EU-GCC Clean Energy Technology Network - Coping with the … · 2016-11-15 · EU-GCC Clean Energy...
Transcript of EU-GCC Clean Energy Technology Network - Coping with the … · 2016-11-15 · EU-GCC Clean Energy...
Coping with the surging waste problem: Zero landfilling is reality or
mission impossible!EU-GCC Clean Energy Network II
Dr. Isam Janajreh, Associate Professor - Mechanical Engineering, Masdar Institute
Q1. Is waste to energy (Waste2Energy)?
a) Only slogan
b) Sustainable business
c) True to some extent
Q2. Is waste management?
a) Individual responsibility and privately driven business
b) Authorities/governments responsibility
c) Equal share responsibilities
Q3. How do you deal with it? Average is 1kg/day per capita and 5kg in some
developing countries!
a) Landfilling with i.e. sporadic scavenging/recycling model no additional cost
b) Regulated & compulsory recycling, costly advanced technologies & zero landfill
c) Optional recycling and incinerate the rest, fixed quota and additional penalty
Masdar’s Mission is clear
Mission
To make Abu Dhabi the
international hub for
alternative/sustainable energy
To create an entirely new
economic sector in Abu
Dhabi to lead this industry
To be a catalyst for change on
a global scale
Advocating zero waste
3
Overview :
Country * MSW Country MSW
(Kg/person/day) (Kg/person/day)
Bahrain 1.3 Austria 0.89
EU-7 1.4 Belgium 0.93
India 0.45 Egypt 0.81
Italy 0.95 France 0.89
Japan 1.12 Jordan 0.6
Kuwait 1.4 Oman 0.7
Qatar 1.3 Portugal 0.7
Spain 0.88 Tunisia 0.41
UAE 1.2-5kg Turkey 0.95
US 2 UK 0.95
Year
Type of Waste (Thousands tons/year)
TotalOrganics Fiber Wood Plastic Paper Glass Metal Others
1995 422 41 41 109 178 29 23 11 854
2000 492 47 47 124 203 32 26 13 984
2005 558 53 53 141 231 37 29 15 1,117
2010 662 63 63 167 273 44 35 17 1,324
2015 736 71 71 185 303 49 38 19 1, 472
2020 830 80 80 209 342 55 43 22 1,661*Al-Salem and Lettiere, European Journal of Scientific ResearchISSN 1450-216X Vol.34 No.3 (2009), pp.395-405
Managing the surging waste problem• Group Leader: Waste to Energy Lab (http://waste2energy.labs.masdar.ac.ae/index.html)
• Editor in Chief: International Journal of Enhanced Research in Science Technology and Engineering (http://www.erpublications.com/)
• Associate editor: International Journal of Thermal and Environmental Engineering (http://www.iasks.org/journals/ijtee)
• Editor: The Journal of Solid Waste Technology and Management (http://www.solid-waste.org)
• Editor: Journal of Energy and Power Engineering (http://www.davidpublisher.org/index.php/home/journal/detail?journalid=28&jx=JEPE)
Material Characterization:• Proximate (TGA)
• Ultimate (CHNSO-Flash)
• Chemical Kinetics (TGA)
• Thermal properties: Bomb Cal/Cp(STA)
• Impurities (GCMS, ICP, FTIR)
• Species determination (Drop. Tube)
0.1 0.25 0.38 0.52 0.66 0.8
Min=0.149 Max=0.788
40 60 80 100 120 140 160
Min=35.0Mpa Max=165.5Mpa
von Mises Strain
von Mises Stress
60
65
70
75
80
85
90
95
100
20 120 220 320 420 520 620 720 820
Weig
ht (
%)
Temperature (C)
5 C/min
10 C/min
15 C/min
20 C/min
High Temperature Pathways:• Incinerations/Combustion
• Gasification (GEK)
• Pyrolysis (Buchi Reactor)
Low Temperature Pathways:• Digestion : Hydrolysis, acido, Aceto &
Methanogenises
• Transesterification
• Plastic recycling/remoulding
OVERVIEWProvide sustainable routes to maximize resource utilization by converting waste to energy, reduce
MENA‘s emission footprint (CO2, NOX, SOX, CH4, etc.), fulfill the emerging stringent environmental
regulations, and reduce landfill deposits.
Waste
Classific
ation
Gasification
Pyrolysis
Trans/esterification
Digestion
Distillation/Oil
Phase-change Material
Compost/Soil
P
o
w
e
r
Waste
Water
Industry Waste Water Treatment
Algae Culture
Sludge
Gray Water
Clean Water
MSW (Dry)
Homog. Ind.
