SCIENTIFIC ABSTRACT AGAFONOV, A.V. - AGAFONOV, B.S.

• Document Type: CREST
• Collection: Scientific Abstracts
• Document Number (FOIA) /ESDN (CREST): CIA-RDP86-00513R000100420019-4
• Release Decision: RIF
• Original Classification: S
• Document Page Count: 100
• Document Creation Date: November 2, 2016
• Document Release Date: June 5, 2000
• Sequence Number: 19
• Publication Date: December 31, 1967
• Content Type: SCIENCEAB

SOV/68-58-11-lV25
AUTHORS: Vorozhtsov N.N. , Corresponding Member of the
Academy of
Science of the USSR, Doctor of Chemical Science,
Lisitsyn V.N., Candidate of Chemical Science,'Agafonov A-V.
and Krasivichev V.V. , Candidates of
Tech~rucal'~'Sci-e-n-t-e~-
and Abayeva B.T., Candidate of Chemical Science
TITLE: Transformation of Higher Homiolo,7ues of Phenol into
Lower
0
Ones (Prevrashcheniye vysshikh gomologov ~Cenola v
nizshiye)
PERIODICAL; Koks i Maimiya, 1958, Nr 11, pp L~2-1+7 (USSR)
ABSTRACT: The results of an investigation on the
dealkylation of
technical xylenol with simultaneous alkylation of benzole
in a pilot plant of the All-Union Scieiltific Research
Institute of -.the Petrolew--a Indusiu-ry in which bead
--aluminosilicate was used are described. This was a
continuation of the previously published work (Ref 1) on
the transformation of xylenols (on interaction with
benzole) into phenols and cresols on cracking under mild
conditions on an aluninosilicate catalyst. The e--.peri-
Card 1/3 "'tal plant used (Fig 1) is outlined. it was
established
that, on passing -.ylonol in mixture with benzole

ISOV/68-58-11-14/25
Transformation of Higher Homologues of Phenol into Lower Ones
Z>
(1 -# 3.65 by weight) over alui-Anosilicate catalyst at
C'
temperatures ill the range 300-WOOC and volume velo-
cities of 0.42-1.47hr-llup to 60,,'~o (on weight of starting
xylenol) of phenolic compounds (phenol, o-, m- and p-
cresols xylenols)including 20-220" of phenolic-cresolic
7 P
fractioN axe obtain~ed. Sir:iultaneously 11-19% of benzene
homologuej with a boiling temperature of 100-1850C and
13-18% of neutral compounds with boiling temperatures
above 1850C are formed. 8-25/"o' of coke is deposited on
the catalyst. The influence of the temperature of the
reaction, the volume velocity of reactants (Table 1),
additions of water vapour and various proportions of
benzole (Table 2) on the transformation of xylenol and
changes in the activity of the catalyst wit1h time of
operation (Table 3) were established. It was found that
at temperatures 300-3200C and volume velocities 0.92-
1.47hr-1 more phenolic-cresolic fraction and less of
neutral compounds and coke on the catalyst is obtained
Card 2/3 (taking into consideration the transformation of
xylenol).
At 3000C and a volume velocity 0.92hr-l 330ka of

O-OV/68-58-11-14/25
Transformation of Higher Homologues of Phanol into Lower
Ones
.0henolic-cresolic fraction and about 200kg of benzene
6mologues with a boiling temperature 100-1850C can be
0
obtained from 1 ton of xylci-iol.
There are 3 cables, 3 figures and 6 references (1+ Soviet,
1 English and 1 German)
ASSOCIATIOII: MTI im. Dj. Mendelayevaj, VM VP
Card 3/3

AGAFONCV, A. V., ZHERDE7A, L. G.. KARASEVA, A. A..
VOZNESENSKAYA, E. V.,
AI%TUMF,-A-.E., KROL, B. B., OROCHKO, D. I.. AKIMOV, V.
S., MIMYLOV, B. B.,
DRUMnMA, A. V.
"Production of Lubricating Oils and Paraffin from
Sulfurous Oils
in the USSR."
Report submitted at the Fifth World Petroleum Congress, 30
May -
5 June 1959. Now York City.

~AGAFONOV, A. V.,, TOPCH=E A, K. V., KALIKO, E.
A., PIGUZOVA, L. I.
AGAFONOV~ A.-V., PANCHEMKOV, G. E., KAYAKIN, X.
E., YIRSIKIY, Y. S.
"Studying the Nature of Activity of
Alumosilicate Catalysts."
Report subritted at the Fifth World Petrolewr
Con..--*ress, 30 Yv -
5 June 1959. New York.

