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

optimisins refined breached d"egdoriz.

end"P,"liH:T'JlJ:;,':'".'#iill,f,::ff'fJ?:',ffivarue

to

provide the stabre

Muhammad vusuf ditong

a

.

,,,--

4nirE

t6rt^n Departmentof chemicatEngineering,

ru"rti'iiEiginiilrg,

u.niviiiiyotsumatera

utara' Medan 20155' lndonesia yusufrit@gmail.com

Vd.s

Nog

(SeP.2012)

32S

lsst\t @7+6846 lndian Journal of Science and Technology

specJon 0-175 g/100 g'

: Distillation, lodine value, Bottom flash distiller standard, Distillate,

Feed ca

il

Tabte t. The composition of IRBDPSFA orhvd-rolv.zed RBDPS

and

ih;"'q';iitv

'

or

i:Ilut"

which

is

produc

HSRBDpSFA(Muhammad,2009)

--=-:-===^-

0'a]una'mmio,

.

20.10;

YYlTTlg

_,r?o'. Abstract

on the commerciar scare, the quarity standard of erenoed siearic Acid Distiiled

(BS{D) courdn't be achieved by normal distilration. BSAD

iodine-;ilJ;;;stry

higher than maximu,

qru'i',iv-"iliio*i1o

z

mg/100 g), with the same iodine

varue (0.80 s/100 s)

"t'i""i'Hvoios"nui"a

spiitt"Jiieois rutry'n.iioi

HiiraDFarA,ieed

ci'pacitv 5'5 ton/hour witt bottom frash dist,rer

t"r"p?riirIiEacning

zil;'c. rt

"ieparation

""oilor"ti"n

of chemical impurities (so sensitive tt oxidation/temp"r.trr"mJui _"r,unging, and

ioi;;"rJ"r

*Ir"

0"r".

ir'"

"tr""t

of the reduction oi feed iodine value (lV) increasing of feed

"upu"ity ano uottom

t"rp"i"tu[?

tiair, aistitt"r

""rrrn

(BFD) w.ere ootimized to observe

BSAD',t

iodine vatue trend by ,.in'g u factorial

q."tig;i3';?

*

sf'utntO

rn" tpiiti*"condition

was found on the

feed lV c

0.60 g/100 g, at tee^o"c-;p'"itv

o.o't"n/hou-r,'J"i

ero iemperature'iifd-

roai"e varue of

BSAD was stable and it

lntroduction

Brended stearic acid dist*rate (BSAD) contains -60

o/o

maximum

-oi-

esnu

tv

specs)

which

is

produce

w/wof parmiticacid(c15H31cooHorc,,o)and

-4oo/owrw

"or*J*iurry

uy

using the. same

lv

(0'80 9/100

g)

<

of stearic acid (c17H35cooH or c1s)'

'n'

*l'nil'"il;-t

H::I**i,

g::*"illfiI'fliil"

''i",,1:'-"i1?li"Ji

:*tt,;,::,j

!?;:'ii';'",8*,i:::'J;'Xii'ii'J'i:tp"J

I'..'"lJ'i

*;;n'tiioimur

and thJ iodine varue was unstabr

achieved

using RBDps

as

raw

,.nri"riui-'rr.,"

bqr!" "r-

ti'"-

practicar

data,

the

increasing

r

composirions

of

snsDpsrR

are

shown

ir"i"nr"

i.

HsRBDpt;Ris-tv'wtrich-is

higher

than 0'80

9/100 RBDps is highry suitabre to obrain oo "2"

c.,u;+o'"7"-c.,ror

proau"li-tt"

r,ign"t

BStq

lV (Yusuf' 2010)' Based c

BSAD by cutring a pario-t

i["

r"*",

and higrrer uoirer

th-an

*',ur"

iiit.,'it'.

