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Design and operation of immobilized enzyme reactors

  • Wayne H. PitcherJr.
Conference paper
Part of the Advances in Biochemical Engineering book series (ABE, volume 10)

Abstract

This review encompasses recent advances in the design and operation of immobilized enzyme reactors for industrial applications. Basic immobilized enzyme reactor engineering concepts are described as a reference point for recent innovations. Although practical examples are cited, the subject is approached from the viewpoint of reactor design and operation and the potential general applicability of new concepts or developments. Areas reviewed include reactor types, reactor performance, operating strategy, and general design and economic considererations. Most of the progress reported in this field is in the form of refinements, rather than basic innovations.

Keywords

Plug Flow Continuous Stir Tank Reactor Mass Transfer Limitation Normalize Residence Time Dispersion Number 
These keywords were added by machine and not by the authors. This process is experimental and the keywords may be updated as the learning algorithm improves.

13 Table of Symbols

am

surface area per unit volume

av

ratio of particle surface area to reactor volume

dp

particle diameter

D

substrate diffusivity

Deff

effective diffusivity=DΘ/τ

D0

bulk diffusivity

E

enzyme activity

Et

total enzyme activity

F

flow rate

Fi

initial feed rate

g

acceleration due to gravity

G

mass velocity per unit superficial bed cross section

H

number of half-lives utilization of IME

J

dimensionless group

k

turnover number

km

mass transfer coefficient

k'm

value of km for a sphere setting at its terminal velocity

kv

reaction velocity constant

K

equilibrium constant

Ki

product inhibition constant

Km

Michaelis constant

K'm

substrate inhibition constant

Kp

constant (Michaelis type for reverse reaction)

L

flat plate thickness

Lc

bed height

m

order of reaction

M

general modulus

N

number of reactors

NGa

Galileo number=d p 3 ρ(ρsρ)g/u2

NPe

Peclet number=dpu/D

NRe

Reynolds number=dpG/μ

(NRe)mf

minimum fluidization Reynolds number

NSc

Schmidt number=μ/ρD

P

product concentration

Pt

total production

r

radial distance

Rp

ratio of low to high production rate

S

substrate concentration

Sb

bulk substrate concentration

S0

initial substrate concentration

Ss

substrate concentration at catalyst surface

St

total substrate concentration if all product coverted to substrate

t

reaction time

t1/2

enzyme half life

tp

total period of time of reactor operation

u

fluid velocity

v

reaction velocity

vi

intrinsic reaction rate

Vm

kE (maximum reaction velocity)

Vs

substrate volume

W

weight of immobilized enzyme

X

(S0 − S)/S0=fractional conversion

Xe

Xt at equilibrium

Xi

St − S0/St

Xt

St − S/St

Y1

mole fraction substrate in feed

Y2

mole fraction substrate in product

z

column height, assuming film diffusion to the rate controlling step

Z

(NRe)mf/RRe

ε

void fraction

η

effectiveness factor

OL

modulus

μ

fluid viscosity

ρ

fluid density

ρs

solid density

Θ

particle internal porosity

τ

tortuosity (ratio of actual diffusion path length to straight line distance)

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Copyright information

© Springer Verlag 1978

Authors and Affiliations

  • Wayne H. PitcherJr.
    • 1
  1. 1.Corning Glass WorksCorningUSA

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