Nanotechnology for Oil Refinery

1. Diesel Fuel Hydroskimming Heavy Catalysts (Nebula Type) Production Technology
Light Hydroskimming Catalyst Production Technology
Catalyst type: carrier: aluminum oxide Active
component: nano-modified cobalt-molybdenum
2020 203020152010
Number of units
Total capacity, kta
Annual consumption,
tons
Annual consumption,
$mln
—
—
—
—
—
—
—
—
—
—
—
—
1–2
1 000–2 000
200–300
10–15
Strategic Goals of Russian Producers
Technology
2020 203020152010
Introduction of Russia's own full-cycle
catalyst production technologies
Leading edge
30%
of Russian
market
40%
of Russian
market
50%
of Russian
market
65%
of Russian
market
Catalyst type: sulfidic
Quality
In inert gas
atmosphere
Electric drying
with inert gas
purging
Alcoxide-Based
Technology
Electric drying
with inert gas
purging
Alcoxide-Based
Technology
In inert gas
atmosphere
Alcoxide-Based
Technology
In inert gas
atmosphere
Electric drying
with inert gas
purging
RussianMarket
Technology Import
Russian R&D
Nanotechnology Applications in Catalytic Petroleum Refining Processes. Hydroskimming
CATALYST MARKETSScientific and Technical
Development
Catalyst Production Technologies Processes and Catalysts (Compounds)
Preparation of
Carrier
Preparation of
Impregnating
Solution
Impregnation Drying Baking Sulfurization
Catalyst Main Production Stages
In inert gas
atmosphere
Circulatory
impregnation
including carrier
vacuum treatment
Electric drying
with inert gas
purging
Purging at 300-
350°С with a fuel
containing sulfur
compounds (in a
separate unit)
Alcoxide-Based
Technology
Blending
of two
solutions in
the presence
of the third
component
1
2
3
4
Productivity(Space
Velocity),hr.^-1
CapitalIntensity
PowerConsumption
ResidualSulfur
Content,ppm
Activity
Strength
CatalystServiceLife
beforeRegeneration,
years
Price,th$/t
Technical and Economic
Characteristics of the
Process
C a t a l y s t S p e c i f i c a t i o n s
Circulatory
impregnation
including carrier
vacuum treatment
Electric drying
with inert gas
purging
Preparation of
nano-structuralized
carriers, e.g. on the
basis of titanium
dioxide
Synthesis of
optimum cobalt-
molybdenum
or platinum
compounds
directly in the
solution
Sulfurization in a
separate installation
(with a special
sulfur-containing
reactant)
In inert gas
atmosphere
On the refinery site
Baking on the
refinery site
Electric drying
with air purging
Complete Process Lines
Circulatory
impregnation
including carrier
vacuum treatment
Blending
of two
solutions in
the presence
of the third
component
Redeposition
Technology
On the refinery
site (in a separate
installation)
Purging at 300-
350°С with a fuel
containing sulfur
compounds (in a
separate unit)
Purging at 300-
350°С with a fuel
containing sulfur
compounds (in a
separate unit))Development
of Activation
Technologies and
Equipment
Development
of Sulphidation
Regimes
Circulatory
impregnation
including carrier
vacuum treatment
Circulatory
impregnation
including carrier
vacuum treatment
Development
of Methods to
Control Carriers'
Honeycomb
Structure
Development of
Active Component
Synthesis
Technologies
Blending of
two solutions
in the presence
of the third
component
Development
of Oxidative
Desulfurization
Technologies
Circulatory
impregnation
including carrier
vacuum treatment
Optimization of
Drying Conditions
Consumption of valuable feedstock
(cobalt and molybdenum content, %) 15–18 15–18 20–24 20–24
10 10 10 10
10 10 6–7 6–7
100 100 100 100
Labor intensity (per 1,000 tons of
products annually), man
Technical and Economic Characteristics
2020 203020152010
Average capital intensity by process stages
(per 1,000 tons of products annually), $mln
Power consumption
Capacity output
70–80 70–80 80–90 80–90
Materials consumption
Technical and Economic Characteristics
2020 203020152010
Capital intensity
Power consumption Medium Medium Medium Medium
High High High High
High Medium Medium Medium
Low Low Medium Medium
Yield ratio, %
Yield ratio, % 95–98 95–98 95–98 95–98
Oxidation Technology
1. Carrier preparation. 2. Preparation of impregnating
solution. 3. Impregnation. 4. Drying. 5. Baking.
Quality improvement: cleaner
fuels
2030 or later
Production stages Advantages Appearance time
Quality improvement: reduction of sulfur and nitrogen
content
2030 or later
Advantages Appearance time
Process:
NZSD (<10 ppm)
2015
2020
х2
х2
х2
1,5
1,2
1,2
х1,2
х1,2
х1,2
<10
<10
<10
х2–2,5
х2–2,5
х2–2,5
х1
х1
х1
1,5–2
1,5–2
1,5–2
25–30
25–30
25–30
Catalyst:
Carrier: alumina
Active component: nano-
modified cobalt-molybdenum
Process:
Low (over 50 ppm)
residual sulfur
content
х1,5
х1,5
х1
х1
>3,5
2,5–3
2,5
2,5
х1,2
х1,2
х1
х1
50
50
350–
50
350
х1,5
х1,2
х1
х1
х1
х1
х1
х1
2
2
3
3
19–25
19–25
19–25
20–22
Process:Very low(over
50 ppm) residual sulfur
content (with low space
velocityspace velocity)
2010
2015
2020
х1,5
х1,5
х1
х1
2–2,5
1,5–2
1,5–2
1,5–2
х1
х1
х1,2
х1,2
50–10
50–10
50–10
50–10
х1,5
х1,2
х1
х1
х1,2
х1,2
х1
х1
2
2
2
2
19–25
19–25
19–25
20–22
Catalyst:
Carrier: alumina
Active component: cobalt-
molybdenum
2030
Process:
NZSD (<10 ppm)
2010
2015
2020
х1,5
х1,5
х1,5
х1,5
1,5
1,5
1,5
1,5
х1
х1
х1
х1
<10
<10
<10
<10
х2,5–3
х2,5–3
х2,5–3
х2,5–3
х0,8
х0,8
х0,8
х0,8
3
2
2
2
50–60
70–80
70–80
70–80
Catalyst:
Nebula type
2030
Process:Very low (50-
10 ppm) residual sulfur
content
2010
2015
2020
х1
х1
х1
х1
3
3
3
3
х1,2
х1,2
х1
х1
50–10
50–10
50–10
50–10
х2,5–3
х2,5–3
х2,5–3
х2,5–3
х0,8
х0,8
х0,8
х0,8
3
3
3
3
50–60
70–80
70–80
70–80
Catalyst:
Nebula type
2030
2010
2015
2020
2030
2030
Process: Very low (10-1 ppm) residual
sulfur content
Catalyst:
Carrier: nano-structuralized titanium dioxide
Active component: cobalt-molybdenum or platinum
Catalyst type: carrier: aluminum oxide
Active component: cobalt-molybdenum
2020 203020152010
Number of units
Total capacity, kta
Annual consumption,
tons
Annual consumption,
$mln
50
70 000
1 500–2 000
100
64
75 000
6 000
250
64–66
75 000
8 000
300
80
90 000
10 000–12 000
400–500
Catalyst type: carrier: aluminum oxide
Active component: nickel-molybdenum
2020 203020152010
Number of units
Total capacity, kta
Annual consumption,
tons
Annual consumption,
$mln
10
10 000
200
6
15
15 000
600
24
20
20 000
1 000
40
20
20 000
1 500
60
WorldMarket
Catalyst type: sulfidic
2020 203020152010
Total capacity, kta
Annual consumption, kta
Annual consumption,
$mln
750–800
50–60
2 200
750–800
60–65
2 500–2 600
800–900
70
2 700–2 800
900–1 100
80
3 000–3 500
Lagging behind
leaders
Application of
purchased foreign
technologies
Catalyst:Carrier: alumina
Active component: cobalt-
molybdenum or nickel-
molybdenum
5
6
Development of
Bimetallic Compound
Synthesis Methods
Blending of
two solutions
in the presence
of the third
component
Synthesis of
optimum cobalt-
molybdenum
compounds directly
in the solution
Legend:
— Low-cost technology
— High-quality production technology
—Normalized assessment of current parameter
values. This assessment is used as the basis for
future estimations of the same parameters in all
analyzed sectors
х1
© State Corporation “Russian Corporation of
Nanotechnologies”, 2010

2. RussianMarket
Catalyst type:Bead aluminosilicate zeolite-
containing catalyst
2020 203020152010
Number of units
Total capacity, kta
Annual consumption, tons
Annual consumption, $mln
11
5 850
7 200
18
7
4 000
4 900
15
3
1 800
2 200
8
—
—
—
—
2020 203020152010
Number of units
Total capacity, kta
Annual consumption, tons
Annual consumption, $mln
16
24 180
10 500
42
19
30 700
14 000
63
22
37 000
16 000
80
25
43 000
19 000
115
2020 203020152010
Number of units .
Total capacity, kta
Annual consumption, tons
Annual consumption, $mln
—
—
—
—
—
—
—
—
2
4 000
1 800
11
5
10 000
4 500
32
Blending of
zeolite and
aluminosilicate
matrix
Electric heating In liquid
phase
Gel-based
zeolite
synthesis
method
Substitution
of sodium
ion with
ammonium
ion or ions
or rare-earth
elements
1. Preparation of
sodium aluminate
and ammonium
nitrate solutions,
separation of rare-
earth elements.
