Providing Vegetable Stearic Acid Super V 1895 S From Hidrogenated Of Crude Vegetable Stearic Acid HCV 1895 S With A Single Fractional Distillation Column

lnternational Journal of Engineering & Technology IJET-UENS

vol;

1l

No; 04

PROVIDING VEGETABLE

STEARIC

ACID

SUPER

V

1895 S FROIVI

HYDROGENATED

OF

CRUDE

VEGETABLE

STEARIC

ACID HCV

1895

S

WITH A

SINGLE

FRACTIONAL DISTILI-ATION COLUMN

Muhammad

yusuf.

Ritongal

l,Chemical Engineering Department, Faculty of Engineering, University of Sumatera Utara, Jl. Almamater Kampus USU, Medan 20155, Indonesia

E-mail : yu s ufrit @ gmail. com

Abstract

ln 2005 stearic acid

V

1895 S is manufactured for l*ttime in Indonesia base on the natural vegetable oil, Crude palm Cil to apply Twin Rivers's demand. One of it specific quality (iodine value 0.15 gll00 g _{maximum) is very influence to}

,re purifying steps, one

of

the steps is purifying of hydrogenated crude

V

1895 S (HCV 1895 S) feed by a single :olumn

of

fractional distillation

to

produce

V

1895 S with the lowest possible

of

it

iodine value, lower than the

naximum value. The results of application and small adjustments of determination operating conditions of the single ;olumn priority based _{on the feed composition, product composition of}

V

_{1895 S and}

it

_{pressure drop character are} ;ompared based on

it

quality standards. This is the method used in this research to provide

V

1895 S and conducted in ihe plant scale of PT.

XXX

factory with production yield 88

-

89 Vo of 0.90mt

HCV

1895 S, unsarurated content is ioiver than 0"15 g/100 g and higher than 98 7o wtw Cl8 purity. In general the specific quality standards of

V

1895 S can be met"

Keywords: quality standards, _{fractionation, composition, unsaturated contenl, adjustments}

1.

Introduction

Fany acid

ofV

1895 Sis meansuper

fatty

acidbased

onnatural

vegetableoilslfots

with

stearic

acid C17I{35COOH

or

C1s compositionis

minimw 95

Vo

wlw. Ithas been never manufactured at

all,

although oleo chemical industryhad been growth in Indonesia in

the

period

1989-2004.

This fatty

acid had

been

produced in America and Europeto consume for:one of the consumption asthe raw material

of

the cosmetic manufacturing that have the lowest skin effect, for exampleto manufacture

the

premium

shampoo Pantene.Thts stearic acidhas

very

low

unsaturated content.Sincethe beginning of the year 2005,South East Asia's begunto see as a

V

1895 S producer. In October 2005Twin Riversas a buyer gave an idea, a standard

quality that had

to

be

followed and

produce

it

according

to

the

process sequences

which

were determined and do

by

PT.

XXX

alone(Figure 1), a

company

that had

been

exist

in

operation inoleo chemical industry, since the last

of

the year 1998.

Quality of

V

1895 S produced had to meet the quality standard which is shown

in

Table 2 below (settled by Twin Rivers).The same quality standard which was

produced

in

America and Europe by the method was

different at all.This was because of the different raw material and the used technology"

In

this research is useda natural vegetable

oil,

Crude Palm Oil (CPO) as raw material for the manufacturing

and refining of stearic acid super

V

I 895 S as shown in Figure lbelow. Manufacturing and refining technique of CPO to produce stearic acid super

V

1895 S (Figure

l)is

so

different compare tothe general alternative manufacturing and refining techrique of fatty acid in Figwe 2 below [12]. Figure 2 is modified to be Figure