Organic Waste
Waste
Oil/ Lipid
MSW (Wet)
Hea
t
Biogas
Bio-diesel
Glycerol
Oil
Syngas
CombustionSensible
heat
Gas
MSW (mixed)
Biomass
Use high temp. conversion: Incineration, gasification and pyrolysis of waste stream into synga
Promote IGCC as the cleanest and most efficient (50%) power generation technology amenable to CO2
capturing and co-firing of MSW
Use trans-esterification of waste cooking and algae oil into biodiesel (2nd and 3rd Generation)
Use digestion (bioreactor) processes to convert organic waste into bio-fuel/landfill gas and compost
What does the feedstock/Waste compose of? Organic waste is a complex collection of polymers
Infer the moisture, volatiles, fixed carbon and ash present in the sample
Heating value: 6-14 MJ/kg that is 1 ton waste = 2 MWh district heating or 0,67 MWh electricity
MATERIAL CHARACTERIZATION
The processes in a burning refuse
bed include:
Drying
Ignition
Pyrolysis
Gasification
Solid-phase combustion
Gas-phase combustion
Material Characterization: Proximate Analysis and Ultimate Analysis
Tuesday, November 15, 2016
Simultaneous DSC/TGA Q600 Parr 6100 Bomb calorimeterFlash 2000 CHNSO analyzer (TCD)
Break away Analyses in Percentile PHC (%) MSW(%)
WWTS (%)
Organic material weight 48 78 10
Moisture content 10 20 90
Volatile Solid (VS) of total organic solids 85 83.5 100
Biodegradable Volatile Solid (BVS) 95 75 90 [1]
BVS to be converted to biogas 95 90 95 [1]
Whereas the entire formula will be converted into Syngas in
thermochemical conv., nearly 50% is converted to CH4 and
CO2 in Anaerobic Digestion.
𝐻𝐻𝑉 𝑀𝐽
𝐾𝑔 = −0.03 𝐴𝑠ℎ − 0.11 𝑀𝑜𝑖𝑠𝑡𝑢𝑟𝑒 + 0.33 𝑉𝑜𝑙𝑎𝑡𝑖𝑙𝑒𝑠 + 0.35 𝐹𝑖𝑥𝑒𝑑 𝐶𝑎𝑟𝑏𝑜𝑛
𝐻𝐻𝑉 𝑀𝐽
𝐾𝑔 = 0.3491 𝐶 + 1.1783 𝐻 + 0.1005 𝑆 − 0.1034 𝑂 − 0.0151 𝑁 − 0.0211 𝐴
Waste
Stream
Molecular formula
PHC CH1.138O0.477N0.004+Moisture +Ash
MSW CH1.58 O0.63N0.016+Moisture +Ash
WWTS CH2.071O0.565N0.0621+Moisture +Ash
Advantages- Control over produced energy
- Capability for carbon capture and storage.
- Flexibility in feedstock and products.
- Alternative to “bury or burn” policy.
- Hydrogen-based energy systems (near zero-CO2 emissions).
- Small scale gasifiers for distributed generation.
O2
CnHmOx
Slag
CO2
H2
CO
Stage 2:
2 -4 burners
1200 1600
Syngas
AshStage 1:
2 -4 burners
CO2,H2O
Temperature, oC
Lower: Stoichiometric O2
upper: Lean O2
Gasification
vs
Combustion
CO C CO2
H2 H H2O
N2 N Nox
H2S S SOx
Gasifier
T=1,000-1,500 C
P=20-40bar
Air Separation
UnitO2
Steam
Air
Gas cleaningCO shift and
CO2 removal CO2 for
storage
Sulfur H2
Combustor
Heat recovery steam
generator
Flue gas
GeneratorSyngas Gas turbine
Steam
turbine Generator
Electric
Power
Electric
Power
CondenserPump
N2
Ash
Gas cooler
Coal
Definition: To convert carbonaceous solid material (CHxOyNzSm) into a mixture of CO and H2 in an O2 deprived environment.