sov/65-59-4-4/14
AUTHORS: Agafonov, A*V*, Abayeval B.T., Andr~eyevaq A*S.s
-Eyge-n-9-5-n-,-- ".., Kantor, I.I. and Ivchenko, Ye-G.
TITLE., Catalytic Cracking of Crude and Hydro-Purified Vacuum
Gas-Oil from Arlan.. Petroleum (Katitlitieheakiy kreking
iskhodnogo i Sidroochishchennogo vakuumnogo gazoylya
arlanskoy nefti)
PERIODICAL: Khimiya i tekhnologiya topliv i masel, 1959, Nr 4,
pp 18-24 (USSR)
ABSTRAM Vapuum gas-oil from Arlan. petroleum contains 3.2%
sulphur compounds, 0.11% nitrogen compounds and 24Y4
tarry substances; these quantities are larger than
the corresponding quantities in heavy gas-oil from
Tatar;*hand Bashkiriya petroleums. These components
block the active surface of the catalyst during ,,
cracking, prevent the access of hydro-carbon molecules
and therefore decrease the degree of conversion of the
crude material. Considerable amounts of coke are
deposited on the catalyst which inhibits secondary
reactions and leads to decreased yields and inferior
quality end-products. Hydro-purification was carried
Card 1/5 out on a continuous apparatus in the VNII NP by

sov/65-59-4-4/14
Catalytic Cracking of-Crude and Hydro-Pur.ified Vacuum
Gas-Oil from
Arlan.'. Petroleum
N#A,Chepurov and R.N.Yudinson; a stationary aluminium-
cobalt-molybdenum catalyst was used at 380 0C, a pressure
of 50 atm and space velocity of the supplied crude
material of 0.7 hour-1. The properties of the starting
material and of the hydro-purified vacuum gas-oll are
tabulated (table 1). The octane number of the end
product was appreciably higher than when using
fractional distillation (58-5 as compared to 41.0)
and contained considerably less su43hur (0-013 as
against 0-17%). The properties of the gas-oil fractions
are listed in table 2. Cracking experiments of both
the crude and hydro-purified vacuum gas-oil were carried
out on a pilot plant with a synthetic bead catalyst at
temperatures within the limits of 430 to 520 0C,
atmospheric pressure and a space velocity of 0.65 to 1.5,
calculated on the volume of the catalyst per hour. The
ratio of the catalyst to the crude material was constant
Card 2/5 in all experiments and equalled 5:1 (table 3).
Optimum

sov/65-59-4-4/14
Catalytic Cracking of Crude and Hydro-Purified Vacuum Gas-Oil
from
Arlan Petroleum
yields of petrol were obtained at temperatures between
450 and 4750C when the optimum space velocity of the
supplied raw material was within the limits of 1.0 to
0.65 hours-1. The hydro-purified vacuum gas-oil
could more easily be processed; an optimum yield of
light components at the same space velocities was
achieved at 50*C. The authors concluded that the
presence of a considerable quantity of light fractions
boillng up to 3500C (37.6 as against 19.4%) influences
the yield of the light components. The optimum yield
at this temperature reached-66 to 67% by weight as
against 58 to 59%. Results of the cracking experiments
indicate (Fig 1) that the hydro-purification of the crude
(by separating thetarry substances, metals, sulphur and
nitrogen) improves the process conditions and also the
yields and properties of the cracking products (compare
table 4). The gasoline obtained by this process is less
unsaturated, contains more aromatic compounds and has
Card 3/5 higher octane numbers (80 to 81.5 as compared to

sov/65-59-4-4/14
Catalytic Cracking of Crude and Hydro-Purified Vacuum Gas-oil
from
Arlan Petroleum
77.7 to 8o.7) (Fig 2). A lower content of unsaturated
compounds renders the gasoline more stable. Its
induction period exceeds 600 minutes. The light
catalytic gas-oils, obtained during the cracking of
hydro-purified crudes, show improved properties. Their
cetane number is 34 to 38 (as against 30 to 33) and they
contain 0.21 to 0-38% sulphur (as against 2.6 to 3.3%)
(Fig 3). These light gas-oils can be used directly as
components of diesel fuels. The heavy catalytic gas-oils
(fractions boiling above 3500C) can be used for the
production of lubricating oils or re-used as recycles.
In both cases 2 to 3% of the tarry (tail) fractions have
to be separated. The gaseous hydrocarbons produced
by this process are of interest as starting materials
for petro-chemical syntheses. The influence of the
temperature on the ratio of unsaturated and saturated
Card 4/5 hydrocarbons in gaseous reaction products, and on the

sov/65-59-4-4/14
Catalytic Cracking of Crude and Hydro-Purified Vacuum
Gas-Oil from
Arlan: Petroleum
content of unsaturated hydrocarbons in the gas, is
shown in a graph (Fig 4). There are 4 figures,
4 tables and 2 English references.
Card 5/5

SOV/65-59-4-5/14
AUTHORSt
Agafonovs A-V-9 Basov, A.Ne, Manakov,
N.Kh. and

Wa _ns ~In ~,, ~ -
TITLE:
Combined Plant for Fractional
Distillation of Petroleum

and of Catalytic Cracking Residues on
a Microspherical

Natural Catalyst (Kombinirovannaya ustanovka
pryamoy

peregohki nefti i kataliticheskogo krekinga
ostatochnogo

syr1ya na mikronferiche&kom prirodnom
katalizatore)
PERIODICAL:
Xhimiya i tekhnologiya topliv i masel,
1959, Nr 4,

PP 25-31 (USSR)
ABSTRACT:
Petroleum refineries have
to process asphalt-tar

substances of petroleum which can be
extremely difficult.

