Post on 11-Jan-2016
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Department of Chemical Engineering
Institute of Technology, Nirma University
Chemists and Chemical Engineers Make the World a Better Place through Modern
Developments in Heterogeneous Catalysis
Presented by
SANJAY PATEL
Chemistry & Chemical Engineering
History of Catalysis
Catalysis
Recent trends in Catalysis
Future trends in Catalysis
Summary
Content
Luxury
Household commodities
Gadgets
Ind
ustrial C
hem
icals
Alternative Fuels
Environment
Po
pu
lati
on
Health
Energy Demand
Research
All other Engg
Chemistry and Chemical Engineering more Integrated to the Society
Society:• Cleaner and safer processes• Well accepted and integrated processesIndustry:• Speed-up processes• Energy and cost effective processes• New catalysts and catalytic processes• New technologiesAcademia:• New innovations• Deeper knowledge and understanding of phenomena• Control of phenomena
Role of Catalysis in a National Economy
• 24% of GDP from Products made using catalysts (Food, Fuels, Clothes, Polymers, Drug, Agro-chemicals)
• > 90 % of petro refining & petrochemicals processes use catalysts
• 90 % of processes & 60 % of products in the chemical industry
• > 95% of pollution control technologies
• Catalysis in the production/use of alternate fuels (NG,DME, H2, Fuel Cells, biofuels…)
Why R&D in catalysis is important
• For discovery/use of alternate sources of energy/fuels/raw material for chemical industry
• For Pollution control• For preparation of new materials (organic & inorganic-eg: Carbon Nanotubes)
Three Scales of Knowledge Application
Some Developments in Industrial catalysis-11900- 1920s
Industrial Process Catalyst
1900s: CO + 3H2 CH4 + H2O Ni
Vegetable Oil + H2 butter/margarine Ni
1910s: Coal Liquefaction Ni
N2 + 3H2 2NH3 Fe/K
NH3 NO NO2 HNO3 Pt
1920s: CO + 2H2 CH3OH (HP) (ZnCr)oxide
Fischer-Tropsch synthesis Co,Fe
SO2 SO3 H2SO4 V2O5
Industrial catalysis-21930s and 1940s
1930s:Cat Cracking(fixed,Houdry) Mont.Clay
C2H4 C2H4O Ag
C6H6 Maleic anhydride V2O5
1940s:Cat Cracking(fluid) amorph. SiAl
alkylation (gasoline) HF/acid- clay
Platforming(gasoline) Pt/Al2O3
C6H6 C6H12 Ni
Industrial catalysis-3 1950s
C2H4 Polyethylene(Z-N) Ti
C2H4 Polyethylene(Phillips) Cr-SiO2 Polyprop &Polybutadiene(Z-N) Ti
Steam reforming Ni-K- Al2O3
HDS, HDT of naphtha (Co-Mo)/Al2O3
C10H8 Phthalic anhydride (V,Mo)oxide
C6H6 C6H12 (Ni)
C6H11OH C6H10O (Cu)
C7H8+ H2 C6H6 +CH4 (Ni-SiAl)
Butene Maleic anhydride (V,P) oxides
C3H6 acrylonitrile(ammox) (BiMo)oxides
Bimetallic reforming PtRe/Al2O3
Metathesis(2C3 C2+C4) (W,Mo,Re)oxides
Catalytic cracking Zeolites
C2H4 vinyl acetate Pd/Cu
C2H4 vinyl chloride CuCl2
O-Xylene Phthalic anhydride V2O5/TiO2
Hydrocracking Ni-W/Al2O3
CO+H2O H2+CO2 (HTS) Fe2O3/Cr2O3/MgO
--do-- (LTS) CuO-ZnO- Al2O3
Industrial catalysis-4 1960s
Xylene Isom( for p-xylene) H-ZSM-5
Methanol (low press) Cu-Zn/Al2O3
Toluene to benzene and xylenes H-ZSM-5
Catalytic dewaxing H-ZSM-5
Autoexhaust catalyst Pt-Pd-Rh on oxide
Hydroisomerisation Pt-zeolite
SCR of NO(NH3) V/ Ti
MTBE acidic ion exchange resin
C7H8+C9H12 C6H6 +C8H10 Pt-Mordenite
Industrial catalysis-5 1970s
Ethyl benzene H-ZSM-5Methanol to gasoline H-ZSM-5Vinyl acetate PdImproved Coal liq NiCo sulfidesSyngas to diesel CoHDW of kerosene/diesel.GO/VGO Pt/ZeoliteMTBE cat dist ion exchange resinOxdn of methacrolein Mo-V-PN-C6 to benzene Pt-zeolite
Industrial catalysis-6 1980s
DMC from acetone Cu chloride
NH3 synthesis Ru/C
Phenol to HQ and catechol TS-1Isom of butene-1(MTBE) H-FerrieriteAmmoximation of cyclohexanone TS-1 Isom of oxime to caprolactam TS-1Ultra deep HDS Co-Mo-AlOlefin polym Supp. metallocene catsEthane to acetic acid Multi component oxide Fuel cell catalysts Rh, Pt, ceria-zirconiaCr-free HT WGS catalysts Fe,Cu- based
