scale-up issues for whole-cell biocatalytic oxidation
TRANSCRIPT
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University College London
Scale-up Issues for Whole-cell Biocatalytic Oxidation
John M Woodley
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Scale-up Issues
Scale
Productivity
Production capacity
Lab equipment Plant equipment
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Scale-up and Implementation
Exquisite (chiral) chemistry, under mild conditions but…..
• availability of biocatalysts• integration with chemistry• productivity limitations
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Productivity Limitations
• Substrate and product instability
• Substrate and product inhibition / toxicity• Biocatalyst instability• Non-natural substrate access into whole cells
and low rates of reaction
• Aqueous media• Integration with neighbouring operations
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Potential Solutions
• Auxiliary phase biocatalysis– two-liquid phase – resin
• Feed and bleed• Catalyst immobilisation• Genetic engineering• Protein engineering
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BVMO
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Model Baeyer-Villiger Reaction
O
O
H
H
O
H
H
O
+O
O2, NADPH, H+ H2O, NADP+
(-) 1(S), 5(R) 2-oxabicyclo[3.3.0]oct-6-en-3-one bicyclo[3.2.0]hept-2-en-6-one
(-) 1(R), 5(S) 3-oxabicyclo[3.3.0]oct-6-en-2-one
Alphand et al 1989 Tet Lett 30, 3663; Alphand and Furstoss 1992 J Org Chem 57, 1306
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BVMO Challenges
• Wild type host is pathogenic, contains contaminating activity and is difficult to grow
• CHMO is susceptible to oxidation and therefore unstable
• Stoichiometric quantities of NADPH are required
• Many reactions suffer from low intrinsic reaction rates and inhibition
• Reactions require molecular oxygen
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Recombinant CHMO (pQR239)
Antibiotic – AmpicillinInducer - Arabinose
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BVMO Fermentation
0 1 2 3 4 5 6Time (h)
0
20
40
60
80
100
120
140
DO
T (%
), C
ER
, OU
R
0
200
400
600
800
1000
1200
1400
0
4
8
12
16
20
Agi
tatio
n sp
eed
(rpm
)
OD
670n
m
Arabinose induction
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1. Choice of Catalyst Form
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Does protease inhibition improve
stability
Free enzyme
Does the R-WC suffer reactant or product toxicity
Is the enzyme the cause of the inhibition
R-WC
Does the R-WC have high enough
activity
Low enough contaminating
activity
Is the low activity due to the cell
barrier
Does the R-WC have high enough
stability
Is a R-WC available
Permeabilise
Is the enzyme the cause of the low
stability
Does the WT-WC suffer reactant or product toxicity
Is the enzyme the cause of the inhibition
WT-WC
Does the WT-WC have high enough
activity
Low enough contaminating
activity
Is the low activity due to the cell
barrier
Does the WT-WC have high enough
stability
Is the pathogenicityof the WT-WC
acceptable
Permeabilise
Is the enzyme the cause of the low
stability
Database of enzymes with
known reactions and e.e.
Does the homogenate have
high enough activity
Low enough contaminating
activity
Free enzyme
Purification
Does free enzyme suffer reactant or product inhibition
Is homogenate stability high
enough
Immobilisedenzyme
Protein engineering
Reactant or product inhibition
Protein engineering
Protein engineering
Loss of activity on immobilisation
Catalyst selection software
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Process options
air Fermentation+
BiocatalysisPurification
Fermentation Biocatalysis Purification
Fermentation Biocatalystpreparation Biocatalysis Purification
air
airsubstrate
substrate
substrate
air
Product
Product
Product
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• Isolation procedure and losses
• Cost of immobilisation support• Number of recycles achievable• Diffusional limitations
(Thiele modulus / Damkohler number)
• Cofactor recycle
Isolated enzyme issues
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Process Options
air Fermentation+
BiocatalysisPurification
Fermentation Biocatalysis Purificationair
airsubstrate
substrate
Product
Product
• Clean media for improved DSP
• Optimise production and use of catalyst
• Catalyst concentration independent of fermentation
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• Effects on downstream process • Side reactions and over metabolism
• Access of substrate to the enzyme• Need for molecular oxygen • Toxic effects on the host cell
Whole cell catalyst issues
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Oxidation activities of different ketones
Ketone Enzyme/Cell
Bicyclo[3.2.0]hept-2-en-6-one 1.7 4-methylcyclohexanone 1.42-hexylcyclopentanone 5.0
Enzyme Microb Technol (2003) 32 347
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Oxidation of bicyclo[3.2.0]hept-2-en-6-one
Catalyst %X %ee g/l/h g/l g/gdcw
Cell 85 98 0.55 04.5 02.6 Enzyme 100 98 0.47 11.0 0.38
• Trade off between downstream process (g/l) and fermentation (g/gdcw)
• Potential to overcome fermentation limit by recycle of immobilised enzyme
Biotechnol Prog (2002) 18 1039, Biotech Bioeng (2002) 78 489
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Scale-up issues
• Process intensity• Feed-rates of reactant / media• Rates of product removal• Robustness to cope with heterogeneity• Oxygen uptake
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2. Oxygen Supply
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Evaluation of Biocatalyst Kinetics and Stability
0
10
20
30
40
50
60
70
0 2 4 6
Ketone concentration (g.l-1)
Volu
met
ric a
ctiv
ity (U
.l-1)
OH
H
= 250 µL scale
= 1 L scale