;rppo."d

that tire lower HSRBDPSFA

cro_ra

in

the

suitabre dist,ration process

;;*Iti;";

;f

!v

toi.tirijil"

p-"!!i

t""d)

can reach, the rower BSA

HSRBD,.FA.

distillatron

process-

L-

rv on

ir,"

iing?t of it-quality standard will be. How mut

The

off

specs

of

BSAD iodine

value

(BSAD

lv)

.llouriin"

orl'l;'I:-*,lY o"'

lt

should be found

ot

created lower competitive level in oleo

"n"rni"jt

,urfet.

li

Based

on

the

experience' practically

the

low

courdn,t

be

produced

in

tne

normar p,oorJiion

"v"r".

nsne'op"-din]v

"un'ue-^obtained

through SRBDPS' producrion

wi,

be

i""*i"i""i

,no *ariing

""Ligv.'it

;

hydrosenition'

This was also

based

on

fatty

ac

overa, items of quarity specs courdn,t

ue.oiiainBt.

Tlr"

rrva.i".aii"n-tneorylRobert'

1990)'Thiswasn'ttheor

off specs rV are tne

laule

of the rower

t"i.i"iutrru

ot

*"v tJ.orr"

*re pro',otem- rodine

vaiue of BSAD was al

BFD corumn. rt

o"crelll;;;;,"

rii;c.-iriii

affecteo

nigher wtren

tre'feed

capailtv higher than 5'5 ton/hc

BSADcompositions,frombigger-lossof

G+ra;iBSii.t9

1;1Y:yf''ZOiol' So the

questibn "what will the optimt smailer weight ratio

of c,u-to

c,r.ol Bq4D"l"o

a5no

aistilraiion "ohdition, to

getthe

in

specs BSAD

lvr

h

compositions tend to

L;+i

tp""t'

tt.i" u big effect to

tire

to be studied'

rower production

yieriLr-s;;;;;

uis t,oudtu arso to

the

t;*,"ru1X#:i,.J,'..,1,15:?l

#i:!ELrr":J,':tl;

U9

No Fatty acid name

Symbols double

bond

SRBDPSFA,

o/o _wlw

HSnaopsrn,

o/o _w/w

1 Lauric acid Ce 0

0,1 0.1

2. Myristic Acid Crl 0 1.3 1.3

3 Palmitic Acid Cro 0 57,4 57.4

4. Stearic Acid Crpo 0 6.1 40.2

tr _{Oleic Acid} Craa 1 27.9

6, Linoleic Acid C'ts-z 2 6.2

ii"g"iJint-ihit,

the

optimum

^feed

lY

^'

oiiifiation" conditions of HSRBDPSFA have to

t"t"ri"n"O

carefully

and

commercially

in

I

study (Peter et' a1.,2004)

ioitinu value

was one

of

the

qu€ oarameters

of the

commercial premium BSt

[".iA"t

its

color, heat stability and fatty z

IJrpoiitions

(Pr.

xxx,

2005)'

99tting,th:lT

the

'better

and

the

more stable

lV'

Heli

iii"""r'"0

Deodorized

Palm

Stea.rin (T?? 10)' There.is

:'ffi

i;

n"J

*uv

for getti'ng the in specs of BSAD in the

was

used

as

raw

material; because

the

chen

i-.,,,riii"s

or impurities that's so sensitive to oxidation

ir"tin""o;u"un

i""t".t"d

from RBDPS to a cenain

k

normal Production cYcle'

lMta*

bft r-Uytt

E,r rdin ad ExvirqnErf GSe)

7t)

lodirBmlrc'

http/Arr,vw.in{st.og

llY.Rt

It

is

so

suitable

to

produce BSAD through hydrolysis, hydrogenation

and

distillation. lmpurities

reduction (includes unsaturated

bondl

of

the

crude

fatty

acid (SRBDPSFA) can reduce fatty acid color and lV through fatty acid hydrogenation (Robert, 1990). The experience shows on the specific conditions, distillation process also separated

the

impurities

to

a

certain level

so

that the amount

of

unsaturated bond (indicated

by

lV)

will

be lower

and

better.

So

hydrogenated SRBDPSFA feed could reduce BSAD'

lt/

also through distillation and/or fractional distillation.

By

using

of

this

HSRBDPSFA,

reduction

of

HSRBDPSFAIV

and

optimization

of

distillation process conditions

which

is

done

in

this research can reduce unsaturated bond

or

obtain lower and more stable arnount of unsaturated bond or BSAD lV according to BSAD lV quality standard.