Industrial catalysis-7 1990s
Industrial catalysis-8 2000+
• Solid catalysts for biodiesel - solid acids, Hydroisom catalysts• Catalysts for carbon nanotubes - Fe (Ni)-Mo-SiO2
For Developed Catalysts MAINLY IMPROVEMENT IN PERFORMANCE by
New Synthesis Methods & use of PROMOTERS
Green Chemistry is Catalysis• Pollution control (air and waste streams;
stationary and mobile)• Clean oxidation/halogenation processes using
O2,H2O2 (C2H4O, C3H6O)• Avoiding toxic chemicals in industry (HF,COCl2 etc)
• Fuel cells (H2 generation)
Latest Trends
Catalysis in Nanotechnology
Methods of Catalyst preparation are most suited for the preparation of nanomaterials
• Nano dimensions of catalysts• Common prep methods• Common Characterization tools• Catalysis in the preparation of carbon nanotubes
Latest Trends
Catalysis in the Chemical Industry
• Hydrogen Industry(coal,NH3,methanol, FT, hydrogenations/HDT,fuel cell)
• Natural gas processing (SR,ATR,WGS,POX)
• Petroleum refining (FCC, HDW,HDT,HCr,REF)
• Petrochemicals (monomers,bulk chemicals)
• Fine Chem. (pharma, agrochem, fragrance, textile,coating,surfactants,laundry etc)
• Environmental Catalysis (autoexhaust, deNOx, DOC)
Latest Trends
HETEROGENEOUS CATALYSISAN INRODUCTION
- Diffusion of Reactants (Bulk to Film to Surface)
- Adsorption
- Surface Reaction
- Desorption & Diffusion of Products
Steps of Catalytic Reaction
reactants
products
reactor
catalyst support
active site
substrate
adsorption
reaction desorption
bed ofcatalyst particles
porous carrier (catalyst support)
product
Role of Chemists & Chemical EngineersTeam Work
Wet impregnation:• Preparation of precursors (Cu & Zn-nitrates) solution• Impregnation of precursors on alumina support• Rotary vacuum evaporation• Drying• Calcination• Reduction
Rotary vacuum evaporator
Catalysts Preparation
Mixer cum shaker
Filteration
Drying @ 125 oC for 12 h
Rotary Vacuum Evaporator
Crushing Sieving, 20/25 mesh
Round bottom flask with Heating mental & Agitator
Drying@ 125 oC for 12 h
Crushing
Sieving, 20/25 mesh
Pelletizing
Crushing
Nitrate Salts solution & Alumina pellets
Nitrate Salts Solution
70 oC, pH=7-8
Precipitates: Ageing for 2 h
0.5M Na2CO3 Dropwise addition
Calcination, 350 oC for 4 h
Calcination,350 oC for 4 h
Catalyst
Catalyst
Wet Impregnation Co-precipitation
Catalysts Preparation
WI CuO/ZnO/Al2O3 Catalyst
Calcined
WI CuO/ZnO/Al2O3 Catalyst
Calcined
Co-precipitation Co/Al2O3
Calcined
Commercial Ni/Al2O3
Spent Commercial Ni/Al2O3
Commercial Fe2O3 catalyst
Spent Commercial Fe2O3 catalyst
Pt, Pd and Rh on the Metox metallic substrates
Pervoskite LATEST Research
Auto-catalysts
Honey Comb Catalysts
CATALYST CHARACTERIZATION
• Bulk Physical Properties• Bulk Chemical Properties• Surface Chemical Properties• Surface Physical Properties• Catalytic Performance
Bulk Chemical Properties• Elemental composition (of the final catalyst)• XRD, electron microscopy (SEM,TEM)• Thermal Analysis(DTA/TGA)• NMR/IR/UV-Vis Spectrophotometer• TPR/TPO/TPD• EXAFS
Surface Properties
• XPS,Auger, SIMS (bulk & surface structure)• Texture :Surface area- porosity• Counting “Active” Sites:
-Selective chemisorption (H2,CO,O2, NH3, Pyridine,CO2);Surface reaction (N2O)
• Spectra of adsorbed species (IR/EPR/ NMR / EXAFS etc)
Physical properties of catalysts• Bulk density• Crushing strength & attrition loss
(comparative)• Particle size distribution• Porosimetry (micro(<2 nm), macro(>35
nm) and meso pores
Catalysts Characterization
Characteristics Methods
Surface area, pore volume & size
N2 Adsorption-Desorption Surface area
analyzer (BET and Langmuir)
Pore size distribution BJH (Barret, Joyner and Halenda)
