†
(2000 7 10 , 2000 12 4 )
Characteristics of Glucose Purification & Concentration Process Using a Ceramic Membrane
Yong-Taek Lee† and Soo-Eun Lee
College of Environment & Applied Chemistry, KyungHee University (Received 10 July 2000; accepted 4 December 2000)
() *+,- $% ./ 012. *+,3 45- , !"# 6 7689 76 , :;(retentate) 16-18<=) >?@ *+,- AB C DE2. F diafiltration- GHI JK DE !- "#L 1 bar=) 2 barM=) N @ *+, OP8 DE2. - Q&=3 cross flow- RS02 cross flow dead end flow T
@ U V WL *+, XY 02.
Abstract−The optimal conditions of glucose syrup purification & concentration(retentate) using a ceramic membrane were investigated. The effects of operating parameters on flux were investigated by changing cross flow velocity, the transmem- brane pressure(TMP) and volumetric concentration factor(VCF). The permeate flux increased with the increase of feed tem- perature, cross flow velocity and transmembrane pressure. The permeate flux abruptly decreased at 16 to 18 of VCF and it needs to be diafiltered. TMP was maintained between 1-2 bar to keep the moderate flux. Cleaning by the combination of cross flow with dead-end flow was better in the flux recovery than that by cross flow only.
Key words: Ceramic Membrane, Glucose, Transmembrane Pressure, Volumetric Concentration Factor, Diafiltration
†E-mail: yongtlee@khu.ac.kr
1.
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39 1 2001 2
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~ ÜÝZ À ±Ú Þà. J áâã ÃÊäN Ø g flux åæ r äN eç è é.
2.
2-1.
ê V dP` 95DE(dextro equivalance) ¦ ëEc SH
AB $ ìà. Dextrose equivalance(DE)h starch ( basic glucose K£ h P9 #¬. dP` ¯? í 70oC ¦
60R `F. î Hï@¦ Brixh 32-34%, suspended solids h 3.75 g/kg ð.
$ H Al2O39 ñ òÏ ÃÄÅ @ u óô Fig. 1 wõöð. Pore sizeh 0.1µm, ÷~} 2.16 m2, ò Ï # ö¤ 6 mm, 7 channel# òÏ øø SùÓ h pilot- scalS:[ORELIS 2KBX-07](France)9 ê é.
2-2.
ê H S: óP9 Fig. 2 wõöð. dP` ¯?#
¹Ph steam² 65-75oC ' é@¦ () 70oC9 - é.
Feed tank h AÎ úâ( tank -ûIh ¯?# ²
<}@ $q ü« Àe ¯? ýv þ: ÑPÿ é. ó ÍÎ Û - h 9 ä@
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¯?# ¹Ph chilled water9 s ' é. J feed * circulation 9 ¯?# «A9 x£ é@¦ crossflow velocityh 5 m/s, TMPh 1.0 2.0 bar9 - 45e(VCF)9 1
ØÄ « ÜÝZ# -9 rs !}@ (.
2-3. TMP
* N 3 N G# q <Î ÍÎ
(transmembrane pressure; TMP) . v ÍÎh ÉPÛ L flux9 h q ¹PÛ , E # w .
óô ÉP # º K/½ ÷~ } h = 1 $2 mn flux# Ú w fouling# $q W
. Q ÉP h ÷~ }. ¦ #
cake load# ( flux] ( [ .. ØÄ º ÉPh 4
P # fouling ׫ h D} äN [10].
È h h « ÍÎ ÉP ' rs outlet
valveÛ input valve9 é@¦ ÉPh óô Ìq(h -û-
-û ø óô# ~}@ w q @ z é.
2-4. 2-4-1. }
# ÃÊ system ¸K ~ ÃÄÅ !C ÷~ Aù. ¤z
# ÃÊ rs "Ið. dP`# $ ÷~ A ù. ¤z# CC ` /01, ä"# -= 9 $ 2 r NaOH# -= (s## FÆ} $[%&
é. J NaOH# OH ¹ -= s)Î# ÀFÛ ¬6=
lOä }@ NaOCl '( H é. w $
d,Iq h (="h )ù h 9 $ 2 r (=# sÎ « (S * ^+, 1
H é. - }@ ÃÊ h î # )Î
ÀF ß åæ. º S}@ Ç H r, .
2-4-2. Clean-in-place(CIP)
# ÃÊäN / x " é@¦ ÃÊ # WL
( dead zone Ö6ß Ñ rs ÃÊ cross flow Û dead end flow9 0" " é. Table 1 ÃÊäN# x 9 wõ1 î ¦ Table 2h ÃÊäN Øg ÜÝZ åæ. wõ1 î .
3.
3-1. TMP
Fig. 3 cross filtration Ï# ä é m ÉP
Fig. 2. Schematic diagram of concentration system using ceramic mem- brane.
1. Feed 4. Circulation pump
2. By-pass valve 5. Chilled water
3. Feed pump 6. Ceramic membrane
Fig. 1. Monolithic membrane module.
Table 1. Method of clean-in-place(CIP)
Process Flushing agent Operating time
Syrup recovery Desweetening Precleaning Washing Basic cleaning Washing Acid cleaning Washing
- - NaOH
- NaOH+NaOCl
- HNO3
-
5 min 15 min 10-15 min 15-20 min 25 min 25 min 15 min 20 min
Øg ÜÝZ# jF9 wõ1 2 . ÉP9 2, 3, 4 3 5 m/s 3 ¸K TMP 3 ÉP( (, ØÄ ÜÝZ( (
h ¤Ú wõöð TMP 200 kpa h 2# « Ï9 Þ
. ÍÎ # « -É b ¤z ÏCIh 4 P 3 cake # Æ} ]Á# ( h î@ ^ +k [11, 12]. Cross filtration Ï# ä Ih -ñ#
4"P ØÄ u D½C 58I¡ D½ rs () § 6g -ñ# 7 .. J 4"# ÏC -ñ# -É ò ö# ¤ # ã 8D G æ9}@ h î@ ^ +k [9]. ê q D½} ÜÝZ9 : r ÉPh
5 m/s î@ wõ;@¦ 5 m/s h ÜÝZ# (( 2# <
= %Ä º <Îe9 (k¹. v º ÉPh óô # º K/½ (kl v º K/½ ÷~ }
Ih =1 $2 fouling ׫ mn î@ >/..
