Presentación de PowerPointweb.abo.fi › projekt › poke › Saarenmaa › High-pressure... · 95...
Transcript of Presentación de PowerPointweb.abo.fi › projekt › poke › Saarenmaa › High-pressure... · 95...
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IGH PRESSURE PROCESSES
High-pressure technology in the processing of biomass
Dr. JUAN GARCÍA SERNA
IGH PRESSURE PROCESSES
hpp.uva.es
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what society needs 0
NEEDS - PROBLEMS
SOLUTIONS
WELFARE STATE - WELLBEING
MEDICINS AND DRUGS
TRANSPORTS and FUELS
COMUNICATIONS and COMPUTERS
PESTICIDES and FERTILIZERS
CLEANING and DISINFECTION PRODUCTS
EXPLOSIVES
PACKAGING and CONTAINERS…
Is it sustainable?
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what society needs 0
PRODUCTS SERVICES
MATERIAL ENERGY
WORK
ECONOMY
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bioeconomy paradigm 1
Infrared Radiation
Solar Radiation
Sustainability Of Eco-system
Photosynthesis
Life & Food Chain
95 billion (109) ton C / y H2O CO2
Organics
Man is a part of the eco-system
The only answer to a sustainable society is
to establish Material Recycle driven by solar energy that is harmonized with the eco-system.
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energy options 2
GAS
SHALE GAS
PETROLEUM CARBON
ETC…
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energy options 2
Biomass circulation by Photosynthesis
95 billion (109) ton C/y
Determining the Sustainable limit of harvest is an important task of the future.
Present world consumption of Fossil Fuel
6.5billion (109) ton C/y
>
Independence from fossil fuels can be achieved by using less than 10% of this circulating Biomass
A Fundamental Sustainable Society Driven by an External Energy can be achieved
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raw material options 3
GAS PETROLEUM
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raw material options 3
Food
Biomass
Non-edible components
Cellulose
Lignin
Hemicellulose
Thermal Energy
H2, CH4
Novel Materials
Oligosaccharides
Glucose
Chemical Products
Chemical Feed Stocks
Liquid Fuels
Fin
e C
he
mic
als
Solubilization
Co
nve
rsio
n
Rea
ctio
ns
Separation
Incineration/SCWO
Gasification
Hydrolysis
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biomass, of course !! 4
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biomass – biofuels generations 4
1st GENERATION
2nd GENERATION
3rd GENERATION
CORN, SOYA…
VEGE OIL
RESIDUES
LIGNOCELLULOSICS
MICRO ALGAE
4th GENERATION BIOCHEMISTRY
PETROLEUM-LIKE
HYDROPROCESS
SOLAR-TO-FUEL
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biomass (2ª G) 4
ESSENTIAL OIL
POLYPHENOLS
HEMICELLULOSE
CELLULOSE
LIGNIN
ASHES
G
R
A
P
E
S
E
E
D
< 1%
< 12-15%
< 15-25%
< 25-35%
< 35%
< 2-3%
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biomass (wood) 4
Fibbers
Glue
Structura 3D SOFTWOOD
(gimnosperms)
Manose, arabinose…
HARDWOOD (angiosperms)
xylose
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biomass 4
OO
HH
H
O
OH
H OH
H
OH
OO
HH
HOH
H OH
H
OH
n
OO
HH
H
OH
H OH
H
OH
O OH
HH
HOH
H OH
H
OH
OH
OOH
HH
H
OHOH
H OH
H
OH
Oligosaccharides
Cellobiose
Glucose
Cellulosek
OO
HH
H
OH
H OH
H
OH
O
HH
HOH
H OH
H
OH
OO
HH
H
OH
OH
H OH
H
OH
O
OH
H
HOH
H OH
H
OH
OH
F * k (1-F)*k
kh;k1;k2
kog
HEMICELLULOSE CELLULOSE LIGNIN
C5 C6 Aromatics C6
Glue Fibbers Structura 3D
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phase equilibria - water 5
HEMICELLULOSE CELLULOSE
LIGNIN
170ºC
220ºC
350ºC
7 24 165
Supercritical
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supercritical fluids - water 5
Tc=374ºC Pc=22.1 MPa
Temperature, ºC
0 100 200 300 400 500 600 700
Densi
ty, kG
m-3
0
200
400
600
800
1000
1200
Ionic
pro
duct
of
wate
r, p
Kw
10
12
14
16
18
20
22
24
Die
lect
ric
const
ant, e
0
20
40
60
80
100
Density
Kw
e
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fractionation via hydrolysis 6
Acid hydrolysis
Enzymatic hydrolysis
Dissolution and hydrolysis in ionic liquids
Hydrothermal processes
SCW processes
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fractionation via hydrolysis 6
BATCH
SEMI-CONTINUOUS
CONTINUOUS
HOURS
MINUTES
SECONDS
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fractionation – semicontinuous 6
H2O
P-01
D-01
E-02
D-02
PCV
01
PI
02
H-01
R-01
E-01
PI
01
PSV
01
Set Pres.
