Optimising Refined Bleached Deodorized Palm Stearin For Its Crude Stearic Acid Iodine Value To Provide The Stable Specification Of Blended Stearic Acid Distillate Iodine Value

32S

Vd.s Nog (SeP.2012)

lsst\t @7+6846

lndian Journal of Science and Technology

optimisins refined breached d"egdoriz. end"P,"liH:T'JlJ:;,':'".'#iill,f,::ff'fJ?:',ffivarue to provide the stabre

Departmentof

Muhammad vusuf ditong a

chemicatEngineering,

ru"rti'iiEiginiilrg, u.niviiiiyotsumatera
yusufrit@gmail.com

.
utara'

M,e,d,-a-n

240n1i5rE5'

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specJon 0-175 g/100 g'

: Distillation, lodine value, Bottom flash distiller

lntroduction Brended

stearic

acid

dist*rate

(BSAD)

contains -60 o/o
-4oo/owrw

il
maximum

standard, Distillate, Feed ca

-oi-
esnu
uy using

tv specs)
the. same

which is produce lv (0'80 9/100 g) <

:*tt,;,::,j *l'nil'"il;t-ht eH::I**i, g::*"il.lfiI'fliil"HSRBD,.FoA"c. relll;;a;;s," L- Tl;ivfo.ll;ri)t" o"'wocaRcBccopoBBscforr/crNSoBoorvwfom2eF41msS3t6ofhou_rAw.eDa.m,tDodraAeTrsTipDteraepdefpuiaaapDorlhcdsnveobcrie,pbsPMopcneiLS,tsreLrcycaiFetairlroiOiiyraittonsousdowatlereirbommtcuitaolnowmimtnaoedhs.mtruhealercnfiyrieitneutupccVentifiiTmiiiiwccsigscrtgdrsccoah.iisApeshancthecaAssAcoAiiocitArcrrp(!gaio,tendurcioyotccicicf?tcdcedenfiniiom1idirdbiagdodtqsdicamdad7;suyteunupHsptn:Hb(cpniisaeRticat'oSeoroiaeSei3,orts1re"fiisRibidBy5trtLoo"'5DlfriiyCCrmotCa;CCBvcCd-*eiifHDoi;r'rtmB'eoLprbDtieniuaspr"+sonsc3"loiotao-ppSspb,lrotl[zi,1elHoieit,es8"uS"-rilsArncvglfo"RcsaF-teoDIg*eirotobsRptA;olor"ei,rrfd;o,B(*a"icHainrbiMn;notcon:c"-o"Dioh;ournol10:,o0ut0duo;o0n,e21Pbre':rsprhdrmolislrcaSe'n)e.dra*tsJuoa'rs,onootFanerm,oao.ih'odccs;liA,irwn"w""frtmo2ei)'evni;h"SaXBtepsuwi'uosa,acGnic"nRors,gres,qdnlorh.i-udgb.urB.ot,n.,vir4/o-n2+d"ioouD;5ee'd2ig0i16i0iir6Dt;rw7""-ri7;,rPr.ur.i.J1ir.0+*j31,"U"eii.a(o2'li4t1auSi9""w"9JBL9iIiloifaivo0loiFfri)",nt";uSei.r''iu)iAnz"igironsiB'uca;eeBA7t:,orT-vt"rdrtfrtfi"D"a.r-hf-tet;.Sp-t"ooRevu''c=ehitr5HBtc".i.rt"r-,ieD-iSJnt.ar.r.re:,Poti"nn"so-eo9Sor/5.4ao01=70."w.IobH*1pa!3.r.Bn.'hr*on41atv'=2.plv/r,orwl".qsysnwiiu;arvsog'sov1"ot=R*dnbrarthsrdoluaaYnniJ"Jerele.!tBetr^os,rii*u':;J"arii"'.isiydro*Diis-t.ii."tu,iifnwau,i*uoeop"t'l"r"p'oi;rii.dZtsn"i0otnirs"-rori[;Ihtrriii,tj""ir'hnJ-iteei"tiuO"i-i;nyaea'ninuott"i"dt;lRii.nreg'd"i"]df""ro"1tgd-tiiopuiiato"ra''i'rAt*nihi"y?tqni.tiX'nsnroiom"pralobtlr'ih"d],'teai"r'-('Je"e'iivoin;e#il;sgePSiit-'t'-etomrTmtto';i"nviiptftin"i"ipe:nno'oft0eeo""trr'hipmIrOie!"wtouuv,ypunrtieeetan:t!c'tt.irssr,nli-r-shr,-otioJaodDxoRswBqri't'a*cveou,entp.cha,eciueotoowc"'aSeac,mndtfn(toe".ado'imbiqhPlrr.a-"dictdl-altgrttlYaed^,ouudeh,ii-iprqa2ioat1eteos1trifo.rey:here)hsaotunrt,.b0ttIn,trshe,Jxaldt'ihsls1lai2cVtlhhltccdz.ruhiaxwtteytina01eivli5baoeeeeo1oaiaisxte0ng(ntnnmiaaf0a'dd:9Ymlr,to"4hhe;id?oeiaHntvnr9sn;pmu)"ied2Palepoaglwdbt,eS0bsrslr0raYsteihoaraetduos)uiaRht0tpecam'evrh'wctw#lhce'chTfacshh5mneBaiYbr'owro"taueiitheh,s)rocaeiiaDo:me,2'uultciumrst!iiuld,lwihtnfltsS0lePalc9Eha1TsmdyHgapBwi1iBobhbetS9el^onl0:whnSeLllreS0Teb'SyalafFtecf-'aenaRrert8t)eAr.itn"ASs5oAmihcr's.shlrnBet0DiHertnwdi'lgDRfe"1Bhf5iahiVgDeoduhnaa'uo:eBtal9?nwuapJf,Peltowelmsttr'ayt/sh(sDorvvlnctlp,1ah,SioTYtieytBrneneHh'adtP0"istmd:?F:rlBqid/?nSyobelomJg0hteuSuTt^AoSauoaw?lrAoncrc€ilhc;tczt''tlti'Ir

