.77
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EPOXIDATION OF ETHYLENE WITH PRODUCTS
191
WC H O, kPa/s
WC H O, kPa/s
2
4
2
4
0.35
0.40
0.35
0.30
0.25
0.20
0.15
0.10
0.05
0.30
0.25
0.20
0.15
0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1.0
0.1
0
620
640
660
680
700
720
T, K
600
n-C4H10/O2
Fig. 4. Dependence of the average rate of accumulation of
Fig. 3. Dependence of the average rate of accumulation of
ethylene oxide on the temperature in the first section of the
ethylene oxide on the butane/oxygen ratio in the first sec-
3
tion of the reactor. T = 673 K, T = 683 K, Q =
1
reactor. C H : O = 0.21, T = 683 K, Q = 1.30 cm /s,
Q = 2.30 cm /s, and P = 86.7 kPa.
1
2
4
10
3
2
2
1
3
3
1.30 cm /s, Q = 2.30 cm /s, and P = 86.7 kPa.
2
2
ylene oxide. A further increase in this ratio leads to a
more than twofold decrease in
ferent temperatures in the first section of the reactor
are presented in Table 3.
.
W
C2H4O
Figure 4 shows the dependence of the average rate
of accumulation of ethylene oxide on the temperature
in the first section of the reactor. The rate of accumu-
lation was calculated based on the data of Table 3.
It is known that the intensity of oxidation of hydro-
carbons depends on the hydrocarbon/oxygen ratio
and passes through a maximum [35, 36]. Obliviously,
the dependence of the concentration of the active
intermediate products promoting the epoxidation of
ethylene on the n-C4H10/O2 ratio also passes through
a maximum, thereby explaining the presence of the
maximum in Fig. 3.
As is seen from Fig. 4, the average rate of accumu-
lation of ethylene oxide is maximum at the tempera-
ture in the first section of T1 = 650–660 K. In the case
of a decrease or increase in the temperature, the rate of
accumulation of ethylene oxide decreases. Obviously,
this is associated with the fact that the oxidation of
butane is a degenerate branched process, as a result of
which the time taken to reach the maximum concen-
tration of active intermediate products, including per-
oxide radicals, in the first section of the reactor
Since the rate of a chemical process and, hence, the
concentrations of active intermediate products
(including radicals) depend on temperature, it is obvi-
ous that the temperature in the first section of the
reactor should affect the rate of formation of ethylene
oxide in the second section. The data obtained at dif- changes with a change in the temperature. At low tem-
Table 3. Influence of the temperature in the first section of the reactor, T1, on the yield of the products. C4H10 : O2 = 0.21,
T2 = 683 K, Q1 = 1.30 cm3/s, Q2 = 2.30 cm3/s, and P = 86.7 kPa
Partial pressure of reaction products, kPa
T1, K
No.
CH3OH
CH3CHO
C2H4O
HCHO
CO
1
2
3
4
5
6
7
8
610
623
638
657
673
683
700
723
0.581
0.563
0.558
0.552
0.562
0.536
0.492
0.465
0.549
0.544
0.536
0.533
0.531
0.512
0.486
0.434
1.186
1.654
1.783
1.773
1.868
1.705
1.668
1.329
0.418
0.443
0.451
0.450
0.448
0.453
0.472
0.479
1.72
1.75
1.78
1.78
1.83
1.91
2.16
2.31
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192
GRIGORYAN, ARSENTEV
Table 4. Influence of the temperature in the second section of the reactor, T2, on the yield of the products. C4H10 : O2 =
0.21, T1 = 673 K, Q1 = 1.30 cm3/s, Q2 = 2.30 cm3/s, and P = 86.7 kPa
Partial pressure of reaction products, kPa
T2, K
No.
CH3OH
CH3CHO
C2H4O
HCHO
CO
1
2
3
4
5
6
7
603
630
663
683
694
710
728
0.5.29
0.532
0.543
0.562
0.558
0.553
0.541
0.537
0.536
0.532
0.531
0.512
0.485
0.473
0.770
1.370
1.602
1.818
1.887
1.702
1.720
0.412
0.441
0.449
0.448
0.470
0.465
0.467
1.65
1.72
1.77
1.79
1.83
1.92
2.14
peratures (T1 < 640 K), the concentration of the active experiments at different temperatures were performed
in the second section of the reactor, i.e., in the epoxi-
dation zone. The concentrations of the main products
experimentally measured upon varying the tempera-
ture in the second section of the reactor are presented
in Table 4.
particles does not manage to reach the maximum
within the set contact time and, because of this, the
rate of accumulation of ethylene oxide in the second
section is lower than the maximum rate. At tempera-
tures T1 > 670 K, the oxidation process starts deceler-
ating at the set contact time because of the consump-
tion of the reactants, as a result of which the concen-
tration of the active particles entering into the second
section decreases. As a result, the rate of ethylene
oxide accumulation also starts decreasing, which leads
to the appearance of a maximum in the dependence of
The data of Table 4 were used to construct the
dependence, shown in Fig. 5, of the average rate of
accumulation of ethylene oxide on the temperature in
the second section of the reactor.
As is seen from Fig. 5, increasing the temperature
in the range of 600–695 K leads to a 2.8-fold increase
in the ethylene oxide accumulation rate. Since the
conditions of butane oxidation in the first section
remain unchanged, i.e., the concentration of the
active components coming into the second section of
on the temperature in the first section.
WC H O
2
4
Earlier [26], the rate constant of epoxidation of
ethylene by alkyl peroxide radicals •RO2 was mea-
sured. It was found that the activation energy of this
reaction is E = 57.7 kJ/mol. Apparently, at such an
activation energy, an increase in temperature should
increase the rate of epoxidation. In this connection,
the reactor remains constant, the growth in
is
W
C2H4O
obviously due to the increase in the rate constant of
epoxidation with temperature. In the case of further
increase in the temperature, the rate of accumulation
of ethylene oxide little changes. Apparently, the
increase in the rate constant of epoxidation is com-
pensated by the accelerating consumption of ethylene
oxide at high (>700 K) temperatures. This is also evi-
denced by the decrease in the concentrations of other
oxygen-containing products (Table 4) and the
increase in the concentration of the deep oxidation
product, carbon monoxide. At the temperature in the
second section of T2 = 683 K, the selectivity of eth-
ylene conversion to ethylene oxide is S ~ 87% at the
degree of ethylene conversion of ~6%.
WC H O, kPa/s
2
4
0.35
0.30
0.25
0.20
0.15
0.10
CONCLUSIONS
620
640
660
680
700
720
720
T, K
600
The character of the dependence of the rate of eth-
ylene oxide accumulation on the butane/oxygen ratio
in the first section of the reactor and temperature in
both sections gives evidence for the initiation of the
ethylene epoxidation process by the products of
n-butane oxidation under the conditions when eth-
ylene itself is very slowly oxidized.
Fig. 5. Dependence of the average rate of accumulation of
ethylene oxide on the temperature in the second section of
the reactor. C H : O = 0.21, T = 673 K, Q =
1
4
10
2
1
3
3
1.30 cm /s, Q = 2.30 cm /s, and P = 86.7 kPa.
2
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193
FUNDING
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Translated by E. Boltukhina
PETROLEUM CHEMISTRY Vol. 60 No. 2 2020