According

to

the

practical

experiences

in

oleo 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 showed

this

fact. These lower fractions

are

easier to 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 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

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

the

other impurities such as:

sterols,

phosphatides,

glycerol

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 lndian Journal of Science and Technology

R€s€ardlatide

olrdian Soddyfor mucatim ard BNiro-rrert (See) 71

w7

Vd.

5

r.b.

9

(Sep.

2012)

lSSilt Cs74 6846

BSAD relatively. The temperature had to be reduced so that lV will be relatively low. This was also based on the down grade acceleration of fatty acid that was affected by

temperature (Brocmann et al., 1987; Ketaren, 2008).

The

providing

was

done

by

recycling

lhe

rubber grade distillare to the drier as the other big potential to increase BSAD

lV,

besides CFAF

lV

and

distillation procqss conditions (the present distillation facility or Feld and Hanh style) (PT. XXX, 2005). ln this research, it will be separated as a byproduct of rubber grade distillate to 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 suitable yet to produce BSAD as its quality standard of lV (0.2 _{9i100 g)} and

itwas

stable. lt has to be studied. The distillation operating conditions weren't optimum also. For this, light end yield will be kept constant on the range 1.5

-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 operating conditions of distillation.

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 fatty acid feed. lt was obtained and will be

purified

on the

same plant

site

of

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:--=

lodirevdLE'

lfipl/lvvrwinq$.sg

Table 2. Steps of the research

Variables al (F=s,50) a2 ( F= 5,75 ) a3(F=6,0)

cr (zraoc)

br1o,z1 bz(o,o) br1o,z1 bz1o,o1 br 10,21 bz1o,o)

X X X X

x

X

cz (zzooc)

x

X X X X

x

X X X X X X

cg {zzzoc)

X X X X X X

X X X X X

x

-7

\r,

l---.]-r -:: =mf,@

,"f-*\

W

-,3,an Joumal _{of Science and Technology}

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

No F, ton/

hour lV,g/1009 BFD, CO BSAD IV, g/1 00 g

1 5,5 0.7 218 220 222 0.150

0.1 60

0,1 70

0.6

218

220 222

0.145

0.1 55

0.1 60

2 5,75

0.7

218 220 222

0.1 60

0,1 70

0,1 70

0.6

218 220 222

0.155

0.1 65 0.16s 3 6,00 0.7 218 220 222 0.165

0.1 75 0,180

0.6

218 220

222

0,1 69 0,170

0.1 75

?98

Vd.s

M.9

(Sep.

2012)

_{lssr\t 09746846}

symbol

of

*

between

two

_symbols

of

this

_process variable states

the

interaction between

two

or

_more variables. So F*lV is the interaction levels of F with lV and so on for the others, dk is degrees of freedom. uk is sum

of

square,

kt is

_{central-squ-are,}

f*"rr-anO

_p4n6yu

ofe distribution test and significance tbstZnJlyiis of variance.

Effe_ct _of process

varilutei-is-iii.rtn"j"i,'

_{tt bono,,.}

pq

_{_}

0.05.

f0y

significance

of

the

_{optimbed process variables} effect on the BSAD iodine vaiue

The results of Factorial anatysis and its significance (Table

4)

_{describe the..influenc6-ot}

ipti-ired

process variables on the BSAD lV. Statistical

,nliyri"

_{shows tttat} feed rrate,-F (p"no,u= _{0,000) ano reeo-lJo-ine value-,}

lV

(P9"o^,=1 _{0,010), B FD (p,nova= 0,0p0)}

*"r"

to*"r. than (po = 0.05), _{the effects were so significint}

tolhl

changinj oi BSAD iV. lnteraction of F and _{iV 1e",*, = ii,gzOl, F and B} FD (Pano,a _{= 0,67g), lV and}

g

fD

ti;"*"

='O,]ZS),

f

ana

lV

also with

B

FD

(pano,a

=

0,di"di

diin,r

_affected significant (Puno,n> po = _{O.OSJ changing'of SSAD lV.}

The

iglT!9f

,"j.chmain factor toihe eS-AdM is shown in the

I

L-l

it

-t,

f--I

l:

:

i

IN.

i-r

lz

I I I

Lr

lndii impur condi had g

T and tl

can b

The e

BSAt TI CAUSE reduc Separi same CFAF condit lV car lower

Table

was done

oasea

riril""o

_Fig.3.

method Tg 1- 64 to anatyse.BsAD tV

(David,2006).