Elemental composition of catalysts
Metal Trace Analyzer / Atomic Absorption Spectroscopy
Phases present & Crystallinity
X-ray Powder DiffractionTG-DTA (for precursors)
Morphology Scanning Electron Microscopy
Catalyst reducibility Temperature Programmed Reduction
Dispersion, SA and particle size of active metal
CO Chemisorption, TEM
Acidic/Basic site strength NH3-TPD, CO2 TPD
Surface & Bulk Composition XPS
Coke measurement Thermo Gravimetric Analysis, TPO
BET Surface Area Analyzer
Surface area, Pore Volume, Pore Size & Pore size distribution
Major role of Chemical Engineer with Chemists for Hardware
0
20
40
60
80
100
120
140
160
180
200
0 100 200 300 400 500 600 700
Relative pressure, P/P 0
Vol
ume
adso
rbed
, cm
3 g
-1 (
STP
)
000.0E+0
1.0E-3
2.0E-3
3.0E-3
4.0E-3
5.0E-3
6.0E-3
7.0E-3
10 100 1000
Pore diameter, A 0
Por
e vo
lum
e, c
m3 g
-1 A
0-1
CZCEA2
CZA2
Pore size distribution by BJH methodN2 adsorption/desorption Isotherm
P2CZCeA
Surface Area and Pore size Distribution
Barret, Joyner, and Halenda (BJH)
P3CZA
P2CZCeA
P2CZCeA Cu/Zn/Ce/Al:30/20/10/40
P3CZA Cu/Zn/Al:30/20/50m
0 k
2 V COSPln
P r RT
Chemisorption Analyzer
Dispersion, Metal Surface area and Metal Particle size; TPR, TPO, TPD
TGA/DTA Analyzers
Coke measurement & TPO
Reactions involved in SRM process
CH3OH + H2O ↔ CO2 + 3H2
CO2 + H2 ↔ CO + H2O
CH3OH ↔ 2H2 + CO
CH3OH + (1-p)H2O +0.5pO2 ↔ CO2 + (3-p)H2
∆H0 = (49.5 - 242*p) kJ mol-1
CH3OH + 0.75H2O + 0.125O2 ↔ CO2 + 2.75H2 ∆H0 = -10 kJ mol-1
∆H300 oC = 0 kJ mol-1
CH3OH + 0.5H2O + 0.25O2 ↔ CO2 + 2.5H2 ∆H0 = -71.4 kJ mol-1 CH3OH + 0H2O + 0.5O2 ↔ CO2 + 2H2 ∆H0 = -192 kJ mol-1
CH3OH + 1.5O2 ↔ CO2 + 2H2O ∆H0 = -727 kJ mol-1
Reactions involved in OSRM process
Catalyst Activity Testing
• Activity to be expressed as:
- Rate constants from kinetics - Rates/weight - Rates/volume - Conversions at constant P,T and SV. - Temp required for a given conversion at constant
partial & total pressures - Space velocity required for a given conversion at
constant pressure and temp
Parameters
Catalyst mass, g 1-3
Contact-time (W/F) kgcat s mol-1 3-15
Temperature, oC 200-300
S/M molar ratio 0-1.8 (SRM)
S/O/M molar ratio 1.5/0-0.5/1 (OSRM)
Pressure, atm 1
Operating Conditions for SRM & OSRM
Schematic diagram of OSRM process
Schematic diagram of OSRM process
L 770mm
Thermocouple
Reactants Inlet
ID 19mm
OD 25mm
Flange
Catalyst bed
Products
T=280 oC, W/F=11 kgcat s mol-1, S/O/M=1.5/0.15/1 & P=1 atm
Characterization and Activities of ZnO & Ceria promoted Catalysts
Co-precipitation P4CZA P3CZA P1CZCeA P2CZCeA P3CZCeA
Cu/Zn/Al Cu/Zn/Al Cu/Zn/Ce/Al Cu/Zn/Ce/Al Cu/Zn/Ce/Al
Composition, wt% 30/30/40 30/20/50 30/25/5/40 30/20/10/40 30/10/20/40
BET SA, m2 g-1 92 106 96 108 101
Pore volume, cm3 g-1
0.26 0.32 0.28 0.34 0.29
Cu dispersion, % 9.4 12.8 10.2 19.6 14.8
Cu SA, m2 g-1 18.3 25.1 20.2 38.6 29.3
Cu particle size, Å 108 80 101 52 69
X, % 60 77 69 100 90
H2 rate, mmol s-1 kgcat
-1
132 180 160 244 217
CO formation, ppm 9400 3400 1400 995 1240
At Lab Scale Activity at Kinetically Controlled Conditions
Scale-up &Commercialization
Major Role of Chemists & Chemical Engineers
Examples of Steam Reformer & Ammonia ReactorExamples of Steam Reformer & Ammonia Reactor
Primary ReformerPrimary Reformer
Ammonia ConverterAmmonia Converter
RECENT TRENDS
Big picture: Sustainable Development
Green Chemistry Is About...
Cost
Waste
Materials
Hazard
Risk
Energy
The drivers of green chemistry
Green chemistry
Lesshazardous materials
High fines for waste
Producerresponsibility
Government legislation
Lowercapital investment
Loweroperating costs
Economic benefit
Pollution control
Saferand smaller plants
Improvedpublic image
Societal pressure
1. Prevention
