Dimethyl Ether Conversion to Gasoline Hydrocarbons over Nanosized Zeolite Catalysts: Effect of Modifier Nature

Article abstract of DOI:10.1134/S0965544119120119

Abstract—: The effect of modifier nature on the catalytic properties of nanosized zeolite catalysts used for the synthesis of liquid hydrocarbons from dimethyl ether is studied. It is shown that selectivity of the catalysts for liquid hydrocarbons depends on both the modifier nature and the initial feedstock composition. The best activity and selectivity for liquid hydrocarbons are exhibited by the samples modified with zinc and magnesium. The content of aromatic hydrocarbons in the products decreases appreciably when the catalysts are additionally modified with noble metals and the reaction is carried out in the medium of hydrogen.

Full text of DOI:10.1134/S0965544119120119

ISSN 0965-5441, Petroleum Chemistry, 2019, Vol. 59, No. 12, pp. 1331–1336. © Pleiades Publishing, Ltd., 2019.
Russian Text © The Author(s), 2019, published in Nanogeterogennyi Kataliz, 2019, Vol. 4, No. 2, pp. 143–148.
Dimethyl Ether Conversion to Gasoline Hydrocarbons over Nanosized
Zeolite Catalysts: Effect of Modifier Nature
Yu. M. Snatenkovaa, *, N. V. Kolesnichenkoa, Z. M. Matievaa, and A. L. Maximova
aTopchiev Institute of Petrochemical Synthesis, Russian Academy of Sciences, Moscow, 119991 Russia
*e-mail: snatenkova@ips.ac.ru
Received June 11, 2019; revised August 7, 2019; accepted August 9, 2019
Abstract—The effect of modifier nature on the catalytic properties of nanosized zeolite catalysts used for the
synthesis of liquid hydrocarbons from dimethyl ether is studied. It is shown that selectivity of the catalysts for
liquid hydrocarbons depends on both the modifier nature and the initial feedstock composition. The best
activity and selectivity for liquid hydrocarbons are exhibited by the samples modified with zinc and magne-
sium. The content of aromatic hydrocarbons in the products decreases appreciably when the catalysts are
additionally modified with noble metals and the reaction is carried out in the medium of hydrogen.
Keywords: liquid hydrocarbons, selectivity, dimethyl ether, nanosized zeolite ZSM-5
DOI: 10.1134/S0965544119120119
At the beginning of the 21st century, views about selectivity of DME in the synthesis of hydrocarbons
the future of world energetics and the role of various compared with methanol [3, 4]. The most efficient
sources of the hydrocarbon feedstock changed consid- catalysts for this process are catalysts based on zeolite
erably. The discovery of zeolite catalysts based on ZSM-5 [5] modified with such metals as Zn [6], Ga
ZSM-5 [1], which efficiently converted light oxygen- [7], Ni [8], and La [9], which favors ethylene oligom-
ates, in particular methanol, to hydrocarbons С5+, erization to hydrocarbons С5+ and ensures the occur-
invoked development of a new method for producing rence of dehydrogenation reactions of paraffins to ole-
liquid hydrocarbons from alternative carbonaceous fins and naphthenes to aromatic hydrocarbons.
raw materials, for example, natural gas [2]. The most
large-scale methane consumer is the process of syngas
production. This process is in most common use in the
chemical industry, for example, for the production of
methanol, which in turn can be converted to valuable
chemical products, such as liquid hydrocarbons. The
processes of synthesizing liquid hydrocarbons from
methanol have been developed over the past three
decades by a number of companies and are currently
being actively implemented in the industry.
At present, the study of processes for producing liq-
uid hydrocarbons from dimethyl ether (DME) is in
progress. Compared with methanol methods the path-
way of methane conversion via dimethyl ether to these
products offers a number of advantages. For example,
a more favorable thermodynamics makes it possible to
synthesize dimethyl ether at a lower pressure than the
methanol synthesis and to reach a higher syngas con-
version per pass. Energy and capital expenditure are
reduced, the degree of beneficial use of natural gas is
increased, and the production price is decreased.
