Nanotechnology Applications in Catalytic Petroleum...
Transcript of Nanotechnology Applications in Catalytic Petroleum...
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
Ru
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Ma
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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
Prod
uctiv
ity (S
pace
Ve
loci
ty),
hr.^
-1
Capi
tal I
nten
sity
Pow
er C
onsu
mpt
ion
Resi
dual
Sul
fur
Cont
ent,
ppm
Activ
ity
Stre
ngth
Cata
lyst
Ser
vice
Life
be
fore
Reg
ener
atio
n,
year
s
Pric
e, th
$/t
Technical and Economic Characteristics of the
ProcessC 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 siteBaking 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 100Labor 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 nitrogencontent
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 oxideActive 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 oxideActive 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
Wo
rld
Ma
rke
t 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: aluminaActive 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
Ru
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Ma
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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 hydroxide3. 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 Cata lyst Product ion 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 heatingIn 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
hydroxide3. Clay drying
block
In fire furnace1
Blending of zeolite and
aluminosilicate matrix
Electric heatingIn 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 hydroxide3. 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
Microsphero ida l Cata lyst Product ion Technology
Yiel
d of
des
ired
prod
uct
(gas
olin
e cu
t) pe
r ton
of
feed
stoc
k (a
nnua
l ope
ratio
n tim
e: 8
,000
hr)
, %
Capi
tal i
nten
sity
(at 6
00
kta
thro
ughp
ut)
Man
ual l
abor
sha
re
Pow
er c
onsu
mpt
ion,
kW
hr/to
n of
feed
stoc
k
Activ
ity (c
rack
ing
conv
ersi
on ra
tio),
%
Mic
ro-a
ctiv
ity, %
Wea
ring
qual
ity, %
Pric
e, 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
Catalysts2020 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
Wo
rld
Ma
rk
et
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
hydroxide3. Clay drying block
4Blending 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
hydroxide3. 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
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 edgeSlightly 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
Prod
uctiv
ity, t
ons
of
feed
stoc
k / t
ons
of c
atal
yst
per h
our
Capi
tal I
nten
sity
Labo
r con
sum
ptio
n
Pow
er c
onsu
mpt
ion
% o
f byp
rodu
cts
Stre
ngth
, kg/
cm
Sele
ctan
ce, %
wgh
t
Pric
e, 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
Reduction in hydrogen
stream
Non-residuum
impregnationContactless
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
Octa
ne N
umbe
r
Gaso
line
Yiel
d, %
wgh
t
ТLab
or c
onsu
mpt
ion
Spac
e Ve
loci
ty),
hr.^
-1
Capi
tal I
nten
sity
Pow
er C
onsu
mpt
ion,
kW
/t
Mic
ro-a
ctiv
ity, %
Wea
ring
qual
ity, %
Pric
e, th
$/t
Technical and Economic Characteristics of the Process
Catalyst Specifications
Ru
ss
ia
n
Ma
rk
et
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 Wo
rld
Ma
rk
et
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
impregnationContact
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
impregnationContact
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
streamКонтактная4 With poly-
sulfides
Chlorination with gaseous
HCl
Low-temperature heating in furnace
Extrusion
Reduction in hydrogen
streamContactless5 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
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
Technica l and Economic Character is t ics o f the
ProcessEconomicCharacter is t ics o f the ProcessProcess
Prod
uctiv
ity (a
mou
nt o
f fe
edst
ock
proc
esse
d,
tons
)
Pow
er c
onsu
mpt
ion
Activ
ity
Sele
ctan
ce
Wea
ring
qual
ity, %
Pric
e, th
$/t
C a t a l y s t S p e c i f i c a t i o n s
Stre
ngth
Wo
rld
Ma
rk
et
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
Ru
ss
ian
Ma
rk
et
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
C
apita
l Int
ensi
ty
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 х0,870 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 х0,3х0,3 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 content5
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
Prod
uctiv
ity, t
ons
of fe
edst
ock
/ ton
s of
ca
taly
st p
er h
our
Capi
tal i
nten
sity
(com
pare
d to
the
curr
ent v
alue
for F
isch
er-T
rops
ch
(ORY
X =
1.5
mm
t of p
rodu
cts
per y
ear,
CAPE
X =
$100
0 pe