Processing methods hitherto applied use
high temperatures

(above 4500C) at high or low pressures. A
high yield of

tarry residues and poor quality gasoline or
distillate.

fractions and petrols of low quality and also hard

residues in the form of petroleum coke are obtained by

thermo-cracking. The temperature is an important factor

during
thermal destructive processes. It has been found

that
temperatures should be selected to give fractions
Card 1/4
with
octane numbers exceeding 70 and that the cetane

sov/65-59-4-5/14
Combined Plant for Fractional Distillation of Petroleum and of
Catalytic Cracking 'Residues on a Microspherical Natural
Catalyst
number of the diesel fuel fraction should not exceed
42 to 43. The VNII NP have developed an economical
catalytic destructive process for the treatment of
residual petroleum crudes which makes it possible to
obtain high grade gasoline and diesel fuels in
industrial quantities. The process was tested under
laboratory, pilot plant and industrial conditions.
The VNII NP is, in collaboration with the Giproneftezavod
Institute, at present designing two plants where the
simultaneous fractional distillation and catalytic
cracking of the petroleum crude can be carried outq one
with an annual capacity of 2 million tons and a second
of 3 million tons. The lay-out of both factories will
be the same as is shown in Fig 1. The asphalt-tar
substances will be subjected to the direct action of
aluminium silicate catalysts which will be sufficiently
active to ensure decomposition of the high molecular
petroleum fractions (boiling above 530 to 550*C). The
light gas-oil fractions of the petroleum will not be
Card 2/4 decomposed and the cetane number of the diesel fuel

sov/65-59-4-5/14
Combined Plant for Fractional Distillation of Petroleum and of
Catalytic Cracking Residues on a Microspherical Natural
Catalyst
fraction, obtained during the process, should be 42 to
43 or higher. The newly-formed fraction of the gasoline
should have an octane number of 76 to 78 and above. The
crude petroleum or fuel oil can be directly supplied into
the reactor. Various further improvements in the process
are described. The percentage composition of the end
product obtained on a natural microspherical catalyst in
an industrial plant is given, as well as experimental
data, obtained by VNII NP during 1958, on fuel oil
subjected to catalytic cracking on a pilot plant. The
coke deposited on the catalyst can be separated by
roasting at a temperature of about 600*C; the importance
of the catalyst is discussed. By using pneumatic
transport for the catalyst in a highly concentrated
current it is possible to decrease the height of the
plant and, therefore, to lower construction costs. The
regeneration of the catalyst is intensified. The
considerable enlargement of the desorption zone in the
Card 3/4 reactor, and also the creation of a counter-current

sov/65-59-4-5/14
Combined Plant for Fractional Distillation of Petroleum and of
Catalytic Cracking Residues on a Microspherical Natural Catalyst
desorption zone in the regenerator for degasification
and activation of the regenerated catalyst, decreases
coke-formation and the yield of methane, gives higher
grade gasoline and simplifies the further separation
of cracking gazes. Practically all the heat,
generated by burning the coke and other component
gases, is utilised. These vapours are used as power
and also for desorption or for heating. The plant is
also equipped for utilising the effluents. Comparative
technical and economical characteristics are listed in
a table. The authors also refer to a relevant article
by Sherwood which was published in "Petroleum", 1959, Nr 2.
There are 2 figures, 1 table and I English reference.
Card 4/4

sov/65-59-4-7/14
AUTHORSs Agafonov, A.V., Soskind, D.M., and Abayeval B*T#
TITLE., -TH-e ~Operation and Methods of Reconstruction of
Catalytic
Cracking Plants Where Bead Ca%:,alysts are Used (Opyt
ekspluatatsii i puti rekonstraktsii ustanovok
kataliticheskogo krekinga s s,harikovym katalizatorom)
PERIODICALtKhimiya i tekhnologiya topliv i masel, 1959, Nr 4,
PP 34-44 (USSR)
ABSTRACT: Investigations were carried (.,ut in the VNII NP which
made it possible to work out conditions and make
recommendations for the manu.,.,"acture of high quality
petrols. Heavy distillates, boiling at temperatures
between 300 and 5000C, can b,jj used. The process is
carried out in one stage and., therefore, the efficiency
of the plant increased by 30 to 35%. The properties of
the gas-oil fractions of Rom.hshkiiya'. petroleum are
given in table 1. It can be seen that the heavy crudes
differ from the kerosine-gas.-oil fractions by their high
boiling and solidification p-)ints, by their high content
of tar, sulphur and aromatic compounds as well as by
Card 1/3 appreciable content of polyc.,rclic aromatic compounds,

sOV/65-59-4-7/14
The Operation and Methods of Reconstruction of Catalytic
Cracking
Plants Where Bead Catalysts are Used
asphaltenes and metal salts. Various investigations
carried out in the Novoufimka - plant during 1954 to
1955, and modifications of the plant carried out at the
time, are discussed in detail. The reconstructions,
carried out at pre-sent, aim to increase the efficiency
of the plant 1-5-fold (first modification) and 1-7-fold
(second modification) without altering the principal
layout of the plant. A further reconstruction is to
achieve a considerable improvement in the conversion
process which will increase the efficiency of the
plant by 100% (third modification), The first
modification is based on recommendations made by the
authors, the Novmxfimk& factory Giproneftemash and
Giproneftezavod. This type of reconstruc-~ion was carried
out on one plant of the NUNPZ and three plants of the
Salavatskiy factory. The various modifications are
listed in a table on page 40 and the most important of
these discussed in detail. Table 2 shows the improvements
achieved during 1956 to 1957 and the first nine months
Card 2/3 C'f 1958 in various plants where the recommended

sov/65-59-4-7/14
The Operation and Methods of Reconstruction of Catalytic
Cracking
Plants Where Bead Catalysts are Used
reconstructions have been carried out. The second
modification was recommended by GrozNII and
Giproneftezavod and the third by VNII NP and
Giproneftemash. The lay-out of the last plant is given
in Fig 3 and the authors suggest that this last
modification should only be incorporated in newly-
erected plants. There are, however, various drawbacks
e.g. the circulation time of the catalyst is rather low,
the generator is not completely efficientt the cooling
pipes of the regenerator are unsatisfactory and this
leads to an increased catalyst consumption. There are
3 figures and 2 tables.
Card 3/3