Cycle Fuel Temp low (oC) Temp High (oC) Carnot (h) Actual (h) Car(h)/Act(h)%
Conventional Steam Power Plant Coal 27 540 63 40 63
Ditto Ultra Super Critical Coal 27 650 67 45 67
IGCC Coal 27 1350 82 46 56
Open Gas Turbine Cycle Gas 27 1210 80 43 54
Combined Cycle Gas 27 1350 82 58 71
Low Speed Marine Diesel (LSMD) Heavy Fuel Oil 27 2000 87 48 55
LSMD with Super Charger Heavy Fuel Oil 27 2000 87 53 61
Thermochemical overview: To Gasify, or not to Gasify
MSW
Equilibrium constant approach
Tuesday, November 15, 2016
Global Gasification reaction
•Elemental balance
•Carbon balance
•Hydrogen balance
•Oxygen balance
•Nitrogen balance
•Equilibrium constant equation
•For Bouduard reaction:
•For CO shift reaction:
•For Methanation reaction:
•Energy balance between reactant and product
•Conversion Metrics
𝐶𝐺𝐸 =𝑥1 283800 + x2 283237.12 + x5 889000
𝐻𝐻𝑉𝑓𝑒𝑒𝑑𝑠𝑡𝑜𝑐𝑘
)()(1_1_
so
N
reacti
iso
N
prodi
i hhnQhhn
𝐶𝐻𝑥𝑂𝑦𝑁𝑧 +𝑚 𝑂2 + 3.76𝑁2 + 𝑛𝐻2𝑂 + 𝑝𝐶𝑂2 → 𝑥1𝐻2 + 𝑥2𝐶𝑂 + 𝑥3𝐶𝑂2 + 𝑥4𝐻2𝑂 + 𝑥5𝐶 +𝑧
2+ 3.76𝑚 𝑁2
)76.32
(
).(
).(
).(
54321
2
1
5
3
42
31
2
3
2
21
mz
xxxxxx
reactionnMethanatioforconstmEquilibriux
xxK
reactionshiftCOforconstmEquilibriuxx
xxK
reactionBoudouardforconstmEquilibriuxx
xK
total
total
total
1) Combustion reactions
2) Reduction reactions
Gasification analysis:
Tuesday, November 15, 2016
H2O Gasification CO2 Gasification
Gasification analysis:
HIGH FIDELITY SIMULATION
Reaction kinetics via Arrhenius equation
Tuesday, November 15, 2016
Arrhenius Equation
•Integral method:
•Direct Arrhenius plot method:
•Method of approximate temperature integral:
A and E can be used in high Fidelity simulation
Heating Rate Events E (KJ/mol) A (sec-1) E (KJ/mol) A (sec-1) E (KJ/mol) A (sec-1)
Drying 15.9 2.22E-01 8.3 3.26E-02 17.0 3.97E-01
Devolatization 64.5 2.19E+02 60.7 1.51E+02 66.7 3.02E+02
Boudouard 152.0 4.71E+05 172.0 7.98E+06 155.8 5.59E+05
Drying 5.9 4.70E-03 8.0 1.96E-02 6.9 1.16E-02
Devolatization 65.8 2.13E+02 64.2 2.16E+02 68.0 2.92E+02
Boudouard 173.8 8.03E+06 182.2 2.76E+07 177.8 9.18E+06
Drying 5.6 2.30E-03 4.7 3.90E-03 6.6 5.80E-03
Devolatization 65.3 1.73E+02 60.5 9.66E+01 67.6 2.38E+02
Boudouard 171.2 3.25E+06 145.3 1.16E+05 175.3 3.76E+06
Drying 10.9 5.80E-03 5.0 1.60E-03 11.9 1.18E-02
Devolatization 65.8 1.17E+02 56.2 2.62E+01 68.0 1.60E+02
Boudouard 168.1 1.61E+06 122.2 4.19E+03 172.2 1.87E+06
5 K/min
20 K/min
15 K/min
INTEGRAL METHODDIRECT ARRHENIUS
PLOT METHOD
APPROX. TEMP.
INTEGRAL METHODMETHODS:
10 K/min
;)1( nXKdt
dX
E
RA
TR
E
T
X
ln
)1ln(ln
2
A
TR
E
TT
XX
x
TTln
1
1
1ln
12
12
u
cb
du
uPd
)(ln
0.001
0.01
0.1
1
60
65
70
75
80
85
90
95
100
20 220 420 620 820
Heat
flow
(W)
Wei
ght (
%)
Temperature (C)
5 C/min
10 C/min
15 C/min
20 C/min
Heat flow-10 C/min (W)
Event 1 (drying/Moisture release) Event 2 (devolatization)
Event 3 (Boudouard reaction/fixed carbon)
)/( RTEeAK
Coupled CFD and reaction kinetics
) )
sourcediffusionadvectiverateTime
Sxx
uxt ii
i
i
) ) ) ii
i
ittmi
i
ii
i
i SRx
mScD
xmu
xm
t
/,
1) Continuity, Momentum, Energy, TKE (k) & TDR (e):
2) Transportation equation for mi species:
;1
,
1
,
,
,
i
N
i
ri
k
ki
N
i
ri SvSvrf
rb
)/(
1
,,,,,
*,)(
RTE
N
j
rjriririri
eAk
CkvvMR rj
h
Mathematical System:
3) Reaction kinetics:
) ) pP
PPPDP u
dt
xdguuF
dt
ud
;
4) Discrete Lagrangian particle:
The procedure for the calculation of pulverized feedstock conversion:(a) Solve the continuous phase
(b) Introduce and solve for the discrete phase
(c) Recalculate the continuous phase flow, using the inter-phase exchange of
momentum, heat, and mass determined during the previous particle
calculation;
(d) Recalculate the discrete phase trajectories in the modified continuous phase
flow field;
(e) Repeat the previous two steps until a convergence solution
])1([ 00)/(
pvp
RTEpmfmAe
dt
dm
)()( 44
pRppfg
p
pp
p
pp TTAhdt
dmTThA
dt
dTcm e
HIGH FIDELITY SIMULATION CONT’D
Geometry & Mesh Generation
200t/d two-stage air blown gasifier and nozzle geometry showing blocking topology
and the resulted 3D mesh same geometry of Chen et al. and Bockelie et al.