r ton
per
yea
r)
ТPow
er c
onsu
mpt
ion
(com
pare
d to
the
cur
rent
val
ue o
f Fis
cher
-Tro
psch
pro
cess
)
Pow
er c
onsu
mpt
ion
(com
pare
d to
the
curr
ent v
alue
of F
isch
er-
Trop
sch
proc
ess)
С5+
sele
ctan
ce, %
Met
hane
sel
ecta
nce,
%
Stre
ngth
, kg/
cm2
Pric
e, th
$/t
Technical and Economic Characteristics of the
Process
Catalyst Specifications
Prod
uctiv
ity, k
g of
pro
duct
(gas
olin
e
Capi
tal i
nten
sity
(com
pare
d to
the
curr
ent v
alue
for F
isch
er-T
rops
ch
(ORY
X =
1.5
mm
t of p
rodu
cts
per y
ear,
CAPE
X =
$100
0 pe
r ton
per
yea
r)
Pow
er c
onsu
mpt
ion,
Whr
/ton
of
feed
stoc
k
Serv
ice
cycl
e, m
onth
s
Tota
l ser
vice
life
, yea
rs
Stre
ngth
, kg/
mm
2
Pric
e, 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
Wo
rl
d
Ma
rk
et
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
Ru
ss
ia
n
Ma
rk
et
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 catalystscirculate 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
Strategic Goals of Russian Producers
Technology Import
Production of carbonnano-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 Preparat ion of Cobal t or I ron Nano-Par t ic les Used as Cata lysts in F isher-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
Ru
ss
ia
n
Ma
rk
et
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
Wo
rl
d
Ma
rk
et
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
blendingIntermitten
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
blendingIntermitten
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
blendingIntermitten
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
5Mechanical 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 grinderFormation of catalyst powder
in spray dryerBaking 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
blendingContinuous
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 Preparat ion of Ox ide Cata lysts for Pyro lys is o f Hydrocarbons in to Carbon Nano-F ibers (CNF
Prod
uctiv
ity, t
ons
of fe
edst
ock
/ ton
s of
cat
alys
t per
hou
r
Labo
r con
sum
ptio
n (c
ompa
red
to
the
curr
ent v
alue
of F
isch
er-T
rops
ch
proc
ess)
Pow
er c
onsu
mpt
ion
(com
pare
d to
the
curr
ent v
alue
of F
isch
er-T
rops
ch p
roce
ss)
С5+
sele
ctan
ce, %
Pric
e, th
$/t
Technical and Economic Characteristics of the Process
Catalyst Specifications
Capi
tal i
nten
sity
(com
pare
d to
the
curr
ent v
alue
for F
isch
er-T
rops
ch
(ORY
X =
1.5
mm
t of p
rodu
cts
per
year
, CAP
EX =
$10
00 p
er to
n pe
r ye
ar)
Stre
ngth
, kg/
mm
2
Serv
ice
cycl
e, m
onth
s
Pow
er c
onsu
mpt
ion,
Whr
/ton
of fe
edst
ock
Tota
l ser
vice
life
, yea
rs
Pric
e, th
$/t
Technical and EconomicCharacteristics of the
ProcessCatalyst Specifications
Capi
tal i
nten
sity
(com
pare
d to
the
curr
ent v
alue
for F
isch
er-T
rops
ch
(ORY
X =
1.5
mm
t of p
rodu
cts
per
year
, CAP
EX =
$10
00 p
er to
n pe
r ye
ar)
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
With low content of
bonding agentIntermittent Intermittent Contact
Mechanical grinding
Mechanical blending2
Continuous Continuous ContactMechanical
grindingMechanical
blending3With medium
content of bonding agent
Intermittent ContactlessUltrasonic grinding
Feedstock activation by
means of ultra sound or magnetic
radiation
4With 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 TechnologiesZeolite-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 170Power consumption (OPEX, $ per ton of alkyl gasoline per year)
Rejection rate, %
Technical and Economic Characteristics
2020 203020152010
Labor consumption
With medium content of
bonding agentIntermittent 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
Ru
ss
ia
n
Ma
rk
et
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
Technical and Economic Characteristics of the Process (as per a ten-point scale)
Prod
uctiv
ity
Capi
tal I
nten
sity
Labo
r con
sum
ptio
n
Pow
er c
onsu
mpt
ion
Activ
ity(e
xter
nal
isob
utan
e : b
utyl
ene
mol
ar ra
tio
Sele
ctan
ce (o
ctan
e nu
mbe
r)
Pric
e, 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 EconomicCharacteristics of the Process
(as per a ten-point scale)
Prod
uctiv
ity
Capi
tal I
nten
sity
Labo
r con
sum
ptio
n
Pow
er c
onsu
mpt
ion
Activ
ity(e
xter
nal
isob
utan
e : b
utyl
ene
mol
ar ra
tio
Sele
ctan
ce (o
ctan
e nu
mbe
r)
Pric
e, th
$/t
C a t a l y s t S p e c i f i c a t i o n s
Crus
hing
stre
ngth
,
kg/m
m2
2030
2020
2015
Legend:
— High-quality production technology
— Low-cost technology
Consistent with platinum salt production method Lower production costs 2030 or later
Production stages Advantages Appearance time
Technology
Injection of nano-sized precursor into the reaction system with subsequent
extraction of precursor from the reaction product and return into the process