L5.383
B/081/63/000/002,/069/088
B160/B144
AUTHORSt Osipov, L. N., Golldshteyn, D. ., Agafonovj A. Vo
TITLEa Hydrofining of diesel fuels
PERIODICALt Referativnyy zhurnal. Khimiyaj no. 2, 19631 461,
abstract
2P128 (Tir. Vses. n.-i.-in-t po pererabotke nefti i gaza i
poluoheniyu iskusety. zhidk. t(,plival no. 81 1959P 54 - 73)
TEM The process of hydrofining sulfurous straight-run
distillates and
secondary distillates was studied in laboralory high-pressure
circulation
equipment with an industrial Al-Co-Ido catalyst. The rate of
hydrating- the
S-compounds and unsaturated hydrocarbons at the given partial
H 2 pressure
is shown to increase as the temperature rises to 42000; at a
higher temper-.
ature of the order of 46000 the rate of hydration decreases.
The optimum
partial H2 pressure in the hydrofining of diesel-fuel
distillates depends-
on the chemical composition of the crude. Hydrofining of
low-aromatic
distillates can be carried out at a comparatively low partial
H 2 pressure
(15 - 20 atm.) and hydrofining of aromatized distillates (e.g.
catalytic-
Card 1/2

11
Hydrofining of diesel fuels
S/08-1/63/000/002/069/088
B160/W44
cracking distillate) at a high partial H2pressure. In the
process of
hydrofining low-aromatic distillates at a comparatively low
partial H2
pressure, the amount of H2consumed in the reaction decreases as
the temper-
ature of the processes rises (> 3800C) as a result of
dehydration of the
naphthene hydrocarbons contained in the crude. Certain gases
containing
H21 which are produced in a number of processes (e.g.
the-ciroulating waste
gas of the hydroforming process) can be used for hydrofining
straight-run
a-ncl other low-aromatic distillates. 16 references.
LAbstracter's notei
Complete translation.)
to
Card 2/2

hG-'AF-ON0k,~ A-
PHASE I BOOK EXPLOITATION SOV/4659
Osnory tekbnologii neftelrbimicheakogo sinteza (Fundamentals of
Synthesis Technologjr
in Petroleum Chemistry) Moscow, Gostoptekhizdat, 1960. 852 P-
3,800 copies
printed.
Eds.: Dintses, Arkadiy Iltich,, Professor, and Lev Aleksandrbvich
Potolovskiy,
Professor; Executive Ed.: L.A. LIvova; Tech. Ed.: B.A. Mukhina.
PURPOSE: This book is intended for engineers and chemisi. s of
petroleum refineries
and cherd-cal plants,, for councils of the national eco~-,omy.
planning organizatioaq
and scitutific research institutes engaged in chemical processing
and large-
scale utilization of petroleum stock for the production of
synthetic products.
COVERAGE: The book describes important connercial methods of
producing hydrocarbun
peiroleum and gas stock and coal stock for the manufacture of
alcohols, aldehyde4
ketones, acids, detergents, synthetic fibers., and synthetic
rubber. Flav sheets
are included, and the badic equipaent of the yetrocbemical
industry is described.
The physicochemical properties and use of intermediate and end
synthetic products
an also described. The state-of the petrochemical industry outside
the USSR
and prospects for its development are covered.- No personalities
are mentioned.
C e nces follow each chapter.'

Fundamentals of Synthesis Technology (Cont.) sov/4659
TABLE OF CWTENTS:
Foreword 3
Cho I*
Development of Petroleum Refining and Petrochemical
Processing
7
I.
From straight-run distillation of petroleum to
the petrochemical

industry (rav materials for the manufacture
of petrochemicals

(A.I. Dintses]
7
II.
Petrochemical processing
industry abroad [L.A. Potolovskiyj
15
Ch. II.
Processes of Raw
Material Production for the Petrochemical Industry

[B.T.
Abayeva and A.V. Agafonov)
40
I.
Destructive
dis"l1atro_aof__j;_fi_62:eum, the main source of raw

materials for petrochemical. processing
40
II.
Thermal cracking
41
III.
Pyrolysis of hyftocaYbon gases and liquid petroleum
products
47
lo
Chemical nature of the pyrolysis process
48
2.
Pyrolysis of 34quid raw materials
51
3.
P7rolysis of gateous
raw materials
-60--
4.
Tube heaters for the pyrolysis process
69
IV.
Cooking of petroleum residue
71
V.
Catalytic cracking of
petroleutn products
716
CtLrd 2M

