58778392 Simulation of Ethanol Production in Membrane Bio Reactor (1)

8/13/2019 58778392 Simulation of Ethanol Production in Membrane Bio Reactor (1)

1/35

1

Simulation of Ethanol Production in Membrane Bioreactor

Mohammad Zaid Bin Mohammad Zaini

0637425

Biotechnology Engineering e!artment

"ulliyah of Engineering

##$M

Su!er%i&or' (&&oc) Prof) r) (hmed *arig +ameel

,o-Su!er%i&or' (&&i&tant Profe&&or Profe&&or r Maan Ma.an /ahmi a&hid (l-1hatib
http://eng.iiu.edu.my/v3/main.php?th=1&id=73&showstaff=atjameelhttp://eng.iiu.edu.my/v3/main.php?th=1&id=73&showstaff=maanhttp://eng.iiu.edu.my/v3/main.php?th=1&id=73&showstaff=atjameelhttp://eng.iiu.edu.my/v3/main.php?th=1&id=73&showstaff=maan


2/35

Simulation of Ethanol Production in Membrane Bioreactor P a g e | 2

ABSTRACT

Membrane bioreactor ha& been the &ub ect of attention for %alue-added !roduct !roduction& inthe&e recent year&) Since the !ea1 of oil !rice in 2006 re&earcher ha& turn their eye& for efficient

!roducti%ity of ethanol !roduction) $ntil recently little &tudy ha& been made to !redict the micro

and heterogeneou& en%ironment of biofilm bioreactor a ty!e of membrane bioreactor for

ethanol !roduction !ur!o&e&) *he !ur!o&e of thi& &tudy i& to &imulate the !roduction of ethanol in

biofilm !ac1ed-bed bioreactor by u&ing , MS Muti!hy&ic&) *he model 8ill co%er the micro

and macro en%ironment of !ac1ed-bed bioreactor that ca!able of !redicting the ma&& and

reaction di&tribution& along the reactor and 8ithin each biofilm !ellet along the reactor length)

*he con&truction of the model 8ill u&e the ad%antage of , MS &oft8are that are able to

&imulate the &!ace-de!endent reacting &y&tem in a heterogeneou& reactor)


3/35


ACKNOWLEDGEMENT

#n the name of (llah the Mo&t Merciful and the Mo&t ,om!a&&ionate

/ir&tly # 8ould li1e to e9!re&& my dee!e&t gratitude to the (lmighty :od for ;i&

ble&&ing& # 8a& able to com!lete thi& re!ort for Pro ect < B*E 4 a& a !artial fulfillment of

the re?uirement of Bachelor of Biochemical-Biotechnology Engineering &ucce&&fully)

# 8ould li1e to ta1e thi& o!!ortunity to 8i&h million of than1& to my &u!er%i&or and co-

&u!er%i&or (&&oc) Prof) r)(hmed *arig +ameel and (&&i&tant Profe&&or Ma.an /ahmi a&hid

(l-1hatib for their !a&&ion and contribution& in guiding me and hel!ing me in any 8ay that bring

u! my !otential in the 8orld of re&earch) *heir indefinite guidance &u!!ort encouragement and

!ro%i&ion in hel!ing me throughout the !ro ect ha%e been a great contribution and moti%ation for

me)

/inally credit goe& to my familie& and friend& for their %ariou& contribution& and &u!!ort

in thi& !ro ect)

*han1 you for your hel!)
http://eng.iiu.edu.my/v3/main.php?th=1&id=73&showstaff=atjameelhttp://eng.iiu.edu.my/v3/main.php?th=1&id=73&showstaff=maanhttp://eng.iiu.edu.my/v3/main.php?th=1&id=73&showstaff=maanhttp://eng.iiu.edu.my/v3/main.php?th=1&id=73&showstaff=atjameelhttp://eng.iiu.edu.my/v3/main.php?th=1&id=73&showstaff=maanhttp://eng.iiu.edu.my/v3/main.php?th=1&id=73&showstaff=maan


4/35


CHAPTER ONE

1.0 Introduction

:lobal 8arming i& an i&&ue that ha& been long been debated but ha& yet to find it&ultimate &olution) *he i&&ue i& cau&ed by many factor& 8hich &ome of it i& &lo8ly been dealt

8ith 8hile many are left unattended) *he !artici!ation of "yoto Protocol by more than