Eifect

of

O-ptim

rlftrr'Iros f

g

r-o4loanalyseBSAD

lV(David,2006).

lffect

of

Optimization

of

the main

_variables

and

_lts The correct results _{will be obtained by keeping}

top

_{lnteraction on BSAD}

lv

temperature of pre-cut column

at

190oc

"no

pr"i"u"r"

Jt

The increasing

orgseo

v

was affected significantly

21

mbar;

Flash

Distiller

pressure

it-

b

'moar

;"d

by the optimizatio-n or _{ttre main variables (increasing of B} temperature _{(B FD) as per the steps shown in}

rior"');

rb,

_{reeo'flow rate}

r

uno o""r"asing of feed iodine value), residue distiller pressure

at

_{1 mbar and}

temperai;;;;i

_{because significance}

iest-anatysis

of

_variance p,no,"

2S0"C.

_{shows,pun*]_olB}

FD

E",_""

of F

_and punouu

of

_{lV were}

The

_{research steps}

were

_based

on

the

factorial

_{lower tnan-ols}

tpol.

5i"

f'"'ir"

4. The trends can be seen method by 3 x 2 x 3 and were repeated 2 times.

f;b|",

in Fig.2. [image:3.612.30.298.57.338.2]

shows steps of research' The symboli

ire

_{useo in}

tre

ih.e _{impact of the optimized main variables on BSAD}

table such

asi

o1,

a.z,

3s

=

variation

of

_CFAF

rate

lV is shown in

ig

,6;using

_{tuinita b 14 software).This} (ton/hour); _{br, bz, bs = varii-tion of feed}

lvlg/l00

g)

and

picture shows

the-'sig;;i";;;effect

_{of the optimized main} c1' G2' c3 ₌ variation _of BFD

("c)'

_variables

o,

_gsAD

iV.'il-"'.ur"

effect is also snown oy

Results and

discussions

_{the average}

values of the increment

of

_{BSAD lV within} The results are provided

in

Table

3.

The effect

of

Tabte 5

u,iJr.oru

o

fi.riig.

_zl.

process variables were analyzed

with

Minitab

Release

The effect

on

increasing

of F

is

_significant

to

_the

14, where, F is feed rare, lV is feed iooine vaiue ano e

iD

in"rurrinj

oGs"AD';V.

Ai"i

of s.5 _{ron/hour BSAD tV is} is the bottom temperature of flash

aisittLiiotumn,

*o u

0.15666/91199

g,

;i i ;

_{5.75 ton/hour BSAD}

IV

_is

Tahta,

rT..An^/t/^-:^--_

- ,

0.164167 g/100

g

and

at F

6.0 ton/how

giAD

rV

i.

Tab/e,4. BSAD tV _{Variance analysis and significaiion}

Source

DK JK _{kt I} tr

anova I banova

Remark Variation

F a _0,0001256

0,0006028 18,08 0.000 Significant

IV 1 0,000278 _0,0002778

8,33 0.01 0 Significant

BFD a _0,0012722

0,00063G1 _{19,08 0.000 Significant}

F-IV

2 0,00000s6 0,0000028 _{0,08 0.920 Not significant}

F*BFD 4 0,0000778 0,00001 94 0,58 0.679 Not significant

IV-BFD 2 0,0000056 0,0000028 0,08 0.920 _{Not significant}

F*IV-BFD 4 0,0000111 0,0000028 0,08 0.986

Not significant

Error _{18 0,0006000 0,0000333}

Total ,tr

Table4.

BSADtvVarianceanalrysandsrgnificaiion

0.170g33

9/100

nl

,H:

source

;;;l

i":?:x'.?*lJrfr?t?;irii

ffi

-"""

t

i

-"

I

""

I

'

from F of 5.5 kg/hour to 5.75

I

r

i r

_{ks/hour ana O.6OOOO6}

9/100 g from F S.75 kg/hour to 6.0

i

B

FD

i ,

i_

o,oorrrz

I

o,o

kg/hour. The averaoe vatue

1,r",J3i,.J""i3,,

i8fi*jx

g/1 00 g.