AGUMNOV., A.V..,- WM=t B.T.; OKMHMGHs N.A.
Distribution of mO-fur in the cracking products, of
heavy oh&rge
stocke& Nbim,sera-i azotorg.soed,sodev neftei
nefteprod. 3j183-192
f6oo (mm 14-.6)
1. VessoyusM nauchno-issledavatellskiy institut po
pererabotke
nefti i gaza i polucheniyu iokusstvennogo zhidkogo
toplivas
(Petroleum ja;duots) (*afur organic compounds)

GOLIDSHTRYNp D,L,; OSIPOV2 L.N*; AGM=t AJ.
Selective ~*Irofining of catalytically cracked poolines,
Khtmeserew
i azotorg.soedsod.v neft.i'nefteprod. 3089-395 .160.
(MIRA 14:6)
1. Vseoo)ruzW nauchno-issledovatellskiy institut po
parerabotke
mfti i gaza i polucheni7u iskuostvannogo zhidkogo
topliva.
(Gasoline), (Graoking process')

s/o65/6o/ooo/oo6/oo6/oo,1i/.,x
E194/E484
AUTHORS:
Agafonov, A. ., Gellms, I,E, and Rabikovich, E.I.

TITLE:
The Felectl-o-n-df Catalyst for CrackingAResidual

Petroleum
Fractions and Study of its Poisoning During

the Process

PERIODICAL:
Khimiya i tekhnologiya topliv i masel, 1960, No.6,

pp.6-12

TEXT: A sp
ecial feature of the operating conditions of
catalyst

when crackin
catalyst by
g residual feed is the high rate of poisoning of the
the combined influence of temperature, steam, sulphur

compounds
an
d resinous substances containing metallo-organic

compounds.
The
poisoning is specially marked with catalyst in

powder form,
The
high molecular hydro.-carbons of the heavy part of

the feed are
the main source of products that are of low stability at

temperatures
used for cracking so that there is no need for a
great

reduction in
the energy of activation. Moreover, the use for
this

purpose of h
igh activity catalysts is accompanied by
considerable

increase in
gas and coke formation. The measure of
the necessary

activity of
catalyst used in cracking residual feed
should be the

production o
f gasoline of good engine properties
combined with

Card l/ 4

S/065/60/000/006/oo6/oo8/xx
E194/E484
The Selection of Catalyst for Cracking Residual Petroleum
Fractions
and Study of its Poisoning During the Process
favourable gas composition and a high rate of conversion of the
residual fractions. It is desirable to use large plants for
cracking residual fractions which requires large quantities of
catalyst of appropriate quality. It is found that the requisite
conditions are satisfied by fire--resistant high.-alumina kaolin
clays,
many kinds of which after simple heat treatment have sufficiently
good and stable catalytic properties. Table I gives the
characteristics of semi-industrial quantities of natural
catalysts
obtained from various natural clays. In this table the activity
of
the catalysts is characterized by the cracking of light feed as
this
gives the more sensitive index of performance, Catalyst poisoning
is then considered and Table 2 gives experimental data about the
deactivation of a simple, natural, microspherin-al catalyst.
Characteristics of the cracker feed-stocks are given in Table 3.
The tests, results of which are given in Table 2, were continued
for
20 days and the observed changes in catalyst properties may be
considered as the results of poisoning by metals and sulphur
combined with poisoning due to reduction in the surface and
porosity
Card 2/4

s/o65/60/000/006/oo6/oo8/xx
E194/E484
The Selection of Catalyst for Cracking Residual Petroleum
Fractions
and Study of its Poisoning During the Process
caused by heat and steam. The selectivity of the catalyst was
much reduced. Comparison between the test results and those of
laboratory tests with artificial poisoning of the catalyst by
metal
showed that in the tests most of the poisoning was due to
metals and
not sulphur, see Table 4. The influence of metals deposited on
the
catalysts on certain characteristics of cracking of distillate
and
crude oil feeds are given in Table 5. Note should be made of the
much smaller degree of poisoning of the catalyst by an equal
quantity of deposited metal when cracking residual feed rather
than
distillateo The influence of steam was studied in the laboratory
and the results are given in Table 6; it will be seen that
treatment of poisoned catalyst by steam promotes recovery of
activity and improves the selectiveness, It is concluded from
the
work that catalytic cracking of' residual feed stock on micro-
spherical natural catalyst is practical and a stable process
can be
achieved. The capital cost of constructing a catalyst
manufacturing works should not be above 500 roubles per ton of
catalyst produced per year, Investment in quarries and other
Card 3/4

S/065/6o/000/006/006/008/XX
E194/E484
The Selection of Catalyst for Cracking Residual Petroleum
Fractions
and Study of its Poisoning During the Process
workings is from 100 to 200 roubles per ton per year. The cost of
one ton of finished catalyst is about 400 roubles, It is
calculated that the use of natural catalyst rather than synthetic
economizes both capital investment in the production of catalyst
and the cost of the first charge by not less than 15 roubles for
each ton per year of feed stock delivered for catalytic
crackings.
Accordingly, the economy that results from the use of natural
rather than synthetic catalyst for cracking residual feed stock
is
considerable,, There are 6 tables and 8 referencesg 2 Soviet and
6 English.
ASSOCIATION: VNII NP
Card 4/4