:'ffi i; n"J *uv for getti'ng the in specs of BSAD in the
normal Production cYcle'

i-.,,,riii"s or impurities that's so
ir"tin""o;u"un i""t".t"d from

sensitive to oxidation
RBDPS to a cenain k

llY.Rt

lMta* bft r-Uytt E,r rdin ad ExvirqnErf GSe)

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-7 w7

lndian Journal of Science and Technology

5 2012)Vd. r.b. 9 (Sep.

lSSilt Cs74 6846

It is so suitable to produce BSAD through hydrolysis, BSAD relatively. The temperature had to be reduced so

hydrogenation and distillation. lmpurities reduction that lV will be relatively low. This was also based on the (includes unsaturated bondl of the crude fatty acid down grade acceleration of fatty acid that was affected by

(SRBDPSFA) can reduce fatty acid color and lV through temperature (Brocmann et al., 1987; Ketaren, 2008).

fatty acid hydrogenation (Robert, 1990). The experience

The providing was done by recycling lhe rubber

shows on the specific conditions, distillation process also

separated the impurities to a certain level so that the

grade distillare to the drier as the other big potential to
increase BSAD lV, besides CFAF lV and distillation

amount of unsaturated bond (indicated by lV) will be procqss conditions (the present distillation facility or Feld

lower and better. So hydrogenated SRBDPSFA feed and Hanh style) (PT. XXX, 2005). ln this research, it will

could reduce BSAD' lt/ also through distillation and/or be separated as a byproduct of rubber grade distillate to

fractional distillation. By using of this HSRBDPSFA,
reduction of HSRBDPSFAIV and optimization of
distillation process conditions which is done in this

separate bigger the impurities of BSAD to obtain lower lV.
See Fig. 1 (the modified Feld and Hanh style). Based on this fact, it's supposed that feed lV wasn't

research can reduce unsaturated bond or obtain lower suitable yet to produce BSAD as its quality standard of lV

and more stable arnount of unsaturated bond or BSAD lV (0.2 9i100 g) and itwas stable. lt has to be studied. The

according to BSAD
According to

lV quality standard.
the practical experiences

in

oleo

distillation operating conditions weren't optimum also. For this, light end yield will be kept constant on the range 1.5 -

chemical industry, crude fatty acid of HSRBDPSFA contains impurities such as; a trace of caproic acid
(CsHllCOOH) or C6, caprylic acid (C7H15, COOH) or Cs
and capric acid (C1gH21COOH) or C16. The light end
composition of the first fractionation column of distillation