I

IV. B

FD

| 2

i

_0,0000056

o,oooA

This is easy

_to

I

t

j

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

impurities

which

_were

,ora,

r

t35i

I

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

Research artide

2

J

1

R*eth

a lrdan S

73 @lrdian Societyfcr E L€atimand Fvirryrrerd

(isee)

frtto,ffiffiT*

tuly.Ritorga

lndianJ.$i.Td"nd.

lndian Journal of Science and Technology

Table 5. The average vatues of BSAD lV as the e{fect of the main factors

-7

gg

Vd.s

hlo.g (Sep.

2012)

lSSilt

g/46846

contrary.

w.

1€ ESS ate )ce. d= lt.

-)te> AD his ain by hin nce ESS l-rat lDa

lof

dB lnd ted -he the Its rtly ,fB re), nova ere )en

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

Notes: t/h (ton/hour)

will

cause

increasing

of

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.

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

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.

No The average value of BSAD production, kg/hour

1 F=5.5Uh F = 5.75 Vh F=6.0Uh

4.943.7 5,168.12 5,400.09

2 lV =0.6 g/100 g lV =0.7 g/100 g

5,171.92 5,169.'13

3 B FD, 218" C B FD,22O. C BFD,222,C

5,148.77 5,161.53 5,201.28

Note: tth =ton/hour

The effect

of

the increasing BFD is

significant

on the

increasing BSAD lV.

This can

be

explained

as

follows: the increasing

in B

FD

causes

blended stearic acid with higher lV

to

evaporate

and

condense

more

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.

Based

on the

average

of

BSAD lV above, the effect of the optimized main variables were significant

for

increasing of BSAD lV, because of the increasing of feed ftow rate F, bottom temperature of 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 can be seen within Table 7 which can be used to consider the optimum conditions in this optimization, distillation conditions to purify CFAF to get the in specs BSAD

tv. :he

'is

is is he IV

. 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 on BSAD lV.

The results of one way ANOVA statistical analysis on

the interaction

of F

with lV

to

the BSAD

lV

are shown 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

F

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 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 increasing of the CFAF mass, which was purified, needed more heat

or

proportional heat

to

maintain

the

same temperature. This was caused by more evaporation and condensation

of

the

BSAD

which

was

purified

or separated, include

the

impurities

of lV in

BSAD' The increasing on F was caused by BSAD that was produced had more BSAD lV on the same feed lV'

)g

75 00 i.0 UE IV 30 to \F he rfe nd F F d. Researdt artide

olrdian Socjetyfor klucdiot ard EUiffin'Ert ($e)

73

lodrcwlue' tttp/

^,rw.inq$.sg

ltv=---l#r i- -r

No

The average value of BSAD lV, g/1 00 g

F=5.5Vh F = 5.75 Vh F=6.0Uh

1 0.1 56667 0.164167 0"170833

2

lV =0.6 g/100 g _{lV =0.7 g/100} g

0.161 1 1 1 0.1 66667

3

B FD, 218"C B FD,22OOC BFD,222"C

0.155833 0.1 65833 0.1 70000

Note: t/h (ton/hour).

No

The average value of BSAD lV,

o/1 00 q

The overall average increasing of BSAD lV, g/100 s

F =5.5-5.75 Vh F=5.75 -6.0 V hr F=5.5-6.0 Vh

1 0.00750 0.006666 0.0070830

2 lV = 0.6-0.7 g/100

g _{lV = 0.6-0.7} g/10Q g

0.0055560 0.0055560

3

BFD=21

8-2200C BFD=220-222'C B FD = 2180-2220C

[image:4.612.35.579.33.365.2]

uF

lndian Journal of Science and Technology

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

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

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

Note: t/h =ton/hour

Table 10. _{Means decreasing of BSAD lV as the interaction effect}

Note: t/h =ton/hour

Table I /. The One way ANOVA of the average BSAD lV as

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

Research atide

: lrdian Socjdy fs ftfi.rcdlm

ai

&rvirtrrrert (See)

330C

Vd.5

Nb.g (Sep.

2012)

ISSNI G746846

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

[image:5.612.73.466.14.749.2]

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 of lV impacted on

lowel

lV

impurities

which

was

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.