It is better to prevent waste than to treat or clean up waste after it has been created.
2. Atom Economy Synthetic methods should be designed to maximise the incorporation of all materials used in the process into the final product.
3. Less Hazardous Chemical Synthesis Wherever practicable, synthetic methods should be designed to use and generate substances that possess little or no toxicity to people or the environment.
4. Designing Safer Chemicals Chemical products should be designed to effect their desired function while minimising their toxicity.
5. Safer Solvents and Auxiliaries The use of auxiliary substances (e.g., solvents or separation agents) should be made unnecessary whenever possible and innocuous when used.
6. Design for Energy Efficiency
Energy requirements of chemical processes should be recognised for their environmental and economic impacts and should be minimised. If possible, synthetic methods should be conducted at ambient temperature and pressure.
The 12 Principles of Green Chemistry (1-6)
7 Use of Renewable FeedstocksA raw material or feedstock should be renewable rather than depleting whenever technically and economically practicable.
8 Reduce DerivativesUnnecessary derivatization (use of blocking groups, modification of physical/chemical processes) should be minimised or avoided if possible, because such steps require additional reagents and can generate waste.
9Catalysis
10 Design for DegradationChemical products should be designed so that at the end of their function they break down into innocuous degradation products and do not persist in the environment.
11 Real-time Analysis for Pollution PreventionAnalytical methodologies need to be further developed to allow for real-time, in-process monitoring and control prior to the formation of hazardous substances.
12 Inherently Safer Chemistry for Accident Prevention
The 12 Principles of Green Chemistry (7-12)
Green Catalytic Processes
• Alternative feedstocks, reagents, solvents, products
• Enhanced process control
• New catalysts
• Greater integration of catalysis and reactor engineering:
membrane reactors, microreactors, monolith technology, phenomena integration
• Increased use of natural gas and biomass as feedstock
• Photodecomposition of water into hydrogen and oxygen
• Catalysts for depolymerizing polymers for recycle of the monomers
• Improvements in fuel cell electrodes and their operation
Cleaner and greener Environment: Catalysis
New directions for research driven by market, social & environmental needs:
• Catalysis for energy-friendly technologies and processes (primary methods)
• New advanced cleanup catalytic technologies (secondary methods)
• Catalytic processes and technologies for reducing the environmental impact of chemical and agro-industrial solid or liquid waste and improving the quality and reuse of water (secondary methods)
• Catalytic processes for a sustainable chemistry (green chemistry and engineering approach)
• Replacement of environmentally hazardous catalysts in existing processes
How to Decrease the Greenhouse Effect?New catalysts for high output fuel cells• Electricity production via electrocatalytic oxidation of hydrocarbons•Chemical energy of hydrocarbon is converted to electricityCatalysts and processes for solar energy conversion and hydrogenproduction•CO2 or other greenhouse gases are not emitted into the atmosphere, • First solar energy is converted into the chemical energy of synthesis gas (CO + H2) via the endothermic reaction of methane reforming•Storage of the synthesis gas•The stored energy can be released via the reverse exothermal methanation reactionCO + 3H2 → CH4 + H2O•Efficiency from 43 to 70 %Catalysts are needed for these reactions!!!