5/35


&ignificantly lo8er the o!erating co&t&) ,a!ital co&t on the other hand may be reduced by u&ing

mechanically &im!le &mall bioreactor& 8ith high rate& of ethanol !roduction) Su!erior ethanol

!roducti%itie& may be achie%ed by em!loying a high concentration of yea&t or bacterial cell& the

cataly&t& for the ethanol !roduction reaction 8ithin the bioreactor) ;o8e%er the !roduction ofethanol u&ing con%entional continuou& !roce&&e& ha& limitation& of maintaining high cell

concentration& in the bioreactor) Such limitation& are a&&ociated 8ith lo8 %olumetric

!roducti%itie& and long fermentation time& in the&e &y&tem&) Pre&ent trend& in immobili&ed yea&t

or bacterial cell bioreactor &y&tem& no8aday& !ro%ide the ethanol indu&try 8ith a method not

only for maintaining high cell concentration& in the bioreactor& but al&o reducing !roce&&ing

time 8ithout &acrificing !roduct ?uality) Production of ethanol ha%e mainly come from a ty!ical

fermenter or bioreactor) *he focu& of the &tudy i& to &imulate ethanol !roduction in a !ac1ed-bed

biofilm bioreactor)

1.1 Eth no!

Ethyl alcohol or ethanol , 2 ; 5 ; i& a clear colorle&& li?uid 8ith a burning ta&te and

characteri&tic agreeable odor) Ethanol i& the alcohol in &uch be%erage& a& beer 8ine and

brandy) Becau&e of it& lo8 freeAing !oint it ha& been u&ed a& the fluid in thermometer& for

tem!erature& belo8 40D , 40D / the freeAing !oint of mercury and for other &!ecial

lo8tem!erature !ur!o&e &uch a& for antifreeAe in automobile radiator&)

Ethanol ha& been made &ince ancient time& by the fermentation of &ugar&) (ll be%erage

ethanol and more than half of indu&trial ethanol i& &till made by thi& !roce&&) Starch from

!otatoe& corn or other cereal& can be the ra8 material) *he yea&t enAyme Ayma&e change& the

&im!le &ugar& into ethanol and carbon dio9ide) *he fermentation reaction re!re&ented by the

&im!le e?uation

, 6;


6/35


containing from 7 to


7/35


/igure


8/35


1." C#!! I$$o%i!i& tion

*he u&e of cell immobiliAation ha& been a common laboratory !ractice 8ithin the la&t fe8

decade& a& a method to im!ro%e the !erformance and the economic& of mo&t fermentation

!roce&&e&)

1.".1 B 'ic Princi(!#'

(lthough immobiliAation techni?ue& differ 8idely the common ob ecti%e can be

&ummariAed a& an attem!t to confine the biocataly&t 8ithin the reactor &y&tem 8hile at the &ame

time allo8ing the media containing the &ub&trate and the !roduct& to flo8 in a continuou&manner) *he o%erall effect i& to tran&form a !&eudo-homogeneou& catalytic reaction C!&eudoC

referring to the &u&!en&ion of the cell& in the media into a ty!ical heterogeneou&ly cataly&ed

&y&tem)

:enerally immobili&ed cell &y&tem& can be cla&&ified into four categorie& ba&ed on the

!hy&ical mechani&m of cell locali&ation and the nature of the &u!!ort mechani&m&' Hattachment

to a &urface I Hentra!ment 8ithin a !orou& matri9 I Hcontainment behind a barrierI and H&elf

aggregationI "arel 5J @illaert and Baron


9/35


/igure 2 ,la&&ification of immobili&ed cell &y&tem& according to the !hy&ical locali&ation and the nature of

the microen%ironment @illaert and Baron


10/35


/igure 3) Ba&ic immobili&ed cell &y&tem& ada!ted from er%a1o& @ebb Ma&&chelein )

,ell immobiliAation in !orou& matrice& can be !erformed by t8o different ba&ic method&)

#n the fir&t method indicated a& gel entra!ment the !orou& matri9 i& &ynthe&i&ed in &itu around

the cell& to be immobili&ed) #n the &econd method cell& are allo8ed to mo%e into a !reformed

!orou& matri9) :enerally both method& !ro%ide cell !rotection from the fluid &hear and higher

cell den&itie& a& com!ared to &urface immobiliAation are reached) ( dra8bac1 of the&e &y&tem&

can be ma&& tran&fer limitation&) ;o8e%er under&tanding of ma&& tran&fer !henomena 8ithin

entra!ment matrice& may allo8 one to &imultaneou&ly !ro%ide different condition& at the carrier