.@

of lodiremlrc" Ittp/Aarr,wlindsLog tvlY.RitorEa lrdanJ.Si.Tednd. BSAD IV

No lV = 0.7 (Funouu = 3.75 ; Punoyu = 0.048)

lV = 0.6

(Funouu _{= 5.65 ;} Punouu = 0.015)

1

F _{= 5.5 t/h} (Fanoua _{= 1.43 ;} Puno*

=

0.26) lV of BSAD _=0.16000

StDev ₌ 0.01095 lV of BSAD --0.15333StDer, = 0.00816 2

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

lV of BSAD =0.16667

StDev ₌ 0.00516

lV of BSAD --0.16'167

StDev _{= 0.00753}

J

F = 6.0 Uh (Funou" _{= 1.22 i} P"nov" _{= 0.296 )} IV of BSAD _--0.17333

StDev ₌ 0.00816

lVof BSAD

=

0.16833 StDev = 0.00753

interaction of increasino F IV

No

The average values of increasing of BSAD lV, gi 100 g

fhe overallo'f increasing BSAD lV,

o/1 00 q

1

lV 0.7 g/100 g F=5.5-5.75

Uh

F=5.75-6.0

Uh F = 5.5 - 6.0 t/h

0.00667 0.00666 0.006665

2

lV 0.6 s/l00 g

F=5.5-5.75

Vh

F=5,75-6.0

i/h F=5.5"6.0Yh

0.00834 0.00666 0.00750

the same F and decreasino feed lV

No

The average value of decreasing of BSAD lV, g/100

o

The overall average of decreasing of BSAD lV

, 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

effect of the interaction of lV and B FD

No

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

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

;

t)-I anova

-4.122

I 0.1 5833

StDev = 0.00753

0.1 6833

StDev _{= 0.00983}

0.'17333

StDev = 0.00516

2

lV = 0.60 o/ 100 q (Funo*=4.33 ; P"nou, _{= 0.033)} 0.1 5333

StDev _{= 0.00816}

0.1 6333

StDev = 0.00816

0.1 6667

lndian Journal of Science and Technology

0.1:0

0.r55

--7

ml

Vd.5

1.b.9 (Sep.

2012)

lsst\t G7+6&16 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

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 0.16667 g/100 g.

It

was

lower than

the

maximum quality standard of BSAD lV (lt's lower than 0.2 9/100 g) and the most BSAD production was 5203'5 kg/hour.

Generally

the

optimum conditions were found

at

6.0 ton/hour

of

Feed rate F, 0.6 g/ 100 g of feed

lV

and 222oC of B

FD.

These conditions produced BSDA with

lV

0'175 g/ 100

g

(Table 1, on the Sth column with bolt alphabet).

An

idea

to

modify

present

distillation technology for befter B SAD purification

The

present distillation facility could be improved

to

produce and purify better BSAD

lV

quality including

color,

compositions of lauric and myristic acid (See Fig. 7).

The present main or flash distiller (Fig. 1)

had

no

tray,

just the

demister that couldn't

'

separate well the iodine of the feed to provide

Fig. 5. Response of BSAD lV Versus feed lV and B FD

Ii*'

?:

{

ar)

d

o a

0,

7.

0,1{J

0*1ss

0.15J

0.1?0

0,165

0,I60

li

il;i :l)r' til:, t

r----

-::l

r-i: l+_{I r 5.731}

qr( _{L_:__jIlJ}

(lt0

0.t6J

&sAO', ,V. Urtoo , _o.r,

,.,,1=-n;

_{| - o''l} O,IJJ 0,?0 [image:6.612.22.600.24.767.2]

,!!:

o

|::orns1

of BSAD tv

*ny:_, ,r!_lv

gaAF'5 Iv, q/1008

i

e fn = bottom flash distiller; ESAD = bpnded dearic

;

IV = iodine valuB. F = fecd IloH rEte

t*-^^-*@*^.,*,

Researdatide

olndan Societyfor Elucatim ard ErvircrrErtft$e) 75

IV o/loog B'6j

2I8 g FD, oc

lV - iodine value j BSAD - blended staric acld distillate;