3% so that BSAD yield will be higher and closer to 93.0 %

(as a normal specific yield of BSAD which could be
obtained practically). To study, the feed capacity will be optimized above 5 ton/hour and BFD temperature will be set until finding new optimum point on the new optimum

showed this fact. These lower fractions are easier to operating conditions of distillation.

oxidize and have bigger potential to form double bond or
increase the iodine value of fatty acid which is being purified (Nur & Septin, 2006; Yusuf, 2010). The other
impurities in crude fatty acid are hydrocarbons,
aldehydes, ketones, sterols, phosphatides, glycerol and

Variables cr (zraoc)

Table 2. Steps of the research

al (F=s,50)

a2 ( F= 5,75 )

br1o,z1

bz(o,o)

br1o,z1

bz1o,o1

XXXX

a3(F=6,0)

br 10,21
x

bz1o,o)
X

un-hydrolyzed RBDPS which also have big potential to increase the lV of fatty acid according to their chemical properties (Ketaren, 2008). The lower the impurities in

cz (zzooc)

xX X XXx
X X X XXX

fatty acid are, the better the fatty acid quality is or the

X X X XXX

bigger the impurities can be separated, lhe better the

fatty acid quality is.

lmpurities of crude fatty acid feed (CFAF) can be separated through distillation process to improve lV of

fatty acid distillate. The impurities such as: fatty acid (<

C12) and C14, hydrocarbons, aldehydes and ketones are

separated as the light end fraction (low boilers) in the first

fractionation column and

sterols, phosphatides,

the other glycerol

impurities such as:
and un-hydrolyzed

triglyceride is separated as heavy fraction (high boilers)

or residue (Brocmann et al., 1981).lt can be also applied

to purify CFAF of HSRBDPSFA.

Providing the BSAD with the same quality standard

as before had been done by increasing light fraction until

5 % of feed capacity, together with increasing precut

column temperature unde;' vacuum pressure to remove

more the impurities, such as color bodies, fatty acids that

are lower than lauric acid (CrrHzaCCOH) or C12, myristic
acid (CrsHzTCOOH) or C1a, hydrocarbons, aldehydes

and/or ketones of HSRBDPSFA (that are sensitive to

color changing which cause it to be darker and increase the lV of fatty acid). lt's follorred by reducing BSAD yield
until 85% (desired higher). The increasing of precut column temperature affected the increasing of BFD temperature and so it was potential to increase lV of

cg {zzzoc)

XX XXXx

Method

The raw material HSRBDPSFA was produced by
hydrogenation of SRBDPS from Splitting Plant

(SRBDPFA was produced by hydrolysis of RBDPS) in

PT. XXX's facility. The raw material HSRBDPSFA was

used as crude
purified on

fatty
the

ascaidmfeeedp. llat wnat ssoitbetaionefd

and will be
the same

manufacturer's facility. Medium pressure steam (11 bars)

was used to perform vacuum pressure and oil thermal

heater was used to heat up fatty acid in order to purify it

and to produce BSAD.

