english version based on the presentation of …kkft.bme.hu/sites/default/files/6 hp conversion...
TRANSCRIPT
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1
English version based on the presentation of
Szalmásné Dr. Pécsvári Gabriella held in 2014
Hydrocarbon processing Conversion processes
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Fractions of crude oil
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Goal of Refining
Main goal: economic production of product structure according to market demand
The whole process is called „refining”.
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Conversion processes
Driving force:
• Product slate according to market demand (quantity
demands/flexibility)
• More valuable product from one unit crude oil
(economicity)
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Cracking
1910, Burton, thermal cracking
Gasoline from crude oil
1920, Eugene Jules Houdry
Catalytic process: gasoline from lignite
1936
First catalytic cracking unit in New Jersey
1942
First fluid catalytic cracking unit
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Crude oil price and high politics
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0
10
20
30
40
50
60
70
80
90
0
1000
2000
3000
4000
5000
6000
7000
8000
9000
m/m
%
kt
Kőolaj feldolgozás, kt Fehérárú hozam, %
DR: crude oil processing and white product yield
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Flexibility of refineries
Alteration of DR product slate in the past
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EU 15 gasoline and diesel demand
0
50
100
150
200
1990
1995
2000
2005
2010
2015
Mil
lio
n T
on
nes/Y
ear
0,0
0,2
0,4
0,6
0,8
1,0
1,2
1,4
Mo
gas/D
iesel
Rati
o
Gasoline Diesel Ratio Gasoline/Diesel
Source: History IEA; Forecast Purvin & Gertz
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Conversion processes
BME VBK
Feedstock conversion of different processes:
According to feedstock:
vacuum distillate
vacuum residue
Hydrogen
introduction
Carbon removal
Thermal/Catalytic
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Cracking processes in the EU refineries
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Goal: cracking of vacuum distillates –
molecular weight and boiling
point reduction
Feed: vacuum distillates
Products: C3-C4 mixture, FCC
gasoline, gasoil (LCO)
Process parameters:
Temperature: 520 - 540 °C
Pressure: 2 – 4 barg
Contact time: 1-2 seconds
Catalyst: zeolites (Al2O3 - SiO2)
Conversion processes – Catalytic cracking
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Cracking reactions:
Thermal cracking
Catalytic cracking
Dehydrogenation
Hydrogen transfer
Polimerisation
• Yield
• Component structure
(olefin, aromatic)
• Quality
(RON, Cetane number)
Catalytic cracking – Reactions
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HC
CC
C
H
H
H
H
H
H
H
H
H
+ H+
CH3
C C2H
5
H H
H
a
b c
H2 + C9H4+
-H+ -H+ -H+
a bc
CH4 + C3H7+ C2H6 + C2H5
+
CH3CH=CHCH3 CH2=CH-CH3CH2=CH2
Main reactions: Starting reaction is the carbenium ion formation
Reaction is taking place on the acidic
centers of the catalyst (Lewis/Bronsted)
via carbenium ions, examples:
Beta chain scission
Hydrogen transfer
Aromatics dealkylation
Isomerisation
C
H
H
H
+
Fluid Catalytic Cracking – FCC
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Houdry fixed bed cracking Reaction is taking place in the „riser”
Fluid bed
Fluid Catalytic Cracking
plyn plyn
Pevné lôžko
lôžko
Fluidizované
U < U mf
Žiadny tok
U > U mf
Tečie
Fluid bed – continuous catalyst activity
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Fluid Catalytic Cracking
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Product distribution:
• Fuel gas 3-5 %
• C3-C4 fraction 7-20 %
• Gasoline 30-60 %
• LCO+HCO 11-20 %
• MCB 10 -15%
• Coke 4-5%
Fluid Catalytic Cracking
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Fluid Catalytic Cracking – FCC complex block scheme
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Fluid Catalytic Cracking
UOP „High-efficiency”
regenerator
Exxon
flexicracking
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View of DR FCC unit
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Goal: Increasing the white product
yield (production of smaller
molecules from the feed
molecules, under hydrogen
atmosphere)
Feed: vacuum distillate, vacuum
residue
Main products: diesel, gasoline
Process parameters:
Temperature: 300 - 450 °C
Pressure: 70 – 250 bar
Catalyst: Co/Mo/Pd/Pt on
SiO2/Al2O3
Conversion processes – Hydrocracking
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HDT and HCK catalysts
HCK catalysts
Acidic matrix
(cracking function)
Dispersed metals
(hydrotreating function)
amorphous
SiO2-Al2O3,
Al2O3,
x-Al2O3
(x=halogen)
Low
zeolite ratio
- amorph
(modif.Y/
SiO2.Al2O3)
Noble metals
(Pt, Pd)
MXSY z VIA gr. (Mo, W)
+ VIIIA gr. (Co, Ni) High
zeolite ratio
(modif.Y+
Al2O3)
In order to have efficient coproduction of the two function, high
active surface is needed
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HDT and HCK reactions
(in the order of occurence)
• C-C bond rupture and hydrogen addition on two function catalysts
• C-C bond rupture and hydrogen addition HDT on active centers (hydrogenolysis)
• Non catalytic: C-C bond radical rupture and hydrogen addition (hydropyrolysis)
• Other reactions
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R
+ 3H2
R Aromatic
hydrogenation
R
+ H2 + RH
hydrodealkylation
R
+ H2 + RH
hydrodealkylation
HDT and HCK reactions
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R
hydrodecyclisation
+ 2H2 R + C2H6 + C2H6
CnH2n+2 + H2 (a + b = n) CaH2a+2 + CbH2b+2 Paraffins
hydrocracking
Paraffins
isomerisation
HDT and HCK reactions
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Feed to the HCK plant: vakuum distillate (VGO)
• Catalyst poisons:
• Basic nitrogen compounds
• Metals (V, Ni, Fe, Na, Cu, Pb, As)
Parameter, unit Range Typical value
Density, @20˘C, kg/m3 905-921 915
Nitrogen, wt. ppm 1200-1600 1350
Sulphur, wt. ppm 1,7-2,0 1,85
CCT, wt. % 0,03-0,25 0,13
Typical values in case of REB crude
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Overall HCK scheme
HCK
gases
gasoline
diesel
Unconverted
feed
AD
VD
gases
gasoline
petroleum
vacuum residue
crude Motor fuels
Vacuum gasoil
disel
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HCK reactor system: simplified scheme
Rec. Gas compressor
Unconverted
feed recirc.
