Acidic and basic properties of zeolite-containing cracking catalyst in the process of butene-1 isomerization

Article abstract of DOI:10.1134/S0036024416080197

The process of butene-1 isomerization in the presence of two groups of samples of zeolite-containing catalyst (ZCC) that earlier participated in the traditional and oxidative catalytic cracking of vacuum gasoil is investigated. It is established that the nature of the reaction mixture and conditions of the cracking process are key factors in forming the acidic and basic properties of the catalyst. It is shown that the highest activity in the butene-1 isomerization into cis-/trans-butene-2 is demonstrated by ZCC samples that participated in the oxidative catalytic cracking (oxycracking). It is suggested that the enhanced catalytic activity of this group of ZCC samples was related to the availability of acid–base centers in the form of radical-like oxygen along with protic- and aprotic-type acidic centers in the structure of the oxidative compaction products.

Full text of DOI:10.1134/S0036024416080197

ISSN 0036-0244, Russian Journal of Physical Chemistry A, 2016, Vol. 90, No. 8, pp. 1533–1538. © Pleiades Publishing, Ltd., 2016.
Original Russian Text © L.A. Mursalova, E.A. Guseinova, K.Yu. Adzhamov, 2016, published in Zhurnal Fizicheskoi Khimii, 2016, Vol. 90, No. 8, pp. 1163–1169.
CHEMICAL KINETICS
AND CATALYSIS
Acidic and Basic Properties of Zeolite-Containing Cracking Catalyst
in the Process of Butene-1 Isomerization
L. A. Mursalovaa, E. A. Guseinovaa, and K. Yu. Adzhamovb
a Azerbaijan State Petroleum Academy, Geotechnological Problems of Oil, Gas, and Chemistry Scientific Research Institute,
Baku, AZ1010 Azerbaijan
b Azerbaijan State Petroleum Academy, Baku, AZ1010 Azerbaijan
e-mail: elvira_huseynova@mail.ru
Received September 1, 2015
Abstract—The process of butene-1 isomerization in the presence of two groups of samples of zeolite-contain-
ing catalyst (ZCC) that earlier participated in the traditional and oxidative catalytic cracking of vacuum gasoil
is investigated. It is established that the nature of the reaction mixture and conditions of the cracking process
are key factors in forming the acidic and basic properties of the catalyst. It is shown that the highest activity
in the butene-1 isomerization into cis-/trans-butene-2 is demonstrated by ZCC samples that participated in
the oxidative catalytic cracking (oxycracking). It is suggested that the enhanced catalytic activity of this group
of ZCC samples was related to the availability of acid–base centers in the form of radical-like oxygen along
with protic- and aprotic-type acidic centers in the structure of the oxidative compaction products.
Keywords: zeolite-containing catalysts, acidic-basic properties, isomerization, oxycracking, products of oxi-
dative compaction.
DOI: 10.1134/S0036024416080197
INTRODUCTION
bizeolite cracking catalyst with IK-17-1 additive [20–
22]. A substantial difference between the catalytic
activity of catalysts of one structural type and chemical
composition during traditional oxidative catalytic
cracking (oxycracking) was established from a com-
parison of the process parameters. In our opinion, the
reason for this phenomenon lies in oxygen affecting
changes in the acid–base properties of the ZCC.
In this work, we present results on the activity of
ZCC samples taken after participating in the tradi-
tional and oxycracking of gasoil during the isomeriza-
tion of butene-1 into cis-/trans-butene-2. The cata-
lytic and acid–base properties of the samples are com-
pared.
Zeolite containing catalysts (ZCCs) play an
important role in development of petrochemical pro-
cesses. They provide the basis for the production of
effective catalysts for processing petroleum fractions,
synthesis gas conversion, solving problems of ecologi-
cal catalysis, and so on [1–12].