&urface and in the interior 8hich could be attracti%e for coimmobiliAation of different cell ty!e&

!erforming con&ecuti%e !roce&&e& @illaert


11/35


*able


12/35


13/35


oy 2 of immobiliAation of actobacillu& in the &hell &ide of hollo8 fiber membrane the

e9!eriment cau&e& the fiber module to be damaged by the gro8ing cell& thu& the cell& 8ere able

to !enetrate the 8all& and contaminate the recycle %e&&el rendering long term o!eration

unfea&ible) (l&o membrane reactor cau&e& , 2 accumulation a& &aid by Mehaia ,heryan3 and !roblem in the 8a&hout)

*able 2) Selection criteria for cell immobili&ation )

uring the la&t 30 year& many different ty!e& of matrice& for immobili&ation ha%e been

de%elo!ed 8hich include& !orou& and non-!orou& !re-formed material& &uch a& 8ood chi!&

diatomaceou& earth %olcanic roc1& ceramic& &tainle&& &teel !orou& bric1 !orou& &intered or&heet gla&& !orou& &ilica E(E cellulo&e PG, chi!& !olyurethane cube& cotton cloth gla&&

fibre and !lant cell matrice&) Se%eral !olymericmatrice& ha%e been u&ed for cell immobili&ation

&uch a& ,alcium alginate 1a!!acarrageenan !olyacrylamide gelatin and e!o9y re&in agar

chito&an and &ilica &ol&) *he choice of cell-&u!!orting material for any &!ecific a!!lication

ideally &hould meet the &e%eral im!ortant criteria &ummari&ed in *able 3)

*able 3) ,riteria for &election of cell immobili&ation matrice&)


14/35



15/35


1."." Ad) nt *#' o+ C#!! I$$o%i!i& tion

*he immediate ad%antage& of cell immobiliAation come from !urely chemical reactionconce!t&' higher concentration& of biocataly&t can be achie%ed 8hich lead to a fa&ter reaction

rate and the &e!aration of the de&ired !roduct& i& more ea&ily carried out in the ab&ence or at

lo8er concentration& of chemically com!le9 &ub&tance& &uch a& cell com!onent&) ,ontinuou&

o!eration at com!arati%ely high flo8 rate& 8ithout 8a&hout of the reactor i& !o&&ible thu&

enhancing !roducti%ity) *here i& al&o &ome e%idence to indicate that bound cell &y&tem&

generally gi%e higher !roduct yield& and allo8 a better remo%al of to9ic metabolite& a& 8ell a&

freedom from nutrient de!letion)

Performance under heterogeneou& catalytic condition& can be carried out in the !lug flo8

mode a& o!!o&ed to 8ell-mi9ed &y&tem& 8hich in &ome ca&e& &uch a& ethanol fermentation

8here !roduct inhibition may be a factor lead& to a more efficient o!eration) ,om!ari&on

&tudie& are a%ailable in the literature for batch %er&u& continuou& o!eration and immobiliAed cell

reactor& %er&u& continuou& &tirred-tan1 reactor&)

1., Who!# C#!! I$$o%i!i& tion T#chni-u# Bio+i!$ / Entr ($#nt

@hole cell immobiliAation techni?ue& con&i&t of t8o ma or grou! mention earlier' entra!ment

and carrier binding) Entra!ment include& both enclo&ure of a cataly&t behind a membrane and

8ithin a gel &tructure) ,arrier binding include& all method& 8here there i& a direct binding of

cell& to 8ater-in&oluble carder& by !hy&ical ad&or!tion or by ionic andOor co%alent bond&) *he

term Cbiofilm reactorC i& u&ed here to re!re&ent a grou! of &y&tem& in 8hich gro8th ta1e& !lace

on the outer layer of a film of microorgani&m& 8hich i& in direct contact 8ith the &urrounding

medium) Potential ma&& tran&fer limitation& are al8ay& !re&ent 8ith entra!ment &y&tem& either

acro&& the gel matri9 or gel occlu&ion or acro&& the &y&tem membrane in membrane reactor&) n

the other hand the carrier binding method allo8& direct contact bet8een the fermentation broth

and the biocataly&t and the medium flo8 in and out of the &y&tem 8ithout re&triction thu&


16/35


minimiAing ma&& tran&fer !roblem&) @hile the &tart-u! of &y&tem& em!loying carrier-binding

method& i& influenced by the nature of the &u!!ort and the &!ecific techni?ue em!loyed after