I

to produce

V

1895 S to apply Twin Rivers's demand with the lowest possible

it

unsaturated content, as the

first technique in the world. Refining

of

raw material on

left

side

of

Figure land Figure

2

can be done by degumming

only

and/or

combined together with bleaching and

or

deodorization process alternatively according to raw material used, product quality have to be met and equipment capability. Refining of fatty acid on the

left

side

of

the both figures can be proceed through distillation and./or combined

with

fractional distillation alternatively, again

it's

very depend on the

I 10404-3737 IJE'I-IJENS (d Augusr 2011 I.lflNS

lntemational Journal of Engineering & Technology IJET-IJENS Vol: 11 No: 04

raw material specs, product quality have to be met and

present equipment capability.

oils and fats ra$'meterial

;-

-=\_-r

Returing

Br.Eflat

+t

$plit

Hvdrogenation

r+

S.pJrtior,

+

Gl1'ceru:ra

t{rt

I

r*uu

e.,al

R.t*s \*.,*Luo'

+

J

{Fanv

Hy&ogenation

Refine

glycerin

Refimng

\/

---*CPo'.-+-

\-*

Refrning

eqfiu$g

{+

Split

Hvdrogenauon

Sepaiation

-r

Glycerin,*

Sil,,

r*tty

roal

R,***

\*rri*r.,,

+

+

{Fauvaud

H1'drogenahon Refine

glvcenn

Refitting H1'drogenahon Refine

glvcenn

Refinurg

Hytuse-

I

₊

pfllcLfilUl

I

Hydrogenated fattv acic

flfr\4

{

Distillahon

Frttyrdd

tyrcid

I

I

_l

_l

1850

I

L+

Resldue

Fnctiopation

-|

pl"lmid.q acid

{J

flv

1$9J S [image:2.612.385.594.115.285.2]

Table 1 .Thespecific quality of CPO to provide

V

1 895 S

Figure 2. General alternative of fatty acid refining

steps

Palm

oil is

one

of

the

source

of

stearic acid (CrzH:aCOOH) or Crs also as a source of unsaturated

fatty

acid oleic acid

(CtrHgsCOOH)

or

C1s-1 and

linoleic acid (CrzHgzCOOH)

or

C1s-2 that could be hydrogenated

to

be

stearic

acid

as also stated by

t7ltl0lll5l

till

the total amount of Crs is around 50 7o

w/w. See the raw material quality CPO that used in this study. The

fatty

acid distillate which

is

obtained of splittedCPO

is

called fatty acid 1850[7]. Crude Palm Oil has the highest C1s content than the others natural vegetable

oils

such as: crude palm kernel

oil

and

coconut oil. This's the reason the raw material CPO is

used in this research.

ecid

iuci;issfrf

-

,

I

Fractiohation---* \'1895

S

I

ll,

S.awrrai+rial

A\tr

SY E?O

cru

c14 8tr6 *13

f,!&-X

C:8-!

c]0

_"u-Ilk

cro

?.6

101:

0:9

0.:

1.1 43.l

,1.4

39.1

10.3 0.4 0.8

io rrcg ." F?ora _$4Xg1f4 C*emirudo,J

0fi

{-qLS-:,

AV= aeidvrlue;

SV =saponificationvelue;I];ftri=unkno*ncomponenUmsterial

Refining steps that are started from CPO refinery

till

distillation step

in

Figure

I

above are intended to separate

the

impurities of CPO

(gum,

trace metals), reduce _{of ;} pigments, odors, short carbon chain of C6

till

C14 fatty acid (as the experience CPO contain trace C6-10 in the light end product of distillation process), Fractional distillation

In this manuscript is discussed priority the results of this study'in the end step of the refining Hydrogenated Crude

V

1895 S (HCV 1895 S) to produce stearic acid super

V

1895 S through a single fractional distillation column

in

Figure 3which

is

equipped

a

packed of structured packing and falling

film

reboiler [6]. The using this column rvill be obtained the better saving of

aldehydes, ketones,

iodine value

(through hydrogenation and distillation) to provide of fatty acid feed quality

(HCv

1895

S in

Table

2

below) that refined in the end step, in a single fractional distillation column (Figure

l).

Each step affect to the each others, agreed also by the researcher [8].

energy

consumption, equipment, operating cost, flexible and product quality compared to the using of

two

fractional distillation columnsthat utilized trays and

live

steam (Figure

4)

tl3l.