Other advantages of this method are reduction in heat
stress at the stage of hydrocarbon synthesis from DME
Zeolite ZSM-5 is a microporous crystalline alumi-
nosilicate known for its catalytic activity and selectiv-
ity in the processes of МеОН and DME conversion to
gasoline hydrocarbons owing to the developed surface
and high thermal stability and chemical resistance
[10]. The activity and selectivity of zeolite ZSM-5
depend on its acidity (the strength and ratio of Brøn-
sted and Lewis acid sites), which can be varied by
either introducing active elements [6–9] or postsyn-
thesis treatment [11, 12]. However, in microporous
structures, such as zeolite ZSM-5, the internal diffu-
sion of bulky molecules is hindered; only active sites
close to the entrance of zeolite pores on their external
surfaces are accessible to them. In recent years, the
interest of many researchers has been focused on the
use of nanosized zeolites with the developed surface in
various processes; owing to a small crystal size mass
transfer and heat transfer processes are improved and
the activity and lifetime of the catalyst grow [13]. One
of the most available methods for synthesizing nano-
sized zeolites ZSM-5 is the ultrasonic treatment of
microporous zeolite ZSM-5 [14].
Despite a wide variety of papers addressing the use
(because of removal of methanol dehydration exother- of catalysts based on nanosized zeolite ZSM-5 in
mic reaction from this stage) and higher activity and methanol conversion to liquid hydrocarbons [15–20],
1331

1332
SNATENKOVA et al.
Table 1. Physicochemical properties of the synthesized nanosized catalysts
Total pore volume
at P/P0 = 0.99,
Vtotal, cm3/g
BET total specific
surface area,
Micropore volume,
t-plot,
Mesopore volume
Crystallite size
(SEM data),
nm
[Me],
wt %
Vmeso = Vtotal –Vmicro
,
Catalyst
SBET, m2/g
Vmicro, cm3/g
cm3/g
MFI
–
600
600
600
600
700
800
451.9
378
426.3
425.0
424.7
390.7
0.249
0.241
0.236
0.239
0.238
0.220
0.120
0.115
0.117
0.114
0.116
0.108
0.129
0.126
0.119
0.125
0.112
0.112
MgMFI
ZnMFI
LaMFI
ZrMFI
CuMFI
1.0
2.0
1.0
1.0
2.0
almost no data are available on the study of DME con- Upon solution evaporation the sample was dried at
version over analogous catalysts.
100°С and calcined at 500°С for 6 h.
This study concerns the effect of active component
Powdered catalyst samples were preliminarily
nature on the catalytic behavior of catalysts based on pressed and calcined at 500°С. Before loading (3 g) a
nanosized zeolite ZSM-5 in the process of DME con- fraction with a grain size of 2–3 mm was prepared.
version to gasoline hydrocarbons.
After loading in a reactor the catalyst used for the syn-
thesis of hydrocarbons was subjected to reduction for
2 h in a hydrogen stream at a pressure of 0.1 MPa and
a temperature of 380°С; then, the temperature was
reduced to a running temperature of 340°С and DME
was fed at a weight hourly space velocity of 2.6 h–1.
EXPERIMENTAL
Zeolite CBV (MFI) with a molar ratio of
SiO2/Al2O3 = 80 (Zeolyst Int.) was used in this study.
The DME conversion was run on a micropilot flow-
circulation unit at a temperature of 340°С and a pres-
sure of 10 MPa. The catalytic properties of the zeolite
catalysts were tested in the medium of hydrogen
(100 vol %) or syngas (30 vol % СО and 70 vol % Н2).
Nanosized zeolites were synthesized by the sonica-
tion-driven dispersion of the original zeolite in dis-
tilled water at a temperature of 25°С for 1 h in an
Elmasonic P30H ultrasonic bath (an ultrasound fre-
quency of 80 kHz and a power of 130 W).
The experimental technique and the analysis of
reaction products were described in detail in [19].
According to the analysis of the feed gas containing
СО, СН4, СО2, DME, Н2О, and N2 and the end gas
as well as the reaction water for the DME content the
conversion of DME ХDME was calculated as
Catalysts containing magnesium, zirconium, or
copper were prepared by the incipient wetness impreg-
nation of the nanosized zeolite with the aqueous solu-
tions of respective nitrate salts, dried for a day in an
oven, and calcined in air at a temperature of 500°С for
6 h. The nanosized zeolite was modified with zinc by
treating the zeolite with a zinc nitrate aqueous solution
at 92–95°С under stirring for 2 h. Afterwards the solu-
tion was evaporated and the sample was dried at
100°С, and calcined at 500°С for 6 h. Modification of
the zeolite with lanthanum was carried out in a similar
manner using a lanthanum nitrate solution. The data
on the modifier content are listed in Table 1.