Improvements in ZCCs that enhance their activity,
selectivity, and stability facilitate the development and
increased efficiency of technological processes. For
example, the evolution of the industrial cracking cata-
lyst of high-boiling petroleum fractions now allows us
to produce high-quality automotive gasoline, and to
provide a reliable base of raw materials for the petro-
chemical industry [7, 8, 13–15]. The future pace of
catalytic cracking development depends on our suc-
cessfully resolving problems related to the processing
of heavy crude oil, which impose stricter requirements
upon the catalytic and operational characteristics of
ZCC.
Industrial catalysts of the KMTs series; LYuKS,
Adamant, and bizeolite cracking catalysts with the
low-modulus additive IK-17-1 (based on ZSM-5-type
zeolite); and others must be included among the suc-
cessful developments in the recent years [16–19].
Earlier, we conducted comparative studies of the ing [23, 24] in the amount of 3 wt %. Techniques for
traditional and oxidative catalytic cracking (oxycrack- conducting traditional and oxidative cracking were
ing) of vacuum gasoil in the presence of oxygen, using described in [20, 21].
EXPERIMENTAL
The process of catalytic cracking in the presence
and absence of oxygen was conducted in a flow reac-
tor with a packed bed of Grace industrial zeolite-
containing catalytic cracking catalyst OMNIKAT-
340. A low-modulus zeolite of the ZSM-5 type (zeo-
lite IK-17-1, manufactured by OAO NZKhK) was
used as an additive. Zeolite additive IK-17-1 was
introduced into the base catalyst by mechanical mix-
1533

1534
MURSALOVA et al.
The specific surface area of the initial and nonre- 30, 45, 60 min) and the conditions of catalytic crack-
generated samples after participating in cracking was ing: four samples had already been used in the oxy-
determined from the low-temperature absorption of cracking and four samples had participated in tradi-
nitrogen at 77 K by means of BET. The samples were tional nonoxidative catalytic cracking.
preliminarily evacuated (10–5 mm Hg) for 5 h at
The data presented in Table 1 indicate that the
350°С. According to BET, the specific surface area
ZCC samples of the same composition but different in
(Ssp) of the OMNIKAT industrial catalyst was
the conditions of cracking operated as different cata-
200 m2/g. The bulk density (ρbulk) was 0.65 g/mL, and
lysts: the degree of butene-1 transformation in the
the pore volume (Vpore) was 0.4 mm3/g. These param-
presence of samples that had participated in cracking
under traditional catalytic conditions were lower than
for the respective samples that had participated in oxy-
cracking. However, the substantial differences were
not obvious at first. For example, the degrees of
butene-1 isomerization in the presence of samples that
had participated in both types of cracking for 15 min
(samples 1CC и 1ОCC) were very close, but the con-
siderable difference between then became apparent
after 30 min of operation (samples 2CC и 2ОCC): the
activity of 2ОCC fell by 1.1, and 5.5% in the case of
2CC. This trend was even more pronounced the lon-
ger the catalysts were subjected to cracking conditions.
eters for the IK-17-1 were Ssp = 300 m2/g and ρbulk
=
500 kg/m3. The components were mixed in a vibrating
ball mill for 1 h with subsequent calcination at 550°С
for 6 h. A technological additive was added to the cat-
alyst at the stage of component mixing, facilitating the
formation of water vapor, strengthening the catalyst,
and assisting the process of granule formation [25].
Butene-1 isomerization was conducted using a lab-
oratory flow unit with a stationary catalyst layer at
300°С and atmospheric pressure. Butene-1 was pro-
duced directly in the setup via the dehydration of
n-butyl alcohol on aluminum oxide pretreated with a
0.05 wt % solution of KОН (to suppress double bond
migration). The volumetric flow rate of the initial
butene-1 was 240 h−1.
The following series was obtained when the activity
of the tested samples in the isomerization of butene-1
into cis-/trans-isomers of butene-2 were compared:
1 ОCC > 2 ОCC > 3 ОCC > 1 CC > 2 CC > 4 ОCC.
Chromatographic analysis of the butene isomer
composition was conducted on a CHROM-5 chro-
matograph equipped with a thermal conductivity
detector. A column packed with Inza brick INZ-600
support modified with 15% mineral oil was used. The
column length was 3 m. The detector current was
60 mA.