This technology in Figure 4 was mostly used in Indonesia since 1989, in oleo chemical industries.

I 10.104--i7J7 IJDT-IJENS {!) Augast 20ll UENS

ITN

[image:2.612.147.361.145.455.2]

--lntemational Journal of Engineering & Technology UET-UENS Vol: I

I

No: 04

\recuum rystem Cl6purge rslight end

V 1895 S asside product

Frsn* akier of

Sottorepro*mt

orresid*e

[image:3.612.46.240.113.268.2]

D

Figure 3. The refining of HCV 1895 S by a single fractional distillation column

Please compare this new technology in Figure 3 above

with

the

old

one

in

Figure

4

below. Refining of blended fatty acid that content

of

at least

two

main

fatty

acid

componentswas

usually used

two

fractionation columns.

The

l't

colurnn

is

used to separate light end and 2od colurnn is used to separate

the top product with bottom product. Light end contain any substances

or

impurities which have the lower boiling point than boi-ling point of the main product in 2'o column (the side or bottom product). The bottom product has the higher boiling point than the boiling

point

of

the

side

product

in

the

same column. Separation

of

the light end

in I't

column and bottom product

in

2od column affect much better to the main products quality.

.[ehlCJ" Quality of feed

]ICV

1E95 S

Vacuum pressure fractional distillation

is

applied in this study as done for distillation because of fatty acid included unsaturated bond inside are so sensitive for oxidation

tl3ltl4l

(whichis so influence into the bed of fatty acid color and odor). This is also according to

the reseachers

tl-3lt9l.

Unsaturated bond in fatty acid is more sensitive. Ifunsaturated bond is higher in fatty acid,it's easier to oxidize [10]. Prevention of fatty acid oxidationis mean to prevent the increment of fatty acid iodine value or unsaturated content, colors and odors.

It

is mean also control closely fatty acid quality which is made"

In

this

research

wasV

1895

S

quality" A researcher explained

in

his disertasion: reduction of bottom temperature of column can reduce stearic acid iodine value or unsaturated content or vice versa _[18]. Fractional distillation

is

shown

in

Figure

3

above is intended to reduce unsaturated content of stearic acid

C16" Separation

of

oleic acid Cls-1

in

the residue of single fractional distillation column

will

reduce oleic acid (C1s.1) content in stearic acid Clsas a side product"

It

is

mean the lower color and odors

in

stearic acid Clsor

V

1895 S. Reduction of fatty

acid

iodine value,

color

and

odors

is

not only

can

be

done by hydrogenation priority, but can be done also through fractional distillation process

to

achieve

the

lower point. How it can be done?

Tab!* fu Quality :*aadsrd o f _*gg{i$ ecid. s up e* V I B 9 5 $

FattS' o*id comy o s itioa,

$i'+-Jw)

Arr]lrditr'rane*

< ctr4

clf

c:6-t

c1?

c!8

cl8-I

C}8.]

C:O

0;5

lorrimus

I0.0 msriuurr

9fi.{ luinillu.m

s,44

artlmuu

cI0-l

fiqgs6; flo I o _{fi fir[ilfl} $:andu da, J 005 Figure 4. The refining of blended fatty acid through 2

fractionation columns

Met*iaX(ltl

C14 CI6 q:8

Clg-l

C30

Seh

Remark*

Quality

rtatus

Status

-$qur*E;

fforo

$flslIs

C*aml *da,261 5

Unsaturated content of HCV 1895 S is higher than the maximum standard (see Table 3 above), because ofit value is over than O.l5 Vo. So

it

has to be reduced

till

meet the standard, Reduction of C1s-lamount

in

C1s is also decrease of arachidic acid (C26) composition and the others impurities that have the same or higher than

stearic acid C18 boiling

point

which

is

so positive influence

to

the

V

1895 S iodine value, unsaturated content, color and odors,

to

be lower. This

will

be

influence to the lower production yield

of

V

1895 S

absolutely, but hopefully with the better quality

V

1895

Check tl.e troruogenous feed tank

sample; GC, !\r and rclor

Appliad tlle main caemting co*&trs** t* *.:in5!e tellmr::o:erd remallised om 8O 96 cf Y 1895 S

gm&xt*teis de.ters*red

Ttre rtain oPer=iing cenditia* are detemine* and Fredict ba3€d on tl.e ccmPo:iticn (GC) of feed. pu.ge, side and bottamProdircts