The introduction of rhodium in an amount of
0.05 wt % into the catalyst composition was conducted
as follows: the preformed suspension composed of
chitosan, which was preliminarily dissolved in water,
and a RhCl3 aqueous solution was added to the modi-
fied zeolite, and the resulting mixture was held for a
day; after that the sample was dried and calcined at
500°С for 4 h. The suspension composed of chitosan
dissolved in water and RhCl3 aqueous solution was
sonicated for 1 h prior to deposition on the zeolite [21].
ХDME = V
× DME inlet – Voutlet;
(
inlet
× DMEoutlet; V inlet × DMEвх
,
)
where Vinlet and Voutlet are the amounts of gas at the
inlet and outlet of the unit, L/h; and DMEinset and
DMEoutlet are the DME concentrations at the inlet and
outlet of the unit, vol %. Gasoline selectivity
calculated according to the formula:
was
SС
5+
SC5+ = DMEbenzene DME
+ DMEgas С1–С4 ×100%,
(
)
benzene
where DMEgasoline is the amount of gasoline in terms of
converted DME and DMEgas С1–С4 is the amount of
gas С1–С4 in terms of converted DME.
The total amount of hydrocarbons was calculated
from the results of analysis of gaseous and liquid
hydrocarbons for the whole testing time.
The palladium sample (palladium content,
0.5 wt %) was prepared by impregnating the nanosized
zeolite MFI, which was modified with zinc in an
amount of 2 wt %, with the aqueous solution of PdCl2.
The content of metals in zeolite samples was deter-
mined by X-ray fluorescence analysis (XRF) on an
ARL Perform’x sequential XRF spectrometer
(Thermo Fisher Scientific, Atkinson, NH, United
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DIMETHYL ETHER CONVERSION TO GASOLINE HYDROCARBONS
1333
States) equipped with a rhodium tube (3.5 kW). The
180
160
140
120
100
80
1
2
metal content in the samples was 1–2 wt %.
3
6
5
Scanning electron microscopic (SEM) images of
the samples were taken on a Hitachi TM3030 scanning
electron microscope. Before imaging the samples were
decorated with gold by vacuum spraying.
Specific surface area was determined by low-tem-
perature nitrogen adsorption on a Micromeritics
ASAP-2000 porosimeter. Specific surface area was
4
calculated
using
the
Brunauer–Emmett–
60
Teller (BET) method at a relative partial pressure of
40
Р/Р0 = 0.2. All samples were preliminarily evacuated
to 4 × 10–1 Pa at a temperature of 350°С for 6 h.
The adsorption of N2 was conducted at a temperature
of 77 К.
20
0
0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1.0
The acidic properties of the zeolites were tested by
the temperature-programmed desorption of ammonia
(TPD-NH3) on an USGA-101 universal sorption gas
analyzer (Unisit). A weighed portion (100 mg), which
was preliminarily calcined in air, was placed in a
quartz reactor, heated in a helium stream at tempera-
ture of 500°С for 1 h, cooled to a temperature of 60°С,
and saturated with ammonia in an ammonia–nitro-
gen stream for 15 min. To remove weakly bound
ammonia the sample was held at 70°С in a dry helium
stream for 1 h. The sample was then rapidly cooled to
room temperature in a helium stream (30 mL/min),
and the TPD-NH3 curves were registered in the mode
of linear temperature rise to 800°С at a rate of
8°C/min using a thermal conductivity detector.
Fig. 1. Isotherms of nitrogen adsorption on catalysts:
(1) nanosized MFI, (2) ZnMFI, (3) LaMFI, (4) CuMFI,
(5) ZrMFI, and (6) MgMFI.
Figure 2 shows the TPD-NH3 profiles of the origi-
nal MFI and modified samples. All tested samples
have two desorption peaks. The first peak at 150–
300°С, which is classified as low-temperature related
to the desorption of a weakly bound NH3, corresponds
to the content of weak and medium-strength acid sites.
In a similar manner the high-temperature peak at
320–550°С corresponds to the desorption of strongly
bound NH3 and defines the content of strong acid
sites.