The catalyst’s activity was characterized on the
basis of the degree of butene-1 conversion relative to
the surface area of the catalyst.
The dependences of the conversion of the vacuum
gasoil and the distribution of compaction products
during catalytic cracking with and without oxygen are
presented in Fig. 1. It can be seen that the degree of
petroleum fraction conversion grew by 14% under
conditions of oxycracking, compared to the traditional
regime. This effect indicates that oxygen is a signifi-
cant promoter of the process. The similarity between
the general patterns of the activity of the ZCC samples
Differential thermal analysis (DTA) and thermo-
gravimetric analysis (TGA) were performed on a
NETZSCH instrument. A linear polythermal regime
of heating at a rate of 10 K/min in air was selected for
our analysis.
Table 1. Characteristics of our samples of zeolite-contain-
ing catalysts
Ssp, m2/g
S, m2
А, m−2
Sample t, min
х, %
Before
catalysis
654.13
202.5
–
–
RESULTS AND DISCUSSION
It is known that the activity and selectivity of cata-
lysts are directly related to their acidity [26–30]. Vari-
ous techniques are used for determining the nature,
number, and strength of acidic centers in catalysts: the
Traditional catalytic cracking
1 CC
2 CC
3 CC
4 CC
15
30
45
60
628.2
603.8
–
188.8
175.1
–
39.4
34.9
29.0
18.6
0.061
0.058
–
temperature-programmed
adsorption–desorption
(TPD) of gaseous bases, amine titration, NMR, the
IR spectroscopy of adsorbed molecules, and others. In
addition, the possibility of a relationship between the
acidic properties of aluminosilicate catalysts and the
activity in the isomerization reaction of hydrocarbons
has been shown by a number of authors [26–32].
In order to compare the dynamics of changes in the
acidity of the ZCC, samples were selected that had
already been used in cracking and differed by the
length of time they were subjected to the process (15,
–
–
–
Oxidative catalytic cracking
1 ОCC
2 ОCC
3 ОCC
4 ОCC
15
30
45
60
598.3
585.7
582.5
524.7
164.8
159.8
156.0
147.9
39.0
37.9
36.9
19.6
0.065
0.064
0.063
0.030
t is the length of time spent under conditions of catalytic cracking;
S is the surface area; S is the specific surface area; х is the degree
sp
of butene-1 conversion; А is activity.
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Table 2. Characteristics of exothermic effects from the data of differential thermal analysis
Tmax, °С
∆mtot, %
Sample
1 ОCC
2 ОCC
3 ОCC
4 ОCC
1 CC
Regime
t, min
∆m, %
start
maximum
end
Oxidative
15
250.4
173.6
274.5
304.5
280.7
250.3
274
398.6
485.2
404.5
503.9
407.5
503.7
404.6
504.1
525.5
672.1
575.7
624.7
574.4
675.9
582.8
814.6
588.4
682.7
2.5
9.7
4
11.05
3.5
11.4
4
12.2
Oxidative
30
15.05
14.9
Oxidative
45
Oxidative
60
16.16
2.58
284.2
354.7
12.16
2.58
Nonoxidative
15
∆m is mass loss; ∆m is total mass loss. The rest of the denotations are the same as in Table 1.
tot
during oxycracking and the subsequent process of medium, and not the duration of the cracking process,
butene-1 isomerization in their presence can also be affected the cis-/trans-butene-2 ratio the most. In
seen. This is even more surprising when we consider addition, this dependence for the samples that had
that according to the data of thermal analysis, the participated in the traditional catalytic cracking pro-
amount of compaction products (CP) formed under cess (Fig. 2, curve 1) was more gradual and almost lin-
identical conditions of the oxidative catalytic cracking ear (approximate level of significance, R = 0.97). The
of vacuum gasoil is higher than under the conditions of concentration of either protic or aprotic acidic centers
traditional nonoxidative cracking (Table 2, Fig. 1), fell sharply as the duration of the ZCC samples’ expo-
and the activity of ZCC under oxycracking conditions sure to the conditions of traditional cracking grew, due
was also higher than under nonoxidative conditions likely to the accumulation of surface products of the
[20, 21].