The research was done by factorial method with 3

independent variables: feed rate (F) at level of 5.5; 5'75
and 6.0 ton/hour, feed lodine Value (lV) at level of 0.7

and 0.6 g/100 g and bottom temperature of flash distiller

(B FD) at 218, 220 and222'C (5 mbar). Factorial method
was designed by constant modet 3 x 2 x 3 and was

repeated 2 times for each factor and BSAD lV was one c'

the quality parameter which was observed. Statistj-i

:analysis was performed by Minitab Release -14 soft"'a'e
(Nur & Septin, 2006). Samples were analyzed e'ie"..
-hours which amounts were 100 ml of ligltt fract:cr :.:':
of BSAD and 100 ml of residue acid. Analysis !'::s:--=

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71

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-,3,an Joumal of Science and Technology

,"f-*\
W

?98
Vd.s M.9 (Sep. 2012) lssr\t 09746846

Tab/e 3. h|teans of the BSAD lV as e{fect of three optimized

No

F, ton/ hour

lV,g/1009

1 5,5

0.7

BFD, CO
218 220 222

BSAD IV, g/1 00 g
0.150 0.1 60 0,1 70

dEosvvsoifaayfsfermrtois_riaaicqnbbbtbuuolfoeloatleifsroro.epnstfh,Srtotaeo*ekctsteoeFbttss*iheaslsVetntwhvrcdisseeea,sentridhgniitnlreknuattieitilfsnw-eircstadiaeq-ocenriustagci-oc-reasietniyriioeet.mbnrs,btsbefnolt*oetZ"f"wvljsnrf"eerriJle,-seo'leaynodftintifostbOmwFtoho.wonfipsuiov4tokhan,p,6rri.rlisyVaopumncsqaecoounesfrm_eeds.

f0y218

0.145

0.05.

0.6

220 222

0.1 55 0.1 60

effect

significance of the optimbed
on the BSAD iodine vaiue

process

variables

soouarsecaeip1Rct(ssm2tr2tamrt41reeeheolo3ft,'e2bm1SmsetsohnGcrwtiultTrew/hdpepehT2h'T0wlhImoht'ueoerssosbhheocdaesre"drsu3obasreeasSsuCae6rt5b=tatvtTdro)tnu,fcue,,ceo;dry0aur7ggid.vrerhpsoFm0;sro5rebea3cstsiru1dnairrerFiraels-,-ilt(oxleebaoteeoialBss6bffactslfmr2e4ierizotpcsaeFcrlsp,pnoxorrehthdrrDoebeeuTTaewse13s-osr)raseDsanca,asauefpb=btsuaaana0tr0le0airhB0/surtuletsnar.see.ls.o.6.vp7cyFr6rt,z7dt,ti4ceeaav4yihsspD,oalwlo..Virslw'e,3edeniloaeniBBiuwT(Br-elesarirf.lttmSs"TBhdisertlSSofypbhAec=1lfe.nsraneAz.reDieeAA)AnsereemsDaev'DhonstodsdybVpDtaTbf^tsbmeaeairaw1/aftluot2Vti2V22e2atpV22sa2i229ra2/2bbors2iav222^12t2e1se21it2e01teil2onr(a2i02-0h80n2(8ie8dti0Vd8o:oadDselntDe^iicLnnhMd3dl-taoci2vi-vao-r".iea_ionbaotrlnenwtgTveiaiibytvmio-fuanutn/htiameuihlaekmdCe0n'pdibmslensey,arF,0penc.e0,0s00e00"n00R00200or.A2o,i.,p,,if..1f,.f1eos,..1e111"111111iafga;i0F*ue877o6n60e765ia6rb77ae6)ncr05509oc5g5"sn50a000r0lrratt|dni;et""o"iaDt6"r6o;ns'uao,rJa;)deit)gi;)fd;leapt.sn;r.iilyfe0i0iTtvpclinslbrhsbVnllE.oirs.aaaFlB=fin(vbf1(gh1cyVe"ePewiiibarTfDaigtiFSr6rti9o,io5cefee0ltsuaetuTTarne"Taeii4Ainnhawdr.6oigrhrcrbal(a0bihrahvcs^e1ePefT"uD!6..ldr5si,5tbltlerhcee2te=ecea96"essnihr6),lotsn1rnosa.uoaise7pe,ooiaoeafVi/oohpiwenn4j'st9m,nu0fg,trofteno.ailgfthc,risn1)w-oJ,gnoefm"pwe,o,lF0oree/iOO(j-now1=reg*G1.aPsdnii1Flinsicc.ngnt-vsz]tg9anpuec0ueope_0ht0shaastris.tnt9litfr0Bshi)t(oart3fi,"fthfimAloamoip,psg6iimeouuAcnieoBtcSl.,ec"ceBDgng7oBcnfareg-anDioAti-n>tBgzolitibsa,onsr'.onhfFiD,sa'F)aoiFSne;p,cof,n6;Veiou5VFDituwncDiDiAriegorifl=lfoo.;anatg.oriVved.oD;htur"(encoc'tt;i=ifrppsn0iErheAeii(ettalsa,"aeFiptool,nfoe-."esiOo;Vgs;0'n.mai,triro;"s""im"_taioni.;0.nfnvdn'"aO'-oi.teFii0i"n.narozao0fraSgglS"ut"lf=c5d.g"oe,svu)ihinfJat1aahnrzo6e.ardifoeeae0gi7s4ctnae7lf"V.tfuc=.nsvmwf,iDn0ih.t5amns00nitya.FcmnaitTe5t1aeFeopfgyrgsi6aittintc0hSifsneocto0oasaaaii-f3rgariense,tiiiof)"-nnoob;nensisadbil3A,cnn"tft/n/l*oe*vdttfheiohht,r*dfga,"f/a"s1onfee9esiehovdot"if'Mnpri4pr-os=cnogeoBluaiul/w"idaioJft(vdtn1dun=syrrleaSiiobidpoinhiaisrio's,ti-dSla0ruOAf-tliggstoBcriioeilsiiuifbcBiScsroimn0zrD"*t,indSassaewel]haA"coOeSAseZiiinrs,Ananosghnziofdlna.ArsDlSgDnVcehsw,envaDtnbrlDntoi)leoVaadianFhennte,flpviwwVBwoilffagr,gI)ucafrniptmfaVesiV.cwSoHn.iVnsaenilt,TnueoncatdnchaA-nTehaeottehjtfd,e(oniiii:iterthhDesnnpns.)tyn,lesicBlolady",eesaBoVtsesti