2. Synthesis of
aluminum hydroxide
3. Clay drying block
In fire
furnace
In fire
furnace
Technology Import
Russian R&D
Nanotechnology Applications in Catalytic Petroleum Refining Processes. Catalytic Cracking
CATALYST MARKETSScientific and Technical
Development
Catalyst Production Technologies Processes and Catalysts (Compounds)
World Market
Technology
2020 203020152010
Introduction of Russia's own full-cycle catalyst production
technologies
Leading edge
80%
of Russian
market + 20% of
CIS market
80%
of Russian
market
60%
of Russian
market
20%
of Russian
market
Marketing
Quality
х1 х1 х1 —
х1 х1 х1 —
х1 х1 х0,9 —
Labor consumption
Technical and Economic Characteristics
2020 203020152010
Capital Intensity
Power Consumption
Bead Catalyst Production Technology
Baking equipment and
filters
Preparation of
zeolite (active
component)
Preparation
of amorphous
aluminosilicate matrix
(carrier)
Zeolite modification
with rare-earth
elements through
ion exchange
Thermocouple
stabilization
Zeolite baking Injection of
modified zeolite
into amorphous
aluminosilicate
matrix
Baking and
thermocouple
stabilization
Forming and
drying
Catalyst Main Production Stages
Blending of
zeolite and
aluminosilicate
matrix
Electric heating
In liquid
phase
Gel-based
zeolite synthesis
method
Substitution of
sodium ion with
ammonium ion or
ions or rare-earth
elements
1. Preparation of
sodium aluminate
and ammonium
nitrate solutions,
separation of rare-
earth elements.
2. Synthesis
of aluminum
hydroxide
3. Clay drying
block
In fire
furnace1
Blending of
zeolite and
aluminosilicate
matrix
Electric heating
In gas
phase
Gel-based
zeolite synthesis
method
Substitution of
sodium ion with
ammonium ion or
ions or rare-earth
elements
1. Preparation of
sodium aluminate
and ammonium
nitrate solutions,
separation of rare-
earth elements.
2. Synthesis of
aluminum hydroxide
3. Clay drying block
In fire
furnace2
In fire
furnace
In fire
furnace
Preparation of
zeolite (active
component)
Preparation
of amorphous
aluminosilicate
matrix (carrier)
Feedstock
preparation
(cleaning)
technology
will be
developed by
2020 resulting
in the growth
of catalyst
selectivity
and activity
Zeolite modification
with rare-earth
elements through
ion exchange
Thermocouple
stabilization
Zeolite baking Injection of
modified zeolite
into amorphous
aluminosilicate
matrix
Baking and
thermocouple
stabilization
Microsphere
formation and
spray drying
Catalyst Main Production Stages
х0,7 х0,6 х0,65 х0,5
х2 х2,2 х2,4 х2,5
х1,8 х1,7 х1,6 х1,5
Labor consumption
Technical and Economic Characteristics
2020 203020152010
Capital Intensity
Power Consumption
Microspheroidal Catalyst Production Technology
Yieldofdesiredproduct
(gasolinecut)pertonof
feedstock(annualoperation
time:8,000hr),%
Capitalintensity(at600
ktathroughput)
Manuallaborshare
Powerconsumption,kWhr/ton
offeedstock
Activity(cracking
conversionratio),%
Micro-activity,%
Wearingquality,%
Price,th$/t
Technical and Economic
Characteristics of the Process
C a t a l y s t
S p e c i f i c a t i o n s
х1,5
х1,5
х1,5
х1,5
56
54
52
50
х0,5
х0,5
х0,5
х0,5
720
750
750
780
78
76
73
70
71
65
58
52
97
93
90
87
6
4
3
2
2015
2020
2030
Catalyst:
Microspheric (dust-like
with average particle
diameter 10-70 mkm)
aluminosilicate zeolite-
containing catalyst with
optimized content of
Process:
«Mili-second» cracker
2010
Catalysts
2020 203020152010
Total capacity, mta
Annual consumption, kta
Annual consumption, $mln
765
300
1 200
780
320
1 450
790
350
1 750
800
360
2 150
WorldMarket
х2,5
х2,5
х2,5
х2,5
60
58
56–58
54
х0,5
х0,6
х0,65
х0,7
750
780
800
820
78
76
73
70
71
65
58
52
97
93
90
87
6
4
3
22010
2015
2020
2030
Catalyst:
Microspheric (dust-like
with average particle
diameter 10-70 mkm)
aluminosilicate zeolite-
Process:
Double regeneration
cracker for heavy
feedstock
х2
х2
х2
х2
60
58
56–58
54
х0,5
х0,6
х0,65
х0,7
720
750
750
780
78
76
73
70
71
65
58
52
97
93
90
87
6
4
3
22010
2015
2020
2030
Catalyst:
Microspheric (dust-like
with average particle
diameter 10-70 mkm)
aluminosilicate zeolite-
containing catalyst
Process:
Lift-reactor cracker
Process:
Moving-bed cracker with
fluidized catalyst bed
х2
х2
х2
53–54
48–50
48–50
х0,8
х0,85
х0,85
780
780
800
75
70
70
55
54
50
92
88
86
4
3
22010
2015
2020
Catalyst:Microspheric
(average particle
diameter 10-150 mkm)
aluminosilicate zeolite-
containing catalyst
Process:
Moving-bed cracker
х1
х1
х1
50–52
50
43–46
х1
х1
х1
600
600
650
68
65
63
50
48
46
88
86
84
2
1,8
1,52010
2015
2020
Catalyst:
Bead aluminosilicate
zeolite-containing
catalyst
Matrix modification
Synthesis of various
types of zeolite,
including those with
wide mesopores, for
catalytic cracking of
heavy crude oil and
for the «mili-second»
process
Development of technologies
for baking in controlled gas
environments
Processing regimes
Optimization of baking
conditions
Blending equipment
Zeolite synthesis
equipment
Spray drying equipment
Baking equipment
including drum furnaces
Ash-based
zeolite
synthesis
method
1. Preparation of
sodium aluminate
and ammonium
nitrate solutions,
separation of rare-
earth elements.
2. Synthesis
of aluminum
hydroxide
3. Clay drying block
4
Blending of
zeolite and
aluminosilicate
matrix
In fire
furnace
Electric heating
Substitution of
sodium ion with
ammonium ion
or ions or rare-
earth elements
Pulp filtration
(centrifugal separation)
equipment
Blending of
zeolite and
aluminosilicate
matrix
Ash-based
zeolite
synthesis
method
In fire
furnace
1. Preparation of
sodium aluminate
and ammonium
nitrate solutions,
separation of rare-
earth elements.
2. Synthesis
of aluminum
hydroxide
3. Clay drying
block
In fire
furnace
In gas
phase
Substitution of
sodium ion with
ammonium ion
or ions or rare-
earth elements
Electric heating
Development of compound
homogenization
technologies
In fire
furnace
In gas
phase
— Normalized
assessment of current
parameter values. This
assessment is used
as the basis for future
estimations of the
same parameters in all
analyzed sectors
Legend:
— Low-cost technology
— High-quality production
technology
х1
Development of
catalysts resistant
to metal poisoning
(vanadium, nickel) to
process fuel oil
3
Feedstock
preparation
(cleaning)
5
Catalyst type:
Microspheric (dust-like with average
particle diameter 10-150 mkm) aluminosilicate
zeolite-containing catalyst
Catalyst type:
Microspheric (dust-like with average particle diameter
10-70 mkm) aluminosilicate zeolite-containing catalyst
with optimized content of rare-earth elements
© State Corporation “Russian Corporation of
Nanotechnologies”, 2010

3. W o r l d M a r k e t
2020 203020152010
Annual consumption,
kta
Annual consumption,
$mln
3 000
450
3 500
550
4 000
625
4 500–5 000
700–750
Technology
Import
Russian R&D
Nanotechnology Applications in Catalytic Petroleum Refining Processes. Light Gasoline Cut IsomerizationRefining Processes. Light Gasoline Cut Isomerization
CATALYST MARKETSScientific and Technical Development Catalyst Production Technologies Processes and Catalysts (Compounds)
Strategic Goals of Russian Producers
Technology
2020 203020152010
Introduction of Russia's own full-cycle
catalyst production technologies
Leading edge
Slightly
lagging
behind
the world
leaders
30%
of Russian
market
40%
of Russian
market
50%
of Russian
market
50%
of Russian
market + 20%
of CIS market
Marketing
Quality
Productivity,tonsof
feedstock/tonsofcatalyst
perhour
CapitalIntensity
Laborconsumption
Powerconsumption
%ofbyproducts
Strength,kg/cm
Selectance,%wght
Price,th$/t
Technical and Economic
Characteristics of the
Process
Catalyst
Specifications
Preparation of feedstock
Preparation of feedstock
Preparation of solution
Preparation of solution
Autoclave
crystallization
Autoclave crystallization
Washing, filtration, wastewater
disposal
Washing, filtration, wastewater
disposal
Ion exchange, modification
Ion exchange, modification
Application of precious
metal
Granulation with binding
substance
Granulation with binding
substance
Drying, baking
Drying, baking
Medium Temperature Catalyst Main Production Stages
High Temperature Catalyst Main Production Stages
R u s s i a n M a r k e t
2020 203020152010
Number of units
Annual
consumption, kta
Annual
consumption, $mln
14
140–150
15–22
18
200–300
30–45
23
350–400
52–60
30
550
85
х1
х1
х1
х1
х1
х1
х1
х1
х1
х1
х1
х1
2–5
