Transcript Diapositiva 1

Estrategia de Repsol YPF para la producción de
combustibles limpios
Fernando Albertos de Benito, Luis Casado Padilla
Presentado por Jesús Muelas Párraga
Jornadas Latinoamericanas de Refinación – Mendoza 30 de Octubre - 2 de Noviembre de 2006
Contents
 Introduction to Repsol YPF
 Fuels production in 2000
 Diesel production assessment definition
 R&D developments
 Assessment results
 Conclusions
Refining capacity (Spain)
BILBAO
CORUÑA
CAPACITY
(Bbl/d)
Gijón
Guipúzcoa
León
Rivabellosa
Pamplona
Vigo
Bilbao
Cartagena
La Coruña
Puertollano
Tarragona
220.000
100.000
120.000
140.000
160.000
Repsol YPF
740.000
Gerona
Burgos
Zaragoza Lérida
Barcelona
Santovenia
TARRAGONA
Salamanca
Torrejón
Villaverde
CASTELLON
Madrid
Valencia
Mérida
Spain
Mahón
Alcázar
PUERTOLLANOAlicante
Palma
Ibiza
1.260.000
Sevilla
740.000
HUELVA
Rota
Córdoba
Málaga Motril
CARTAGENA
ALGECIRAS
TENERIFE
REFINERIES REPSOL YPF
OTHER REFINERIES
Fuels Production in 2000
Specification at that time:
 Gasoline:
150 ppm S maximum
 Diesel:
350 ppm S maximum
New projects under way

High pressure HVGO Hydrocracker

VGO/HCGO Mild Hydrocracker units

FCC naphtha splitters for FCC based refineries
Fuels Production in 2000
Cartagena:
Puertollano
 Hydro skimming
 Mild HC + FCC + Delayed coker
 Two HDS Units
 Five HDS Units
 100% Diesel pool hydrotreated
 100% Diesel pool hydrotreated
Coruña:
Tarragona
 Mild HC + FCC + Delayed coker
 ISOMAX + HVGO HC
 Two HDS Units
 Three HDS Units
 100% Diesel pool hydrotreated
 > 60% Diesel pool hydrotreated
Petronor
 VGO HDT + FCC + Visbreaker
 Three HDS Units
 100% Diesel pool hydrotreated
Study Scenarios
1. To make sure refining capacity for 100% fuels
production complying with the 50 ppm sulphur spec
2. To
define
refineries
capacity
to
produce
simultaneously fuels complying with the 50 and 10
ppm sulphur spec
3. To define refining schemes, revamps and new
projects for adapting 100% of our fuels production to
the 10 ppm sulphur spec
Study Scenarios
Technical and
Engineering
Divisions
Strategic Planning
Department
Working
Team
Refineries
R&D
R&D Developments
 Kinetic models for ULSD production
 Deactivation models for industrial HDS unit operation
 Classification of commercial catalysts performance
 General HDS unit simulation model
Kinetic Models for ULSD
Main Characteristics
 Derived from pilot plant data and validated with industrial data
 Calculate
the
main
processes
that
take
place
during
hydrotreatment:
HDS, HDN, HDA, HYD, HC
 Relatively simple empirical models, obtained by simultaneous
parameters fitting, and based on measurements readily available
on refinery operation
Kinetic Models for ULSD
Pilot Plant tests
OPERATING VARIABLES
WABT, ºC
280 - 390
LHSV, h-1
0.5 – 1.5
Pressure, kg/cm2
30 - 60
H2 /HC, Nm3/m3
200 - 400
FEED PROPERTIES
Type
LSR; HSR; LCO; LCGO
Origin of crude oil
West Africa; North Africa; Middle East; America
Sulphur, ppm
2500 - 16000
Nitrogen, ppm
100 – 350
Density, g/cc
0.82 – 0.88
D86 10% ºC
220 – 305
D86 90% ºC
280 – 365
CATALYST TYPE
CoMo and NiMo, fresh and used (SOR and EOR)
Kinetic Models for ULSD
Example: Sulphur conversion
XS =
f1 (CATALYST) x f2 (OP. CONDITIONS) x
f3 (FEED PROPERTIES) x f4 (UNIT CALIBRATION)
Kinetic Models for ULSD
f1 (CATALYST)
Activity factors obtained from pilot plant results
ACTIVITY FACTORS
1,6
1,4
HDS
1,2
HDN
1
HDA
0,8
0,6
0,4
Cat 1. Ref
Cat 2
Cat 3
CATALYSTS
Cat 4
Kinetic Models for ULSD
f2 (OP. CONDITIONS): Takes into account the effect of operating
conditions on the reaction considered
Example: Sulphur conversion
f2 (T, LHSV, PH2 , PSH2)
Feed properties affecting PH2
Olefin content
Aromatic content
Nitrogen content
Sulfur content
Distillation curve
Kinetic Models for ULSD
f3 (FEED PROPERTIES): reflects differences in feed reactivity
Correlations obtained from different feed properties
k0 = f(Density, Sulphur, Nitrogen)
k0 = f(S DBTs, Basic Nitrogen)
2,5E+09
2,0E+09
k0 measured
k0 measured
2,5E+09
1,5E+09
1,0E+09
5,0E+08
5,0E+08
2,0E+09
1,5E+09
1,0E+09
5,0E+08
1,0E+09
1,5E+09
k0 model
2,0E+09
2,5E+09
5,0E+08
1,0E+09
1,5E+09
k0 model
2,0E+09
2,5E+09
Kinetic Models for ULSD
f3 (FEED PROPERTIES) based on ρ, S and N
f3 (FEED PROPERTIES) based on S DBTs and basic N
New Analysis
routines
implemented in
refineries
General HDT Simulation Model
Schematic model operation
Inputs
Outputs
• Process Diagram Flow
• Products quality.
• Loading Scheme.
• Yields.
• Operation Conditions.
• Reactor Temperature Profile
• Feed Properties.
& Quench Flow required.
• Make up quality.
• Hydrogen consumption.
• Run length.
Model:
• RVA Catalysts Factor.
• Kinetic Model.
• Deactivation Model.
• Thermodynamic model.
Assessment Results
Procedure