Classic Route to Ibuprofen
Ac2O
AlCl3
COCH3
HCl, AcOH, Al Waste
ClCH2CO2Et
NaOEt
OEtO2C
HCl
H2O / H+
OHC
AcOH
NH2OH
OHNN
H2O / H+
HO2C
NH3
Examples of Green Catalysis
H o e c h s t R o u t e T o I b u p r o f e n
O
H F
A c O H
A c 2 O
H 2 / N i
OH
C O , P d
H O 2 C
Examples of Green Catalysis
“The use of auxiliary substances (e.g. solvents,separation agents, etc.) should be minimized”
Examples of Green Catalysis
Poly lactic acid (PLA) for plastics production
Examples of Green Catalysis
Polyhydroxyalkanoates (PHA’s)
Examples of Green Catalysis
‘‘TiOTiO22’ A GREEN CATALYST: ’ A GREEN CATALYST: CLEAN ENVIRONMENTCLEAN ENVIRONMENT
Examples of Green Catalysis
PhotocatalysisPhotocatalysis
Photocatalyst
Starch + O2
Organic compound
Chlorophyll
CO2
H2O
CO2 + H2O
Organic Compound
+ H2O + O2
PhotocatalyticPhotocatalytic Applications Applications
Self-Cleaning EffectSelf-Cleaning Effect
TiOTiO22 - Photocatalysis - Photocatalysis
3.12 eV (380 nm)
Photocatalytic ReactionsPhotocatalytic Reactions
TiO2 + h TiO2 (e- + h+)
h+ + H2O OH + H+
O2 + e- O2 -
O2 - + H+ HO2
HO2 + HO2 H2O2 + O2
O2 - HO2+
H2O2
O2 + HO2-
HO2- +
H2O2 + h OH2
H2O2 + O2 - HO + OH- + O2
H2O2 + e-HO + OH-
Microreactors – FutureCatalytic processes
• Uniform channel structure, fractal catalyst supports
• Scale-up
• How microreactor is connected to the macroworld?
• Operating regimes
• Controlled periodic processing
• Programmable reactor
• Process control
• Miniaturized sensors and actuators
• Local feedback and programmable regimes
• Advanced structure, materials, process control
• Multiscale – finely defined; locally targeted – globally optimized
Random Vs Structured Catalysts
Structured Bedsof Tomorrow
Random PackedToday
Monoliths (Structured) vs Pellets (Random)
Monolith catalyst extruded from
commercial catalyst support material
Conventional pellets made from the same material
Does the configuration alone improve performance?