100 barg
D-01
H2O FEED
VESSEL
P-01
H2O FEED
PUMP
R-01
EXTRACTOR-
REACTOR
D-02
PRODUCT
VESSEL
E-02
PRODUCT
COOLER
E-01
PREHEATER
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fractionation – semicontinuous 6
SOLVENT
RESERVOIR
PUMP
REACTOR PRODUCT
VESSEL
C1
C2
Time
Instantaneous
Cumulative
Cumulative
Instantaneous
SOLVENT CONTINUOUS BIOMASS BATCH
SEMICONTINUOS MODELLING KINETICS OF THE PROCESS
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fractionation – semicontinuous 6
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22 / 22
SOLVENT
RESERVOIR
PUMP
REACTOR PRODUCT
VESSEL
C1
C2
Time
Instantaneous
Cumulative
Cumulative
Instantaneous
SOLVENT CONTINUOUS BIOMASS BATCH
SEMICONTINUOS MODELLING KINETICS OF THE PROCESS
EXPERIMENTAL PROCEDURE - SEMICONTINOUS
H2O only H2O + EtOH
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BIO-OIL PRODUCTION 23 / 22
H2O only
SR BO SG Mass
Balance
250 36% 21% 23% 80%
300 28% 26% 27% 81%
340 26% 32% 29% 86%
60 min
SOLID RESIDUE BIO-OIL SUGARS/ SOLUBILISED
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24 / 22
H2O only
BIO-OIL PRODUCTION – SIMPLE KINETICS FOR SOLID
Ea = 13850 J/mol
k0 = 0.995 g/min
Only considering the solid with zero order can be explained, however mass is needed to explain the whole.
10 mL/min
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POLYPHENOL EXTRACTION 25 / 22
H2O + EtOH
𝑚𝐺𝐴𝐸 = 𝑞 · 𝑐𝐺𝐴𝐸0 · 𝑒−𝑏·𝑡=
𝑞·𝑐𝐺𝐴𝐸0𝑏
1 − 𝑒−𝑏·𝑡 𝑡
0
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VARIATION OF pH AND ACETIC ACID FORMATION
26 / 22
H2O + EtOH 10 min 50 mL 12.5 mL/gbiomass
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C5/C6 EXTRACTION + OLIGOMERS 27 / 22
H2O + EtOH
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28 / 22
H2O + EtOH
C5/C6 EXTRACTION + OLIGOMERS
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29 / 22
H2O + EtOH
C5/C6 EXTRACTION + OLIGOMERS
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30 / 22
H2O + EtOH
C5/C6 EXTRACTION + OLIGOMERS
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CARBONIZATION SEM 31 / 22
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heat transfer 7
HEAT FLOW = ENTHALPY * FLOW
HEAT FLOW = U · S · DT
DH = Cp · DT
DH = Cp · DT + DHvap
Liquid :
Vapor-supercritical:
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HEAT INTEGRATION 33 / 22
H2O
P-01
D-01
E-02
D-02
PCV
01
PI
02
H-01
R-01
E-01
PI
01
PSV
01
Set Pres.