According to the literature data [33–35], the ratio
of cis-/trans-isomers allows us to suggest one possible
reactions of oligomerization, polymerization, and
condensation.
The dependence of the cis-/trans-butene-2 ratio on
nature of the acidic centers. Based on this concept, we the duration of the oxycracking process (Fig. 2, curve 2)
analyzed the ratios of cis- and trans-butene-2 yields for is more complicated and changes almost exponentially.
the ZCC samples, depending on the regime of their Two time intervals can be identified in this dependence
participation in the cracking process (Fig. 2). The pre- that differ significantly in character: in the initial time
sented dependences are of a notable antisymbatic period (15 min), the ratio of cis-/trans- isomers is char-
character. Comparative analysis of the obtained acterized by notable dominance of the cis-butene-2,
graphic dependences showed that the reaction followed by a minimum (30 min) after which the sec-
20
15
10
5
100
60
20
0
15*
15
30
45
60
t, min
Fig. 1. Effect of the duration of the oxycracking process on the conversion of vacuum gasoil (solid line), butene-1 (dashed line),
and the dynamics of mass accumulation and loss for endoeffects: Т = 398–407, 485–504°С. 15* is the sample from oxycrack-
max
ing for 15 min at Т
= 525°С, where Т
is the temperature of the maximum of the exothermic effect.
max
max
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1536
Ratio of cis-/trans-isomers
MURSALOVA et al.
centration of protic centers responsible for the trans-
1.7
1.5
1.3
1.1
stereospecificity observed for the samples subjected to
traditional cracking was due to the requirements on
this type of industrial catalyst [17, 18, 33, 34], for
which the protic acidity due to the availability of sur-
face OH-groups responsible for the protonation of
both alkanes and olefins is fundamental [2–4]. The
observed fast deactivation of the group of samples sub-
jected to traditional cracking suggests that most of the
protic centers in the ZCC were on the outer surface of
the zeolite, since the sizes of the initial butene-1 and
the cis-/trans-isomers of butene-2 molecules are very
close and much smaller than the diameter of channels
in the zeolite.
1.62
R2 = 0.6062
1.15
2
1.21
1.1
1.22
R2 = 0.9652
0.9
0.7
0.5
0.3
1.0
0.71
0.78
1
Compared to these samples, not only was there no
drop in the isomerization activity of the ZCC for the
oxycracking samples in which the surface fraction of
protic centers fell almost immediately; it actually grew,
due to formation of cis-butene-2.
15
30
45
60
t, min
The ratio of butene-1 to trans-butene-2 is another
important indicator of the contribution from protic
acidic centers to the general acidic and basic properties
observed for the catalysts during the process of
butene-1 isomerization (Fig. 3). Once again, the
medium in which the catalytic cracking was con-
ducted made the main contribution: the samples that
had participated in the process of oxycracking were
characterized with higher contents of not only cis- but
also trans-butene-2. The experimental dependences
also displayed high levels of significance (R = 0.95–
0.98).
Fig. 2. Dependences of cis-/trans-butene-2 ratio in the
presence of the catalyst samples that had already partici-
pated in (1) traditional and (2) oxidative catalytic cracking
on the duration of the process.
tion of a resumed substantial increase in the cis-
butene-2 yield is observed. In our opinion, the nonlin-
earity of this dependence is related to the development
of the oxycracking catalyst, which is accompanied by a
change in the acid–base properties of the catalyst in
the presence of oxygen.