B FO = bottom flash distiller

Fig. 6. Yeld of BSAD as effect of the interaction of the

,.'....** iE:i'r ?;ili tr tt, C a

0,11 0,16

' r?10

f croo

- 51e'l

rE

: F ;1?6

< 5rov

I 515il

I

i {14i1 : i

1

I

t

t,

ll

l

"l_i

*-21*

acid iistillatel

lodrrwlrc'

fflp/

^!wjnq$.sg

21,3 3?i 22r

IvtY.Rito'ga

lrdanJ.$i.Tedrd

'@

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'-Fig.2. The average effect ptot of the main variables on BSAD

lV

?, *,r

a

aie

:io

217

Fig. 3. Mean effect plot of interaction of main variables !j;g r*ra:riq C:;.::f;iS ffi{

3@ lrdianJournalof

scienceandrechnotogy @

vd.5

tb.9 (sep.2012)

_{rsst\t@746846}

Fig. 7. An idea to modify the present distillation facility to provide BSAD

with

inciudes BSAD.

the befter and stable iodine

value

Conclusions

purification through distillation

are:

0.60 g/100 g of feed lV, 6.0 ton/hour of feed flow

r'ntd!'t*

r

_{botton flush distillei}

ts

FEjl on the BSAD

r

this optimization met the BSAD's lV quality

:

standard

by

separating

rubber

grade

i i,iili erd, c1113 r'att1 *t d i;1e. rerjr, ri 10 .::.:. :-4t:y .,:,d. _{distillate aS bypfOdUCt. All thg main faCtOfS}

C... . '-F::r ;c f ;i_:,du, {*5,6,-6 .ii_. }-. f

lV

_{0.175 9/100}

g.

Blended Stearic Acid Distillate of RBDPS which was obtained in

Table /2. The _{average of BSAD lV as effect of the interaction of the sam/ lV}

and

The improvement

is

believed will be able lmprovement of this equipment

wiil

be

,""t

o"rriii"

i"

:1:"1?d the BSAD lV' These factors.can be manipulated achieve lower

lv

and more expansive

"upuii1!?i5ni5

and,controlled to achieve better and more stable BSAD

purification through fractionat

distiilation,'"i;;";;"-;H

lv^'.lncreasing

of

the

feed

flow

rate

F,

temperature of

i",ist'e. capabilit|

to

compete

in

the

,.,.,r"t"'"i

H!t!,-,"'ir.J,S:",:,:T#t"?SSXJ]irrJ,r"l1i"':r#t,,:il1

"'.TH[:TfllitY

o""n

cristiler corumn

to

main

The interactions betwe-en the main fact.rs had impact on

fractionationitor 1z'; cotumn in Fig. 7) with

rp""Lr

irrr" :f-

PSAD

lV,

although some

of

the interaction effects (that have highei efficiency) and "doubte

"#d*;;;;;;

yu-f-.not

significant'

These

interactions

had

to

be

partial conderisers will increise efficiency

t"

1"*";

o"irirJ

manipulated

and

controlled carefully

and

exactly to point (includes _{iodine value or double Uo|Ol}

u-"alr;;;

i:.TI"

BSAD lV which is according to the specs.

boilinj

point

in sefiration

of

DoA

una

i,i.,irn:ti;;:;;;

sussestions

i""#:tffi,?d';:l,lni,"u;*ixLas,*i*ilijs"*m

ed;yT0'.1y":::?x1','I

3l'i"":i;'iJ""Hffii:

S1,X1,HI*iaJ::liru:fif:f

;:t"1[i*:1"##;ti

;:"?"""J::'31Xi11il1X':'['i,,"

va,ue or 0 6 _s/100 g or and odor better also. The partial

conoensel'iliti;;;

lower

by

improving

the

present

hydrogenation easier separation of tight end, cotor ano oooi,

;[; ilj;;

.

iperating

conditions

value (that can't be

ieparated

more

on

th;

;;;

';i'j;

2'