As follows from Table 2, the total acidity decreases
in the sequence MFI > CuMFI > ZrMFI > LaMFI >
MgMFI > ZnCMFI (from 631 to 565 μmol/g). Note
that modification of the nanosized zeolite with active
metals causes a reduction in the proportion of strong
acid sites (ratio II/I decreases from 1.1 for MFI to 0.46
for CuMFI).
RESULTS AND DISCUSSION
The catalytic properties of the modified zeolite cat-
alysts are influenced by many factors. The modifier
nature, its concentration, introduction technique, and
catalyst pretreatment conditions exert a strong effect
on the properties of zeolite catalysts [15, 19].
The reaction was run out in the medium of
syngas (30 vol % СО and 70 vol % Н2) and hydrogen
(100 vol %). Hydrogen was selected since the two-step
technology developed for the production of hydrocar-
bons С5+ from СО and Н2 through DME [3, 4]
involves the use of a unit composed of two reactors: a
reactor for DME synthesis from СО and Н2 and a
reactor for the synthesis of hydrocarbons from DME;
these reactors are united by a common circulation
contour. When the syngas of composition: N2, 1;
CO, 17; CO2, 7; and H2, 75 (vol %) enters the reactor
of DME synthesis, then the end gas fed to the reactor
of hydrocarbon synthesis consists almost exclusively
of hydrogen (СО, 1−2 vol %; Н2, 90–95 vol %
(Table 3).
Nitrogen adsorption isotherms obtained for
MeMFI catalysts (Fig. 1) are typical type I isotherms
with micropores [22]. A well-defined hysteresis
observed at a relative pressure of P/P0 = 0.4–0.9 sug-
gests the presence of mesopores connected to the
external surface through micropores [23]. Modifica-
tion of the zeolites with metals leads to a slight reduc-
tion in the specific surface areas of the zeolite and the
volumes of micropores and mesopores (Table 1).
Reduction in the micropore volume in the catalysts
compared with the original zeolite indicates a partial
arrangement of the modifier in zeolite channels.
Among the modified samples the highest specific sur-
face area (426.3 m2/g) is exhibited by ZnMFI; the
lowest specific surface area, by MgMFI and CuMFI.
Sample MgMFI is characterized by a considerable
mesopore volume (0.126 cm3/g), while the sample
promoted by copper has the lowest micropore volume
(0.112 cm3/g).
In the presence of all catalysts the reaction occurs
with a fairly high conversion in the medium of both
syngas and hydrogen (Table 3) except ZrMFI, and
selectivity for liquid hydrocarbons considerably
PETROLEUM CHEMISTRY Vol. 59 No. 12 2019

1334
SNATENKOVA et al.
Aromatic
0.45
0.40
0.35
0.30
0.25
0.20
0.15
0.10
0.05
Hydrocarbons
2
1
Olefins
6
Cycloparaffins
N-paraffins
Isoparaffins
1
3
4
2
5
0
10 20 30 40 50 60 70 80 90 100
Fig. 3. Hydrocarbon group composition of the mixture of
liquid hydrocarbons obtained in the presence of Rh-
ZnMFI in the medium of (1) syngas and (2) hydrogen.
0
100 200 300 400 500 600 700 800
Fig. 2. TPD-NH profiles of nanosized catalysts:
3
It is known that in the presence of group VIII met-
als (often more accessible Pd in an amount of up to
1 wt %) the isomerization and hydrogenation reac-
tions are accelerated over zeolite catalysts. In this
regard, Rh is a poorly studied modifier. Therefore, the
synthesized catalysts were additionally modified with
rhodium and tested in DME conversion to liquid
hydrocarbons (Table 4).
As is clear from Table 4, all samples are character-
ized by a high conversion in both hydrogen and syngas
media. However, selectivity for liquid hydrocarbons
decreases upon the introduction of Rh into the cata-
lyst composition. In the presence of rhodium catalysts
the liquid product contains a somewhat higher
amount of isoparaffins and a lower amount of aro-
matic hydrocarbons; this effect is more pronounced in
the hydrogen medium. The hydrocarbon group com-
position of the mixture of liquid hydrocarbons synthe-
sized in the presence of sample Rh-ZnMFI is shown
in Fig. 3.