ffi It r ii r I "" I ' ;;;l i":?:x'.?*lJrfr?t?;iriiVaria-t"io"n"

F

DK JK

kt

-"a 0,0001256 0,0006028

IV 1 0,000278 0,0002778

i FD ,BFD i o,oF-IV

a

o0,,0o01o2r7r2rz2
i_

I

0,00063G1

2 0,00000s6 0,0000028

i8fi*jxF*BFD

4 0,0000778 0,00001 94

I
I

IV.-BBFFDD |

22 i 0,,0000000005656 0o,0,0o0o00o28A

t jF*IV-BFD 4 0,0000111 0,0000028

Itr anova
18,08 8,33 19,08 0,08 0,58 0,08 0,08

Ib anova

Remark

0.000 0.01 0 0.000 0.920 0.679 0.920 0.986

Significant Significant Significant Not significant Not significant Not significant Not significant

from F of 5.5 kg/hour to 5.75

ks/hour ana O.6OOOO6 g from F S.75 kg/hour

9/100 to 6.0

kg/hour. The averaoe vatue

1,r",J3i,.J""i3,,
g/1 00 g.
This is easy to

Hl,"J;,S,.r,"?u"",,."",'..,tI

rError
T,ootarla,

t35i I18 0,0006000 0,0000333 ,tr

impurities which were
r_l;l:ffi:::r:I,",35?,",Y;,,iT

Research artide
(isee)@lrdian Societyfcr E L€atimand Fvirryrrerd
72

frtto,ffiffiT*

tuly.Ritorga lndianJ.$i.Td"nd.

lndii
I
iLt-l
ft--,-
lI :
:
iIi N-r.
lz
I
I
LI r
impur condi had g
T and tl can b The e BSAt
TI CAUSE
reduc Separi same CFAF condit lV car lower
Table
2
J
1
R*eth
a lrdan S 73

w.
lndian Journal of Science and Technology

-7 gg Vd.s hlo.g (Sep. 2012) lSSilt g/46846

1€

ESS

Table 5. The average vatues of BSAD lV as the e{fect of the main factors The average value of BSAD lV, g/1 00 g

contrary.
The effect of the increasing BFD is significant on the increasing BSAD lV.