It was also noted that for both groups of the ZCC
Since it was established for the samples subjected to
samples with the shortest length of stay in the cracking traditional cracking that the ratio of the formed cis-
zone, the dependences are characterized by fairly high /trans-butene-2 and butene-1/trans-butene-2 was
contents of trans-butene-2. The relatively high con- close to 1 in the course of butene-1 isomerization, it is
y
1.5
1.2
0.9
0.6
0.3
0
1.39
2
0.96
0.75
0.93
0.68
R2 = 0.9512
0.85
R2 = 0.9773
1
0.54
0.59
20
15
25
30
35
40
45
x, %
Fig. 3. Dependences of the ratio of butene-1 to trans-butene-2 (y) in the presence of catalyst samples that had already participated
in (1) traditional and (2) oxidative catalytic cracking on the degree of butene-1 isomerization (х).
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worth noting that n-alkene activation was accompa- cates that the POC formed during oxycracking is dif-
nied by the formation of side products (carbocations) ferent, i.e., less condensed.
in the first minutes of the isomerization process. Car-
bocations are very active particles that react with
adsorbed particles at exceptionally high rates, resulting
in the accumulation of tightly adsorbed, high molecu-
lar weight structures on the surface of a catalyst,
thereby increasing the carbonization of the surface,
blocking the aprotic active centers of the catalyst, and
thus reducing olefin conversion and catalyst activity
for a short period of time.
Further investigation of the location of the stabili-
zation and coordination environment of oxygen is
required in order to fully understand the mechanism
of hydrocarbon activation with the participation of
such centers, and the possible role of radical-like oxy-
gen in the process. The authors plan to conduct such a
study in the future.
CONCLUSIONS
Analysis of dependences of the ratio of butene-2
isomers produced during butene-1 isomerization in
the presence of ZCC samples that had participated in
the oxycracking process suggests that the acidic and
basic properties of these samples were determined not
only by the protic acidic centers of the catalyst samples
but by their basic centers as well. The availability of
such centers follows from the clearly pronounced cis-
stereospecific isomerization of butene-1. The forma-
tion of this type of isomer is likely related to the avail-
ability of Lewis acidic centers [29, 34, 35]. On the
other hand, the high degree of carbonization of the
samples subjected to oxycracking casts some doubt on
their contribution in this particular case. It follows that
other active centers prone to display electron acceptor
properties participated in the activation of the initial
olefin. Since the enhanced isomerization activity
observed in our studies correlated with the activity in
the process of oxycracking, we assume that the struc-
tural features of this type of active centers were based
on their having emerged and evolved under the influ-
ence of the reaction medium and oxygen. The nature
of these centers is as yet unknown, but we speculate
that carbonate and carboxylate oxycomplexes form in
the process of oxycracking, and in turn form products
of oxidative compaction (POC) on a catalyst’s surface.
The results obtained in our investigation of butene-1
isomerization show that the formation of cis-/trans-
isomers of butene-2 in the presence of samples that
had already participated in the process of traditional
catalytic cracking occurs with the participation of
protic acidic centers. It was established that the higher
isomerization ability of the samples that had already
participated in the process of oxycracking was due to
changes in the structure of active centers, particularly
the formation and participation of surface oxygen cen-
ters embedded in the structure of the products of oxi-
dative compaction. Our conclusions on the change in
the nature of the active centers of ZCC samples allows
us to explain the enhanced activity and stability of the
samples that had already participated in the process of
oxycracking and butene-1 isomerization.
REFERENCES
1. G. K. Boreskov, The Application of Zeolites in Catalysis
(Nauka, Novosibirsk) [in Russian].
2. J. A. Rabo, Zeolite Chemistry and Catalysis (Amer.
Chem. Soc., Washington, 1976), Vol. 1.
3. K. G. Ione, Polyfunctional Catalysis on Zeolites (Nauka,
Novosibirsk, 1982) [in Russian].
4. Kh. M. Minachev and V. V. Kharlamov, Redox Catalysis
on Zeolites (Nauka, Moscow, 1990) [in Russian].
The catalytic activity of POC has been verified
experimentally a number of times [32, 36–39]. In
addition, the availability of the atomic О– anion-radi-
cal, which according to present concepts plays a key
role in a number of processes of oxidative catalysis, is
not inconceivable [4, 40–45]. The oxygen atom in the
POC composition displays high affinity toward elec-
trons and is therefore capable of polarizing the double
bond in butene-1 and playing the role of a basic center.