Unit simulation
Kinetic evaluation (SOR WABT, cycle length etc)
Consultations to catalyst vendors and licensors
Test runs for specific units
Refinery hydrogen and sulphur balances
Conclusions and recommendations
Study Cases
Scenario 1: 100% 50 ppm diesel production
Scenario 2: Simultaneous production of 50 and 10 ppm diesel
Scenario 3: New projects for 100% 10 ppm diesel production
Scenario 1:
100% 50 ppm diesel production
Conclusions:
 Under way HC and MHC projects would allow desulfurize middle
distillates in traditionally VGO HDT Units (two refineries)
 One new MHC Unit prepared to treat LCO  extra capacity
available in existing HDS Units
 One new HDS Unit defined
 Minor modifications in rest of the Units
 LCO and coker gasoil being segregated to non road gasoil and
heating oil pools.
 Exploitation of more active catalyst available in the market
Scenario 2:
Simultaneous production of 50 and 10 ppm diesel
Analysis of existing Units for producing 10 ppm
products:
 Low pressure units (H2 partial pressure below 25 bar)
 Kerosene
 Light straight run distillates
 Low sulphur mixtures of straight run LD and HD
 Moderate pressure units (H2 partial pressure in the range 25-40
bar)
 Mixtures of SR GO and cracked feedstock (mainly light coker gasoil)
 High pressure units (H2 partial pressure above 40 bar)
 Moderate percentages of LCO (15-25%)
Scenario 2:
Simultaneous production of 50 and 10 ppm diesel
Scenario 3:
New projects for 100% 10 ppm diesel production
Main measures adopted
 Use of high activity catalysts
 Dense loading
 Feedstock segregation (when possible)
 Installation of high performance distributor trays in critical
units
 Installation of online sulphur analysers for diesel product
 Hydrogen purity improvement when possible
 Reducing space velocity (new reactor in series to existing)
Scenario 3:
New projects for 100% 10 ppm diesel production
Final remarks

The pathway followed by Repsol YPF to analyse the refineries capacity
to produce diesel with 10 and 50 ppm has been explained.

This procedure has allowed Repsol YPF to fully exploit the installed
capacity for producing 10 and 50 ppm fuels

To support this analysis an important R&D effort was launched. This
work produced a number of tools, including a simulation model fully
validated for the industrial units

As a final outcome from this project, a number of revamps and
modifications were approved and are now under construction

RepsolYPF is now in a better situation to understand the HDT process,
and to obtain the best performance from industrial units