13D
D
D/3D/4
1.6D
Combustor
Throat
Diffuser
Reductor
Top view
Inputs
Top view
The 3D mesh consists of 1,500,000 finite volumes.
Fitted within 30 volumes of surface sweep Boundary
layer (i.e. y+<20).
Captures the exact gasifier topography.
HIGH FIDELITY VALIDATION CONT’D
Parametric study for the input velocity of oxidizer:
Assembled biomas Gasifier At MIVelocity distribution (m/s)Temp. distribution (K)
Geometry and mesh
Reaction Kinetic Parameters Aj , Ej [kJ/mol]
R1 2 𝐶𝑂 + 𝑂2 → 2 𝐶𝑂2
𝐴 = 1017.6[(m3mol-1)-0.75s-1], 𝐸 = 166.28
R2 2 𝐻2 + 𝑂2 → 2 𝐻2𝑂 𝐴 = 1𝑒11 [m3mol-1s-1], 𝐸 = 42
R3 𝐶𝑂 + 𝐻2𝑂 ↔ 𝐶𝑂2 + 𝐻2 𝐴 = 0.0265, E= 65.8
R4 𝐶 𝑠 + 𝑂2 → 𝐶𝑂2 𝐴 = 5.67𝑒9 [s-1], 𝐸 = 160
R5 𝐶 𝑠 + 𝐶𝑂2 → 2 𝐶𝑂 𝐴 = 7.92𝑒4 [m3mol-1 s-1], 𝐸 = 218
R6 𝐶 𝑠 + 2 𝐻2 → 𝐶𝐻4 𝐴 = 79.2 [m3mol-1 s-1]𝐸 = 218
R7 𝐶 𝑆 + 𝐻2𝑂 → 𝐶𝑂 + 𝐻2 𝐴 = 7.92𝑒4 [m3mol-1 s-1], 𝐸 = 218
R8 𝑣𝑜𝑙 + 0.4 𝑂2 → 1.317 𝐶𝑂 + 2.09 𝐻2
+ 0.064 𝑁2 𝐴 = 1𝐸15 [m3mol-1 s-1], 𝐸 = 1𝐸8
Coping with the surging waste problem: zero landfilling is reality or
mission impossible!
Dr. Isam Janajreh, Associate Professor - Mechanical Engineering, Masdar Institute
Q1. Is waste to energy (Waste2Energy)?
a) Only slogan
b) Sustainable business
c) True to some extent
Q2. Is waste management?
a) Individual responsibility and privately driven business
b) Authorities/governments responsibility
c) Equal share responsibilities
Q3. How do you deal with it? Average is 1kg/day per capita and 5kg in some
developing countries!
a) Landfilling with i.e. sporadic scavenging/recycling model no additional cost
b) Regulated & compulsory recycling, costly advanced technologies & zero landfill
c) Optional recycling and incinerate the rest, fixed quota and additional penalty
Tuesday, November 15, 2016
Abu Dhabi : Current Waste Management Practices
Abu Dhabi : Current Waste Management Practices
Avg. HHV:
12HH MJ/kg
Foreign Incineration Technology in Steady Development About 2100 waste incineration plants in 2006, daily capacity of 620kt/d, treating 165 million tons
of waste every year, currently is close to 3000 and treating over 225 million tones
Waste incineration plants are mostly located in developed regions, about 35 countries own waste
incineration plants, EU 38%, Japan 24%, US 19%, East Asia 15%
ZDWT
Chen Zefeng , Chairman of ZDWT (middle), Petra Roth, the Frankfurt Mayor (left), and RetoFrancioni, Deutsche Boerse CEO (right) Celebtate the listing
• Founded in 1996, 19 years in
environmental protection
industry, subsidiary Fengquan
Environmental Protection
Holdings Co.Ltd.