Micro Process Micro Process PlantPlant
Chemistry & Catalysis
Raw Materials & Feedstocks
CatalystCharacterization
Reaction Pathways & Mechanisms
Reaction Kinetics
Micro Systems Engineering
Tools, Fabrication & Assembly
Microprocess Components
Materials of Construction
Component Integration
Multi-scale Transport
Micro Process Analytical
Integrated Sensors
Sampling Sensors
Data handling & Chemometrics
Micro PAT Systems Integration
Micro Analyzers (GC, LC, MS, TOF)
Process Engineering
Flowsheet Synthesis
Control Systems
2D & 3D CAD Solids Modeling
Microscale Design Modules
Flow Patterns
Simulation & Optimization
Multiscale Transport
• High surface-to-volume area; enhanced mass and heat transfer;
• high volumetric productivity;
• Laminar flow conditions; low pressure drop
Some Advantages of Microreactors & Monoliths
• Residence time distribution and extent of back mixing controlled – “precise reaction engineering”
• Low manufacturing, operating, and maintenance costs, and low power consumption
• Minimal environmental hazards and increased safety due to small volume
• “Scaling-out” or “numbering-up” instead of scaling-up
Some Potential Problems
• Short residence times require fast reactions• Fast reactions require very active catalysts that are stable (The
two most often do not go together)• Catalyst deactivation and frequent reactor repacking or
reactivation• Fouling and clogging of channels• Leaks between channels• Malfunctioning of distributors• Reliability for long time on-stream• Structural issues
So far there are only two major commercial uses of micro-channel systems (monoliths) –
• Automotive catalytic convectors (major success) • Selective catalytic reduction (NH3 – SCR) of power plant NOx
Applications of the Process Utilizing Biomass Streams
Biomass
Waste
Aqueous
Biomass
Stream
Extraction
Extraction
PEM
Fuel Cell
SOFC
ICE
Genset
Microturbine
Genset
Hydrogen
APR
Fuel Gas
APR
Energy
Crops
Process
Hydrogen
CATALYSIS IN THE PRODUCTION OF FUTURE TRANSPORTATION FUELS
Biofuels Life Cycle
Technology for Green & Biofuels
Biomass Sources For Biofuels
• LignoCellulose (Cellulose, Hemicellulose, Lignin)• Starch • Sugars• Lipid Glycerides (Vegetable Oils & Animal Fats)
Structures in Lignocellulose
Pathways to Renewable Transportation Fuels
Biomass
Gasifier
Pyrolysis
Hydrolysis
Syngas
Bio Oils
Methanol,Ethanol,
FT( diesel,etc)
Refine to Liquid Fuels
Ferment to ethanol,butanol
Aqueous phaseReforming
Hydrogen
Gasoline additives
Veg OilsAlgae Oils
Biodiesel
Bioethanol Overview - Global
• Current bioethanol production in US is 12 billion gallons. • Most cars on the road in US today can run on blends of up to 10% ethanol.• US DOE has estimated that there is a potential to produce over 80 Billion gallons
of bio-ethanol from cellulose and hemi-cellulose present in corn biomass in the 9 major US corn producing states.
• This equates to over 250 Million tons of bio-ethanol and >$160 Billion revenue.• Iogen’s Demo plant producing cellulosic ethanol from wheat straw in Canada
since 2004. • DuPont-Danisco JV has started demonstration of cellulosic ethanol from corncobs
since Jan., 2010 in USA.• Brazil currently blends 25% ethanol in gasoline and bioethanol is produced
directly from sugarcane. • Brazilian flex cars are capable of running on just hydrated ethanol (E100), or just
on a blend of gasoline with 20 to 25% anhydrous ethanol, or on any arbitrary combination of both fuels
• China uses 10% bioethanol in gasoline .
2nd Generation Bioethanol Technology Overview
Hydrolysis based Technology PlayersCompany
Location
Technology Present Status
DuPont- Danisco
USA Feed stock - Agri residue. Alkaline pretreatment , enzymatic hydrolysis + C5/C6 Co-fermentation
Pilot Plant started
Iogen/
Shell
Canada Feed stock – Agri Biomass. Pretreatment – steam explosion. Enzymatic hydrolysis & fermentation of C5/C6 sugars
Demo. Plant operating, since 2004. Commercial Plant expected to be commissioned in 2011.
Lignol Canada Feed stock - wood, agribiomass. Organosolv pretreatment & sepn. Of high purity lignin. Enzymatic hydrolysis and fermentation of C5 & C6 sugars separately
Technology proven at Bench scale.
Pilot Scale under Engineering design.
Enzymatic based Cellulosic Ethanol Process
Biomass
Lignin
Pretreatment
C5/C6 SugarsHydrolysis Distillation/
dehydration
Bioreactor
Ethanol 99.7 wt%
Enzyme
Production
Microbe
Second Generation Bioethanol
Gasification based Technology Players
Company Location Technology Present Status
COSKATA USA Feed stock - Agri residue, pet coke, MSW.
Gasification to syn-gas & direct fermentation to ethanol.
Completed pilot scale optimization.
INEOS Bio
USA Feed stock - Agri residue, MSW. Conventional Gasification to syn-gas & its fermentation to ethanol.
Process under study in pilot plant.