Leading edge
Process:Standard
Process:Standard
Russian R&D
Nanotechnology Applications in Catalytic Petroleum Refining Processes. Production of Isopropyl Benzene
CATALYST MARKETSScientific and Technical Development
Technology for Preparation of Zeolite-Based Catalysts Processes and Catalysts (Compounds)
Preparation of feedstock
Preparation of solution
Crystallization Ion exchange Granulation, injection of
bonding agent
Drying and baking
Catalyst Main Production Stages
Capital intensity ($ 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 1,2Power 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
Ru
ss
ian
Ma
rk
et
With medium content of
bonding agentContact
Mechanical grinding
Mechanical blending
1
With low content of
bonding agentContactless
Mechanical grinding
Mechanical blending2
ContinuousUltrasonic grinding
Feedstock activation
by means of ultra sound or magnetic
radiation
4 Continuous
IntermIttent IntermIttent ContaCtlessUltrasonIC
grIndIng
FeedstoCk aCtIvatIon by
means oF Ultra soUnd or magnetIC
radIatIon
3WIth 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
Te c h n i c a l a n d E c o n o m i c C h a r a c t e r i s t i c s o f t h e
P r o c e s s ( a s p e r a t e n - o i n t s c a l e )
Prod
uctiv
ity
Capi
tal I
nten
sity
Labo
r con
sum
ptio
n
Pow
er c
onsu
mpt
ion
Activ
ity (e
xter
nal
benz
ene
: pro
pyle
ne m
olar
ratio
Isop
ropy
l ben
zene
se
lect
ivity
, % w
ght
Pric
e, th
$/t
C a t a l y s t S p e c i f i c a t i o n s
Crus
hing
stre
ngth
,
kg/m
m2
2030
2020
2015
Russ
ian
Alte
rnat
ive
Tech
nolo
gy
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
—
—
— —
Wo
rld
M
ar
ke
t
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
Wor
ld A
ltern
ativ
e Te
chno
logy
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, $mln
—
—
—
—
—
—
—
—
—
—
—
—
1
150
9–15
0,7
Continuous Continuous
Research in application of modern all-purpose disintegrators-activators
Research in effects of ultrasound or magnetic radiation, in particular MRET (Molecular Resonance Effect Technology), on feedstock activation and, subsequently, catalyst activity
Consistent with platinum salt production method Lower production costs 2030 or later
Production stages Advantages Appearance time
Technology
Injection of nano-sized precursor into the reaction system with subsequent
extraction of precursor from the reaction product and return into the process
Continuous Continuous
Creation of demonstrational stand units to research continuous ion exchange
Creation of demonstrational stand units to research continuous crystallization
With low content of
bonding agent
Research in finding efficient bonding agent
Contactless
Research in application of microwaves for contactless baking
Legend:
— High-quality production technology
—Low-cost technology
With low content of
bonding agentIntermittent Intermittent Contact
Mechanical grinding
Mechanical blending2
Continuous Continuous ContactMechanical
grindingMechanical
blending3With medium
content of bonding agent
Continuous ContactlessMechanical
grindingMechanical
blending4With low
content of bonding agent
Continuous
Ru
ss
ia
n
Ma
rk
et
Wo
rld
M
ar
ke
t
Wor
ld A
ltern
ativ
e Te
chno
logy
Technology Import
Russian R&D
Nanotechnology Applications in Catalytic Petroleum Refining Processes. Production of Ethyl Benzene
CATALYST MARKETS
Strategic Goals of Russian Producers
Scientific and Technical Development
Catalyst Production TechnologiesZeolite-based
Processes and Catalysts (Compounds)
Preparation of feedstock
Preparation of solution
Crystallization Ion exchange Granulation, injection of
bonding agent
Drying and baking
Catalyst Main Production Stages
Capital intensity ($ 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 1,2Power 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 agentIntermittent 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
Russ
ian
Alte
rnat
ive
Tech
nolo
gy
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 ContactlessWith low
content of bonding agent
IntermittentIntermittent
Equipment for feedstock activation by means of ultra sound or magnetic radiation
Ultrasonic grinding equipment
Technical and Economic Characteristics of the Process (as per a ten-point scale)
Prod
uctiv
ity
Capi
tal I
nten
sity
Labo
r con
sum
ptio
n
Pow
er c
onsu
mpt
ion
Activ
ity (e
xter
nal b
enze
ne :
ethy
lene
mol
ar ra
tio
Crus
hing
stre
ngth
,
kg/m
m2
Ethy
lene
ben
zene
sele
ctiv
ity, %
wgh
t
Pric
e, 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 ContinuousUltrasonic grinding
Feedstock activation by
means of ultra sound or magnetic
radiation
6 ContactlessWith 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
TechnologyInjection 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