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Transcript of # 7, HYDROROCESSING Part 1 Final Slide for Presentation Final
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8/6/2019 # 7, HYDROROCESSING Part 1 Final Slide for Presentation Final
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Training Programme Mumbai July,2007
HYDROCRACKING-Fundamentals, catalysts, process technologies and recent
developments.
Part 1
Sobhan Ghosh
Managing I nnovation
Process & research Consultant
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Training Programme Mumbai July,2007
PERSPECTIVESPERSPECTIVES IN MODERN PETROLEUM REFININGIN MODERN PETROLEUM REFINING
Deteriorating Crude Oil Quality and Fluctuating
Prices in International Markets
Constraint of Source of Crudes and Market Demand
Increasing Environmental Regulations For
Cleaner Products/ Processes And Growing
Demand For Quality Products
Declining Refining Margins
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Training Programme Mumbai July,2007
UP GRADATION P ROCESSES
� Carbon rejection
± Visbreaking , Hsc - ROSE, ART, FCC
±
Delayed coking, fluid coking, Fexi coking,
� Physical separation
± Solvent deasphalting, ROSE, DEMEX
� Hydrogen addition ± Hydrocracking,Resid hydrotreating, LC
Fining, H ± oil etc.
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Training Programme Mumbai July,2007
CDU
VDU SecondaryProcessing
Resid
Processing
Crude
Atmospheric Resid
Gases and LPG
Light Naphtha(C5-85)
Hy Naphtha (85-127)
Kerosene( 127-293)
Diesel ( 293-370)
HGO
VGO
Vac.Resid
Hydrocracker/FCC
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Training Programme Mumbai July,2007
Chemical transformations
in Different Processes
� 1. FCC : Cracking: Isomerisation, Aromatisation
etc.
� 2. Hydricracking : Cracking and hydrogenation
� 3. Reforming : Isomerisation, Cyclization,
Aromatization, Hydrogen
removal & olefinbuilding
� 4. Coking: Severe cracking leading to
coke formation
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Training Programme Mumbai July,2007
Carbon
( C )(Solid) Gas Gas
Hydrogen
( 2H2 )
Methane
( CH4 )
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Training Programme Mumbai July,2007
Saturated Straight Chain HydrocarbonC7 H16 ( Cn H 2n+2)
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Training Programme Mumbai July,2007
Saturated Straight Chain HydrocarbonC7 H16 ( Cn H 2n+2)
Removed
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Training Programme Mumbai July,2007
Unsaturated Straight ChainHydrocarbon (C7 H14 ( Cn H 2n)
Removed
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Training Programme Mumbai July,2007
Unsaturated Straight ChainHydrocarbon: C7 H14 ( Cn H 2n)
Double bond
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Training Programme Mumbai July,2007
Saturated Straight Chain HydrocarbonC7 H16 ( Cn H 2n+2)
Removed
Result?
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Training Programme Mumbai July,2007
TOLUENE: C7 H8
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Training Programme Mumbai July,2007
?