100 barg
D-01
H2O FEED
VESSEL
P-01
H2O FEED
PUMP
R-01
EXTRACTOR-
REACTOR
D-02
PRODUCT
VESSEL
E-02
PRODUCT
COOLER
E-01
PREHEATER
E-03
HEAT
RECOVERY
E-03
HEAT SAVINGS = 76% (high flowrate) to 82% (low flowrates)
COLD SAVINGS = 87% (high flowrate) to 98% (low flowrates)
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ultrafast - supercritical reation 8
Reactor
Cellulose
Suspension
Water
Heater
Valve
Flash
Coolers
Samples
Pressurization Heating Reaction Cooling
Max T=400ºC
Max P=40 MPa
Long.= 0.03-6 M
Flow C= 1.5 kg/h
Conc. Cel. = 10 % w/w
Water flow= 10 kg/h
Res time = 0.004 – 40 s.
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ultrafast - supercritical reation 8
Hot water
Cellulose
z=0
z
PF Reactor
Decompression
TRICK
HEAT QUICK
COOL QUICK ?
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1st step of hydrolysis: oligosaccharides
OO
HH
H
O
OH
H OH
H
OH
OO
HH
HOH
H OH
H
OH
n
OO
HH
H
OH
H OH
H
OH
O OH
HH
HOH
H OH
H
OH
OH
OOH
HH
H
OHOH
H OH
H
OH
Oligosaccharides
Cellobiose
Glucose
Cellulosek
OO
HH
H
OH
H OH
H
OH
O
HH
HOH
H OH
H
OH
OO
HH
H
OH
OH
H OH
H
OH
O
OH
H
HOH
H OH
H
OH
OH
F * k (1-F)*k
kh;k1;k2
kog
D Cantero; M D Bermejo; M J Cocero. Kinetic analysis of cellulose depolymerization
reactions in near critical water. J Supercritical Fluids,. 75 - 48, pp. 48 - 57.. 2013.
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(♦) 300ºC, (■) 350ºC and (▲) 400ºC depending on residence time, dotted
vertical lines are the residence times for total conversion at 300ºC, 350ºC and
400ºC respectively
Hydrolysis reactions selectivity
0%
10%
20%
30%
40%
50%
60%
70%
80%
90%
100%
0,001 0,01 0,1 1 10 100
Tota
l Su
gars
Sele
ctiv
ity,
Carb
on
Basi
s
Residence time, s
A
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Selectivity at 400ºC for: (▲) total soluble sugar, (■) glucose-
fructose-cellobiose, (♦) pyruvaldehyde, (●)5-hydroxy methyl
furfural, (+) Carbon Balance
Hydrolysis reactions selectivity
0%
10%
20%
30%
40%
50%
60%
70%
80%
90%
100%
0,001 0,01 0,1 1 10
Sele
ctiv
ity,
To
tal C
arb
on
Basi
s
Residence time, s
B
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OOH
HH
H
OHOH
H OH
H
OHGlucoseO OH
HH
H
OHOH
H OHOH
H
Fructose
OOOH
5 - HMF
O
OH
OHGlyceraldehyde
CH3
O
O
Pyruvaldehyde
kgf
kfgl
kglyp
kggl
CH3
OH
OH
O
CH2
OH
Okpkla
Lactic AcidAcrylic Acid
khmf
Cellulose
Oligosaccharides
Reaction Pathway
Kabyemela, B.M., et al., Industrial & Engineering Chemistry Research, 1997. 36(6): p. 2025-2030
wfhmf
w
hmfCCk
M
D
dl
dn.
