Biotechnology Advanced -...
Transcript of Biotechnology Advanced -...
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Graduate School of Engineering, Osaka UniversityGraduate School of Information Science, Osaka UniversityInternational Center for Biotechnology, Osaka University
Graduate School of Engineering, Osaka UniversityGraduate School of Information Science, Osaka UniversityInternational Center for Biotechnology, Osaka University
Biotechnology AdvancedNo. 6: Design and Operation
of Biological Reactors
Biotechnology AdvancedNo. 6: Design and Operation
of Biological Reactors
Handai Cyber University
Suteaki SHIOYA
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No. 6: Design & Operationof Biological Reactors
I. IntroductionII. ModelingIII. Optimal DesignIV. Operation
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I. Introduction
1. Industrial Production
2. BPSE for Design and Operation
3. BPSE and Modeling
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cellsubstrate
Process networkProcess datapH, DO, CO2, O2Cell conc. Sub.conc
MetaboliteMeta
objectproductivityyield
Cell-cell network
Process operationoptimizationcontrolproduction
schedulePlant design
expressiontranscription
genome
transcriptome
proteome
metabolome
metabolite
metabolic control
Object-oriented BioProcess Systems Engineering
gene
protein
Intracellular network
Measurementgrowthsubstratemetaboliteproduct
Metabolic flux analysisflux control analysis Genome information
micro arrayDNA chip2D electrophoresisLC-Massin vivo NMR
BPSE based on genome information
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Industrial BioIndustrial Bio--ProductionProductionResearch Process DevelopmentUp-stream Middle-stream Down-streamStrain preparation Bioreactor Bioreactor SeparationImprovement medium Design OperationDesign Operation Purificationby strainmutation microorganisms centrifugationgenetic eng animal cell chromatographycell fusion tissue culture distillationDNA manipulation ……..…….
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BPSE
DESIGN OPERATION
Optimization Monitoring Control
MODELING
Fig.1 Decision by BioProcess Systems Engineering
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II. Modeling
1. Mass Balance Equation 2. Batch, Fed-batch, Continuous
Reactors3. Rate Equation Model
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Classification of the modelPure culture
• Lumped parameter system (uniform-system)• Cell environmental variable level• Metabolic reaction level• Molecular reaction level
(gene expression, protein, signal transduction, transportation …)
• Distributed parameter system (Cell population system)cell cycle, age-distribution
Co-culture• Lumped• Distributed
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Cell
Phosphoenolpyruvate
Pyruvate
r2
r3
Lysine
r4
r6
NAD +ATP
NADH2
r7
r10
r9 Glucose
r1
r5
Glucose-6-phosphate
Fructose-6-phosphate
Glyceraldehyde-3-phosphate
r11
ATP
ADP
r8
61.3107
17.419.3
30.590.0
67.4215
47.3160
20.0106
9.9262.1
11.431.7
41.50
78.0322
0.0210.2
Glucose
rg 100(extracellular)
(intracellular)
Fig. Metabolic pathway
Metabolic Reaction LevelMetabolic Engineering