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Training Programme Mumbai July,2007
TWO ATOMS OF HYDROGEN MUST BE PROVIDED, OR,
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Training Programme Mumbai July,2007
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Training Programme Mumbai July,2007
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Training Programme Mumbai July,2007
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Training Programme Mumbai July,2007
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Training Programme Mumbai July,2007
Net result: one Saturated and one unsaturated compound
Formation of double bond
Saturated Unsaturated
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Training Programme Mumbai July,2007
HYDROPROCESSING/HDROREFINING
DIS I E E
HYDROCR CKING HC
HDS
HDN
HD
HYDROGEN ION
HYDROFINISHING
HYDROISO ERIS ION
HYDRO RE ING
HYDROPROCESSING
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Training Programme Mumbai July,2007
T ypical Prod ct slate ydrocracki g
Gasoline
Boili g ra ge, o
ield, vol%
5-220
55
5-180
30
Diesel
Boili g ra ge, o
ield, vol%
, ppm
romatics, wt%
eta e I dex
220-360
20
5000
70
21
180-370
80
<5
20
56
Feed stock California VGO
Boiling range, oC 238-562
N, wppm 2660
S, wt% 1.18
Aromatics, wt% 32
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Training Programme Mumbai July,2007
Hydrocracking
� Feed : VGO, Resid, Distillates
�Typical Operating Conditions:
Conversion: 50 ± 100%
(normally lo for once thru¶ high for recycleconfiguration)
Temperature: 350 ± 425oc
H2 Pressure: 100 ± 200 bar
LHSV: 0.5 ± 2.0 h-1
H2:Oil Ratio: 700 ± 2000 nm3 / m3
�Catalyst: Ni/Mo or Ni/W on amorphous SiO2/Al2O3 or,
Zeolite
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Training Programme Mumbai July,2007
HYDROCRAC ING
CATALYST
(dual function)
Cracking Function
( acid support)
Hydrogenation Function
(metals)
POROUS SUPPORT HAVING
ACIDIC SITES
ZEOLITE>SILICA-ALUMINA
METALS DISPERSED
ON POROUS SUPPORT
Pt or Pd>Ni-W>Co-Mo
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Training Programme Mumbai July,
2007
Chemistry of Hydroprocessing
1. S²Org. --------- H2 S + Org.
+ H 2
2. M ± Org. -------- M + Org.
3 N ± Org ------- NH3 + Org.
4. Olefin ---------- Parafin
5. Aromatics --------- Cyclic compounds ----
Parafins
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Training Programme Mumbai July,
2007
MAJOR REACTIONS IN A
HYDROCRAC ER
Hydrocracking
Demetallisation>Olefin Saturation > desulfurisation >
Denitrogenation > Aromatic saturation>Cracking of
naphthenes>Cracking of paraffins
� Isomerisation
� Hydrocracking� Aromatic ring saturation and opening
� Dealkylation
� Naphthenic ring opening
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Training Programme Mumbai July,
2007
Hydrotreatment
M AJOR REACTIONS IN
HYDROCRACKING
� Hydrodesulfurisation
� Hydrodenitrogenation
� Olefin saturation
� Hydrodemetallisaion Hydrotreating is a lo er pressure operation than
Hydrocracking. Higher Hydrogen P ressure± Higher
Severity
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Training Programme Mumbai July,
2007
Coke formation
Polyaromatics Alkylation CyclizationCoke
precursor
+ Olefins - H2 - H2
Resins, asphaltenes & otherpolyaromatics have strong coking
tendency
Polynaphthenes & Polyaromatics are
converted on large pore amorphouscatalyst.
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Training Programme Mumbai July,
2007
HYDROCRAC ING
CATALYST
Gasoline & light
products
Middle-distillate
Strong cracking activity
- Zeolites
Moderate hydrogenation
- Ni/Mo sulfides
Weaker acidity
Weaker zeolite
Strong hydrogenation
- Ni/W, Pd, Pt
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Training Programme Mumbai July,
2007
NiMo promoted(1st step HCK)
NiMo(Resid HDS)
NiMo/ CoMo
(GASOLINE)
CoMo promoted(Diesel)
NiMo promoted(Diesel,
Cracked GO,VGO)
HYDRO P ROCESSING CATALYSTS
Hydrotreating catalysts
for various feedstocks
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Training Programme Mumbai July,
2007
CATALYT CO M P ONENTS FOR
HYDRO P ROCESSING
� Metals of group vi-a with
group - VIIIA metals as promoter
- W / Mo promoters Ni / Co