Feed
Hydrotreating Rx
Cracking Rx
HP separator
H2O
Rx outlet
Make up gas
Recirc. gas
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Different HCK designs
• “Once Through” (without recirculation, simple scheme, baseoil production)
• Single step, UCO (UnConverted Oil) recirculation main fractionator bottom recirculation
↑ distillate yields, conversion ~ 30-60%
↑ energy consumption
• Double step, UCO recirculation separation of reaction steps, complex scheme
↑ investment cost
↑ yields, conversion ~ 100%
↑ energy consumption
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The BR VGO HCK Unit
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Conversion processes – Residue upgrading
31
R e s i d u e u p g r a d i n g p r o c e s s e s
Non catalytic
Solvent asphalt removal
Thermal
Delayed coking
Fluid coking
Flexicoking
Visbreaking
Gasification
Catalytic
Residue fluid catalytic cracking (RFCC)
Residue hydrocracking
fixed bed
ebullated bed
Feed:
Vacuum
residue
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Carbon removal or hydrogen introduction
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Goal: viscosity reduction of fuel oil
like reidues
Feed: fuel oil components
Products: fuel oil, gasoline, diesel
components (needs
desulphurisation)
Process parameters:
Temperature: 450 - 500 °C
Pressure: 5 – 20 bar
Residue upgrading – Visbreaking
Yield structure:
• H2S 0,2 %
• Fuel gas 0,7 %
• C3/C4 1,1 %
• Gasoline 4,1 %
• Diesel 11,7 %
• Residue 82,2 %
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Residue upgrading – Delayed coking
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Goal: production of valuable lighter
components (need
hydrotreating), while forming
solid coke residue
Feed: vaccum residue
Products: gases, gasoline, diesel,
coke
Process parameters:
Temperature: 480 - 520 °C
Pressure: 1 – 5 bar
Residue upgrading – Delayed coking
Steam
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• Heaviest components of the feed are converted to solid coke due to very
complicated series of reactions (aliphatic C-C bond rupture, isomerisation,
ring formation, hydrogen removal, dehydrogenation, polymerization of
unsaturated compounds, dealkylation and condensation of aromatic ring),
while majority of the feed is converted to valuable lower boiling range
components.
• The coking procedure is so complicated, that it cannot be depicted with
concrete chemical reactions. However, three main steps may be derived:
– The feed, flowing through the heater pipes, is partially evaporated and mildly
cracked (viscosity breaking);
– The hydrocarbon vapors are further cracked, while travelling through the coke
drum;
– The liquid, entrapped in the coke drum, are converted to coke and vapors, via
polymerization and cracking reactions.
• Product yield and quality are determined by three parameters:
– Temperature
– Pressure
– Recirculation rate.
Residue upgrading – Delayed coking
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Delayed coking – Scheme
Main
co
lum
n
Co
ke d
rum
Feed
Furnace
Co
ke d
rum
Heavy gasoil
Light gasoil
Pit
Coke
Compressor +
Absorber/
Stripper
Gas p
urific
atio
n
co
lum
ns
Fuel gas
De
bu
tan
ise
r
Nap
hth
a
Sp
litter
Heavy naphtha
Light naphtha
C3/C
4
Sp
litter C4
PP
Sp
litter
Propane
Propylene
C1-163°C
163-333°C
333+°C
C2-
C3+
C4-
C5+
79-163°C
C5-79°C
C3
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Delayed coking – Blockscheme
Kokszoló
Koksz-
kezelő
GCUAminos
mosó
LPG
Merox
LPG
Frakciónáló
Alapanyag
LCO
HCO
Koksz
Könnyű
benzin
LPG
FG
Fűtőgáz
LPG
LPG
Koksz C4
frakció
Propilén
Nehéz
benzin
Propán
Coker Amine
wash
Coke
handling Fractioner
Feed
Coke
Coke
Light
gasoline
Heavy
gasoline
Fuel gas
fraction
Propylene
Propane
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Delayed coking – Yields
• Fuel gas 3,5 %
• C3 3,8 %
• C4 1,0 %
• Lt gasoline 2,7 %
• Hvy gasoline 8,0 %
• Gasoil 15,6 %
• V. distillate 38,7 %
• Coke 24,6 %
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Delayed coking – Coke parameters
Total S (%) 3,96
Nitrogen (s%) 1,47
Ni+Va (wppm) 1026
VCM (s%) max. 11
H2O (s%) 14
Caloric power (kJ/kg) 35647
HGI (Hard Grove Index) 50-80
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Residue upgrading – Delayed coking
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