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Metabolic Reaction Modelr1: Glucose + ATP -> Glucose-6-phosphate r7: 3Glucose-6-phosphate -> Fructose-6-phosphate + r2: Glucose-6-phosphate -> Fructose-6-phosphate Glyceraldehyde-3-phosphate + 3CO2 + 6NADPHr3: Glucose-6-phosphate + ATP -> 2Glyceraldehyde-3-phosphate r8: Phosphoenolpyruvate + Pyruvate + 2NH3 + NADH + 3NADPH + 2 ATP r4: Glyceraldehyde-3-phosphate -> -> Lysine
Phosphoenolpyruvate +ATP +NADH r9: a Glucose + b Pyruvate + NH3 + MW/YATP ATP + c NADPH -> biomassr5: Phosphoenolpyruvate -> Pyruvate +ATP r10: O2 + 2NADH -> 2(P/O) ATPr6: Pyruvate -> 3CO2 +ATP + 14/3NADH r11: ATP -> ADP
⎥⎥⎥⎥⎥⎥⎥⎥⎥⎥⎥⎥⎥⎥⎥⎥⎥⎥⎥⎥⎥⎥⎥
⎦
⎤
⎢⎢⎢⎢⎢⎢⎢⎢⎢⎢⎢⎢⎢⎢⎢⎢⎢⎢⎢⎢⎢⎢⎢
⎣
⎡
1-000000000000000c-3-6000000
01-00000000000002-01-014/301000
001-000000000001-2(P/O)MW/YATP-2-01111-01-
0001-000000000000b-1-01-10000
00001-0000000000001-001-1000
000001-0000000000001001-200
0000001-0000000000020001-10
00000001-00000000003-00001-1
000000001-0000000010000000
0000000001-0000001-2-0000000
00000000001-00000003300000
000000000001-0001-000000000
0000000000001-000a-00000001-
00000000000001-00100000000
=E
Balancing Equation
r=[r1,r2,r3,r4,r5,r6,r7,r8,r9,r10,r11,rX,rg,ro,rc,rn,rL,rG6P,rF6P,rGAP,rPEP, rpyr,rATP,rNADH,rNADPH]T
Arc - Brm =0where,
rc=[r1,r2,r3,r4,r5,r6,r7,r8,r9,r10,r11, rn,rL]T to be calculated
rm=[rX,rg,ro,rc,rG6P,rF6P,rGAP,rPEP, rpyr,rATP,rNADH,rNADPH]T measured
Determination of Metabolic Reaction Rates
rc =(ATA)-1ATBrm
Er=0
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Network of Metabolites
Network of Genes
Network of Proteins
Physiology
Hierarchical Network Control of BioSystem
Environmental Conditions
Molecular Reaction Level
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Lactococcus lactis subsp. Lactis
L-lactate
Maltose
<Growth inhibition>
Nisin
Organic acids
Kluyveromyces marxianus
O2
CO2
<cannot assimilate>
Abu
AbuAbuAla Ala
Dhb
Dha
Dha
Ala Ala
AlaAla
AlaAla
IleIle
Ile
Leu
Leu
Abu
Pro Gly GlyLys
Lys
LysM et
GlyAsn
M et
His
His
Ser
Val
S
COOH
NH 2
Dha: Dehydroalanine Dhb: Dehydrobutyrine Aba: Am ino butyric acidAla-S-Ala: Lanthionine Aba-S-A la: β-M ethyl lanthionine
S
S
S
S
Nisin: Antimicrobial Peptide:produced by Lactococcus lactis ATCC 11454
(1) A safe and natural food preservative (GRAS)
(2) Wide range of growth inhibition spectrum for gram positive bacteria.
Interaction of microorganisms
Nisin Production by Mixed Culture
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<< Comparison of TGGE patternComparison of TGGE pattern>>FirstFirst
SecondSecond0 24 48 72 96 120 168 216144 (h)
0 5 24 48 72 96 120 168 216 (h)
In the second composting, the change of main microflora occurred faster than the first composting.
In the second composting, the change of main In the second composting, the change of main microfloramicroflora occurred faster than the first composting.occurred faster than the first composting.
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Type of reactors
Complete Stirred Tank Reactor (CSTR) Air-lift Reactor
Air
Air
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Type of operation
Batch
Fed-Batch
Continuous steady state
Vol
ume
Time
Vol
ume
Time
Vol
ume
Time
Time
cell
conc
.Time
cell
conc
.
Time
cell
conc
.