2
4
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Hydrolysis products: Sugars
0%
10%
20%
30%
40%
50%
60%
0,01 0,1 1 10
Cellb
+ G
luc
+ F
ruc,
% C
Time, s
400-27
400-25
400-23
0%
10%
20%
30%
40%
50%
60%
0,1 1 10C
ello
+ G
luc
+ F
ruc,
% C
Time, s
350-18
350-23
350-27
High selectivity at lower Pressure
At 400ºC the selectivity reaches 98% if oligosaccharides are taken into account
(cellotriose + cellotetraose + cellopentaose + cellohexose)
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Hydrolysis products: Pyruvaldehyde
0%
10%
20%
30%
40%
50%
60%
1 10 100
Pyr
uva
ldehyd
e, %
C
Time, s
300-27
300-23
300-18
0%
10%
20%
30%
40%
50%
60%
0,1 1 10
Pyr
uva
ldehyd
e, %
C
Time, s
400-27
400-25
400-23
0%
10%
20%
30%
40%
50%
60%
0,1 1 10
Pyr
uva
ldehyd
e, %
C
Time, s
350-18
350-23
350-27
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Hydrolysis products: 5-HMF
0%
5%
10%
15%
20%
25%
30%
0,1 1 10
5 H
MF,
% C
Time, s
350-18
350-23
350-27
0%
5%
10%
15%
20%
25%
30%
0,1 1 10
5 H
MF,
% C
Time, s
400-27
400-25
400-23
0%
5%
10%
15%
20%
25%
30%
1 10 100
5 H
MF,
% C
Time, s
300-27
300-23
300-18
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Reaction Conditions
Temperature: 327 – 387 ºC Pressure: 30 MPa Reaction Time: 0.35 – 0.5 s
Solid-Liquid separation
Initial Effluent
Effluent after 24h
Cellulose solid
Separation of Cellulose from Lignin and Hemicellulose degradation liquid products
24 h
High purity cellulose
Cellulose purity: 89.8- 100%
wheat bagasse separation 9
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Conditions Selectivity
P Residence time (s) Catalyst / Reagent Pyruvaldehyde Lactic Acid Acrylic Acid
230 20.0 ±0.3 - 0.85 0 0.01
230 43.5±1.7 NaOH 0 0.08 0.03
270 12.1±0.1 H2O2 0.26 0 0.14
270 10.0±0.1 H2O2 0.2 0 0.01
270 10.2±0.1 H2O2 0.11 0 0.03
270 10.2±0.1 H2O2 + NaOH 0.09 0 0.02
270 40.1±0.5 H2O2 + NaOH 0 0.4 0.05
270 30.0±0.5 NaOH 0 0.05 0.01
270 33.2±0.5 H2O2 + NaOH 0 0.06 0.03
glucose conversion 9
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Pretreatment Fractionation
Hydrolysis
Rapid Hydrolysis
SOLID BIOMASS
H2O @ 450ºC
H2O
20ºC?
HEAT RECOVERY?
HEAT RECOVERY?
SUB
- C
RIT
ICA
L S
UP
ER
-
CR
ITIC
AL
optional process 10
PLANTROSE PROCESS
RENMATIX
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in a nutshell... 11
THE SWEET LIFE OF AN IDEAL GRAPE
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in a nutshell... 11
OILY LIFE OF A BIOHYDROTHERMALISED GRAPE SEED
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in a nutshell... 11
THE FORGOTTEN URBAN
TREES BEING HAIRDRESSED
Cheap
Rapid
Precise
Deacetylation occurs inside
H+ must come out
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in a nutshell... on going 11
QUANTITATIVE SIMULATION OF THE TGA
COMBINED PROCESS SUBCRITICAL + SUPERCRITICAL
EXTRACTION OF HEMICELLULOSES AT HIGH
MOLECULAR WEIGTH FROM HOLM OAK
(at Åbo Akademi, Turku)
MODELLING OF BIOMASS DEPOL. POPULATION BAL.
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GRACIAS