� Noble metals
- Pt, Pd
� Supports
- alumina- silica alumina
- zeolites
� Non noble metal catalysts are active in sulfided form
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Training Programme Mumbai July,
2007
ROLE OF SUPPORT
� Diffusivity
� Dispersion of active metals
� Provides acidity
� Structural Integrity
�Wetting of Oil on the Catalyst surface
�Low pressure drop and good Radial mixing
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Training Programme Mumbai July,
2007
Important Prameters of Catalystsupport
� Pore structure & pore size distribution
� Surface area
� Acid strength & acid sites distribution
�Crush Strength
�Metal dispersion
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Training Programme Mumbai July,
2007
TYPICAL PORE SIZE DISTRIBUTION OF
HYDROTREATING CATALYSTS
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Training Programme Mumbai July,
2007
TYPICAL SHAPE OF CATALYST PARTICLES
size and shape influences the pressure drop in the reactor
and for effective reactant contact
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Training Programme Mumbai July,
2007
CLASSIFICATION OF HYDROCRAC ING PROCESSES
( HC: Hydrocracking; HT: Hydrotreating; R: Reactor)
Hydrocracking Processes
Single-stage ( no intermediate
separation of products)
HT +HC (2R)
� Dual catalyst
�Fractionation of HT
effluent ( separate HT)
� Recycle to HC reactor
HT+HC (2R or 3R)
� Dual or triple catalyst
�Fractionation of
effluent from 1st HC
reactor
� Recycle to 2nd HC
reactor
Without recycle
(³ once-through´)
With recycle to HC
reactor
HT + HC ( 1R or 2R)
� Dual catalyst
� High N & S feed
HC only ( 1R)
� Single catalyst
�lo N & S feed
Two stage ( separations of
products between stage 1 &2)
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Training Programme Mumbai July,
2007
ACTIVATION OF CATALYSTS
Commercial catalysts are supplied in calcined (oxide)form having no/less activity
To be activated prior to their use in reactors
In-situ activation
± Non-noble metal catalysts (Co/Mo, Ni/Mo)
� sulfiding with H2S, DMS, DMDS etc. ± Noble metal catalysts (Pt, Pd)
� reduced to zero valent state
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Training Programme Mumbai July,
2007
CATALYST REGENERATION AND
REACTIVATION
Regeneration of catalyst bed when ³end of run´
condition is reached
Burning of deposited coke bed
± Metal sulfides are converted to oxides
Reactivation
± Sulfiding for non-noble metal catalysts
± Reduction for noble metal catalysts
Rejuvenation
± Restoration of hydrogenation activity lost due to
agglomeration of noble metals
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Training Programme Mumbai July,
2007
CATALYST DEACTIVATION & P OISONING
Loss of catalyst activity due to
� Deposition of coke
� Poisoning of active sites
± Basic nitrogen compounds
± Sulfur compounds
� Deposition of coke or metal at pore mouth
� Sintering & volatilisation of active material at high
temperature.
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Training Programme Mumbai July,
2007
Hydrocracking Reaction
� Tpical Gas -Solid ±Liquid three Phase reaction� Trickel Bed Reactor
� Activation energy for VGO = 47.7 cal/gm-mole
� 15 oC rise in Temp. doubles the Reaction rate
� High Pressure ± Higher Reaction Rate, low coke
make and lower severity.
Individual reaction rates vary with reactant type and
boiling range
Ratio of hydrocracking rate for
C20:C15:C10:C5 $$ 120:72:32:1
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2007
HYDROCRACKING KINETICS
Adsorption strength :
Heteroatomic > Multi-ring aromatic >
Monoaromatic > Multi-ring naphthene >
Mononaphthene > Paraffin
Reaction dependent on strength of
adsorption on catalyst surface
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2007
Higher SurfaceArea
Optimum PoreSize Distribution
Modification of Chemical Nature
Shaped Carrier (trilobe,quadrilobe)
Goodmechanicalstrength
Optimum MetalsDispersion
Enhancement of Promoter Effects
FACTORS INFLU ENCING
HYDRO P
ROCESSING CATALYSTS P ERFOR M ANCE
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In P art 2 e shall deal ith the
hard are and integration of HC ith other processes.