Depend on feeding type
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Mass balance equations-1
Example: CSTRPrinciple of mass balance
Accumulation = Input – Output + Generation Term
Cin
FinCoutFout
tΔ V
[m3 h-1] [m3 h-1]
[m3
]C
CSTR
• C = Cout : same concentration
• Volume change
Accumulation
ttVrtCFtCFtCtVttCttV Coutinin Δ+Δ−Δ=⋅−Δ+⋅Δ+ )()]()()()([Input Output Generation Term
[kg m-3][kg m-3]
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Mass balance equations-2
dtdVC
tVC
t=
ΔΔ
→Δlim
0)(tVrCFCF
dtdVC
Coutinin +−=
outin FFdtdV
−=
VrrCFCFFFCdtdCV
dtdVC
dtdCV
dtdVC
ccoutininoutin ++−=−+=+= )(
VrCCFdtdCV Cinin +−=∴ )(
or Cinin rCC
VF
dtdC
+−= )(
ttVrtCFtCFtCtVttCttV Coutinin Δ+Δ−Δ=⋅−Δ+⋅Δ+ )()]()()()([
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Example
X; cell concentration [kg m-3] S; substrate (glucose) concentration [kg m-3] P; product concentration [kg m-3] C: dissolved oxygen concentration [kg m-3]
SinFin S
FX, S, P
μ; growth rate[h-1]ν; specific substrate uptake rate [h-1]ρ; production rate[h-1]
t [h]
XVFXX
VF
dtdX inin )( −=+−= μμ
XSSVF
dtdS
inin ν−−= )(
PVFX
dtdP in−= ρ
)()( * CCakCCVF
dtdC
Linin −+−=
outin FFdtdV
−=
P
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XVFXX
VF
dtdX inin )( −=+−= μμ
XSSVF
dtdS
inin ν−−= )(
PVFX
dtdP in−= ρ
)()( * CCakCCVF
dtdC
Linin −+−=
outin FFdtdV
−=
0== outin FF 0,0 =≠ outin FF0≠= outin FF
if Batch Fed-Batch
Chemostat (continuous culture)
DVFin =
Δ
D1
(dilution rate), [h-1] : average retention time, [h]
Other example; tubular type reactor
CrxCu
xCD
tC
+∂∂
−∂∂
=∂∂
2
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Rate Term Model
XdtdX μ=
SKS
S
m
+=
μμ
IS
m
KSSK
S2
++=
μμ
XdtdS ν−=
μνsxY /
1=
ksx
mY
+= μ/
1
XdtdP ρ=
X)( βαμρ +=
μ
S
μ
S
Monod’s model
Luedeking-Piret modelor
Substrate inhibition
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III. Optimal Design1. Optimization
2. Static optimization
steady state
3. Dynamic optimization
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Design -Optimization-
1. Definition of optimization•Degree of freedom
Optimization Objective = economic, enviroment•cost•efficiecy
…
Steady state
J
uux Min),( ⇒J
0uxf =),(Subject todim: −nxdim: −rudim: −nf
wherestate variabledecision variable
degree of freedom = r
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2. Static optimization: Example
DVFXJ Max⇒=
0)( =−= XDdtdX μ
0)(1
/
=−+−= SSDXYdt
dSin
Sx
μ
DMaxDXJ ⇒=
)(/ SSY inSx −= μμμ =−⇒=
∂∂ )(0 SSSJ
FS
SKS
S
m
+=
μμ 2)( SKK
S
Sms +=
μμ
)/1
11(Sin
m KSD
+−= μ
• Chemostat
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Stability
XDdtdX )( −= μ
XY
SSDdtdS
Sxin
/
)( μ−−=
if MinS μμμ ≤≤)(
Equilibrium point
S
x
S 2S 1
S in wash outx = Yx/s(Sin-S)
11 : SSE =)( 1/ SSYX inSx −=
22 : SSE =)( 2/ SSYX inSx −=
inSSE =:30=X wash out (stable)
(stable)
(unstable)
D=μμ
SS1 S2 Sin
μM
μ(S)
E1
E3
E2
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3. Dynamic optimization: Example
μρ Max
0⇒= ∫
ftVXJ
• Batch or fed-batch culture (Maximum Production)
μ
ρ
μC μ1
Relationship between μ and ρ
Maximum principle
μttC tf
μC
μ1
=optμ 1μ
cμfor