• In 2007.7.6, ZDWT listed in
German stock market
• Managed over 100 projects, one
of the top performing companies
• Address:Listed company:
Frankfurt ,Germany
Operation headquarter:
Beijing, China
Production base:
Fuzhou, China
Waste Incineration and Water Cogeneration
中国 印尼 越南 印度
Reverse Osmosis
(RO)
Desalination
Steam Heat/
Exchanger
Multi Effect
Destillation (MED)
Waste Treatment
Plant
Turbine/
Generator
Business Case:
Waste to Energy with RO & MED (Thermal) based only on selling
fresh water
Electricity
Steam
Process Flow
Flash evaporation (MED)
Reverse Osmosis (RO)
Device Configuration
1000t/d x 10,000kJ/kg Over all efficiency near 28%
Avg. 30MW
1000 t/d 1000 t/d
500 t/d
500 t/d
30MW
• 1000 t/d plant throughput
• Waste Incineration based
• Dual Incinerator
• Steam turbine
Main Equipment
Hydraulic Bridge Crane
Origin: Germany ( DEMAG )
Reverse-acting Grate
Origin: Germany (MARTIN)
Burner
Origin: Germany ( SAACKE )
Flue gas purification system
Origin: Belgium ( SEGHRS )
Bagfilter
Origin: United States ( GORE)
Instrument Control System
Origin: Belgium ( SEGHS )
DCS system
Origin: Germany ( SIEMENS )
Summary:Parameters of system
project parameter
Incineration processing capacity
1000t/d
Waste low heating value ( design value )
10,000kJ/kg
System working time 24h/d(8000h/y)
System Configuration 2x500t/d(Incineration System)+30MW
(Power generation systems)
Incineration System German Martin incinerator
Flue gas purification system technology
Belgium Seghers
Investment in equipment 150 million US dollars
Electric Power generation 22450kwh/h
Flue gas emission standards EU standards
What you need to know
• Thermochemical conversions is making a strong comeback as sustainable energy source and efficiency enhancement.
• This technology can be deployed as renewable source for million of tons of waste streams disposed of at landfill and risking our ecological system.
• High fidelity analyses and simulations are needed at the conceptual level to increase the process efficiency and throughput.
• This can open wide collaboration door on multiple feedstock gasification technology, conventional, plasma and plastic, biomass etc.
Tuesday, November 15, 2016
Thank you
Tuesday, November 15, 2016
CFD: Improved modeling resultsParticle temperature pathlines showing
the effect of swirl.
HIGH FIDELITY SIMULATION CONT’D
Kinetics of the Gasification Process
Reaction Activation Energy
(𝑬𝒂)
Pre-Exponential
Factor (A)
N
𝐶 +1
2𝑂2 → 𝐶𝑂
9.23 × 107 2.3 1
𝐶 + 𝐶𝑂2 → 2𝐶𝑂 1.62 × 108 4.4 1
𝐶 + 𝐻2𝑂 → 𝐶𝑂 + 𝐻2 1.47 × 108 1.33 1
Reaction Activation Energy
(𝑬𝒂)
Pre-Exponential
Factor (A)
N
𝐶𝐻4 +1
2𝑂2
→ 𝐶𝑂 + 2𝐻2
1.25 × 108 4.4 × 1011 0
𝐻2 +1
2𝑂2 → 𝐻2𝑂
1.67 × 108 6.8 × 1015 -1
𝐶𝑂 +1
2𝑂2 → 𝐶𝑂2
1.67 × 108 2.24 × 1012 0
𝐶𝐻4 + 𝐻2𝑂
→ 𝐶𝑂 + 3𝐻2
1.25 × 108 3 × 108 0
𝐶𝑂 + 𝐻2𝑂 → 𝐶𝑂2 + 𝐻2 8.37 × 107 2.75 × 109 0
Heterogeneous Reactions
Homogeneous Reactions
HIGH FIDELITY SIMULATION CONT’D
MethodologyTheory of anaerobic digestion
• The operations of a bioreactor landfill is comparable to modern municipal waste water treatment plants in pursuing a controlled decomposition of organic waste
• It differs from classical dry landfill with moist addition and faster biodegradation
• Bioreactor landfill can fully degrade waste in several years instead of decades as in the classical dry tomb landfill.