5. D. Breck, Zeolite Molecular Sieves (Wiley, New York,
1974).
6. G. G. Volkova, S. D. Badmaev, L. M. Plyasova, and
E. A. Paukshtis, Bifunctional Catalysts for Production of
Ethyl Acetate, Hydrogen and iso-Alkanes (Inst. Katal.
SO RAN, Novosibirsk, 2013) [in Russian].
7. R. R. Aliev, Catalysts and Petroleum Refining Processes
(VNIINP, Moscow, 2010) [in Russian].
8. S. N. Khadzhiev, Cracking of Petroleum Fractions on
Zeolite-Containing Catalysts (Khimiya, Moscow, 1982)
[in Russian].
The data from thermal analysis also indicate the
products of compaction that formed on the ZCC sam-
ples during both types of cracking differ in structure.
The sample subjected to traditional cracking for
15 min was characterized by the presence of a single
exothermic peak with a maximum at 525.5°C. The
samples that had already participated in the process of
oxycracking for 15–60 min displayed two exothermic
peaks with maxima at 398–407 and 485–504°С,
respectively (Table 2, Fig. 1). The observed 40–125°С
reduction in the maxima of exothermic peaks indi-
9. S. Raseev, Thermal and Catalytic Processes in Petroleum
Refining (CRC, Boca Raton, FL, 2003).
10. A. V. Vosmerikov, Extended Abstract of Doctoral
(Chem.) Dissertation (Inst. Petroleum Chemistry
Siberian Branch of RAS, Tomsk, 2009).
11. N. A. Zakarina, O. K. Kim, and L. D. Volkova, Nefte-
pererab. Neftekhim., No. 3, 30 (2011).
12. M. Nikazar, K. Gholivand, and K. Mahanpoor, Kinet.
Catal. 48, 214 (2007).
RUSSIAN JOURNAL OF PHYSICAL CHEMISTRY A Vol. 90 No. 8 2016

1538
MURSALOVA et al.
13. E. V. Smidovich, Technology of Oil and Gas Refining. 29. K. Tanabe, Solid Acids and Bases: Their Catalytic Prop-
Ch. 2: Cracking of Petroleum Raw Materials and Refin-
ing of Hydrocarbon Gases (Khimiya, Moscow, 1980) [in
Russian].
erties (Academic, New York, 1971; Mir, Moscow,
1973).
30. B. V. Voitsekhovskii and A. Korma, Catalytic Cracking.
Catalysts, Chemistry, Kinetics (Khimiya, Moscow,
1990) [in Russian].
14. V. M. Kapustin and A. A. Gureev, Technology of Petro-
leum Refining. Ch. 2: Destructive Processes (KolosS,
Moscow, 2008) [in Russian].
31. V. P. Shmachkova, N. S. Kotsarenko, and E. A. Pauk-
15. V. P. Sukhanov, Catalytic Processes in Petroleum Refin-
shtis, Kinet. Catal. 45, 554 (2002).
ing (Khimiya, Moscow, 1979) [in Russian].
32. T. G. Alkhazov and A. E. Lisovskii, Oxidative Dehydro-
genation of Hydrocarbons (Khimiya, Moscow, 1980) [in
Russian].
16. V. A. Likholobov, Ross. Khim. Zh., No. 4, 6 (2007).
17. A. V. Glazov, V. N. Generalov, V. I. Gordenko, et al.,
Ross. Khim. Zh. 51 (4), 57 (2007).
33. E. A. Paukshtis, L. V. Malysheva, N. S. Kotsarenko,
and L. G. Karakchiev, Kinet. Katal., No. 2, 455 (1980).
18. V. P. Doronin, P. V. Lipin, O. V. Potapenko, et al.,
Katal. Promyshl., No. 5, 82 (2014).
34. Yu. G. Egiazarov, M. F. Savchits, and E. Ya. Usti-
lovskaya, Heterogeneous Catalytic Isomerization of
Hydrocarbons (Nauka Tekhnika, Moscow, 1989) [in
Russian].