When Rh-MgMFI and Rh-CuMFI catalysts are
used, the highest amount of methanol is detected in
the aqueous phase of the liquid product (Table 4). In
the case of ZSM-5 methanol is formed via the interac-
tion of methoxy groups with Н2О. Most probably, in
the presence of these catalysts the highest amount of
methoxy groups is formed; as a consequence, the
amount of the produced methanol is increased [25].
Table 5 presents the comparative data on the effect
of two hydrogenating metals Pd (0.5 wt %) and Rh
(0.05 wt %) on the catalytic behavior of nanozeolite
zinc-containing (2 wt %) catalysts. The nature of the
additional modifier considerably affects the behavior
of the catalyst. At an almost similar DME conversion,
the rhodium catalyst is characterized by a much higher
selectivity than the palladium catalyst. However, the
resulting mixture contains a higher amount of isopar-
affins, while the amount of aromatic hydrocarbons is
small and the concentration of methanol in the aque-
ous phase of the liquid product is low (6.8 wt %).
(1) nanosized MFI, (2) ZrMFI, (3) LaMFI, (4) ZnMFI,
(5) CuMFI, and (6) MgMFI.
depends on the nature of the active element. For
example, in the syngas medium, the sample MgMFI
exhibits the highest selectivity for liquid hydrocarbons
(86.9 wt %) and is characterized by the highest amount
of aromatic hydrocarbons (33.5 wt %) and the
lowest amount of isoparaffins (54.5 wt %). The
ZnMFI sample also shows high selectivity for liquid
hydrocarbons (85.0 wt %) with a high content of iso-
paraffins (68.2 wt %) and the lowest content of aro-
matic hydrocarbons (17.8 wt %). Note that for the
zinc-containing sample the aqueous phase of the liq-
uid product contains a much higher amount of meth-
anol (12.5 wt %).
These results showed that the composition of the
concomitant gas exerts a strong effect on the distribu-
tion of liquid hydrocarbons. For example, in the pres-
ence of ZnMFI a high selectivity for isoparaffins
(78.3 wt %) and the lowest amount of aromatic hydro-
carbons (10.9 wt %) are observed. This is explained by
the fact that in the hydrogen medium hydrogenation
reactions are accelerated; as a result, a smaller amount
of aromatic hydrocarbons is formed [24].
Table 2. Acidic properties of the catalysts according to
TPD-NH3
Number of sites, μmol/g
Catalyst
II/I
type I
type II
total
MFI
309
419
348
359
344
310
322
192
252
230
241
255
631
615
600
595
585
565
1.04
0.46
0.72
0.64
0.70
0.82
CuMFI
ZrMFI
LaMFI
MgMFI
ZnMFI
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DIMETHYL ETHER CONVERSION TO GASOLINE HYDROCARBONS
1335
Table 3. Effect of modifiers on catalyst activity and selectivity in DME conversion to liquid hydrocarbons
Selectivity
for liquid
hydrocarbons,
Gasoline composition, wt %
DME conversion,
Catalyst
MeOH, wt %
aromatic
isoparaffins
CDME, %
hydrocarbons
wt %
,
SС
5+
Syngas medium
MFI
99.8
99.9
98.9
99.8
99.2
99.8
81.4
78.7
85.0
80.0
86.9
79.8
56.7
55.1
68.2
56.2
54.5
58.7
26.7
28.9
17.8
28.3
33.5
24.5
3.9
2.5
12.8
4.0
2.7
3.5
ZrMFI
ZnMFI
LaMFI
MgMFI
CuMFI
Hydrogen medium
MFI
99.9
99.9
98.3
99.7
99.5
99.5
79.8
64.9
65.1
78.3
68.9
61.1
63.2
17.3
16.5
10.9
13.5
20.9
17.8
2.5
1.3
20.4
5.9
3.8
5.7
ZrMFI
ZnMFI
LaMFI
MgMFI
CuMFI
76.2
84.2
77.8
83.8
75.3
Table 4. Influence of Rh on the activity and selectivity of catalysts of DME conversion to liquid hydrocarbons
Selectivity
for liquid
hydrocarbons,
Gasoline composition, wt %
DME conversion,
Catalyst
MeOH, wt %
aromatic
isoparaffins
CDME, %
hydrocarbons
wt %
,
SС
5+
Syngas medium
Rh-ZrMFI
99.9
98.8
99.8
99.2
99.8
78.4
85.6
79.8
84.9
76.8
57.4
69.7
64.2
60.5
63.7
25.1
16.7
20.3
27.5
19.5
2.8
12.8
5.0
Rh-ZnMFI
Rh-LaMFI
Rh-MgMFI
Rh-CuMFI
12.7
3.5
Hydrogen medium
Rh-ZrMFI
Rh-ZnMFI
Rh-LaMFI
Rh-MgMFI
Rh-CuMFI
99.9
99.6
99.4
96.9
98.8
71.2
68.8
86.8
70.2
68.7
70.3
14.2
3.7
12.5
18.4
11.4
2.3
6.9
7.8
77.8
60.1
68.6
47.7
27.1
14.8
Thus, the effect of modifier nature on the activity amount of isoparaffins and a decrease in the content
of aromatic hydrocarbons and methanol in the aque-
ous phase of the liquid product.