Gasification based Technology Players
Biomass
Gasification based Cellulosic Ethanol Process
Gasifier
Bioreactor
Distillation/
dehydration
Microbe
Ethanol 99.7 wt%
Syn-gas
4 - 6% ethanol
Transportation Fuels from Cellulosic Biomass (Pyrolysis Route)
Transportation Fuels from BiomassBIODIESELS
• First generation biodiesel
Fatty Acid methyl esters (FAME); methyl esters of C16 and C18 acids.
• Second generation Biodiesels
“Hydrocarbon Biodiesels” ; C16 and C18 saturated, branched Hydrocarbons similar to those in petrodiesel; High cetane number (70 – 80).
• Third Generation Biofuels
From (hemi)Cellulose and agricultural waste; Enzyme technology for (hemi) Cellulose degradation and catalytic upgrading of products.
First Generation Biodiesels Fatty Acid Methyl Esters
• Veg Oil + methanol FAME + glycerine• Catalysts:Alkali catalysts( Na/K methoxides); CSTR;
Large water, acid usage in product separation
Fuel Quality Problems in First Generation Technology
• Lower glycerol purity; Not suitable for production of chemicals (propanediol, acrolein etc) without major purification; Salts and H2O to be removed from Glycerol.
• Residual KOH in biodiesel creates excess ash content in the burned fuel/engine deposits/high abrasive wear on the pistons and cylinders.
Catalysts for 2nd Generation Biodiesel. “Hydrocarbon Biodiesel “Technology
• “Hydrocarbon Biodiesel” consists of diesel-range hydrocarbons of high cetane number
• Deoxygenation and hydroisomerization of Veg Oil at high H2 pressures and temp.
• Catalysts:NiMo(for deoxyg), Pt-SAPO-11(for isom); H2 at high pressure needed;Yield from VO is lower;C3 credit.
• Can be integrated with petro refinery operations;Greater Feedstock flexibility.
• Suitable for getting PP < - 20 C (Jet Fuels).• 40000 tpy plant in Finland; 200K tpy in Singapore;100K tpy plant using soya
in SA.
Convert Veg Oil to HC Diesel in Hydrotreaters in Oil Refineries
• Hydrotreat /Crack mix of VO + HVGO(5-10%); S=0.35%;N(ppm)= 1614;KUOP = 12.1; density=0.91 g/cc);Conradson C = 0.15%; Sulfided NiMo/Si-Al Catalyst; ~350C,50 bar; LHSV = 5; Diesel yield ~ 75%wt.
• Advantages over the Trans Esterificat Route
- Product identical to Petrodiesel (esp.PP )
- Compatible with current refinery infrastructure
- Engine compatibility; Feedstock flexibility
107
Capital Costs : EIA Annual Energy Outlook 2006
Natural gas to Transportation Fuels : Options
• Natural Gas Syngas
• I. Syngas Methanol (DME) Gasoline
• II. Syngas Fischer-Tropsch Syndiesel
Syndiesel Can use existing infrastructure
• III. Syngas H2 Fuel Cell – driven cars: Stationary vs On-board supply options for Hydrogen
• Natural Gas Electricity;MCFC and SOFC can generate electricity by direct internal reforming of NG at 650C;Ni/ Zr(La)Al2O4, loaded on anode
Catalysts for conversion of NG to Transportation FuelsI.Syngas Preparation- Hydrodesulphurisation(Co/Ni-Mo-alumina)- Syngas generation(H2/ CO); POX, steam, autothermal, “dry”
reforming; Ni(SR),Ru(POX) – based catalysts; Pt metals for POX for FT.
2.Fischer Tropsch Synthesis: Co – Wax and mid dist; Fe - gasoline; Cu & K added. Supported Co preferred due to its lower WGS activity &
consequent lower loss of C as CO2.
3.Product Work up: Wax Conversion to diesel and gasoline. Mild Hydro-cracking/Isom catalysts (Pt metal- acidic oxide support )
Petroleum - vs- Syngas :: Diesel
Property Petro- Syn- Boiling Range,oC 150-300 150-300Density at 15 C,kg/m3 820-845 780S, ppm vol 10 - 50 <1Aromatics,% vol 30 <0.1Cetane No >51 >70CFPP, oC -15 -20Cloud point,oC -8(winter) -15
Due to lower S, N and aromatics, GTL diesel generates less SOx and particulate matter.
Power and fuels from Coal / PetCoke Gasification Texaco EECP Project
FEED:1235 TPD OF PetCoke
PC SG (75%)Power Plant
25%FT fuel(tail gas Power)
• 55 MW Electricity; Steam.