2–5
2–5
5–8
60–80
60–80
50–70
50–70
95–98
95–98
95–98
92–95
80
75
75
702010
2015
2020
2030
Catalyst:
Chlorinated alumina;
zirconium oxide
promoted with
sulfate, molybdate, or
tungstate ions
Process:
Low-temperature isomerization
5
5
4
4
х2,75
х2,75
х2,75
х2,75
х1,3
х1,3
х1,3
х1,3
х2
х2
х2
х2
10–15
10–15
10–15
10–15
60–80
60–80
50–70
50–70
85–90
85–90
85–90
85–90
155
150
150
1302010
2015
2020
2030
Catalyst:
Based on mordenite-
type zeolites (containing
sodium in a volume of
2-3 ppm) modified with
0.4-0.5% whgt. platinum
Process:
Medium-temperature
isomerization
0,5–1,5
0,5–1,5
0,5–1,5
0,5–1,5
х3
х3
х3
х3
х1,3
х1,3
х1,3
х1,3
х3
х3
х3
х3
15–25
15–25
15–25
15–25
60–80
60–80
50–70
50–70
75–85
75–85
75–85
75–85
155
150
150
1302010
2015
2020
2030
Catalyst:
Based on fluorinated
alumina or ZSM-5 type
medium-porous zeolites
Process:
High-temperature isomerization
0,5–1,5
0,5–1,5
0,5–1,5
0,5–1,5
Belt-type baking
furnaces for
continuous baking
at temperatures
up to 600°С
Development
of methods for
simultaneous
application of
precious metals
and sulfate
Improvements in
wet formation of
bead catalyst in
oil column
Development
of technologies
for catalyst
granulation
without binding
agents
х2 х2 х1,8 х1,8
х0,5 х0,5 х0,6 х0,6
х2,5 х2,5 х2,5 х2,5
х2,5 х2,5 х2,5 х2,5
> 85 % > 90 % > 95 % > 95 %
Labor consumption
Technical and Economic Characteristics 2020 203020152010
Capital Intensity
Power consumption
Technology for Preparation of High-Temperature Catalysts on the Basis of ZSM-5 Type Medium-Porous Zeolites
Yield ratio, %
Productivity
х1 х0,8 х0,7 х0,7
х1 х1,2 х1,5 х1,5
х1 х0,7 х0,6 х0,6
х1 х0,8 х0,7 х0,6
> 90 % > 95 % > 95 % > 95 %
Labor consumption
Technical and Economic Characteristics 2020 203020152010
Capital Intensity
Power consumption
Improvement of continuous zeolite synthesis technology
Yield ratio, %
Productivity
х2 х2 х2 х2
х0,3 х0,3 х0,3 х0,3
х3 х3 х3 х3
х3 х3 х3 х3
> 85 % > 90 % > 95 % > 95 %
Labor consumption
Technical and Economic Characteristics 2020 203020152010
Capital Intensity
Power consumption
Technology for Preparation of Medium-Temperature Catalysts on the Basis of Mordenite-Type Zeolites (Containing Sodium in a Volume of 2-3
ppm)
Yield ratio, %
Productivity
Mechanical grinding in ball crushers
(preparation of water – process condensate,
electrical desalination
Mechanical grinding in ball crushers
(preparation of water – process condensate,
electrical desalination
Filtration in continuous-type scroll
centrifuges / intermittent filtration in regular
centrifuges
Filtration in continuous-type scroll
centrifuges / intermittent filtration in regular
centrifuges
Filtration in continuous-type scroll
centrifuges / intermittent filtration in regular
centrifuges
Filtration in continuous-type scroll
centrifuges / intermittent filtration in regular
centrifuges
Filtration in nutch filters or press filters
Mechanical grinding in planetary crushers
(preparation of water – distillation, ion-
exchange resins), possible ultrasonic crushing
of inoculant
Mechanical grinding in planetary crushers
(preparation of water – distillation, ion-
exchange resins), possible ultrasonic crushing
of inoculant
Mechanical grinding in planetary crushers
(preparation of water – distillation, ion-
exchange resins), possible ultrasonic crushing
of inoculant
Mechanical grinding in planetary crushers
(preparation of water – distillation, ion-
exchange resins), possible ultrasonic crushing
of inoculant
Multiple intermittent ion exchange in
agitators with heating at atmospheric
pressure
Single-time intermittent ion exchange
in autoclaves at high pressure and
temperature
Single-time intermittent ion exchange
in autoclaves at high pressure and
temperature
Single-time intermittent ion exchange
in autoclaves at high pressure and
temperature
Intermittent ion exchange in agitators
with heating at atmospheric pressure
Intermittent ion exchange in autoclaves
at high pressure and temperature
Intermittent ion exchange in autoclaves
at high pressure and temperature
Intermittent ion exchange in autoclaves
at high pressure and temperature
Granulation in screw extruders
integrated with z-shape blade
mixers
Granulation in screw extruders
integrated with z-shape blade
mixers
Intermittent in muffle furnace /
intermittent or continuous in shaft
furnaces
Intermittent in muffle furnace /
intermittent or continuous in shaft
furnaces
Intermittent in muffle furnace /
intermittent or continuous in shaft
furnaces
Continuous in regular or vacuum
belt furnaces
Intermittent in muffle furnace /
intermittent or continuous in shaft
furnaces
Intermittent in muffle furnace /
intermittent or continuous in shaft
furnaces
Granulation with binding substance in
screw extruders integrated with z-shape
blade mixers
Granulation with binding substance in
screw extruders integrated with z-shape
blade mixers
Granulation with binding substance in
screw extruders integrated with z-shape
blade mixers
Wet formation of bead catalyst in
oil column
Mechanical grinding in ball crushers
(preparation of water – process condensate,
electrical desalination
Mechanical grinding in ball crushers
(preparation of water – process condensate,
electrical desalination
Solution of salts in water,
mechanical blending
Solution of salts in water,
mechanical blending
Solution of salts in water,
mechanical blending
Solution of salts in water,
mechanical blending
Solution of salts in water,
mechanical blending
Solution of salts in water,
mechanical blending
Solution of salts in water,
mechanical blending
Solution of salts in water,
mechanical blending
Intermittent
Intermittent
Continuous
Filtration in nutch filters or
press filters
Intermittent impregnation
(possibly combined with ion
exchange)
Intermittent impregnation
(possibly combined with ion
exchange)
Continuous in regular or
vacuum belt furnaces
Continuous impregnation (by
analogy with preparation of
reforming catalysts)
Continuous impregnation (by
analogy with preparation of
reforming catalysts)
Intermittent
Intermittent
Continuous
Preparation of active componentPreparation of solution Application of precious
metal
Catalyst granule thermal
treatment
Low-Temperature Catalyst Main Production Stages
Solution of salts in water, mechanical blending
(agitation units)
Solution of salts in water, mechanical blending
(agitation units)
Solution of salts in water, mechanical blending
(agitation units)
Redeposition with agitation and heating combined with
modification by means of sulfate ions
Redeposition with agitation and heating combined with
modification by means of sulfate ions and ultrasonic dispergation
Redeposition with agitation and heating combined with
modification by means of sulfate ions and ultrasonic dispergation
Intermittent impregnation / intermittent
impregnation combined with ion exchange
Continuous impregnation (by analogy with
preparation of reforming catalysts)
Continuous impregnation (by analogy with
preparation of reforming catalysts)
Granulation with binding substance in screw extruders
integrated with z-shape blade mixers
Wet formation of bead catalyst in oil column
1
4
5
8
9
2
3
Intermittent in muffle furnace / intermittent or
continuous in shaft furnaces
Intermittent in muffle furnace / intermittent or
continuous in shaft furnaces
Continuous in regular or vacuum belt furnaces
Continuous in regular or vacuum
belt furnaces
Continuous
Continuous
Blending of active component with
alumina and subsequent granulation
Granulation with binding substance in screw extruders
integrated with z-shape blade mixers
Agitating
autoclaves with
a heating range
of up to 200°С
for zeolite
synthesis
Equipment for wet
formation of bead
catalyst in oil
column
Wet formation of bead catalyst
in oil column
Wet formation of bead catalyst
in oil column
Filtration in continuous-type scroll
centrifuges / intermittent filtration in regular
centrifuges
Filtration in continuous-type scroll
centrifuges / intermittent filtration in regular
centrifuges
Scroll centrifuges
for continuous
filtration and
washing of wet
synthesized
products
Improvement
of continuous
zeolite synthesis
technology
11
10
7
6
— Normalized assessment of current
parameter values. This assessment is used
as the basis for future estimations of the
same parameters in all analyzed sectors.