3-2.
«}@ ÜÝZ À ¹P# ±Ú ! ? #¬9 %
^+k [13]. Fig. 4h ÉPÛ TMP9 « ¹P Øg dP`# fluxjF9 wõ1 2 . u ¹P( (, ØÄ flux( ( h ¤Ú Þ @¦ v b ¹P( (, ØÄ ¯?# »P Jh ?É d,Iq h A-=1# sP( ( h î [14, 15]. dP` $ ¯?#
¹P( 70oC ¤8 ¯?# C jF(dP`# @j) $
# 1 ] . ^+k . Û/ dP`# $
« ¹P9 3, ØÄ () } ~}@ flux9 (Ó
@¦ Kñ ¤e9 Ë .
3-3. (retentate) flux !
7 channel# ÃÄÅ óô dP`# fluxjF 3 TMP#
jF9 p u Øg 45e(retentate) jF9 Fig. 5 wõöð
. u 45. Øg flux# jFh TMP( (, ØÄ (
h ¤Ú ^ ð. Fig. 5 ^ A K}@ fluxh dP`# 45 ½# (Û ¸KR ØÄ ËE h ¤Ú Þ !
. J 45 ½ (, ØÄ flux( ËE m TMP9
0.1 bar /r (Ô@ fluxP ( h ¤Ú wõö
. uvw 45e(VCF)( í 18 (¸KR 9R s`)9 K¢
s flux# Ú2 uB # C( D¿y [¦ TMP( ( §ÄP fluxh § ( Ñà. v b -ñ ]Á óE# @ ÷bF @¦ 45 ½# G ¯?# »P 3 A -=1(suspended solids) (Ó = %Ä û H 9 3
÷~# H @ # ]Á(resistence of membrane) 3 e(W } lO(resistence due to irreversible fouling) mn 6h ]Á GI flux9 ËEßh î@ ÞIq [16-21].
(1)
J: flux
µ: viscosity resistance of membrane Rm: resistance of membrane
Rp: resistance due to concentration of polarization
Fig. 5 P feed?# A-=1 4P( ØÄ flux# D¿ jF ( JIð@¦ 45?# A-=1 63 g/kg A wõw
í 160 g/kg fouling «q;[22, 23]. Fig. 6 45e# ( Øg A-=1(suspended solids)# ( 2 wõ1 î î F ~ /.
Suspended solids(g/kg) = 4.5678(X)−1.0334 (2)
Xh VCF
v feed# 4P( (ÿ fouling 6K « qw mn feed# 4P9 3 ¸K h î ¤$} p~
.
Fig. 7 45e Øg fluxjF 3 TMPjF9 wõ1 Fig. 5Ûh i
J ∆P
µ(Rm+Rp) ---
= Table 2. Flux recovery depending on clean-in-place(CIP) process
Cross flow Dead-end-flow & cross flow Standard water flux 6,900 l/m2/hr(at 4 bar, 25oC, 6 mm channel)
Water flux after CIP 4,560 5,527
% 66 80
Fig. 3. Flux as a function cross-flow velocity.
Fig. 4. The effect of temperature on flux.
Fig. 5. Flux change at different concentration ratios.
39 1 2001 2
« 45e(5 ) q# fluxjFÛ TMP9 wõöq eç é. u ¸KR ¤, ØÄ flux( ËE h ¤Ú Þ
! . J 15R ¢ TMP( ( §ÄP flux( 'LM Ë E @w flux# ËE Ph Fig. 5 es u N Ñ@¡
45e 5 ¸K §ÄP flux( O8 Ç} î ^ .
î 45e( Pr9 þ Ñ ¸K ¤8 4P ( Q ¯? !û# tC(diafiltration) ¸KR É 3 ÃÊ(cleaning)
# Û Q9 h .
3-4. Diafiltration
Fig. 8 Fig. 5Û / 45e Øg dP`# fluxjFÛ TMP# j F9 ^Þ ¸KR 15R ¢ flux( D¿y RqS m diafiltration . «}@ ] =1 45?@AB
$2 2w L?p@AB å ¤8 diafiltration Pû.
u Fig. 8 wõ4 TÛ / diafiltration ¢ flux( 45e 5 # @ åæ î@ Þ « -@ S¸K rsh U t @ >/.. Û / ê°9 TV@
pilot scale ¸K 45. ØKh flux# ² TMP jF À ò òz9 WX@Õ diafiltration H Û flux ] < ¯
? Ç}@ SR 45 h ©}# {z .
4.
'Ù@ TMP, ÉP, ¯?# 4PÛ ¹P9 i ~ ÜÝZ À ±Ú C µ 3 ê Ys Þà. TMPh 1 bar 2 bar »}@ ( D½} flux9 : r ÉP h 5 m/s . ¯?# ¹P À ±Ú 70oC # ÜÝZ( 60oC Þ í 13% P § ¶ ÜÝZ9 wõöð. ÃÊ ¢ water fluxh cross flowÞ dead endÛ cross flow9 0s h î § w î
@ JIð.
Zn ¤[ÀÆçÛ ¤P# $6 Æ \E] «£@
". ¦ ¯s !^ (!)_ ËH `%.
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