&ome time of o!eration a biocataly&t film i& gro8n and common characteri&tic& to all &y&tem& are

found thu& allo8ing grou!ing a& &o-called biofilm reactor&)

1.,.1 Bio+i!$ R# ctor' Ad) nt *#' o)#r C#!! Entr ($#nt S 't#$

Biofilm reactor& !re&ent &e%eral ad%antage& o%er entra!!ed &y&tem&) /ir&t a& !ointed out

by Blac1 4 it i& highly ad%antageou& to be able to inoculate a fermentor in the normal 8ay

and to allo8 cell& to become immobiliAed &im!ly a& a con&e?uence of their gro8th) *hi&

com!are& fa%orably 8ith the re?uirement of &!ecial techni?ue& to entra! cell& into matrice& !rior

to u&e in the reactor&) Secondly gro8th i& a re?uirement for entra!!ed &y&tem& due to the lo&& of

%iability) of the cell& in the matrice& 8hich ma1e& reacti%ation 8ith richer media nece&&ary)

E%en &o &tability of &uch &y&tem& i& generally not good unle&& &ome of the biocataly&t i& re!laced

regularly) #n biofilm reactor& gro8th i& re?uired and mu&t be !romoted during &tartu!) ;o8e%er

a& &oon a& a high cell den&ity i& achie%ed it i& no longer nece&&ary to !romote cell gro8th &o

that a &a%ing& in nutrient& can be obtained) #n gel entra!ment &y&tem& the mo&t acti%e cell& are at

the gel &urface &o that agitation of the bead& in &ome in&tance& ha& led to a 50 lo&& of acti%ity

due to the lea1age of the outer layer) ther di&ad%antage& of cell entra!ment include the

re?uirement in &ome ca&e& of a continuou& &u!!ly of chemical& to maintain the hardne&& of the

bead& &uch a& ,a,#2 for ,a-(lginate matrice&26 the lac1 of &trength of &ome bead& to &tand

hydro&tatic !re&&ure& in !ac1ed bed column& and ru!ture of the matrice& due to , 2 !re&&ure)

1.,." Bio+i!$ R# ctor' Ad) nt *#' o)#r Su'(#n'ion Cu!tur#

ne 8ay to enhance the !roducti%ity of fermentation for %alue-added !roduct

!roduction& i& to increa&e the bioma&& in the bioreactor& emirci 2007 ) Biofilm reactor& &ho8

many ad%antage& o%er &u&!ended cell reactor& e&!ecially in their higher bioma&& den&ity and

o!eration &tability) Biofilm reactor& can retain fi%e to ten time& more bioma&& !er unit %olume


17/35


8hen com!ared to &u&!ended reactor& 8hich contribute& to the increa&e of !roduction rate&

reduction of 8a&hing out ri&1 8hen conducting a continuou& fermentation at high dilution rate

and elimination of the need for reinoculation during re!eated-batch fermentation /u1uda


18/35


#t ha& been noted that a mi9ed culture en%ironment in the reactor &omeho8 !ro%ed to be

more efficient in term of !roducti%ity for &ome mi9ture of microorgani&m 8herea& !ro%ed

other8i&e for other&) "unduru and Pometto


19/35


*he !ac1ed bed reactor i& one of the mo&t common reactor& in the chemical indu&try for

u&e in heterogeneou& catalytic !roce&&e&) #n e&&ence the reactor con&i&t& of a container filled

8ith cataly&t !article&) *he&e !article& can be contained 8ithin a &u!!orting &tructure li1e tube&

or channel& or they can be !ac1ed in one &ingle com!artment in the reactor)

*he &tructure that i& formatted by the !ac1ed cataly&t !article& ma1e& the modeling of

ma&& and energy tran&!ort in the reactor a challenging ta&1) *he difficulty lie& in the de&cri!tion

of the !orou& &tructure 8hich gi%e& tran&!ort of different order& of magnitude& 8ithin the

!article& and bet8een the !article&) #n mo&t ca&e& the &tructure in bet8een !article& i& de&cribed

a& macro!orou& and the !article radiu& can be of the order of magnitude of < mm) @hen a

!re&&ure difference i& a!!lied acro&& the bed con%ection ari&e in the macro!ore&) *he !ore&

in&ide the cataly&t !article& form the micro&tructure of the bed) *he !ore radiu& in the !article& i&

often bet8een one and ten micrometer)