Legend:
— High-quality production
technology
— Low-cost technology х1
© State Corporation “Russian Corporation of
Nanotechnologies”, 2010

4. Reduction
in hydrogen
stream
Non-
residuum
impregnation
Contactless
Uniform
refluxing With poly-
sulfides
Chlorination
with the use
of CCl4 or
C2H4Cl2
Evaporation
by means of
microwaves
Low-
temperature
heating in
furnace
By the
ammonia-
hydrocarbon
formation
method
Technology Import
Russian R&D
Nanotechnology Applications in Catalytic Petroleum Refining Processes. Catalytic Reforming
CATALYST MARKETSScientific and Technical Development Catalyst Production Technologies Processes and Catalysts (Compounds)
Strategic Goals of Russian Producers
Technology
2020 203020152010
Introduction of Russia's own full-cycle
catalyst production technologies
Application
of purchased
foreign
technologies
Leading edge
80%
of Russian
market
60–70%
share of Russian
market
50%
of Russian
market
20%
of Russian
market
Marketing
Quality
х1 х1 х1 х1
х1 х1 х1,1 х1,15
х1 х1 х1 х1
6–8 6–8 6–8 6–8
Labor consumption
Technical and Economic Characteristics
2020 203020152010
Capital Intensity
Power consumption
Technology for Preparation of Bead «Platinum of Alumina» Catalysts by the Ammonia-Hydrocarbon
Formation Method
Rejection rate, %
х1 х1 х1 х1
х1 х1 х1,1 х1,1
х1 х1 х1 х1
8–10 8–10 8–10 8–10
Labor consumption
Technical and Economic Characteristics
2020 203020152010
Capital Intensity
Power consumption
Technology for Application of Platinum on Alumina (Extrudate Preparation)
% брака
х1,1 х1,1 х1,02 х1
х1,1 х1,15 х1,2 х1,2
х1,2 х1,2 х1,3 х1,3
6–8 6–8 6–8 6–8
Labor consumption
Technical and Economic Characteristics
2020 203020152010
Capital Intensity
Power consumption
Technology for Preparation of Zeolite Platinum Containing Catalysts
% брака
OctaneNumber
GasolineYield,%wght
ТLaborconsumption
SpaceVelocity),hr.^-1
CapitalIntensity
PowerConsumption,kW/t
Micro-activity,%
Wearingquality,%
Price,th$/t
Technical and Economic
Characteristics of the Process
Catalyst
Specifications
RussianMarket
Catalyst type:
Zeolitic, platinum containing
2020 203020152010
Number of units
Total capacity, kta
Annual consumption,
tons
Annual consumption,
$mln
3
3 000
50
1
5
5 000
85
2,15
8
8 000
135
3,6
12
12 000
200
6,4
Catalyst type: Platinum on alumina and zeolitic platinum
containing
2020 203020152010
Total capacity, mta
Annual consumption, kta
Annual consumption,
$mln
525
8 750
175
560
9 300
230
600
10 000
270
675
11 250
360
WorldMarket
Moistening by
water vapor
Preparation
of carrier
(formation)
Water
evaporation
Drying Baking Reduction
in hydrogen
stream
SulfurizationChlorination
(activation)
Main Stages of Technology for Application of Platinum on Alumina (Extrudate Preparation)
Reduction
in hydrogen
stream
Non-
residuum
impregnation
Contact
Uniform
refluxing3
With
elementary
sulfur
Chlorination
with
gaseous
HCl
Heating in
furnace
Low-
temperature
heating in
furnace
Extrusion
Moistening by
water vapor
Bead Formation Water
evaporation
Drying Baking Reduction
in hydrogen
stream
SulfurizationChlorination
(activation)
Main Stages of Technology for Preparation of Bead «Platinum of Alumina» Catalysts by the
Ammonia-Hydrocarbon Formation Method
Reduction
in hydrogen
stream
Non-
residuum
impregnation
Contact
Uniform
refluxing With poly-
sulfides
Chlorination
with
gaseous
HCl
Heating in
furnace
Low-
temperature
heating in
furnace
Impregnation
of carrier with
platinum and
rhenium solutions
Moistening by
water vapor
Preparation
of carrier
(formation)
Water
evaporation
Drying Baking Reduction
in hydrogen
stream
SulfurizationChlorination
(activation)
Main Stages of Technology for Preparation of Zeolite Platinum Containing Catalysts
Reduction
in hydrogen
stream
Контактная4 With poly-
sulfides
Chlorination
with gaseous
HCl
Low-
temperature
heating in
furnace
Extrusion
Reduction
in hydrogen
stream
Contactless5 With poly-
sulfides
Chlorination
with the use
of CCl4 or
C2H4Cl2
Evaporation
by means of
microwaves
Low-
temperature
heating in
furnace
Extrusion
х0,75
х0,8
х0,85
х0,85
103
102
101
100
3
2,4
2,2
2
х2
х1,9
х1,8
х1,8
160
170
175
180
60
65
68
70
300–350
280
270
250
80–100
80
70
40–60
Catalyst:
Platinum on
alumina
Process:
Moving catalyst bed
92
90
89
87–89
2020
2015
2010
2030
х0,75
х0,8
х0,85
х0,85
105
104
103
102
3,2
2,8
2,4
2,2
х2
х1,9
х1,8
х1,8
160
170
175
180
59
65
66
67
300–350
300
290
280
80–100
80
70
40–60
Catalyst:
Zeolitic, platinum
containing
Process:
Moving catalyst bed
94
92
91
90
2020
2015
2010
2030
Catalyst type:
Platinum on alumina
2020 203020152010
Number of units
Total capacity, kta
Annual consumption,
tons
Annual consumption,
$mln
58
20
330
6,6
60
22–25
420
9,4
60
22–25
420
10,5
62
30
500
15
х0,8
х0,9
х1
х1
100
98
96
95
2,5
2
1,9
1,7
х1
х1
х1
х1
120
125
130
130–140
59
59
60
62
220
190
170
120–150
80–100
80
70
40–60
Catalyst:
Zeolitic, platinum
containing
Process:
Fixed catalyst bed with intermediate
heating between the reaction zones
90
89
88
85–87
х0,8
х0,9
х1
х1
98
97
96
93–95
2
1,7
1,5
1,3–1,5
х1
х1
х1
х1
120
125
130
130–140
60
61
63
64
220
190
170
120–150
80–100
80
70
40–602010
2015
2020
2030
Catalyst:
Zeolitic, platinum
containing
Process:
Fixed catalyst bed with intermediate
heating between the reaction zones
90
88
86
82–852
Development
of catalysts
ensuring high
octane numbers
at smooth
processing
regimes
Development of
hydrogen yielding
catalysts
Equipment for
reduction in
hydrogen stream
Drying
equipment
— Normalized
assessment of current
parameter values. This
assessment is used
as the basis for future
estimations of the
same parameters in all
analyzed sectors
Legend:
—Low-cost technology
— High-quality production
technology
х1
2020
2015
2010
2030
1
By the
ammonia-
hydrocarbon
formation
method
Development
of catalysts
with improved
mechanical
strength and high
catalytic activity
for moving-bed
installations
Carrier
production
equipment
Uniform
refluxing
Uniform
refluxing
Heating in
furnace
Non-
residuum
impregnation
Non-
residuum
impregnation
Impregnation
of carriet with
platinum and
rhenium solutions
Impregnation
of carriet with
platinum and
rhenium solutions
© State Corporation “Russian Corporation of
Nanotechnologies”, 2010

5. Catalyst type:
On the basis of amorphous and crystalline
alumosilicates containing sulfide nano-particles of
NiWS phase
2020 203020152010
Number of units
Total capacity, kta
Annual consumption,
tons
Annual consumption,
$mln
2
5
300
10,5
4
10,4
600
21
5
12,4
800
28
7
17,4
1 000
35
Technology Import
Russian R&D
Nanotechnology Applications in Catalytic Petroleum Refining Processes.Hydrocracking
CATALYST MARKETSScientific and
Technical
Development
Catalyst Production Technologies Processes and Catalysts (Compounds)
Strategic Goals of Russian Producers
Technology
2020 203020152010
Introduction of
Russia's own
full-cycle catalyst
production
technologies
Application
of purchased
foreign
technologies
Slightly lagging behind the
world leaders
Not produced in
Russia
Not produced in
Russia
—
—
—
—
50%
of Russian
market
65%
of Russian
market
Marketing
Quality
Technical and Economic
Characteristics of the
ProcessEconomicCharacteristics
of the ProcessProcess
Productivity(amountof
feedstockprocessed,
tons)
Powerconsumption
Activity
Selectance
Wearingquality,%
Price,th$/t
C a t a l y s t
S p e c i f i c a t i o n s
Strength
WorldMarket
Preparation of
Carrier
Preparation of
Carrier
Preparation
of zeolite
component (or
alumosilicate)
Preparation of
Zeolite Compound
Preparation of
Impregnating
Solution
Preparation of
Impregnating
Solution
Impregnation
Impregnation
Drying
Drying
Baking.
Baking
Sulfurization
(transition into
sulphide phase)
Reduction
(treatment to
bring platinum
into metallic state
Main Catalyst Production Stages
Main Catalyst Production Stages
—
—
Single-stage
Single-stage
With polysulfide
compounds
In hydrogen
stream
Extrusion,
drying and
baking
Extrusion,
drying and
baking
Preparation
of common
tungsten-nickel
solution
Preparation
of platinum
containing
solution
1
1
Productivity
Productivity
х1 х1 х1 х1
х1 х1 х1 х1
х1 х1 х1 х1
х1 х1 х1 х1
х1 х1 х0,98 х0,96
х1 х1 х0,98 х0,96
х1 х0,98 х0,96 х0,94
х1 х0,98 х0,96 х0,94
Labor consumption
Labor consumption
Technical and Economic Characteristics
Technical and Economic Characteristics
2020
2020
2030
2030
2015
2015
2010
2010
Capital Intensity
Capital Intensity
Power consumption
Power consumption
Technology for Preparation of Catalysts on the Basis of Amorphous or Crystalline Alumosilicates Containing
Sulfide Nano-Particles of NiWS Phase
Technology for Preparation of Catalysts on the Basis of Crystalline Alumosilicate (Zeolites) Containing
Platinum Nano-Particles
Yield ratio, %
Rejection rate, %
97–98 97–98 98 99
97–98 97–98 98 99
Hydrothermal
synthesis
Hydrothermal
synthesis
Electrical
drying in air
or nitrogen
stream
Electrical
drying in air
or nitrogen
stream
2 Hydrothermal
synthesis
Extrusion,
drying and
baking
—
In fume
gases
Preparation
of platinum
containing
solution
With feedstock
containing
dimethyl
disulfide
Single-stage
2
With
feedstock
containing
dimethyl
disulfide
Hydrothermal
synthesis
Extrusion,
drying and
baking
Preparation
of common
tungsten-nickel
solution
Single-stage —In fume
gases
Equipment
for catalyst
impregnation
(fixation of bimetallic
compounds on
carrier surface)
2010
х1
х1
х1
х1
х1,06
х1,04
х1,03
х1
х0,97
х0,97
х0,97
х1
5
5
4
4
9
8
7
7
9
8
7
6
4
3
2
2
17–22
17–22
14–18
14–18
2030
2020
2015
Catalyst:
On the basis of amorphous
alumosilicates containing sulfide
nano-particles of NiWS phase
Process:
Single-stage
hydrocracking
2010
х1
х1
х1
х1
х1,6
х1,57
х1,55
х1,5
х1,2
х1,3
х1,4
х1,5
10
9
8
7
9
8
7
7
9
8
7
6
10
8
7
6
20–24
20–24
16–20
16–20
2020
2015
Catalyst:
On the basis of crystalline
alumosilicates (zeolites)
containing platinum nano-
particles
Process:
Two-stage
hydrocracking
2030
RussianMarket
Catalyst type:
Alumosilicate-based
2020 203020152010
Total capacity, kta
Annual consumption, kta
Annual consumption, $mln
22–26
25–30
875–1 050
26–30
30–35
1 050–1 220
30–35
35–40
1 220–1 400
39–44
45–50
1 575–1 750
2010
х1,4
х1,4
х1,4
х1,4
х1,06
х1,04
х1,03
х1
х0,97
х0,97
х0,97
х1
9
8
7
6
9
8
7
7
9
8
7
6
9
7
5
4
20–24
20–24
16–20
16–20
2030
2020
2015
Catalyst:
On the basis of crystalline
alumosilicates (zeolites)
containing sulfide nano-particles
of NiWS phase
Process:
Single-stage
hydrocracking
х1 — Normalized assessment
of current parameter values.