for
Ctt ≤≤0
fC ttt ≤<
VXdt
dVP ρ=
Growth phase
Production phase
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IV. Operation & Control
1. Exponential Fed-batch Culture
2. Feedforward/Feedback Controller
3. Example: PHA production
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VXdt
dVX μ=
Expotential Fed-batch Culture
outSx
FSVXYdt
dVS+−= μ
/
1
FdtdV
=
0)(1
/
=−+−= SSFVXYdt
dSV outSx
μ
.const=S .const)( =Sμ )exp()( 0 tVXVX μ=
0=dtdS
SxoutSxout YStVX
YSSVXF
/
0
/
)exp()()(
μμμ=
−=
)exp(0* tVF μμ=
SxoutYSX /0 =)exp(0 tVV μ=
if
if
if
then
then
then
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Programed-controller/Feedback-compesatorsystem
Programedcontroller
Pre Compensator Bio-Plant H(x)
y Δε+
- +
+
F
ΔF yF
MRAC or PI
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Example : Maximu Production in Fed-batch culture
Co-polymerization Control of Polyhydroxyalkanoatesin Fed-batch Culture based on a Metabolic Reaction Model
Deleted based on copyright concern.
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Metabolic pathway of P(3HBMetabolic pathway of P(3HB--coco--3HV) synthesis.3HV) synthesis.
nn--PeOHPeOH MetabolismMetabolism EtOHEtOH MetabolismMetabolism
CHCH33CHCH22CHCH22CHCH22CHCH22OHOH
CHCH33COCHCOCH22COCO--SCoASCoA
CHCH33CHCH22CH(OH)CHCH(OH)CH22COCO--SCoASCoA
3HV unit3HV unit
CHCH33CHCH22OHOH
CHCH33COCO--SCoASCoACHCH33CHCH22COCHCOCH22COCO--SCoASCoA
CHCH33CH(OH)CHCH(OH)CH22COCO--SCoASCoA
3HB unit3HB unitTCA cycleTCA cycle
CHCH33CHCH22COCO--SCoASCoA
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ttff
∫∫ ρρ((VXVXRR)dt)dt MaxMaxJ =J =00
Optimal profile of Optimal profile of μμ
Growth stageGrowth stage Production stageProduction stage
μμ = = μμ maxmax
Carbon source : Carbon source : EtOHEtOH
Set point of Set point of EtOHEtOH = 0.5 g/l= 0.5 g/l
C/N = 10C/N = 10
μμ = = μμcc
Carbon sources : Carbon sources : EtOHEtOH and and PeOHPeOH
Set point of Set point of EtOHEtOH = 0.5 g/l with = 0.5 g/l with 3HV mole fraction control strategy3HV mole fraction control strategy
C/N = 50C/N = 50
Performance IndexPerformance Index
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0 10 200
20
40
60
80
100 0
5
10
0 10 200
20
40
60
80
100 0
5
10
P(3H
B-c
o-3H
V) (
g)P(
3HB
-co-
3HV
) (g)
3HV
in P
(3H
B-c
o-3H
V)
(mol
%)
3HV
in P
(3H
B-c
o-3H
V)
(mol
%)
Comparison of optimal P(3HB-co-3HV) production. Target of HV mole fraction : 35 mol %
(●▲:μmax→μc、●▲:μc)
Comparison of optimal P(3HB-co-3HV) production. Target of HV mole fraction : 35 mol %
(●▲:μmax→μc、●▲:μc)
Time (h)Time (h)
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Graduate School of Engineering, Osaka UniversityGraduate School of Information Science, Osaka UniversityInternational Center for Biotechnology, Osaka University
Graduate School of Engineering, Osaka UniversityGraduate School of Information Science, Osaka UniversityInternational Center for Biotechnology, Osaka University
Biotechnology AdvancedNo. 6: Design and Operation
of Biological Reactors
END
Biotechnology AdvancedNo. 6: Design and Operation
of Biological Reactors
END
Handai Cyber University