20/35


CHAPTER TWO

".1 Pro%!#$ St t#$#nt

,urrently there i& little &tudy on the heteregenou& en%ironment of biofilm !ac1ed-bed

bioreactor) #n addition the model that co%er& tho&e a&!ect for ethanol !roduction ha& yet to be

con&truct)

"." O%5#cti)#'

*he model mu&t &er%e many !ur!o&e&J initially it 8ill hel! to determine reaction rate&

!roduction rate gro8th rate and other !arameter& by correlating analytical !rediction& 8ith

e9!erimental data)

nce the !hy&ical con&tant& of the &y&tem are better under&tood the model 8ill function

to !redict the o!erating beha%ior of current de&ign& under different o!erating condition&) /inally

the model 8ill be u&ed to o!timiAe future de&ign&)

/or the !ac1ed-bed reactor en%ironment u&ing a multigeometry a!!roach the model

!ro%ide& the ma&& and reaction di&tribution& along the reactor and 8ithin each cataly&t !ellet

along the reactor length) *hi& ma1e& it !o&&ible to e%aluate the utiliAation of biofilm &tartu!

o!timal !ellet &iAe or inlet tem!erature)

/or u&tification the !ro ected model 8ill be com!are to an e9i&ting model or re&ult from

e9!erimental data) #n addition to that the !ro ected model 8ill be com!are 8ith other &oft8arenamely Matlab Ber1eley Madonna)


21/35


CHAPTER THREE

,.0 M#thodo!o*

*o !redict a !ac1ed-bed biofilm en%ironment t8o model& 8ill be con&tructed'

a) Biofilm !ac1ed-bed model u&ing , MS Multi!hy&ic& 3)5' *o !redict the ma&& and

reaction di&tribution& along the reactor and 8ithin each cataly&t !ellet along the reactor

length) b eacting &y&tem model u&ing , MS eaction Engineering ab


22/35


,.1 Bio+i!$ P c3#d4%#d Mod#! u'in* COMSOL Mu!ti(h 'ic' ,.2

,.1.1 6!o7 Ch rt

ModelDefinition

AddGeometry

Add Ma !ran "ortMode

Add PD#Mode

GenerateMe $

GeometryModeling

%om"&tingt$e

Po t"ro(e ing


23/35


,.1." Mod#! D#+inition

Since , MS already !ro%ided a modeling e9am!le of a !ac1ed-bed bioreactor the

!rocedure that define the model can be &et a& e9am!le but it i& &ub ected to future modification

to &ati&fy the biofilm !ellet condition)

*he !rocedure done by , MS i& a& follo8&'

8hereby the r9 de&cribe the cell formation rate r!

de&cribe the ethanol formation rate r& de&cribe the &ub&trate u!ta1e rate&'

8here f P and f ' P are the ethanol inhibition relation&hi!&) *he e?uation& need to be

modify to &ati&fy the heterogeneou& en%ironment)

3, efining the rate and ad&or!tion con&tant from (rrheniu& e9!re&&ion&)

8here ( i& acti%ating energy +Omol and E i& the fre?uency factor&)


24/35


4, ,alculating the !re&&ure dro! in the reactor i& de&cribed by the Ergun e?uation

8here P i& the !re&&ure 1Pa Q the !oro&ity D p the !article diameter m R denote& the

ga& %i&co&ity 1gO m & T the ga& den&ity 1gOm3 and x the reactor length m ) u i& the

reactor flo8 %elocity mO& that de!end& on the !re&&ure dro! according to

8here ufeed i& the inlet %elocity and C the total concentration molOm 3 )

5, efining the ma&& tran&!ort in the reactor i& gi%en by the con%ection and diffu&ion

e?uation

8here D i& the diffu&ion coefficient m 2O& and R i& a &ource term molO m3 & ) *he

e?uation need& to be &ol%ed for all &!ecie& !artici!ating)

6) ,alculate the from ma&& balance e?uation'

;ere D !c i& the effecti%e diffu&ion coefficient in the !article c ! i& the concentration in the

!article and R ! i& the reaction rate for the heterogeneou& reaction in the !article) #n the

biofilm !ore& tran&!ort ta1e& !alace by diffu&ion only)


25/35


Becau&e the !ellet i& &!herical the e?uation become&

8here r m i& the inde!endent %ariable for the !o&ition along the radiu& of the !article)

7, efining the boundary condition& of the !article'

8here U denote& the !oro&ity of the !article and c and c ! re!re&ent the &!ecie&

concentration&) *hi& im!lie& &ymmetry at the center of the !article)