• It generates faster Landfill gas (LFG) for fuel utilization.
Tuesday, November 15, 2016
Landfill, or not to landfill?
(C6H10O5)n + n H2O → n C6H12O6
C6H12O6→ CH3 (CH2)2 COOH + 2H2 + 2 CO2
C6H12O6 + 2H2→ 2 CH3CH2COOH + 2H2O
C6H12O6 + 2 H2O → 2CH3COOH + 4H2 + CO2
CH3(CH2)2COOH + 2H2O → 2 CH3COOH + 2 H2
CH3CH2COOH + 2H2O → CH3COOH + 3 H2 + CO2
CH3COOH → CH4 + CO2
4H2 + CO2→ CH4 + 2 H2O2
Tuesday, November 15, 2016
• The first stage of the anaerobic biodegradation is
hydrolysis. In the hydrolysis step, the complex organic
compounds are solubilized and converted into smaller
sized organic compounds by extracellular enzymes.
• The acidogenic process begins and the end products of
hydrolysis are oxidized to organic acids. The organic
acids are then broken into acetic acid.
• The formation of acetic acid in the acidogenic process
marks the beginning of the acetogenesis stage. In this
stage, conversion of propionic and butyric acids into
acetic acid occurs as described in the following
reactions
• The final stage, methanogenesis, involves the
formation of methane either from acetate or carbon
dioxide reduction with hydrogen, as shown in the
following reactions
Anaerobic digestion protocol?
• Numerous samples solid samples analyzed in our lab subjected to homogenization, ball mill and sieving, TGA, Elemental and bomb clorimetery.
• The estimated theoretical yield follows the biodegradation stoichiometric:
CaHbOcNd + (4a-b-2c-3d)/4 H2O → (4a+b-2c-3d)/8 CH4+ (4a-b+2c-3d)/8 CO2 + dNH3 [1]
Anaerobic Gas Yield PHC MSW WWTSWeight of the methane (kg) per 100 kg of waste 16.45 20.09 0.356Weight of carbon dioxide (kg) per 100 kg of waste 41.4 48.14 0.669Volume of the methane (m3) 10.39 12.64 0.225Volume of carbon dioxide (m3) 9.512 11.03 0.153Percentage of the methane % 52.21 53.39 59.49Percentage of carbon dioxide % 46.65 46.60 56.56Process efficiency % 34% 26% 3.5%
As Received Dried Dried &Sieved
CH1.13O0.477N0.004 + 0.474H2O → 0.5215 CH4+ 0.4785 CO2 + 0.004NH3
Process effeciency?
Tuesday, November 15, 2016
Coping with the surging waste problem: zero landfilling is reality or
mission impossible!
Dr. Isam Janajreh, Associate Professor - Mechanical Engineering, Masdar Institute
Q1. Is waste to energy (Waste2Energy)?
a) Only slogan
b) Sustainable business
c) True to some extent
Q2. Is waste management?
a) Individual responsibility and should be privately driven business
b) Authorities/governments responsibility
c) Equal share responsibilities
Q3. How you deal with it? Average is 1kg/day per capita and 5kg in some
developing countries!
a) Landfilling with i.e. sporadic scavenging/recycling model no additional cost
b) Regulated & compulsory recycling, costly advanced technologies & zero landfill
c) Optional recycling and incinerate the rest, fixed quota and additional penalty
LOW FIDELITY SIMULATION
Gibbs energy minimization approach
Δ𝐺𝑓𝑖𝑜 + 𝑅𝑇 ln
𝑛𝑖
𝑛𝑡𝑜𝑡𝑎𝑙 + 𝜆𝑘𝑎𝑖𝑘
𝑘
= 0, 𝑖 = 1,2, … , 𝑛
Gibbs Energy minimization using Lagrange :
multiplier
C(g) CH CH2 CH3 CH4 C2H2 C2H4 C2H6 C3H8 H H2