19. A. B. Bodryi, E. M. Rakhmatullin, G. F. Garieva, and
R. S. Ilibaev, Katal. Promyshl., No. 5, 19 (2014).
20. E. A. Guseinova, L. A. Mursalova, and K. Yu. Adzhamov,
in Proceedings of the 8th All-Russia Conference with Inter-
national Participation of Young Scientists on Chemistry
Mendeleev-2014, St. Petersburg, Sect. 5, p. 238. http://
mendeleev.spbu.ru/files/Theses_Mendeleev_2014_2.pdf.
35. F. Trifiro and S. Carra, React. Kinet. Catal. Lett. 2, 411
(1975).
36. J. M. L. Nieto, Top. Catal. 15 (24), 189 (2001).
37. I. G. Danilova, E. A. Paukshtis, A. V. Kalinkin,
A. L. Chuvilin, G. S. Litvak, A. A. Altynnikov, and
V. F. Anufrienko, Kinet. Catal. 43, 698 (2002).
21. E. A. Guseinova, L. A. Mursalova, and K. Yu. Adzhamov,
Azerb. Khim. Zh., No. 3, 37 (2014).
22. Inst. Katal. SO RAN, New Technologies and Catalysts
38. A. A. Knyazeva, O. V. Vodyankina, and L. N. Kurina,
for
Petroleum
Processing
and
Chemistry.
Russ. J. Phys. Chem. A 75, 872 (2001).
http://www.nccp.ru/upload/iblock/47f/47fab8b8dde2
39. A. E. Lisovskii, Extended Abstract of Doctoral
b459ed04808fa6c81e52.pdf.
(Chem.) Dissertation (Moscow, 1983).
23. L. A. Mursalova, E. A. Guseynova, M. R. Salayev, and
K. Yu. Adjamov, in Proceedings of the 12th European
Congress on Catalysis EuropaCat-XII, Kazan, Russia,
Aug. 30–Sept. 4, 2015.
24. R. B. Sedgkhi, Extended Abstract of Cand. Sci.
(Chem.) Dissertation (Gubkin Russ. State Oil and Gas
Univ., Moscow, 2013).
40. G. I. Panov, K. A. Dubkov, and E. V. Starokon, Catal.
Today 117, 148 (2006).
41. A. M. Volodin, S. E. Malykhin, and G. M. Zhid-
omirov, Kinet. Catal. 52, 605 (2011).
42. I. L. Zil’berberg, Extended Abstract of Doctoral
(Chem.) Dissertation (Boreskov Inst. Catalysis, Siber.
Branch RAS, Novosibirsk, 2013).
43. A. N. Il’ichev, M. D. Shibanova, A. A. Ukharskii,
A. M. Kulizade, and V. N. Korchak, Kinet. Catal. 46,
387 (2005).
25. I. P. Mukhlenov, Technology of Catalysts (Khimiya,
Leningrad, 1979) [in Russian].
26. T. S. Glazneva, N. S. Kotsarenko, and E. A. Paukshtis,
Kinet. Catal. 49, 859 (2008).
44. V. B. Kazanskii, Kinet. Katal. 14, 95 (1973).
27. I. I. Reshetov and V. A. Dobrotvorskii, Heterogeneous
Catalysis: Physicochemical Principles (Khimiya, Lenin-
grad, 1985) [in Russian].
28. K. V. Topchieva and Ho Shi Thoang, Activity and Phys-
icochemical Properties of High-Silica Zeolites and Zeo-
lite-Containing Catalysts (Mosk. Gos. Univ., Moscow,
1976) [in Russian].
45. R. M. Kenzhin, Extended Abstract of Cand. Sci.
(Chem.) Dissertation (Inst. Catalysis named by
G. K. Boreskov, Siber. Branch of RAS, Novosibirsk,
2014).
Translated by L. Brovko
RUSSIAN JOURNAL OF PHYSICAL CHEMISTRY A
Vol. 90
No. 8
2016