,.1., Th# Ph 'ic' S#ttin*

*he &ubdomain and boundary condition of e%ery mode add of e%ery &!ecie& in%ol%e in

the reaction& ha%e to be in!ut'

1. Subdomain SettingsConvection and Diffusion

2. Boundary ConditionsConvection and Diffusion

. Subdomain SettingsPD!" Coefficient #orm

$. Boundary ConditionsPD!" %enera& #orm


26/35


,." R# ctin* S 't#$ Mod#! 8'in* COMSOL R# ction En*in##rin* L % 1.2

,.".1 6!o7 Ch rt

*he flo8 chart re!re&ent& the &trategy &ugge&t by , MS eaction Engineering ab


27/35


,."." Th# Mod#!in* Proc#dur# +or Bio+i!$ Bior# ctor S 't#$

Since the &y&tem i& heterogeneou& &y&tem thu& it i& a S!ace- e!endent eacting

Sy&tem&' 8ith Garying *em!erature in *ime) *he modeling !rocedure according to , MS in

the eaction Engineering ab i&'

1

) Start , MS eaction Engineering ab)

"

) Select the ty!e of fluid and acti%ate the energy balance)

,

) Set u! a ne8 reaction and enter the e9!re&&ion for the reaction de&cribed)

) Set the initial concentration&)

2

) Set the thermodynamic !ro!ertie&)

9

) Set the tran&!ort !ro!ertie&)

:

) E9!ort to the ,hemical Engineering Module)

;

) Set the boundary condition& and com!ute the &olution in , MS Multi!hy&ic&)

#n order to !erform the e9!ort &te! in the modeling !rocedure you need &ome data to calculatethe &y&temV& tran&!ort !ro!ertie&'


28/35



29/35


CHAPTER 6O8R

E=(#ct#d r#'u!t'

*he benchmar1 of the re&ult can be the re&ult from the e9am!le of the !ac1ed-bed reactor

model !ro%ided by , MS team'

/igure 5' *he concentration of reactant& and !roduct& along the reactor length) *he !ellet radiu& r p i&

2)5mm)


30/35


/igure 6' *he concentration of in-!ellet , a& function of reactor !o&ition) *he &caled !ellet radiu& i& gi%en

on the r-a9i& and the reactor !o&ition along the 9-a9i&)


31/35


)

/igure >-7=' *he concentration of in-!ellet , 3; 6 at three different reactor !o&ition& 5


32/35


CHAPTER 6I>E

Conc!u'ion / R#cco$#nd tion'

*hi& !reliminary &tudy for &imulating biofilm !ac1ed-bed bioreactor for ethanol

!roduction ha& achie%ed it& !ur!o&e) /rom the !a&t re&earch of cell immobiliAation techni?ue it

ha& &ho8n that biofilm !ro%e& to be the &uitable &y&tem for anaerobic fermentation) (nd it ha&

been &ugge&ted that !ac1ed-bed i& the &uitable method for ethanol 8hich de&cribe !roduct

inhibition) Biofilm !o&e a heterogeneou& catalytic condition& can be carried out in the !lug flo8

mode a& o!!o&ed to 8ell-mi9ed &y&tem& lead& to a more efficient o!eration)

*he fle9ibility of , MS &oft8are i& ca!able to achie%e the target ob ecti%e&) Pre%iou&

&imulation re&earch ha& !ro%e that , MS ha& the ca!ability to con&truct com!rehen&i%e

model of heterogeneou& catalytic condition& of biofilm !ac1ed-bed bioreactor that co%er the

S!ace- e!endent eacting Sy&tem&)


33/35


RE6ERENCES

;or%ath B) E) = Mammalian cell culture &caleu!' i& bigger betterW Bio*echnology 7 46>-46=)

*);) Par1 and #);) "im ;ollo8-fiber fermenter u&ing ultrafiltration (!!l) Microb) Biotechnol)

22


34/35


"unduru M Pometto ( ###


35/35


aymond M, Neufeld + Poncelet 2004 Enca!&ulation of bre8ing yea&t in chito&an coated

carrageenan micro&!here& by emul&ificationOtermal gelation) (rtif ,ell& Blood Sub&tit

#mobil Biotechnol 32'275K2=

58778392 Simulation of Ethanol Production in Membrane Bio Reactor (1)

Documents

Transcript of 58778392 Simulation of Ethanol Production in Membrane Bio Reactor (1)