To _-improve

2nd

column

of

the

present distillation cotumn, because

ot

freaiitiess

;t;;,

i;i"";i;r;) ;"

facility

becomes fractionation column

with

partiat BSAD quatity _{wiu be better and more stabte.}

;;;i';ii";;

condenser

to

get

lower

BSAD

lv,

higher

plant is effeci to darker coror and odor of ruttv u"io'

pltirii.,

;iffi,?t[

33Xo1too

vield,

better

and

more stable

FD

No

The average values of the increasing of BSAD lV, q/100o

The overall average of the increasing of BSAD lV, g/100 g

lV 0.7 q/100 q

1 BFD=218"Cto

22Q"C

B _{FD = 22AoC}

to222oC B FD = 219 "C to 2220C

0.01 0.005 0,0075

2

lV 0.6 q/l00q

BFD=218oCto

2200C B FD = 220oCto222oC

BFD=21goC:

222',C

0.01 0.0034 0.0067

Table /3. The average of BSAD lv decreasing as the effect of the interaction

ll/

and the same B FD.

No The average values of the decreasing ofBSAD lV, g/1009

The overallaverage of the decreasing of BSAD lV,

o/1 00o

I B FD 218 0C B FD 220 "C BFD 222OC

lV = 0.7 to 0.6 o/100 o

lV

=

0.7 to

0.6 s/100 q lV = _{0.6 s/100} 0.7 toq lV

=

0.7 to 0.6 9/100 g

0.005 0.005 0.00555 0.00518

to cover usage of the other bed quality of raw material, such as CPS (Crude palm

Stearin)

or

PFAD (Patm Fatty

Acid

Distillate)

to

produce _the better

of

others main distillate products.

References

1.

Brocmann R, Demmering G, Kreutzer U,

Lindeman M, Plachinka J and Steihrner

U

(1987) Fatty

acid.

Henket KGaA,

Dusseldorf.

Federal

Republlc

of

German.

David

F

(2006) Officiat method and

recommended practices of the American

oil

chemists society.

d'

Ed.,

2nd

Printing. AOCS Press, USA.

Ketaren

S

(2008) Pengantar teknologi minyak dan lemak Pangan.

Ui

press. Jakafta.

Nur

lriawan

and

Septin

Puji

Astuti (2006) Mengolah data statistik dengan

mudah

menggunakan

minitab

14.

Penerbit Andi, Yokyakarta.

IilYRitorga lrdanJ.fti.Tednd. a

Z.

3.

4.

Researd artide

olrdian Soci@ fa ElLratim ard EnvirCI nBt (See)

-5

[image:7.612.57.559.27.695.2] [image:7.612.73.588.438.761.2]

-3303

Vd.s

tS.g

(Sep.

2012)

lsst\t @746846

d;G;1\

rdian Journalof science and

rechnologv

'it[ryj|fl

5.

Muhammad YR (2009) Refined bleached deodorized palm oil (RBDPO) Sebagai Bahan B-aku Pembuatan

V tegs

S" J. Sisiim Teinik lndust., Fakultas Teknik,

usu.

10(1),769-780.

5.

Muhammad YR (2010) Optimization of palmitic acid

composition

in

crude

oleic

acid

to

provide

specifications of titer and cloud point of distillate oleic

acid

using a flash distiller.

J.

Technol' & Sci' IPTEK, LPPM, lTS. 21(4), 203-213.

7.

Muhammad

Vn

1ZOt1) Providing vegetable stearic acid super

V

1895

S

from hydrogenated

of

crude vegetabie stearic

acid

HCV 1895

S

with

A

single fraltionation column. |JET/IJENS. 1 1(4)' 5-15'

8.

Peter W, Faesler, Karl Kolmezt and Wang SengKek (2004) Revamp strategies

for

fatty .acid distillation section

in

oteo-chemical plants. Sulzer Chemtech' Singapore.

9.

pf

iiX

(2005) Production planning control' Medan, lndonesia.

10. Roberl

C

Hastert (1990) Hydrogenating fatty acids: Hardening, furlher, faster a-nd cheaper' Proc' World Conf. Oleohemical into

2'l't

Century, AOCS, Kuala Lumpur. _PP: 16S171'

11. Yusuf Riionga M (2010) Optimization of the providing of stearic

aiid

based on refined bleached deodorized palm stearin (RBDPS) which

is

stable according to ihe quality standard. FM\PA, USU. Medan, lndonesia' pp: 2-6.

Researd artide

o lrdian Society fcr tlucdim ard Envirmrcri (See) 77

lodirE\alrc'

htipl^ rw.inq*W

lVtYRitorga