5/06~~/61/000/004/00.5/011
F
a94
AUTHORS: Bogov, S. P., Danilevicb, A.
F., Golldebtayn. D. L.,
Pjrnakov, M. V. and Agefonov A. V.
TITLE: Ey`&-6rI]M_S__c? Wbricating Oils
F" ODICAL: rhimiya I tekhnologiya topliv
I masel, 1961. No. 4,
pp. 23-.27
TE= 2 Hydrarining in under consideration
as a replacement
for earth treating In finishing of
solvent rarfinaten. This
-article describes tests on the
hydrofining of distillates (spi MI a
all and machize oil Type AC-S
(AS-5))'and residual do-waxed pheno,
rafrizates of the Novoku7bysbevsk MIZ.
The bydrofining was carried
out on a large leberatoz7 pilot plant
with gas circulation,
rinishing with ateam stripping. A study
was first made of the
Influence of pressure and it wan
concluded that the pressure of 40
atmogheres, the highest tried. was the
beat in respect at izprov-
Ing he viscosity index, reducing the
coke number and sulphur
content and Improving the colour of the
finished oils. The ratio
of volumes of oil per haur to volume of
catalyst ranged from I to
4. The Influence of treatment
temperature was then studied using
Card 1/5
an the one hand an
a1undnium-cobalt-mol7bdonum catalyst and
on the
other an aluminium-mol,7bdeaum catalyst.
Thane tests were made with
machine oil Type AS-5 at a total
pressure of 40 atm and a delivery
rate by volume relative to catalyst of 3
1/hours and a gas circul-
ation rate of 300 litres at n.t.p. per
litre of food at temperature;
of 275,, 300. 325 and 3W0. It was shown
that increasing the
temperature has Imuch the same effect an
decreasing the feed rate.
In a rule Increasing the temperature
somewhat increases the pour
KInt which rose from -28*0-vith a
treatment temperature of 350*C.
ables are t2jen given of the
characteristics of hydrofized spindle
(Table 3) and residual (Table 4) oils
under optimum process
conditions. Table 3 wan obtained vJtb an
aluminium-molybde=uz
catalyst and Table 4 with
aluminlum-cobalt-zolybdenum catalTat.

0/065/61/000/004/003/011

B194/E284

Hydraflaing of lubricating Oi
lo

Table 3

Yeed
Treated
Oil

500,

Viscosity contistok*s-

at 5O'C
19.03
18.74
18.25
at 100*C
4.87
4.80
4.77
Viscosity index
92.3
93.8
95.7
Pour
point *C
-14
-13
-12
Plash point *0
190
200
198
Colour KPA
2.5
1.5
1.5
Sulphur content %
weight
0.96
0.92
0.86
Coke So. % weight 2
Corr~
Jivit
Pinkovich
ma/m
0.03
6
65
0.02
2
13
0.01
-
,
y
g
Yield % weight
.
IOD.O
.
99.4
"a
Card 3/5

S/065/61/000/004/003/011
Z194/E284
Hydrofining of lubricating Oils
Table 4
Viscosity cantistokes: Feed Trestod Oil
at 50* 159-35 153-87
at 100 20.98 20.80
Viscosity index 85.1 88.4
Pour point *C -10 -8
71ash point *0 246 270
Colour IPA 6.5 3.5
Sulphur content % weight 1.03 0.81
Coke No. % weight 0.38 0.27
Yield % weight 200 ".1
The hydrogen consumption in treating the
distillate oil was 0.13%
weight and In treating the residual oil
0.15% weight. The results
of hydrofining and earth finishing are
then compared and It is
Card 4/,S
shown that hydrofinishing gave the
greater yield, about 2% c
di tillates and 4% an residual
lubricants. The hydrofineeL oils
ha:e lower coke number but there is some
loss In the viscosity and
a sligbt Increase in the pour point.
Hrdrofimln has little
Influence on-the chemical composition of
the lubricants. The
increase Is. TiBCOBity index on
b.7drafining mainly results from
newly formed paraffinic. naphthenic and
light aromatic hydrocarbons.
Pre"minary technical and economic
calculations show that hydro-
finishing of lubml-ants is promising an
a replacement for earth
treatment. There is not much to choose
between the performance
of the two catalysts tested but the
aluminium-molybdenum catalyst
Is cheaper. Pull scale tests carried out
at the tiovokuybysbovsk
11PZ confirm d the laboratory test
results of the MI NP. There
&r66 table: and 2 non-Soviat references.
ASSOCIATION: VNII KP
Card 5/5

AWANOVs A.V.o RrSAKOVI M.V., OOLDSiMN, D.L., GUSUMU,
YE.A.m
-...................r
.......-
Jlkf~VAJ,
TZ.A.,j POSHITNOVO V.N..,
Gewinming 'Von Motorenolen aus schwafelhaltigen
Raholen, dunh
Wdrierung.
Report to be submitted for the bmosium Lubricants "
Lubricatioup Dresden,. 27-30 June 1961