This assessment is used as
the basis for future estimations
of the same parameters in all
analyzed sectors.
Legend:
—Low-cost technology
—High-quality production
technology
Score indicated as per a
ten-point scale
Development of
technologies to form
catalysts in solutions
of bimetallic
compounds with
particle sizes of
about 1 nm
CapitalIntensity
© State Corporation “Russian Corporation of
Nanotechnologies”, 2010

6. Nanotechnology Applications in Catalytic Petroleum Refining Processes. Processing of Associated Petroleum Gas – Part I
CATALYST MARKETSScientific and Technical Development Catalyst Production Technologies Processes and Catalysts (Compounds)
Strategic Goals of Russian Producers
Technology
2020 203020152010
Introduction of Russia's own full-cycle
catalyst production technologies
Leading edge
Not produced in
Russia
—
—
5%
of Russian
market
10%
of Russian
market
20%
of Russian
market
Marketing
Quality
Preparation of feedstock Preparation of solution Кристаллизация
в автоклавах
Washing, filtration, wastewater
disposal
Ion exchange, modification Application of precious
metal
Granulation with binding
substance
Drying, baking
Main Stages of Technology for Preparation of Zeolite Catalyst to Synthesize Gasoline from Dimethyl Ether
х1 х1 х1 х1
х1 х1 х1 х1
х1 х0,9 х0,8 х0,8
х1 х0,9 х0,8 х0,8
60 70 80 95
Labor consumption
Technical and Economic Characteristics 2020 203020152010
Capital Intensity
Power consumption
Technology for Preparation of Cobalt or Iron Nano-Particles Used as Catalysts in Fischer-Tropsch Process
Yield ratio, %
Valuable feedstock consumption
х1 х1 х1 х1
х1 х0,8 х0,7 х0,7
х1 х1 х0,8 х0,8
х1 х1 х0,8 х0,8
70 70 80 95
Labor consumption
Technical and Economic Characteristics 2020 203020152010
Capital Intensity
Power consumption
Technology for Production of Catalysts of the Basis of ZSM-5 Type Zeolites to Synthesize Gasoline from Dimethyl Ether
Yield ratio, %
Valuable feedstock consumption
Mechanical grinding in ball crushers
(preparation of water – process condensate,
electrical desalination
Mechanical grinding in ball crushers
(preparation of water – process condensate,
electrical desalination
Filtration in continuous-type scroll
centrifuges / intermittent filtration in regular
centrifuges
Mechanical grinding in planetary crushers
(preparation of water – distillation, ion-
exchange resins), possible ultrasonic crushing
of inoculant
Mechanical grinding in planetary crushers
(preparation of water – distillation, ion-
exchange resins), possible ultrasonic crushing
of inoculant
Многократный периодический ионный
обмен в аппаратах с перемешиванием и
подогревом при атмосферном давлении
Однократный периодический ионный
обмен в автоклавах под давлением
и при повышенных температурах
Granulation in screw extruders
integrated with z-shape blade
mixers
Granulation in screw extruders
integrated with z-shape blade
mixers
Intermittent in muffle furnace /
intermittent or continuous in shaft
furnaces
Intermittent in muffle furnace /
intermittent or continuous in shaft
furnaces
Intermittent in muffle furnace /
intermittent or continuous in shaft
furnaces
Solution of salts in water,
mechanical blending
Solution of salts in water,
mechanical blending
Solution of salts in water,
mechanical blending
Solution of salts in water,
mechanical blending
Crystallization
Intermittent
Continuous
Washing, filtration, wastewater
disposal
Intermittent impregnation
(possibly combined with ion
exchange)
Intermittent impregnation
(possibly combined with ion
exchange)
Continuous in regular or
vacuum belt furnaces
Continuous impregnation (by
analogy with preparation of
reforming catalysts)
Continuous impregnation (by
analogy with preparation of
reforming catalysts)
Preparation of micro-emulsionsPreparation of salt solutions Catalyst activation
Main Stages of Technology for Preparation of Cobalt or Iron Nano-Particles Used as Catalysts in Fischer-Tropsch Process
Preparation of invert micro-emulsion Evaporation of water from micro-emulsions Thermal treatment in hydrogen stream
Thermal treatment in carbon oxide stream
Thermal treatment in hydrogen stream
Thermal treatment in carbon oxide stream
Preparation of water solutions1
2
3
4
Preparation of suspensions
Wet formation of bead catalyst
in oil column
7
8
10
9
—Low-cost technology
— High-quality production
technology
— Normalized assessment of current parameter
values. This assessment is used as the basis for
future estimations of the same parameters in all
analyzed sectors.
х1
х0,5 х0,5 х0,4 х0,4
х2 х2 х4 х6
90 90 95 95
Трудоемкость
Technical and Economic Characteristics 2020 203020152010
Capital Intensity
Энергопотребление
Technology for Preparation of Membrane-Catalytic Catalyst for Fischer-Tropsch Process (Compared to ZSM-5 for Aromatization)
Выход годных, %
Valuable feedstock consumption
х0,5 х0,5 х0,4 х0,3
х0,3 х0,3 х0,2 х0,2
Preparation of powdersCo-deposition Membrane baking and catalyst
activation
Passivation of membrane-catalytic
element
Main Stages of Technology for Preparation of Membrane-Catalytic Catalysts for Fischer-Tropsch Process
Co-deposition of common hydroxocarbonate (HOC) of Co
and Al and promoting components
Blending and compaction of complex-shape membrane
defined by reactor geometry
Membrane baking and catalyst activization
Passivation of membrane-catalytic elementPreparation of powders of Со-Al HOC, metallic copper
and malachite with specified fraction composition and
moisture content
5
Blending and compaction of membrane
Passivation of membrane-
catalytic element
ПPreparation of powders of Со-Al HOC, metallic
aluminum and malachite with specified fraction
composition and moisture content
Co-deposition of common hydroxocarbonate of Co and Al
and promoting components
Blending and compaction of complex-shape membrane
defined by reactor geometry
Membrane baking and catalyst activization6
Productivity,tonsoffeedstock/tonsof
catalystperhour
Capitalintensity(comparedtothe
currentvalueforFischer-Tropsch
(ORYX=1.5mmtofproductsperyear,
CAPEX=$1000pertonperyear)
ТPowerconsumption(comparedtothe
currentvalueofFischer-Tropschprocess)
Powerconsumption(compared
tothecurrentvalueofFischer-
Tropschprocess)
С5+selectance,%
Methaneselectance,%
Strength,kg/cm2
Price,th$/t
Technical and Economic
Characteristics of the
Process
Catalyst
Specifications
Productivity,kgofproduct(gasoline
Capitalintensity(comparedtothe
currentvalueforFischer-Tropsch
(ORYX=1.5mmtofproductsperyear,
CAPEX=$1000pertonperyear)
Powerconsumption,Whr/tonof
feedstock
Servicecycle,months
Totalservicelife,years
Strength,kg/mm2
Price,th$/t
Technical and Economic
Characteristics of the
Process
Catalyst
Specifications
х0,8
х0,9
х1
х1
х0,9
х0,9
х1
х1
х0,8
х0,9
х1
х1
90
87
85
80
<5
8
8
10
—
—
—
—
25
25
20
202010
Catalyst:
Cobalt or iron nano-
particles
Process:
Fischer-Tropsch
0,7
0,5
0,4
0,3
2030
2020
2015
х0,8
х0,8
х0,9
х1
170
170
185
185
>2
>2
>2
>2
1,4
1,4
1,4
1,2
>3
>3
>3
>3
120
115
110
1002010
Catalyst:On the
basis of ZSM-5
type zeolites to
synthesize gasoline
from dimethyl ether
Process:
In single-loop two-
reactor module
0,8
0,8
0,7
0,7
2030
2020
2015
х0,7
х0,9
—
—
х1
х1
—
—
х1
х1
—
—
85
80
—
—
8
15
—
—
1,5
1
—
—
40
50
—
—2010
Catalyst:
Membrane-catalytic
Process:
Fischer-Tropsch
1
0,7
—
—
2030
2020
2015
—
—
—
—
—
—
—
—
>2
>2
>2
>2
2,2
2,2
2,2
2,2
>3
>3
>3
>3
30
25
25
202010
Catalyst:Alumina-
based metal-oxide for
synthesis of dimethyl
ether from associated
petroleum gas
Process:
In single-loop two-
reactor module
—
—
—
—
2030
2020
2015
Catalyst type:
Membrane-catalytic
2020 203020152010
Total capacity, mta
Annual consumption, kta
Annual consumption,
$mln
—
—
—
—
—
—
20
2
0,02
100–200
6–10
0,1–0,15
Catalyst type:
Cobalt or iron nano-particles
2020 203020152010
Total capacity, mta
Annual consumption, kta
Annual consumption,
$mln
2 000
1 000
20
3 000
1 500
30
3 000
1 500
30
4 000
1 500
40
WorldMarket
Catalyst type
Cobalt or iron nano-particles
2020 203020152010
Number of units
Total capacity, kta
Annual consumption, tons
Annual consumption,
$mln
—
—
—
—
1
20
4
0,13
5
100
20
0,5
20
1 000
200
5
Catalyst type:
Membrane-catalytic
2020 203020152010
Number of units
Total capacity, kta
Annual consumption, tons
Annual consumption,
$mln
—
—
—
—
—
—
—
—
1
10
1
0,02
2–3
50–60
3–5
0,06–0,1
Catalyst type:
Metal-oxide
2020 203020152010
Annual consumption, tons
Annual consumption,
$mln
—
—
72
1,5
360
7,5
1 440
30
Catalyst type:On the basis of ZSM-5
type zeolites
2020 203020152010
Number of units .