*e _Pr*dicted

Dislillate a' 189f $ PuitY conttol

Reduce side stream &aw off rste

Stored as ttrc in rpe* V 1895 S in fhe fiael

lntemational Journal of Engineering & Technology IJET-IJENS Vo1:

1l

No: 04

S

than

HCV

1895

S will

be

achieved' The above question is answered'

Operating conditions

of

single fractional distillati,on co'lumn

ias

tobe determined and predict carefully beforeby Roult's Law [5][16]. Oleic acid content.Cls-thad

toie

a main consideration

in

this study'

It

is so sensitive

to

the oxidation and heating' Increment of unsaturated

content

or

iodine value

should

be

protected, should be lower in

V

1895 S' The prediction

Lf

the single fractional distillation column operating conditionsis done base on the capacity and column characters (the pressure drop on the top, bottom.and feed tray location

of

the column), feed compostuon

HCv

friSS S, product composition

of

V

1895 S and residue

produit

composition

is

predicted'-.{ctual application

of

this prediction

will

change a

little

bit depend on the actual product quality

is

made' The

2" Method

Semi

trial

and error method

is

used

in

this researctr'

Operating conditions are determined, predict first-and uppty

to-*".t

V

1895 S specs' _{The glalClnC.is fone} u'"lorOlng to the actual

tetoltt

V

1895 S

is

obtained' based

oi

it

quality standard (priority

it

composition'

changing

have

to

be

predicted

and

make better

;;ft"?

to the quality standard' The understanding of fru.iionuf distillation, physical and chemical properties oi th" tobrtur.e, e*pJti"nc" in this process and filling

t"urr-ftur"

the big conffibution to do the changing of

tfr"

operating conditions

tl{'

The

-. operati^ng "orOl,iont arJ determined

and predict

1" for

807o

proJr"ri",

yield of

V

1895 S according to the specs- of

V

rasS S composition to get

in

specs and the higher reflux rate

in

ihe

single column, according

to

C13-1

ptop.tti"t

that so sensitive to theoxidation and heating'

it.'trigt

reflux rate has

to

be made as

it

value is

;;hi";."d

on the actual 807o production

leld

of V 1895

S or higher, that's limited by

V

1895

-S composttion'

*rut*u',"4'"ontent,

colorar; achieved on the actual operating conditions are applied., to^ get the higher yield. What are the suitable conditions?

unsaturated content) and production yield' See Figure 5

b"lo,". Proc"dure of anaiysis refers to AOCS Ce l3e-Oiana

fg

l-64 to do iodine value analysis of fatty acid

"f."

eO6S

1-62 to do fatty acid composition

analysis t4t.

Product:V1895S Ilurit]' : 90 i'b minirrum

C:s-t : fi,15 0,6maximum Crc : 1O -qio maxirctr'

Figor.

s=u.ti;;uto#

"or

and quality

v

1895 s as it standard

Intemational Journal _{of Engineering & Technology IJET-UENS}

vol:

_I

I

_{No: 04}

3.

Results and Discussions

T-r_rPp

,l

intended to separate stearicacid (C1s) super

uV

1895 Sandfarty acid residue C1s_2s of the feed

UiV

1895 S to _{reduce unsaturated content}

of

V

lg95

_S. lhere is no light end draw off in this study because of color (not shown here), C16 and C1s of HCV 1g95 S is

in

specs. The final quality

of

V

1895 S

is

shown in Table 4 below. The off specs one

V

1895 S in the final storage tank is caused _{of by production yield increment} over than 87 Vo (see Table 5 and Figure 7 below).