O O2 CO CO2 OH H2O H2O2 HCO HO2 N N2
NCO NH NH2 NH3 N2O NO NO2 CN HCN HCNO S(g)
S2(g) SO SO2 SO3 COS CS CS2 HS H2S C(s) S(s)
Species
List of species considered in the model
),....,,( 21, N
t
PT nnngG
Ultimate AnalysisUltimate Analysis
(DAF wt. %)
Utah Bituminous
Coal
El-Lajjun Jordanian
Oil Shale
Tires
Carbon 81.810 49.373 80.06
Hydrogen 5.610 4.976 7.57
Nitrogen 2.490 1.001 0.29
Oxygen 8.960 36.438 10.72
Sulfur 1.130 8.212 1.36
Proximate Analysis
(wt. %)
Utah Bituminous
Coal
El-Lajjun Jordanian
Oil Shale
Tires
Moisture 2.304 1.82 1.02
Volatile 30.19 21.21 67.31
Fixed Carbon 57.20 13.70 22.93
Ash 10.306 63.27 8.74
Utah Bituminous
Coal
El-Lajjun Jordanian
Oil Shale
Tires
Heating Value
(MJ/kg)
34.38 7.66 29.52
Proximate Analysis
Bomb Calorimetry
HIGH FIDELITY SIMULATION CONT’D
Predictive Modeling of the Gasification of Oil Shale in an O2-Blown BYU Atmospheric Gasifier
Schematic Diagram of the O2-
Blown BYU Atmospheric Gasifier
Boundary Conditions
HIGH FIDELITY SIMULATION CONT’D
Predictive Modeling of the Gasification of Oil Shale in an O2-Blown BYU Atmospheric Gasifier
1010
700
400
0.05
0.02
0.00
0.0166
0.0083
0.0000
0.0007030
0.0000352
0.0000000
Temperature (oC) Mole Fraction of CO Mole Fraction of CO2
Mole Fraction of H2
HIGH FIDELITY SIMULATION CONT’D
2800
1600
400
Temperature (oC)
0.3523
0.1761
0.0000
Mole Fraction of CO
0.4913
0.2456
0.0000
Mole Fraction of CO2
Mole Fraction of H2
0.32
0.16
0.00
Predictive Modeling of the Gasification of Utah Bituminous Coal in an O2-Blown BYU
Atmospheric Gasifier
Mole Fraction of H2
HIGH FIDELITY SIMULATION CONT’D
Predictive Modeling of the Gasification of Tire Crumbs in an Air-Blown Drop Tube Reactor
0.1870
0.0934
0.0000
0.1680
0.0925
0.0000
0.2300
0.0104
0.0000
6.11e-3
3.05e-3
0.0000
Mole Fraction of CO Mole Fraction of CO2
Mole Fraction of O2Mole Fraction of H2
Schematic Diagram of the DTR at
Masdar Institute
HIGH FIDELITY SIMULATION CONT’D
Mole Fraction\Fuel Coal Oil Shale Tire
Hydrogen 0.2832 8.62e-6 4.28e-3
Carbon Monoxide 0.3516 0.0461 0.1523
Carbon dioxide 0.2249 0.0154 0.0836
Cold Gasification Efficiency
69.6 18.5 43.2
Comparative Mole Composition of the Product Gases at the
Exit and the Cold Gasification Efficiency
HIGH FIDELITY SIMULATION CONT’D
Model Boundary and Operating
Conditions
Feedstock Composition Taiheiyo Bituminous Coal
Ultimate (wt%)
C 77.6
O 13.9
H 6.5
N 1.13
S 0.22
Proximate (wt%)
FC 35.8
V 46.7
M 5.3
A 12.1
HHV (MJ/kg) 27.4
Gas flow rate (kg/s)
Combustor burners 1 4.708
Combustor burners 2 4.708
Diffuser burners 1.832
Particle loading (kg/s)
Combustor burner 1 0.472
Combustor burner 2 1.112
Diffuser burner 1.832
Wall Temperature (K)
Combustor 1897
Diffuser 1073
Reductor 873
Pressure (MPa) 2.7
Turbulence Model K-e Standard
Selected Model Parameters & Operating Conditions:
Modeled Reactions:
HIGH FIDELITY SIMULATION CONT’D
Can a zero dimensional model predict the gasifier performance?
MODELING:
Simplest level of modeling.
No dimension nor time is variable.
Entrained flow gasifiers are amenable to equilibrium.