Total capacity, kta
Annual consumption, tons
Annual consumption, $mln
Annual consumption,
—
—
—
—
—
1
100
60
36
3,6
5
500
300
180
18
20
2 000
1 200
720
72
RussianMarket
Technology Import
Dimethyl ether production
Fischer-Tropsch process
Fischer-Tropsch process
Dimethyl ether production
Russian R&D
Development of stable micro-
emulsions
Development of efficient
methods to separate nano-
sized catalysts from synthesis
products
Belt-type baking furnaces
for continuous baking at
temperatures up to 600°С
Agitating autoclaves for
decomposition in organic
media at high (up to 350°С)
temperature
Improvement of methods to
promote nano-size catalysts
Scroll centrifuges for
continuous filtration
Electrical and magnetic filters
Improvement of technologies
for continuous synthesis of
ZSM–5 type medium-porous
zeolites
Development of efficient methods to
regenerate and recirculate nano-sized
catalystsббrecirculate nano-sized catalysts
circulate nano-sized catalysts
Development of more efficient
methods to modify zeolites to
improve their selectance
Evaporation of water from micro-emulsions
Evaporation of water from micro-emulsions
Evaporation of water from micro-emulsions
Preparation of invert micro-emulsion
Preparation of invert micro-emulsion
Preparation of invert micro-emulsion
Blending equipment
Continuous
Filtration in continuous-type scroll
centrifuges / intermittent filtration in regular
centrifuges
Filtration in continuous-type scroll
centrifuges / intermittent filtration in regular
centrifuges
Scroll centrifuges for
continuous filtration
Wet formation of bead catalyst
in oil column
Equipment for wet formation
of bead catalysts
Autoclaves for continuous
zeolite crystallization
Development of
technologies for catalyst
granulation without
binding agents
Single-time intermittent ion exchange
in autoclaves at high pressure and
temperature
Single-time intermittent ion exchange
in autoclaves at high pressure and
temperature
Improvement of technologies
for wet formation of bead
catalyst in oil column
Legend:
Preparation of water solutions
Preparation of water solutions
Preparation of water solutions
© State Corporation “Russian Corporation of
Nanotechnologies”, 2010
T
e

7. Strategic Goals of Russian Producers
Technology Import
Production of carbon
nano-fibers
Associated petroleum
gas aromatization
Associated petroleum
gas aromatization
Production of carbon
nano-fibers
Russian R&D
Nanotechnology Applications in Catalytic Petroleum Refining Processes. Processing of Associated Petroleum Gas – Part II
CATALYST MARKETSScientific and Technical
Development
Catalyst Production Technologies Processes and Catalysts (Compounds)
Technology
2020 203020152010
Introduction of Russia's own full-cycle catalyst
production technologies
Leading edge—
—
20%
of Russian
market
10%
of Russian
market
5%
of Russian
market
Not produced in
Russia
Marketing
Quality
Medium Medium Medium Medium
High High High High
Medium Medium Medium Medium
Medium Medium Medium Medium
Labor consumption
Technical and Economic Characteristics
2020 203020152010
Capital Intensity
Productivity
Power consumption
Technology for Preparation of Cobalt or Iron Nano-Particles Used as Catalysts in
Fisher-Tropsch Process
Preparation of
solution
Preparation of
feedstock
Preparation of composite
material
Autoclave
crystallization
Loading of composite material
into activating grinder
Washing,
filtration,
wastewater
disposal
Ion exchange,
modification
Mechanochemical activation
Granulation with
binding substance
Drying, baking
Thermal treatment
Application of
dehydration
component
Forming
Main Stages of Technology for Preparation of Catalysts for Aromatization of Associated
Petroleum Gas on the Basis of ZSM-5 Type Zeolites
Main Stages of Technology for Preparation of Oxide Catalysts for Pyrolysis of
Hydrocarbons into Carbon Nano-Fibers
RussianMarket
Catalyst type:
Cobalt or iron nano-particles
2020 203020152010
Number of units
Total capacity, kta
Annual consumption, tons
Annual consumption, $mln
—
—
—
—
2
100
20
0,65
20
1 000
200
6,5
50
2 500
500
16,5
Catalyst type:
On the basis of ZSM-5 type zeolites
2020 203020152010
Number of units .
Total capacity, kta
Annual consumption, tons
Annual consumption, $mln
—
—
—
—
2
0,4
12
0,02
8
2
50
0,07
100
50
1 000
1
Catalyst type:
Membrane-catalytic
2020 203020152010
Number of units
Total capacity, kta
Annual consumption, tons
Annual consumption, $mln
—
—
—
—
2
0,4
12
0,02
8
2
50
0,07
100
50
1 000
1
Catalyst type:
Iron or nickel nano-dispersed
2020 203020152010
Total capacity, mta
Annual consumption, kta
Annual consumption, $mln
0,2
70
0,5
1,5
600
4
8
3 000
20
40
10 000
80
Catalyst type: Powdered micron systems composed of
nickel and iron nano-particles
2020 203020152010
Total capacity, mta
Annual consumption, ktaт
Annual consumption, $mln
0,8
0,4
2
8
3
20
40
12
100
200
50
500
Catalyst type:
On the basis of medium-porous ZSM-5 type zeolites
2020 203020152010
Тotal capacity, mta
Annual consumption, kta
Annual consumption, $mln
—
—
—
200
60
2,1
2 500
750
26
12 500
3 800
110
WorldMarket
х0,1
х0,1
х0,1
х0,1
0,5 – 1,5
0,5 – 1,5
0,5 – 1,5
0,5 – 1,5
0,2 – 0,3
0,2 – 0,3
0,2 – 0,3
0,2 – 0,3
0,3 – 0,4
0,3 – 0,4
0,3 – 0,4
0,3 – 0,4
32,7
32,7
32,7
32,7
70 – 72
70 – 72
40 – 45
40 – 452010
2015
2020
2030
Catalyst:
On the basis
of ZSM-5 type
zeolites
Process:
Aromatization of associated petroleum
gas in adiabatic reactors with fixed
catalyst bed
Development of more
efficient methods to modify
zeolites to improve their
selectance
Improvement of
technologies for wet
formation of bead catalyst
in oil column
Thermal treatment
equipment
Spray dryers
Granular materials
classification equipment
Autoclaves for continuous
zeolite crystallization
Improvement of
technology for
continuous synthesis of
ZSM-5 type zeolites
1
Mechanical grinding in
ball crushers (preparation
of water – process
condensate, electrical
desalination
Solution of salts in
water, mechanical
blending
Intermitten
Filtration in nutch
filters or press
filters
Intermittent ion
exchange in agitators
with heating at
atmospheric pressure
Granulation in
screw extruders
integrated with
z-shape blade
mixers
Intermittent
impregnation
(possibly
combined with
ion exchange)
Intermittent in
muffle furnace
/ intermittent or
continuous in
shaft furnaces
2
Mechanical grinding in
ball crushers (preparation
of water – process
condensate, electrical
desalination
Solution of salts in
water, mechanical
blending
Intermitten
Filtration in
continuous-type
scroll centrifuges
/ intermittent
filtration in regular
centrifuges
Intermittent ion
exchange in
autoclaves at
high pressure and
temperature
Granulation in
screw extruders
integrated with
z-shape blade
mixers
Intermittent
impregnation
(possibly
combined with
ion exchange)
Intermittent in
muffle furnace
/ intermittent or
continuous in
shaft furnaces
3
Mechanical grinding in
ball crushers (preparation
of water – process
condensate, electrical
desalination
Solution of salts in
water, mechanical
blending
Intermitten
Granulation in
screw extruders
integrated with
z-shape blade
mixers
Continuous
impregnation
(by analogy
with preparation
of reforming
catalysts)
Continuous in
regular or vacuum
belt furnaces
5
Mechanical blending of metal
oxides and catalyst carrier
Blending of oxide composite material
with (possibly ceramic) grinding
bodies in specified proportion (weight
of grinding bodies / weight of blend)
In planetary grinder
Formation of catalyst powder
in spray dryer
Baking of formed catalyst under
specified regime
6 —
7 —
4
Mechanical grinding
in planetary crushers
(preparation of water –
distillation, ion-exchange
resins), possible
ultrasonic crushing of
inoculant
Solution of salts in
water, mechanical
blending
Continuous
Wet formation of
bead catalyst in oil
column
Continuous in
regular or vacuum
belt furnaces
Low Medium High High
х1 х1 х0,9 х0,7
х1 х1 х0,8 х0,6
х1 х1 х1 х1
80 80 90 95
Labor consumption
Technical and Economic Characteristics
2020 203020152010
Capital Intensity
Productivity
Power consumption
Yield ratio, %
Technology for Preparation of Oxide Catalysts for Pyrolysis of Hydrocarbons into