No F=5.5Vh

F = 5.75 Vh

F=6.0Uh

1 0.1 56667

0.164167

0"170833

ate lV =0.6 g/100 g

lV =0.7 g/100 g

)ce. d= 2 0.161 1 1 1

0.1 66667

B FD, 218"C B FD,22OOC

BFD,222"C

l)tt. e>-

3 0.155833

0.1 65833

0.1 70000

This can be explained as follows: the
increasing in B FD causes blended

stearic acid with
and condense

higher
more

lV to evaporate
at the same

conditions. This was supported by the

average BSAD lV (Table 3). At bigger B FD, BSAD with relatively higher lV was

produced.

Note: t/h (ton/hour).

nce
ESS

Tabte 6. The average increasing of BSAD lV as the effect of the main variables.

Based on the average of BSAD lV above, the effect of the optimized main

l-rat lDa

The average value of BSAD lV, o/1 00 q
No F =5.5-5.75 Vh F=5.75 -6.0 V hr

The overall average increasing of BSAD lV, g/100 s
F=5.5-6.0 Vh

variables were significant for increasing of BSAD lV, because of the increasing of feed ftow rate F, bottom temperature of

lof
dB lnd
ted -he

1 0.00750

0.006666

lV = 0.6-0.7 g/100 g
2
0.0055560

0.0070830 lV = 0.6-0.7 g/10Q g
0.0055560

the flash distiller B FD and feed lV. All the
optimized main variables affected BSAD lV quality. The average value of BSAD production as effect of the main variables

the

BFD=21 82200C

BFD=220-222'C

B FD = 2180-2220C

can be seen within Table 7 which can be used to consider the optimum conditions

3 0.01000

0.004167

0.0070835

in this optimization, distillation conditions

Its

Notes: t/h (ton/hour)

to purify CFAF to get the in specs BSAD

ofrtly
,fB
re),
nova
ere )en

will cause increasing the amount of these
impurities which were separated from CFAF at the same conditions. This increasing caused the produced BSAD
had greater lV. The effect of reducing feed lV on BSAD lV reduction
and the effect of increasing B FD on increasing BSAD lV can be seen on the same tables, Table 5 and Tables 6.

tv. . Based on the average value of BSAD lV in Table 5, the best BSAD lV is 0.161111 g/100 g. Based on Table 7 above the best BSAD production is obtained on the feed flow rate (F) is 6.0 ton/hour, feed lV is 0.6 g/100 g and B
FDis222"C. The effect of feed flow rate and iodine value interaction

AD his

The effect of feed iodine value reduction is significant on BSAD lV reduction.

on BSAD lV. The results of one way ANOVA statistical analysis on
the interaction of F with lV to the BSAD lV are shown

ain by hin
:'hise
Fis
is he IV
)g
75

The average of BSAD lV reduction happened and caused the reduction of feed iodine value (lV). This
reduction of iodine value (lV) caused more difficult
separation of the iodine value together with BSAD at the same conditions. So the purifying that had been done on CFAF with lower lV produced lower BSAD lV at the same conditions. These data proved that the reduction of feed lV can improve quality of BSAD lV. So raw material with
lower lV will produce BSAD with lower lV or on the
Tabte 7. The average BSAD production as the effect of the main variables.

within the Table 8. Based on the data, significance test analysis of variance Punoru = 0.048 for the interaction of increasing F at the same lV (0.7 9/100 g) and Puno,, = 0.015 at the same lV (0.6 g/100 g). Both values of Panoua are tbwer than 0.05 (Po). That's why the interaction of
increasing with the same lV, shows significant
increasing on BSAD lV, also based on the factorial
analysis within Table 4. See also Table 9 as supportive of such explanation. These values explained that the etfect
of the interaction of the increasing F factor with the same
lV on the increasing of BSAD lV is significant on the
same feed lV. The interaction trend of these 2 factors can

00 i.0
UE

No The average value of BSAD production, kg/hour

1 F=5.5Uh F = 5.75 Vh

F=6.0Uh

be seen on the Fig. 3 and 3D surface plot on the Fig. 4'
It can be understood that the fact of this result is according to the mass and heat balance principles. The