Category Entrained-FlowAsh condition Dry Ash Slagging Dry Ash Agglomerating Slagging
Typical processes Lurgi BGL Winnkler, HTW, CFB KRW, U-Gas Shell, Texaco, E-Gas, Noell, KT
Feed characteristics
Size 6-50mm 6-50mm 6-10mm 6-10mm <100 m
Acceptability of fines Limitted Better than dry ash good better unlimitted
Acceptability of caking coal yes (with stirrer) yes possibly yes yes
Prefered coal rank any high low any any
Operating characteristics l
Outlet Gas Temperature low (425-650C) low (425-650C) moderate (900-1050C) moderate (900-1050C) high (1250-1600C)
Oxidant demand low low moderate moderate high
Steam demand high low moderate moderate low
Other characteristics hydrocarbone in gas hydrocarbone in gas lower carbon lower carbon pure gas, high c conversion
Moving Bed Fluid Bed
Source: Adapted from Simbeck et al. 1993
Advocating zero waste
43
Overview :
Country * MSW Country MSW
(Kg/person/day) (Kg/person/day)
Bahrain 1.3 Austria 0.89
EU-7 1.4 Belgium 0.93
India 0.45 Egypt 0.81
Italy 0.95 France 0.89
Japan 1.12 Jordan 0.6
Kuwait 1.4 Oman 0.7
Qatar 1.3 Portugal 0.7
Spain 0.88 Tunisia 0.41
UAE 1.2 Turkey 0.95
US 2 UK 0.95
Year
Type of Waste (Thousands tons/year)
TotalOrganics Fiber Wood Plastic Paper Glass Metal Others
1995 422 41 41 109 178 29 23 11 854
2000 492 47 47 124 203 32 26 13 984
2005 558 53 53 141 231 37 29 15 1,117
2010 662 63 63 167 273 44 35 17 1,324
2015 736 71 71 185 303 49 38 19 1, 472
2020 830 80 80 209 342 55 43 22 1,661*Al-Salem and Lettiere, European Journal of Scientific ResearchISSN 1450-216X Vol.34 No.3 (2009), pp.395-405
To Gasify, or Not to Gasify?
Accurately model flow and
conversion
•Particle dispersion
•Turbulence-chemistry-radiation interactions
Space efficiency
Accurately model flow and
temperature distribution
•Turbulence-chemistry-radiation interactionsInjector failure
Accurately model wall
interactions, thermal stresses,
pressure effects and abrasion
•Particle dispersion and inhomogeneous heat distribution
•Turbulence-chemistry-radiation interactions
•Slag wall build up
Wall/refractory
failure
Accurately flow modeling,
conversion, ash distribution and
pollutant formation
•Particle dispersion and inhomogeneous distribution
•Agglomeration, swelling and fragmentation particle
mechanisms
•Nitrogen and sulfur production
Downstream fouling
and poisoning
Accurately models slag flow,
composition and temperature
distribution and turbulence
•Turbulence-chemistry-radiation interactions
•Accurate Slag characterization
Slag
blockage/removal
Accurately models fuel switching
and associated reactions
•Dynamic and intrinsic behavior
•Feedstock and char characterization –proximate&ultimate
analysis
Feedstock flexibility
Modeling implementationPhysical aspectCurrent needs
& technology
challenges
Accurately model flow and
conversion
•Particle dispersion
•Turbulence-chemistry-radiation interactions
Space efficiency
Accurately model flow and
temperature distribution
•Turbulence-chemistry-radiation interactionsInjector failure
Accurately model wall
interactions, thermal stresses,
pressure effects and abrasion
•Particle dispersion and inhomogeneous heat distribution
•Turbulence-chemistry-radiation interactions
•Slag wall build up
Wall/refractory
failure
Accurately flow modeling,
conversion, ash distribution and
pollutant formation
•Particle dispersion and inhomogeneous distribution
•Agglomeration, swelling and fragmentation particle
mechanisms
•Nitrogen and sulfur production
Downstream fouling
and poisoning
Accurately models slag flow,
composition and temperature
distribution and turbulence
•Turbulence-chemistry-radiation interactions
•Accurate Slag characterization
Slag
blockage/removal
Accurately models fuel switching
and associated reactions
•Dynamic and intrinsic behavior
•Feedstock and char characterization –proximate&ultimate
analysis
Feedstock flexibility
Modeling implementationPhysical aspectCurrent needs
& technology
challenges
Cycle Fuel Temp low (oC) Temp High (oC) Carnot (h) Actual (h) Car(h)/Act(h)%
Conventional Steam Power Plant Coal 27 540 63 40 63
Ditto Ultra Super Critical Coal 27 650 67 45 67
IGCC Coal 27 1350 82 46 56
Open Gas Turbine Cycle Gas 27 1210 80 43 54
Combined Cycle Gas 27 1350 82 58 71
Low Speed Marine Diesel (LSMD) Heavy Fuel Oil 27 2000 87 48 55
LSMD with Super Charger Heavy Fuel Oil 27 2000 87 53 61
Challenges
Model Sample Results
Temperature field distribution. (A)
Showing complete geometry. (B, C)
Closer look at the combustor and diffuser.
Average gasifier temperature = 1493 K
A B C
b:CO2 wt fraction c:H2O wt fraction
d:CO wt fraction e:H2 wt fraction
Model Sample Resultsa:T (K)
f: Oxygen wt fraction
g: Volatiles wt fraction h: Char concentration (kg/s)
Velocity (m/s*100)