Carbon Nano-Fibers (CNF
Productivity,tonsoffeedstock/tons
ofcatalystperhour
Laborconsumption(comparedto
thecurrentvalueofFischer-Tropsch
process)
Powerconsumption
(comparedtothecurrentvalue
ofFischer-Tropschprocess)
С5+selectance,%
Price,th$/t
Technical and Economic
Characteristics of the Process
Catalyst
Specifications
Capitalintensity(comparedtothe
currentvalueforFischer-Tropsch
(ORYX=1.5mmtofproductsper
year,CAPEX=$1000pertonper
year)
Strength,kg/mm2
Servicecycle,months
Powerconsumption,
Whr/tonoffeedstock
Totalservicelife,years
Price,th$/t
Technical and Economic
Characteristics of the
Process
Catalyst Specifications
Capitalintensity(comparedtothe
currentvalueforFischer-Tropsch
(ORYX=1.5mmtofproductsper
year,CAPEX=$1000pertonper
year)
х0,8
х0,9
х01
х1
х0,9
х0,9
х1
х1
50 – 80
30 – 50
30 – 40
20 – 30
Multiple
Multiple
Single
Single
95
90
80
80
1
1,4
1,6
1,6
2015
2020
Catalyst:
Powdered micron systems composed of
nickel and iron nano-particles
Process:
Catalytic pyrolysis with
CNF yield
2010
2030
х0,9
х1
х1
—
х0,8
х0,9
х1
—
70 – 90
50 – 80
30 – 50
—
Multiple
Multiple
Single
—
80
80
70
—
1,6
1,4
1
—2010
2015
2020
Catalyst:
Iron or nickel nano-dispersed
Process:
Catalytic pyrolysis with
CNF yield
2030
Filtration in
continuous-type
scroll centrifuges
/ intermittent
filtration in regular
centrifuges
Filtration in
continuous-type
scroll centrifuges
/ intermittent
filtration in regular
centrifuges
Scroll centrifuges for
continuous filtration
Equipment for wet
formation of bead
catalysts
In planetary grinder (one-stage
catalyst preparation: after
activation, powder does not need
to be dried or baked)
In planetary grinder
Blending of oxide composite material
with (possibly ceramic) grinding
bodies in specified proportion (weight
of grinding bodies / weight of blend)
Blending of oxide composite material
with (possibly ceramic) grinding
bodies in specified proportion (weight
of grinding bodies / weight of blend)
Mechanical blending of metal
oxides and catalyst carrier
Mechanical blending of metal
oxides and catalyst carrier
Continuous
impregnation
(by analogy
with preparation
of reforming
catalysts)
Intermittent ion
exchange in
autoclaves at
high pressure and
temperature
Intermittent ion
exchange in
autoclaves at
high pressure and
temperature
Development of
industrial technologies
for mechanochemical
synthesis of catalysts
Formation of catalyst powder
in spray dryer
Optimization of
mechanochemical synthesis
of catalysts for associated
petroleum gas pyrolysis
Development of method
to prepared catalysts
with the use of massive
metallic articles and
alloys based on metals
of 8th group
—
— Normalized assessment of current
parameter values. This assessment is
used as the basis for future estimations
of the same parameters in all analyzed
sectors
Legend:
— High-quality production
technology
— Low-cost technology х1
High-capacity planetary
grinders
© State Corporation “Russian Corporation of
Nanotechnologies”, 2010

8. With low
content of
bonding agent
Intermittent Intermittent Contact
Mechanical
grinding
Mechanical
blending2
Continuous Continuous Contact
Mechanical
grinding
Mechanical
blending3
With medium
content of
bonding agent
Intermittent Contactless
Ultrasonic
grinding
Feedstock
activation by
means of ultra
sound or magnetic
radiation
4
With low
content of
bonding agent
Intermittent
Russian R&D
Nanotechnology Applications in Catalytic Petroleum Refining Processes. Isobutane-Butylene Alkylation
CATALYST MARKETSScientific and Technical
Development
Catalyst Production Technologies
Zeolite-based
Processes and Catalysts (Compounds)
Preparation of
feedstock
Preparation of
solution
Crystallization Ion exchange Granulation,
injection of
bonding agent
Drying and
baking
Catalyst Main Production Stages
Capital intensity ($ per ton of
alkyl gasoline per year)
— 115 110 100
Medium Medium Low Low
Medium Medium Low Low
— 190 180 170
Power consumption (OPEX,
$ per ton of alkyl gasoline per
year)
Rejection rate, %
Technical and Economic Characteristics
2020 203020152010
Labor consumption
With medium
content of
bonding agent
Intermittent Intermittent Contact
Mechanical
grinding
Mechanical
blending
Strategic Goals of Russian Producers
Technology
2020 203020152010
Introduction of Russia's own full-cycle
catalyst production technologies
Leading edge
Not produced in
Russia
—
—
50%
of Russian
market
60%
of Russian
market
80%
of Russian
market
Marketing
Quality
RussianMarket
Catalyst type:
Y type (faujasite)
2020 203020152010
Number of units
Total capacity, kta
Annual consumption, kta
Annual consumption, $mln
—
—
—
—
1
50
10–15
0,5
3
550
110–165
6
9
1 750
350–525
18
Catalyst type:
Fluorine hydride
2020 203020152010
Number of units
Total capacity, kta
Annual consumption, kta
Annual consumption, $mln
—
—
—
—
1
250
15–25
0,001
1
250
15–25
0,001
1
250
15–25
0,001
Catalyst type:
Sulfuric acid
2020 203020152010
Number of units
Total capacity, kta
Annual consumption, kta
Annual consumption, $mln
7
1 100
78–112
5
9
1 600
113–162
7
9
1 600
113–162
7
9
1 600
113–162
7
1
Research in effects
of ultrasound or
magnetic radiation,
in particular
MRET (Molecular
Resonance Effect
Technology), on
feedstock activation
and, subsequently,
catalyst activity
Creation of
demonstrational
stand units to
research continuous
crystallization
Research in
application of
modern all-purpose
disintegrators-
activators
Creation of
demonstrational stand
units to research
continuous ion
exchange
Research in finding
efficient bonding
agent
Research in
application of
microwaves for
contactless baking
TechnicalandEconomic
CharacteristicsoftheProcess
(as per a ten-point scale)
Productivity
CapitalIntensity
Laborconsumption
Powerconsumption
Activity(external
isobutane:butylene
molarratio
Selectance(octane
number)
Price,th$/t
C a t a l y s t
S p e c i f i c a t i o n s
Process:
Standard
2010
2015
2020
2030 7
7
7
7
6
6
6
6
4
4
5
6
7
7
7
7
10
10
10
10
96
96
96
96
0,05
0,05
0,05
0,05
Catalyst:
Sulfuric acid
Process:
Standard
2010
2015
2020
2030 7
7
7
7
6
6
6
6
4
4
5
6
7
7
7
7
10
10
10
10
96
96
96
96
0,05
0,05
0,05
0,05
Catalyst:
Fluorine hydride
Process:
Standard
2010
5
5
5
—
8
8
8
—
4
4
5
—
8
8
8
—
10
10
10
—
1,4
1,4
1,4
—
98
98
98
—
40
40
40
—
Catalyst:
Y type (faujasite)
Technical and Economic
Characteristics of the Process
(as per a ten-point scale)
Productivity
CapitalIntensity
Laborconsumption
Powerconsumption
Activity(external
isobutane:butylene
molarratio
Selectance(octane
number)
Price,th$/t
C a t a l y s t
S p e c i f i c a t i o n s
Crushingstrength,
kg/mm2
2030
2020
2015
Legend:
— High-quality production
technology
— Low-cost technology
Consistent with platinum salt production
method
Lower production costs 2030 or later
Production stages Advantages Appearance time
Technology
Injection of nano-sized precursor into the reaction system with subsequent
extraction of precursor from the reaction product and return into the process
© State Corporation “Russian Corporation of
Nanotechnologies”, 2010

9. Leading edge
Process:
Standard
Process:
Standard
Russian R&D
Nanotechnology Applications in Catalytic Petroleum Refining Processes. Production of Isopropyl Benzene
CATALYST MARKETSScientific and Technical
Development
Technology for Preparation of Zeolite-Based Catalysts Processes and Catalysts (Compounds)
Preparation of
feedstock
Preparation of
solution
Crystallization Ion exchange Granulation,
injection of
bonding agent
Drying and
baking
Catalyst Main Production Stages
Capital intensity ($ per ton of
isopropyl benzene per year)
70 65 65 60
Medium Moderate Low Low
Medium Medium Low Low
1,4 1,2 1,2 1,2
Power consumption (OPEX,
$ per ton of alkyl gasoline per
year)
Rejection rate, %
Technical and Economic Characteristics
2020 203020152010
Labor consumption
Strategic Goals of Russian Producers
Leading edge
2020 203020152010
Introduction of Russia's own full-cycle
catalyst production technologies
Not produced in
Russia
—
—
50%
of Russian
market
50–80%
share of Russian
market
100%
of Russian
market
Marketing
Quality
RussianMarket
With medium
content of
bonding agent
Contact
Mechanical
grinding
Mechanical
blending
1
With low