IV

4.943.7

5,168.12

5,400.09

increasing of the CFAF mass, which was purified, needed

30

2 lV =0.6 g/100 g

lV =0.7 g/100 g

more heat or proportional heat to maintain the same

to

5,171.92

5,169.'13

temperature. This was caused by more evaporation and
condensation of the BSAD which was purified or

\F

3 B FD, 218" C B FD,22O. C

BFD,222,C

separated, include the impurities of lV in BSAD' The

he

5,148.77

5,161.53

5,201.28

increasing on F was caused by BSAD that was produced

rfe nd

Note: tth =ton/hour

had more BSAD lV on the same feed lV'

F Researdt artide F olrdian Socjetyfor klucdiot ard EUiffin'Ert ($e)
d. 73

lodrcwlue'
tttp/ ^,rw.inq$.sg

ltv=--l#r i- -r

uF

lndian Journal of Science and Technology

.@

330C
Vd.5 Nb.g (Sep. 2012) ISSNI G746846

Table 8. The One way ANOVA for the interaction of F and lV to

BSAD IV

No

lV = 0.7 (Funouu = 3.75 ; Punoyu = 0.048)

lV = 0.6
(Funouu = 5.65 ; Punouu = 0.015)

F = 5.5 t/h (Fanoua = 1.43 ; Puno* = 0.26)

1 lV of BSAD =0.16000
StDev = 0.01095

lV of BSAD --0.15333 StDer, = 0.00816

F = 5.75 Uh (Fanov" = 1,8 ; Panora = 0.209)

2 lV of BSAD =0.16667

lV of BSAD --0.16'167

StDev = 0.00516

StDev = 0.00753

F = 6.0 Uh (Funou" = 1.22 i P"nov" = 0.296 )

J IV of BSAD --0.17333 lVof BSAD = 0.16833

StDev = 0.00816

StDev = 0.00753

Notes: St.Dev = Standard devbtion; yh =ton/hour

Table 9. The average of increasing of BSAD lV as effect of the

interaction of increasino F

IV

The average values of
No increasing of BSAD lV, gi 100 g

fhe overallo'f
increasing BSAD lV, o/1 00 q

lV 0.7 g/100 g

F=5.5-5.75 F=5.75-6.0

1
Uh

Uh

F = 5.5 - 6.0 t/h

0.00667

0.00666

0.006665

lV 0.6 s/l00 g

F=5.5-5.75 F=5,75-6.0

2 Vh

i/h

F=5.5"6.0Yh

0.00834

0.00666

0.00750

Note: t/h =ton/hour

Table 10. Means decreasing of BSAD lV as the interaction effect
ofthe same F and decreasino feed lV

The average value of

The overall average of

decreasing of BSAD lV, g/100 decreasing of BSAD lV

No o

, q/'100 q

lV from 0,7 to 0,6 o/100o

1

F=5.5Uh

F = 5.75 Uh

F=6.0
UN

F=5.5to
6.0 uh

0,00667

0,00500

0,00500 0,0055567

Note: t/h =ton/hour
Table I /. The One way ANOVA of the average BSAD lV as effect of the interaction of lV and B FD

lV = 0.70 g/ 10C g (Funnuu= 5.83 ; Puno,u = 0.013)

No B FD 218 OC

B FD 220,C

BFD222,C

Funon"= 1,22; Punoru = 0.296

Fanovu = 0.92; Punoru = 0.36

Funoru = 2.86
It)a-no; va 4.122

I 0.1 5833

0.1 6833

0.'17333

StDev = 0.00753 StDev = 0.00983

StDev = 0.00516

lV = 0.60 o/ 100 q (Funo*=4.33 ; P"nou, = 0.033)

2 0.1 5333

0.1 6333

0.1 6667

StDev = 0.00816 StDev = 0.00816

StDev = 0.00816

Note: StDev = standard deviation.
So the increasing of feed flow rate F on the same feed lV is a variable which has a significant effect on

increasing BSAD lV. lt effect can't be neglected and very
important to be controlled or manipulated exactly to

obtain the in specs of BSAD lV.