BVMO catalysed lactone synthesis
[Doig et al (2002) Biotech. Bioeng., 80, 41]
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Product formation during reaction
Time (min)
Pro
duct
–La
cton
e (g
/L)
0
0.5
1.0
1.5
2.0
2.5
3.0
3.5
0 50 100 150 200 250
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Oxygen Supply
[Catalyst]
Rat
e Oxygen supply
Reaction
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75L scale (10 g/L dcw)
0 1 2 3 4 5 6Time (h)
0
20
40
60
80
100
120
140
DO
T (%
)
0
200
400
600
800
1000
1200
1400
0
4
8
12
16
20
Agi
tatio
n sp
eed
(rpm
)
OD
670n
m
7 8 9 100
1
2
3
4
5
6
Ket
one
/ Lac
tone
(g/L
)
biomass CHMO reaction
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75L scale (5 g/L dcw)
0 1 2 3 4 5 6Time (h)
0
20
40
60
80
100
120
140
DO
T (%
)
0
200
400
600
800
1000
1200
1400
0
4
8
12
16
20
Agi
tatio
n sp
eed
(rpm
)
OD
670n
m
0 1 2 30
1
2
3
4
5
6
Ket
one
/ Lac
tone
(g/L
)
biomass CHMO reaction
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Biomass (g/L)
Process limitationsIn
itial
Pro
duct
ion
rate
(g/L
.h)
0
1.0
2.0
3.0
6.0
4.0
5.0
max specific activity(0.65g/g.h)
0 2 4 6 8 10 12
SF/1.5L
1.5LSF75L
1.5LSF75L
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% Oxygen in air
Enriched air supplyIn
itial
Pro
duct
ion
rate
(g/L
.h)
0
1.0
2.0
3.0
6.0
4.0
5.0
0 20 40 60 80 100
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Biomass (g/L)
Process limitationsIn
itial
Pro
duct
ion
rate
(g/L
.h)
0
1.0
2.0
3.0
6.0
4.0
5.0
max specific activity(0.65g/g.h)
0 2 4 6 8 10 12
SF/1.5L
1.5LSF75L
1.5L – 10%O2
1.5L – 21%O2
1.5L – 40%O2
1.5L – 60%O2
SF75L In
crea
se in
Oxy
gen
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Whole Cell Reaction Model
Biomass concentration
Oxy
gen
dem
and
Metabolism
Metabolism+ Reaction
supplyO2
O2 limitation
O2 limitation
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Time (min)
Productivity LimitationsOxygen limitation
(Rate)Biocatalyst lifespan
(Time)
Product Inhibition(concentration)
Pro
duct
–La
cton
e (g
/L)
0
0.5
1.0
1.5
2.0
2.5
3.0
3.5
4.0
4.5
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Biocatalyst concentration
Time (min)
Pro
duct
–La
cton
e (g
/L)
0
0.5
1.0
1.5
2.0
2.5
3.0
3.5
4.0
0 100 200 300 400 500
0.2 g/L
1.0 g/L
3.0 g/L5.0 g/L
4.5
7.0 g/L
[Cel
l]
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3. Product Concentration
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O
O
O
Resin Based Reactor Concept
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air
VCYCLE
.
fixed bed of adsorbent
glycerol
biocatalyst/cell exchange
pH-sensorO -sensor2
1M H PO , 4M KOH3 4
Recycle Reactor with Fixed Bed
entry fermenter
outlet fermenter
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Oxidation of bicyclo[3.2.0]hept-2-en-6-one
Catalyst %X %ee g/l/h g/l g/gdcw
Cell 85 98 0.55 04.5 02.6 Enzyme 100 98 0.47 11.0 0.38
Cell* 100 98 1.02 20.0 3.40
• Integration with ISPR is critical
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4. Process Integration
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Bioconversion time
O2 Stability
[Product]
Prod
uct c
once
ntra
tion
[Cell]
Effect of cell concentration
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Catalyst Concentration
• Determines interaction with fermentation
• Determines what is limiting productivity in the reactor– catalyst preparation – conversion– downstream processing
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Catalyst Preparation
Fermentation Dewater Biocatalysis
Fermentation
Fermentation
Dilution Biocatalysis
Biocatalysis
Concentration
Dilution
Direct
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Catalyst Concentration Map
AB
[Catalyst] in reaction
[Catalyst]in
fermentation
ineffective
ineffective
ineffective
Expression
Dilution Concentration
Direct
A – Rate limitedB – Product / Catalyst stability limited
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Process Drivers
Catalyst Production
Conversion Downstream Processing
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Reaction profiles
AB
C
Time
[Product]
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Process Metrics
Metric Cost
g/g catalyst productiong/l/h conversiong/l downstream process
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Regime analysis
A B
[Catalyst]
Metric
Stability Product Ratelimited limited limited
Cg/g
g/l/hr
g/l
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Process Mapping
Trans I Chem E C (2002) 80 51
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CHMO Available….
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Products available….
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Productivity Targets
gproduct/L
g pro
duct/g
biom
ass
Optimise [Cell]and oxygen
100
10
1.0
0.10 5 10 15 20 25 30
ISPR
Optimise [Cell]and oxygen+ ISPR
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Conclusions
• Recombinant Escherichia coli containing CHMO – 300 L scale• Conversion using CHMO – 200 L and 50 L scale / 1 Kg• Oxygen supply – modelled and understood limitations• Product inhibition – modelled and implementation of ISPR
• Scalable process using whole cell CHMO
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Future
• Rapid methods of removing product
• Adequate means of oxygen supply
• Modelling for process analysis
• Isolation of product
• Improving stability of whole cells
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Acknowledgements
• Jenny Littlechild, Exeter, UK• John Ward, UCL, UK• Dick Janssen, Groningen, NL• Marcel Wubbolts, DSM, NL
• Giacomo Carrea, CNR Milan, IT• Roland Wohlgemuth, Sigma-Aldrich Chemie, CH• Roger Cripps, Consultant, UK• Roland Furstoss, CNRS Marseille, FR
• European Commission• BIO4-CT98-00267• QLK3-CT01-00403
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EC BVMO Programme