and selectivity of nanosized zeolite catalysts of
dimethyl ether conversion to liquid hydrocarbons is
studied. The nature of the active element considerably
influences both the physicochemical and catalytic
properties of the catalyst. In the presence of all of the
catalysts a fairly high DME conversion is reached in
both syngas and hydrogen media. Introduction of the
additional modifier (Rh) entails an increase in the
ACKNOWLEDGMENTS
The work was performed using the equipment of the
Shared Research Center New Petrochemical Processes,
Polymer Composites, and Adhesives.
PETROLEUM CHEMISTRY Vol. 59 No. 12 2019

1336
SNATENKOVA et al.
Table 5. Effect of Pd and Rh on the nanosized zinc catalyst for synthesizing liquid hydrocarbons from DME. Tests were run
in the hydrogen medium
Selectivity
for liquid
hydrocarbons,
Gasoline composition, wt %
DMEconversion,
Catalyst
MeOH, wt %
aromatic
isoparaffins
CDME, %
hydrocarbons
wt %
,
SС
5+
Rh-ZnMFI
Pd-ZnMFI
99.6
97.4
77.8
83.9
86.8
83.8
3.7
6.8
6.9
28.9
FUNDING
8. O. Kedia and H. A. Zaidi, IJARSE 3, 350 (2014).
9. X. F. Gao, C. Ding, W. Liu, J. Wang, K. Zhang, and
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CONFLICT OF INTEREST
12. P. Losch, C. Bernardon, B. Louis, A. Palcic, and
V. Valtchev, Appl. Catal., A, 509, 30 (2016).
A.L. Maximov is the editor-in-chief of the journal
Petroleum Chemistry; other authors declare that there is no
conflict of interest.
13. S. Mintova, M. Jaber, and V. Valtchev, Chem. Soc.
Rev. 44, 7207 (2015).
14. N. V. Kolesnichenko, N. N. Ezhova, O. V. Yashina, and
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ADDITIONAL INFORMATION
Yu.M. Snatenkova, ORCID: https://orcid.org/0000-
0002-6221-4034
15. Yu. M. Snatenkova, D. A. Ionin, N. V. Kolesnichenko,
and Z. M. Matieva, Pet. Chem. 59 (5), 535 (2019).
16. Z. Hajjar, A. Khodadadi, Y. Mortazavi, S. Tayyebi, and
N.V. Kolesnichenko, ORCID: https://orcid.org/0000-
0003-2534-2624
S. Soltanali, Fuel 179, 79 (2016).
17. Wen Z. Zhiyong, C. Wang. Chun, Wei J. Jian, Sun J. Ji-
an, Guo L. Lisheng, Ge Q. Qingjie, and H. Xua
Hengyong, Catal. Sci. Technol. 6, 8089 (2016).
Z.M. Matieva, ORCID: https://orcid.org/0000-0001-
8076-5844
A.L. Maximov, ORCID: https://orcid.org/0000-0001-
9297-4950
18. J. Li, D. Han, T. He, G. Liu, Z. i, Z. Wang, J. Wu, and
J. Wu, Fuel Process. Technol. 191, 104 (2019).
19. Zh. Ke, S. A. Kurumov, Su Xiaofang, Yu. M. Snaten-
kova, Z. M. Bukina, N. V. Kolesnichenko, and
S. N. Khadzhiev, Pet. Chem. 57 (12) 1036 (2017).
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PETROLEUM CHEMISTRY
Vol. 59
No. 12
2019