• 20 tpd diesel; 4 tpd naptha
• 82 tpd Wax(60 tpd diesel); 89 tpd S;
• H2: CO = 0.67;Once-thru slurry(Fe) FT reactor; RR = 15 % at a refinery site.
Coal To Syngas To Fuel Cells
Catalysis in Coal / PetCoke gasification
• SR: C + H2O CO + H2 (+117 kJ/mol)
Combust:2C+ O2 2CO (H = -243 kJ/mol)
WGS :CO + H2O H2 + CO2 ( -42 kJ/mol)
Methan: CO+3 H2 CH4 + H2O(- 205 kJ/mol)
• Methanation can supply the heat for steam gasification and lower oxygen plant cost. K & Fe oxides lower temp of gasification
• H2/CO ~0.6 in coal gasification;Good WGS is needed;
• MCFC and SOFC can use H2,CO, & CH4 as
fuel to generate electricity.
• Low rank coals, Lignites gasify easier.
Hydrogen Production Costs(The Economist / IEA)
SOURCE USD / GJCoal / gas/ oil/ biodiesel 1-5NG + CO2 sequestration 8-10Coal + CO2 sequestration 10-13Biomass(SynGas route) 12-18Nuclear (Electrolysis) 15-20Wind (Electrolysis) 15-30Solar (Electrolysis) 25-50
Sugar Cane Juice to H2
AQUEOUS PHASE REFORMING
• C6H12O6 +6H2O 12H2 +6CO2(APR)• Pt-alumina catalysts, 200 oC• 1 kg of H2 ($3-4) from 7.5 kg Sugar Fuel Efficiency of H2 >> diesel/gasoline
H2 Production from Glycerin
• Available from Veg oils(40-98% in H2O)
• C3H8O3 +3H2O 7H2 + 3CO2
• Ru – Y2O3 catalysts; 600 oC
• 1 kg H2 from 7 kg glycerine
H2 production from Biomass is less economically viable than production of ethanol and biodiesel from biomass.
Catalytic Direct Methane Decomposition to H2 and Carbon Nanotubes
Catalytic Auto Thermal Reforming of Methanol, Ethanol, DME to HYDROGEN for FUEL CELL
Pure H2 Supply
• Compressed H2
• Liquid H2
• H2 Hydride
H2 from Reformed liquid HC
H2
Fuel
• Methanol
• Ethanol
• DME
H2 Combustion EngineSimilar to Gasoline Internal Combustion Engine
Pure H2 Supply
• Compressed H2
• Liquid H2
• H2 Hydrid
H2 from Reformed liquid HC
H2
Fuel
• Methanol
• Ethanol
• DME
PEM Fuel Cell
Pure H2 Supply
• Compressed H2
• Liquid H2
• H2 Hydrid
H2 from Reformed liquid HC
H2
Fuel
• Methanol
• Ethanol
• DME
PEM Fuel Cell
H2 Production from Fossil & Renewable
Sources
Catalysts for H2O and CO2 Photothermal SplittingUsing Sunlight
1. H2O H2 + 0.5 O2
2. CO2 CO +0.5 O2
• FT Synthsis: CO + H2 (CH2)n petrol/Diesel
Sandia’s Sunlight To Petrol Project: Cobalt ferrite loses O atom at 1400o C; When cooled to 1100o C in presence of CO2 or H2O, it picks up O, catalyzing reactions 1 and 2; Solar absorber provides the energy.
Challenge: Find a solid which loses / absorbs O from H2O / CO2 reversibly at a lower temp.
Splitting H2O
124
125
Splitting H2O with visible light
Future Fuels: Catalysis Challenges
• Meeting Specifications of Future Fuels Remove S,N, aromatics, Particulate Matter• Power Generation - Lower CO2 Production in Catalytic Gasification - Lower CO2 and H2/CO ratio in Syngas generation• FT Synthesis: Lower CH4 and CO2 ;Inhibit metal sintering; Increase
attrition strength; Reactor design• Biomass:1.Cellulose to Ethanol ( enzymes) 2. Biomass gasification catalysts. Decentralized Production/ Use of H2 and Biofuels will avoid costs
due to their storage and distribution. “Holy Grail “ Challenges• Direct Conversion of CH4 to methanol and C5
+. • Catalytic Water and CO2 splitting using solar energy
Thanks
Discussion