The effect of the interaction of same feed flow rate F and
decrbasing feed lW Based on the one way ANOVA

analysis (Table 8, 6) the interaction of the same F and
decreasing feed lV isn't significant on decreasing of

BSAD lV, because Punouu is greater than Pcr = 0,05 (for F
= 5,5 ton/ hour, Punouu = 0,26 ; for F = 5,75 ton/hour ;
Punoru = 0,209 and for F = 6,0 ton/ hour ; Purou, = 0.296). This means interaction of F and lV within the Table 4 did

not.significantly affect the decreasing of BSAD lV.

Table 10 supports the explanation of effect of the
interaction of the same F and decreasing feed lV.

Decreasing of feed lV has impact on the decreasing of
BSAD lV. Feed lV greatly affected BSAD lV. This interaction is also very important to be controlled or

manipulated exactly to get the in specs of BSAD IV. The

optimum one was achieved at F = 6 ton/hour, lV = 0.6 g/ 100 g and BSAD lV of 0.16833 g/ 100 g (Table 8).
The effect of interaction of feed iodine value and

temperature of the bottom flash distiller on BSAD lV

The interaction of lV and B FD is shown in the Fig. 3
and Fig. 5. Based on the data in the Table 11,

significance test analysis of variance Punou" = 0,013 for lV

of 0.7 9/100 Qi Panova = 0,033 for lV of 0.6 9/100 g. Both
Prnor" are lower than 0.05 (Po). lncreasing of B FD

affected the increasing of BSAD lV or vice versa.
Higher the B FD, more the lodine value and the BSAD lV also increased. The optimum BSAD lV was
found at the same feed lV 0.6 g/ 100 g and at a B FD 222oc with BSAD tV of 0.16667 g/ 100 g (This is tower

than 0.2 g/100 g).

The effect of the interaction of lV decreasing and the same B FD.' Based on the Table 1''1, the interaction of

decreasing of lV and the same B FD did not significantly
affect the decreasing of BSAD lV, because all P"no* values >0,05 (Punovu = 0,296 ; 0.36 and 0]22for each of the B FD 218; 220and 220oC). This means lV.B FD

interaction did not significantly affect the decreasing cf

BSAD lV as shown Table 2. See the overallaverage of

the decreasing of BSAD lV in Table 13.

The decreasing of BSAD lV in this case (see Fig. 5)

can happen, because the decreasing
lowel lV impurities which was

of lV impacted on evaporated and

condensed together with BSAD. This matches the

principle of garbage in garbage out.
Although the effect of this interaction was not

significant on the decreasing of BSAD lV, the data in the

Table 12 show that BSAD lV was decreased. That's why
the effect of this interaction are also so important to

control, and manipulate in order to obtain the in specs
according to BSAD lV quaiity standard, besides the

interaction of the same lV and lncreasing of BFD. These
two factors are so sufficient to be controlled or
manipulaied tc obtain the quality of BSAD lV as its

standard specs which were settled.

Research atide
ai: lrdian Socjdy fs ftfi.rcdlm &rvirtrrrert (See)

lodiremlrc" Ittp/Aarr,wlindsLog

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--7

lndian Journal of Science and Technology

'@

ml Vd.5 1.b.9 (Sep. 2012) lsst\t G7+6&16

Fig.1. The modified distillation process schema t9 Provide
BSAD- with tle be!91e sbble B_SAD tV .

Jaei

ft{":i ({i!r;l

Fn!'" clSi! it. i'tilite c;s:rilt'-

The optimization of the distillation process
conditions will be better to conclude (to find out feed flow rate F) by looking at Fig. 6. The production yield of BSAD is relatively better on the lV of 0.6 g/ 100 g than lV of 0.7 gl 100

g on the increasing of B FD.
Based on the data above, optimum

Ii*'

conditions were obtained for distillation on the
interaction of lV 0.6 g/100 g and B FD222oC on F 6.0 ton/hour (from Table 11, on the third
column), with the average of BSAD lV of

;:i.:t r.-:,