S/06 61/000/007/003/005
B124YB2o6
AUTHORSs Agafonov, A. V., Dubinin, M. M., Onusaytis, B. A.,
~ToIrocheshnikov, N. S.
TITLEg Studies on production and application of new selective
Ftdsorbents - molecular sieves - in the USSR
PERIODICALi Khimicheskaya promyshlennost', no. 7, 1961, 26 - 30
TEXTs The authors give a short summary of the main results of
studies in
the field of synthetic zeolites conducted in various
scientific institutes
in 1960 on the basis of the coordination plan of the Komissiya
po tseolitam
(Zeolite Commission). The Zeolite Commission under the
chairmanship of
Academician M. M. Dubinin was established at the Otdeleniye
khimicheskikh
nauk AN SSSH (Department of Chemical Sciences, AS USSR) in
1959, in order
to coordinate studies in the field of synthesis and
application of synthetic
zeolites. Its activities comprised: 1) development of
synthesis- and N/
technological processes for synthetic zeolites; 2)
investigation of struc-
tural properties and adsorption of synthetic and natural
zeolites, and
3) study of the application of synthetic zeolites for the
drying and sepa-
ration of gases. Crystallization of zeolites and their ion
exchange prop-
Card 1/5

Studies on production...
S/064/61/000/007/003/005
B124/B206
erties were investigated at the Institut fizicheskoy khimii AN
USSR
(Institute of Physical Chemistry, AS USSR) under the direction of
I. Ye. Neymark, zeolites of the types CaA, KA, LiA, BeA etc
having been
produced (the authors use the designations NaA, CaA, NaX and CaX,
approved
by the above-mentioned Commission, instead of the customary
designations
4A, 5A, 1OX and 13X). One of the institutes of the chemical
industry under
the direction of G. I. Mikulin and V. Ya. Nikolenko investigated
the tech-
nological conditions for the synthesis of zeolites, and one of
the insti-
tutes of the petroleum industry under the direction of Ya. V.
Mirskiy the
conditions for the production of crystalline zeolites of the type
NaA and
CaA in the laboratory and pilot plant. Optimum conditions for the
synthesis
of zeolites of the types NaA and NaX,as well as the ion exchange
for the
production of the CaA and CaX zeolites were studied in the
laboratory under
the direction of M. S. Misin and L. M. Maksimova. The conditions
for the
synthesis of zeolites of the types A and X were studied at the
institut
neftyanoy promyshlennosti (Institute of the Petroleum Industry)
under the
direction of A. V. Agafonov, L. I. Piguzova and B. A. Lipkind,
applying the
process used by N. S. Kurnakov (Ref. 31 Izv. AN SSSR# 69 1381s
(1937)) for
the production of Permutit. The use of aluminum sulfate and
aluminum oxy-
Card 2/5

S/064/61/000/007/003/005
Studies on production... B124/B206
chloride in the synthesis of zeolites was studied in a
laboratory of the
chemical industry under the direction of V. S. Vinogradova
and L. S. Kof-
man. The institut khimii AN Gruz. SSR (Institute of Chemistry
of the
Georgian SSR) under the direction of G. V. Tsitsishvili dealt
with the
kinetics of the crystallization of the NaA zeolites, and the
Institut
khimii silikatov AN SSSR (Institute of Silicate Chemistry, AS
USSR) under
the direction of S. P. Zhdanov with the optimum conditions
for the produc-
tion of Na zeolites by hydrothermal synthesis in the
temperature range of
from 70 to 2000C from strongly basic aluminum silica gels
with a base ex-
cess of 300 - 500%. The studies by the laboratoriya GEOKhI AN
SSSR
(Laboratory of the GEOKhI, AS USSR) under the direction of N.
I. Khitarov
dealt with the drying of gases by means of the natural
zeolites natrolite,
desmine, thomsonite and limonite, while the use of the
chemical-catalytical
method for the production of natrolite granules was tried
out* at the IGI
AN SSSR (IGI, AS USSR) under the direction of B. A. Onusavtis.
D. P. Dobychin elaborated a process for the proauction of
porous glasses
of the molecular sieve type yielding a molecular sieve with a
porosity
close to that of the CaA zeolite from the Uo,-7/23 (Na--7/23)
glass, and one
with a porosity similar to that of the NaX zeolite from the
14arlO/30
Card 3/5

S/064/61/000/007/003/005
Studies on production... B124/B206
(Na-10/30) glass. A number of investigations of the
structure and ad-
sorption of synthetic and natural zeolites was conducted at
the Institute
of Phvsical Chemistry, AS USSR under the direction of M. M.
Dubinin. The
distribution curves of the zeolite crystals were determined
by the elec-
tron microscope investigation conductad by V. M.
Luklyanovich.
D. P. Timofeyev studied the kinetics of steam adsorption,
A. V. Kiselev
the adsorption of nitrogen, benzene vapors and hexane on
the molecular
sieves NaA and CaX as well as the adsorption of benzene and
n-hexane and
their mixtures on the molecular sieve CaA. X-ray
photographic investiga-
tions were made under the direction of N. A. Shishakov.
Studies conducted
under the direction of I. Ye. Neymark at the Institute of
Physical
Chemistry, AS USSR showed that tha equilibrium adsorption
on zeolites is
well described by the potential theory, and that the
thermal stability of
zeolites drops in the sequence CaA>KA>Nak>NH 4A. The
properties of Soviet
and American molecular sieves during drying of gases were
compared at the
Leningradskiy tekhnologicheskiy institut im. Lensoveta
(Leningrad Techno-
logical Institute imeni Lensovet) under the direction of T.
G. Plachenov
and G. M. Belotserkovskiy. Studies on the drying and
purification of gases
by means of molecular sieves were conducted at the
Moskovskiy khimiko-,
Card 4/5