content of
bonding agent
Contactless
Mechanical
grinding
Mechanical
blending2
Continuous
Ultrasonic
grinding
Feedstock
activation
by means of
ultra sound
or magnetic
radiation
4 Continuous
INTERMITTENT INTERMITTENT CONTACTLESS
ULTRASONIC
GRINDING
FEEDSTOCK
ACTIVATION BY
MEANS OF ULTRA
SOUND OR MAGNETIC
RADIATION
3
WITH LOW
CONTENT OF
BONDING AGENT
2010
7
7
7
7
6
6
6
6
4
4
5
6
7
7
7
7
8
8
10
10
1,4
1,4
1,4
1,4
85
85
85
85
50
50
50
50
Technical and Economic
Characteristics of the
Process(as per a ten-oint
s c al e)
Productivity
CapitalIntensity
Laborconsumption
Powerconsumption
Activity(external
benzene:propylene
molarratio
Isopropylbenzene
selectivity,%wght
Price,th$/t
C a t a l y s t
S p e c i f i c a t i o n s
Crushingstrength,
kg/mm2
2030
2020
2015
RussianAlternative
Technology
Catalyst type:
Aluminum chloride (AlCl3)
2020 203020152010
Number of units
Total capacity, kta
Annual consumption, kta
Annual consumption, $mln
4
600
4 200
23
2
300
2 100
11,5
1
150
1 050
5,7
—
—
—
—
World
Market
World Market
2020 203020152010
Total capacity, kta
Annual consumption, kta
12 600
800–1 300
15 300
1 000–1 500
17 300
1 100–1 700
18 000
1 200–1 800
WorldAlternative
Technology
Catalyst type: H3PO4 (phosphoric acid on carrier)
2020 203020152010
Number of units
Total capacity, kta
Annual consumption, kta
18
5 400
16 000
9
2 700
8 000
3
680
2 000
—
—
—
2010
8
8
8
8
5
5
5
5
4
4
5
6
6
6
6
6
5
5
6
6
1,4
1,4
1,4
1,4
90
90
90
90
60
60
60
60
Catalyst:
MCM-22
2030
2020
2015
Catalyst:
BETA zeolite
Catalyst type:BETA zeolite
2020 203020152010
Number of units
Total capacity, kta
Annual consumption, kta
Annual consumption,
$mln
—
—
—
—
2
300
19–30
1,25
3
450
29–45
1,9
3
450
29–45
1,9
Catalyst type:MCM-22
2020 203020152010
Number of units
Total capacity, kta
Annual consumption, kta
Annual consumption,
$mln
—
—
—
—
—
—
—
—
—
—
—
—
1
150
9–15
0,7
Continuous Continuous
Research in
application of
modern all-purpose
disintegrators-
activators
Research in effects
of ultrasound or
magnetic radiation,
in particular
MRET (Molecular
Resonance Effect
Technology), on
feedstock activation
and, subsequently,
catalyst activity
Consistent with platinum salt production
method
Lower production costs 2030 or later
Production stages Advantages Appearance time
Technology
Injection of nano-sized precursor into the reaction system with subsequent
extraction of precursor from the reaction product and return into the process
Continuous Continuous
Creation of
demonstrational stand
units to research
continuous ion
exchange
Creation of
demonstrational
stand units to
research continuous
crystallization
With low
content of
bonding agent
Research in finding
efficient bonding
agent
Contactless
Research in
application of
microwaves for
contactless baking
Legend:
— High-quality production
technology
—Low-cost technology
© State Corporation “Russian Corporation of
Nanotechnologies”, 2010

10. With low
content of
bonding agent
Intermittent Intermittent Contact
Mechanical
grinding
Mechanical
blending2
Continuous Continuous Contact
Mechanical
grinding
Mechanical
blending3
With medium
content of
bonding agent
Continuous Contactless
Mechanical
grinding
Mechanical
blending4
With low
content of
bonding agent
Continuous
RussianMarketWorld
Market
WorldAlternative
Technology
Technology Import
Russian R&D
Nanotechnology Applications in Catalytic Petroleum Refining Processes. Production of Ethyl Benzene
CATALYST MARKETS
Strategic Goals of Russian Producers
Scientific and Technical
Development
Catalyst Production Technologies
Zeolite-based
Processes and Catalysts (Compounds)
Preparation of
feedstock
Preparation of
solution
Crystallization Ion exchange Granulation,
injection of
bonding agent
Drying and
baking
Catalyst Main Production Stages
Capital intensity ($ per ton of
ethyl benzene per year)
75 70 65 60
Medium Medium Low Low
Medium Medium Low Low
1,6 1,4 1,4 1,2
Power consumption (heat
consumption, GJ per ton of
ethyl benzene per year)
Rejection rate, %
Technical and Economic Characteristics
2020 203020152010
Labor consumption
Technology
2020 203020152010
With medium
content of
bonding agent
Intermittent Intermittent Contact
Mechanical
grinding
Mechanical
blending
Introduction of Russia's own full-cycle catalyst
production technologies
Leading edge
Not produced in
Russia
—
—
20% of Russian
market
50% of Russian
market
80% of Russian
market
Technology:AlCl3
2020 203020152010
Number of units
Total capacity, kta
Annual consumption, kta
Price, th$/t
Marketing
Quality
RussianAlternative
Technology
Catalyst type:Aluminum chloride (AlCl3)
2020 203020152010
Number of units
Total capacity, kta
Annual consumption, kta
Annual consumption, $mln
3
575
6 900–8 600
5,5
2
440
5 250–6 600
5,5
1
345
4 150–5 200
5,5
—
—
—
—
Catalyst type:ZSM-5
2020 203020152010
Number of units
Total capacity, kta
Annual consumption, kta
Annual consumption, $mln
1
230
7–8
40
—
—
—
—
—
—
—
—
—
—
—
—
Catalyst type:BETA zeolite
2020 203020152010
Number of units.
Total capacity, kta
Annual consumption, kta
Annual consumption, $mln
—
—
—
—
2
450
8–11
50
3
542
11
50
3
542
11
50
Catalyst type:Transalkylation, type Y
2020 203020152010
Number of units
Total capacity, kta
Annual consumption, kta
Annual consumption, $mln
—
—
—
—
2
450
8–10
40
3
545
9–12
40
5
1100
19–24
40
Catalyst type:MCM-22
2020 203020152010
Number of units
Total capacity, ktaг
Annual consumption, kta
Annual consumption, $mln
—
—
—
—
—
—
—
—
—
—
—
—
2
545
11–13
60
Catalyst Type:Zeolite catalysts
2020 203020152010
Number of units
Total capacity, kta
Annual consumption, kta
52
21 700
660
58
23 700
720
64
26 200
800
70
28 700
870
17
6900
82,8–103,5
5,5
12
4900
58,8–73,5
5,5
6
2500
30–37,5
5,5
—
—
—
—
1
Ultrasonic
grinding
Feedstock
activation by
means of ultra
sound or magnetic
radiation
5 Contactless
With low
content of
bonding agent
IntermittentIntermittent
Equipment for feedstock
activation by means of
ultra sound or magnetic
radiation
Ultrasonic grinding
equipment
TechnicalandEconomic
CharacteristicsoftheProcess
(as per a ten-point scale)
Productivity
CapitalIntensity
Laborconsumption
Powerconsumption
Activity(externalbenzene:
ethylenemolarratio
Crushingstrength,
kg/mm2
Ethylenebenzene
selectivity,%wght
Price,th$/t
C a t a l y s t S p e c i f i c a t i o n s
Process:
Standard
2010
2015
2020
2030 5
5
5
5
8
8
8
8
4
4
5
6
8
8
8
8
10
10
10
10
1,4
1,4
1,4
1,4
80
80
80
80
40
40
40
40
Catalyst:
Transalkylation,
type Y
Process:
Standard
2015
2020
2030 5
5
5
5
8
8
8
8
4
4
5
6
9
9
9
9
8
8
8
8
1,4
1,4
1,4
1,4
80
80
80
80
40
40
40
40
Catalyst:
ZSM-5 (pentasil)
Process:
Standard
2010
2015
7
7
7
7
6
6
6
6
4
4
5
6
7
7
7
7
5
5
6
6
1,4
1,4
1,4
1,4
85
85
85
85
50
50
50
50
Catalyst:
BETA zeolite
Process:
Standard
2010
2015
2020
5
5
5
5
8
8
8
8
4
4
5
6
6
6
6
6
3
3
4
4
1,4
1,4
1,4
1,4
90
90
90
90
60
60
60
60
Catalyst:
MCM-22
Исследования
по влиянию
ультразвука или
магнитного излуче
ния, в частности,
технологии MRET
(Molecular
Resonance Effect
Technology)
на процесс
активации сырья
и вдальнейшем
на активность
катализатора
Continuous Continuous
Ultrasonic
grinding
Feedstock
activation by
means of ultra
sound or magnetic
radiation
6 Contactless
With low
content of
bonding agent
Research in effects
of ultrasound or
magnetic radiation,
in particular
MRET (Molecular
Resonance Effect
Technology), on
feedstock activation
and, subsequently,
catalyst activity
Research in
application
of modern
all-purpose
disintegrators-
activators
Creation of
demonstrational
stand units to
research continuous
crystallization
Creation of
demonstrational stand
units to research
continuous ion
exchange
Research in finding
efficient bonding
agent
Research in
application of
microwaves for
contactless baking
2010
2030
2020
2030
Consistent with platinum salt production
method
Lower production costs 2030 or later
Production stages Advantages Appearance time
Technology
Injection of nano-sized precursor into the reaction system with subsequent
extraction of precursor from the reaction product and return into the process
Legend: — High-quality production
technology
— Low-cost technology
© State Corporation “Russian Corporation of
Nanotechnologies”, 2010