S/064/61/000/007/003/005
Studies on production... B124/B206
tekhnologicheakiy institut im. D. I. Mendeleyeva (Moscow
Institute of
Chemical Technology imeni D. I. Mendeleyev) under the
direction of
N. S. TorooheRhnikov and N. V. Kelftsev, and bv V, S,
Vinngradova,
L. S. Kofman and Ya. V. MirBkiy. In 1960 the Zeolite
Commission held
three meetings (in Moscow, Leningrad, and Groznyy) in the
form of scientific
colloquia with 120 - 150 participants. There are 4
referenoess 2 Soviet-
bloc and 2 non-Soviet-bloc. The two references to
English-language
publications read as follows: *R. Me Barrer, Brit. Chem*
Engel No* 5P 1
(1959) and US Patents 2882243t 28822449 1959-
Card 5/5

26520
S/065/61/000/008/003/009
01~0 E030/E135
AUTHORS: Rogov, S.P., Golldshteyn, D.L., Osipov, L.N.j and
Agafonov, A.V.
TITLEt Hydrofining the high-sulphur kerosine-gas oil fraction
of Arlan crude
PERIODICAL: Khimiya i tekhnologiya topliv i masel,
jL96lkNo.8, pp. 13-19
4
TEXT: The preparation of satisfactory diesel fuels from
Arlan crudes has been investigated by VNII NP. In the laboratory
straight fractions were hydrofined; this process lowers the
flash
point and it *as found necessary to remove subsequently the
fractions boiling up to 180 OC to keep the flash point in the
60-65 OC region. However, the diesel fuel then fails
specification
rocr 4749-49 (GOST 4749-49) and 305-58, on pour point (-9 OC
instead of -10 OC). However, hydrofining cat. cracked products
gives satisfactory diesel fuels, and it is recommended that
these
be blended with the straight run components. In order to
increase
the output of the benzine fractions, without raising the diesel
pour point, hydrofining experiments were then conducted on a
Card 1/2

Hydrofining the h'gh-sulphur ....
26520
s/Ob5/61/000/008/003/009
E03O/El35
tungsten-nickel oxide catalyst at 300 atmospheres pressure. one
can then obtain~about 20% benzine and 80% diesel fuel, the latter
being of satisfactory quality. However, the benzine octane number
is only about 50 and it should be used either for motor spirit
blending or for further platinum reforming.
There are 6 tables, and 3 Soviet references.
ASSOCIATION: VNII NP
Card 2/2

GLIENAN, L.S.; BOCHAROVp I.V.; VIEHMANP G.L.1 ABROSIMOV,
BOZ.; KIRILOVI
Ye.A.,- MELINIKOV; S.M.; ~GAFOIIOV, A.V.; SOSKIND, D.M.
Rebuilding catalytic e-raoking units with a combined
reactor-regenerator.
KHm. i takh. topl. i masel 6 no.llt6-10 N 161. (MIRA 14sU)
1. Gosudarstvennyy nauchno-issledcyvatellskiy i proyektnyy
institut
neftyanogo mashinostroyeniya.
(Craqking prociess)

SOV/6246
PHASE I BOOK EXPLOITATION
Boveshohaniye po tseolitem. lot, Leningrad, 1961.
Sintetiaheskiya tseolity; poluoheniye, isoledovaniya I
primenenlye
(Synthetic Zeolites: Production, Investigation,and
Use). Mos-
cov, Izd-vo AN SBBR, 1962. 286 p . (Series: Itst
Doklad~)
Errata Blip inserted. 2500 copies printed.
Sponsoring Agenoys Akademiya nauk SSSR. Otdeleniye
khimichaskikh
nauk. Nomisiya po tseolitam.
Rasp. Edo.: M. M./Dubinin, Academician and' V. V.
Serpinskly, Doctor
of Chemical-,Sciences; Bd.: Ye. 0. Zhukovskayaj Tech.
Ed.s Be Pe
Golub'.
PURPOSE: This book is Intended for scientists and
onginser:)ongaged
in the produation of synthetic zoolites (molecular
sieve .and
for.ohemisto in general.
Card 1/*,/j

Synthetic Zeolitess (Cont.) SOV/6246
COVERAGEs The book in a collection of reports presented at
the First
Conference on Zeolites, held In Leningrad l6 through 19
March 1961
at the'Leningrad Technological Institute imeni Lensovet,
and is
purportedly the first monograph on this subject. The
reports are
grouped into 3 subject areas: 1) theoretical problem of
adeorp-
tion on various types of zoolites and methods for their
investi-
gation, 2) the produation of xeollteap and 3) application of
zeolites. No personalities am mentioned. References follow
in-
dividual articles.
TABLE OF CONTENTS
Foreword
Dubinin, X. X. Introduction,
Card 2/0

Synthetio Zoolitesi (cont.)
30V/6246
MisInA M. 3.m L. M.
~hkeimova, V. A. Litvinova, and L. B.

Khandros. Produotion
and Adsorption Properties of

NaA, NaP, CaA and CaP Zoolites
135

O
Klein, It. S L r3k va, V. A. Lltvinova, L. B.
*
'

Nia and L Urin. Produotion
v
Khandros:
:?~t.P=rO1y:=F