1S

I+h}fl.*" Unsaturated content o f HCV I I 9 5 S and.

\r

1 895 S (96:*rsr)

9S,06 \r1s95

S

0.s9

1"12

!S

.Qgs.r.;5g;

f'lora

$mCr{s S&fil{n{dg, .?00i

The results of,

this

research show that unsaturated content

in

this step came down to beaverage

of

0.19

Vo(based on Twin _{River's analysis) or iodine value of}

\/

1895 S came down ro be average of 0.12

gr l2fi00

g. Comparison

of

unsaturated content

Clg-l

of HCV 1895 S and

V

1895 S can be seen in Table 4 above"

Actual color of

V

1895 S is in specs, but not shown in Table 4 above, discussionis centered to the unsaturated

iEl-l

rrra,

34.r-r45

i$

F€€d"

HgV

1895 S

CI4

O,

cl6

?",6

fl.?6

cI

I 980.5

98.S9

ci&l

].-l

0-11

c:0

9,:

0.9?

total 999.7

l{0.0

iliii

iir*

*t*

:63-X64:9.

trB-t

>ff,

tr$-1. C30 are .lPees Feed

cl8-1

> C18-l is

content which is off specs. See inTable 3 and Table 4 above.

The operating conditions are determined and predict,

can bee seen in Figure 6 below.This prediction is made base

on

the fatty acid

compositiononly. please, compare this one with the actual operating conditions in Table 6, in discussion 3.3.

eoffdsrr:rer

Li_Eht Eud

lnol

rs'ei-e]rt

1',) e

35f

184

c14

0.{0

cx6

]..05

ct

E

0.4_i

C,.0S

76.S0 3fl.08

total

1,,50

to0.0s

ri.r

l895

_{S ?i,f*ad]}

s.8 x9 98.S4I s.s4 o,30

totstr

?99.?6

I00.0tl

cI6

6_55

cl8

?!1.}0

cl8-r

ff.33

c30

*.53

cls

c!3

ct8-1

ct0

o 18s.86

I.9S ?.6$

s.g5 95.03

x.ffo

3_ E3

tot,sl

EgS.4O

IflS.8

Figure 6.The operating conditions design forthe providing

ofHCV

1895 S by a single fractional distillationcolumn

Il{)40.+-3737 tJEl,ltUNS @ Augusr20II IJENS

[image:5.612.60.524.375.687.2]

lnternational Joumal of Engineering & Technology UET-IJENS Vol: 11 No: 04

3.1.

How

to

minimize unsaturated

content

in

V1895

S?

10

Based on Table 5 and Figure 7 below no doubt at all that

Cl8

purityis over than 95 7o, althoughv 1895 S

production yield are (80.0 - 95'0 %). This is caused by

bt6

feed is lower than

I

Va (Table

4

above).If C16 amount

in

the feed

HCV

1895 S

is

kept as

is

in

V 1895 S feed and no

light

end draw offor total reflux in this system./study, ClS purity

will

not be lower than

90 7o wlw. This

also affect

to

the

bigger C16

concentration

in V

1895

S

that can

minimize unsaturated

(Cl8-1)

content

in

V

1895 S, the others components too, C20 and unknown (Unk) (in Table 5)' The higher S production yield of

V

1895 affect to the smaller C16 content and the higher C20 and unknown relatively.

It

affected

to

the

off

specs unsaturated content

in

V

1895 S.

It

can't be allowed. Please, see

also

both

figures, Figure

7

and Figure

8

below'

s7

0,3

5

99,.13

1.1

5

9?,58

0,16

0,11 0,f s

111:

0s-1.0 6.8-0-9

In *pecs

3rr specs

$ff

sprcr

0"04

0,0:

CIJ6

oJ3

8?"0

s3$

s*foh+Eff.ectof,*B*if,:oati:omgreductitr:,xi€K*]s#wr,ra{a.ratesccnlerr1oflxlEEs$

99

fl

ss.:

E99

:

_{3 91"5}

@

96.J

4

fl"39

1,Xl

97 Sawqe: F/ara Sqrtt'ifs

C]e*ind+. lS$J

100

99"J

9d

95"5

0.11 95

off

[image:6.612.389.577.516.634.2]

The influence of the reduction of

V

1895 S production yield on C18-l content in

V

1895 S and reflux rate in Figure

7

can be used as the evidence

to

support to state; reduction

of

V

1895

S

production yield

will

reduce unsaturated content

in

the

main

product' Reduction of

V

1895 S production yield is cause of the

increasing

of

reflux

rate which reduced the

BT

of fractionation column

(in

Figure

9

at discussion 3.4)"

The same thing that had been done by a researcher to reduce stearic acid iodine value or unsaturated content in stearic acid distillate; by reducing BT of distillation column

[18].

The

reduction

of

BT

affect

to

the reduction

of

evaporation rate

of

unsaturated content, reduce

it

amount

into

V

1895 S,

of

course also the other components. This is according to the distillation principles

t5ltl llt17l.

Figure 8. The influence of

V

1895 S production yield

on C18-lcontent in

V

1895 S and reflux rate

*o rbditryfifd tJ lti [!gJE _$ii

Figure 7. The influence

ofV

1895 S production yield

on C18 purity in

V

1895 S

Separation of amount C18 into fatty acid residue (see

Figure 5 above) affect to the lower amount ofV 1895 S.

Reduction the production yield

of

V

1895 S. This is cause of C16 amount ratio to the total amount of side product

V

1895 S is bigger. Finally although without iight end draw off, color of

V

1895 S met the quality standard (not shown in discussion). So the decision not to draw off light end is the exact consideration in the beginning of this study, one technique to minimize the unsaturated content or not reach 0.15 Vo. The ratio can

be

changed depend

on

the changing

of

V

1895 S

production yield. So in this study reduction of

V

1895

S production yield is also the other technique to control or reduce unsaturated (C18-1) content as

it

specs (see

Figure 8).

1.8

? 1.6

c

cl

> 0.8

:

0.6

E 0.4

UO

-0.2 91.J8)

*.l* Production yield vs Reflux rale

---*- Production yield vs C18-l conrcnt

p.od,iJtion yi"ro ,li$ rsss s i&i)

I I 0 104--1737 Ll U I''lJ IjNS (cl,\u gu sl l0 I I IJ E^-S

@

International Journal of Engineering & Technology IJET-IJENS Vol: I 1 No: 04

-1,i.

Prediction

versus

actual

V

1895 S

production yield

;

::-:uon

_of

V

₁₈₉₅₅ unsaturated content was done in

,: . ,:.rdy.Theproduction yield of

V

1895 S is tried first

r.

'-:

asthe design and prediction

of

the operating

. ,::::rons(Figure 5 above). ReJlux rate is also made so

.:-,

rgh

in the beginning, on the intervall5OO

-

1600

.;

-,- _This

reflux rate

is

_intended

to

_suppress the

:

.:,:iation rate

of

unsaturated component as low as

:..,::le

because

of

the boiling point

of

unsaturated

.

-.

.cid Cls-1is lower than C1s boiling point[16]. This

-:

l-r

rate is made also because of the amount of C1s-1

:

---: feed HCV 1895 S is so small (0.23 7o in Table 4

-:,-,:r.

also the other components (Table 4). On the -

'::

reflux rate,

it's

more

difficult to

be separated

:-l

,rnto the bottom product

or

residue (Figure 5

-;.,r3). Of course the amount of Cra

will

be bigger in

--.

::sidue.

It's

a risk

of

a high reflux rate. The feed --.:,s

ried first

_{onl.000 kg/hr. These predictions} are

.::

according

to

the experience

in

the

fatty

acid

'

_{.:..ation and fractionation in the previous"}

'-.

:roduction yield

of

V

1895 S

is

then increased

:ii-)'(as

shown

in

Table

5

above) after fractional -

.:-iation

conditions

_werestable

for

80.0

7o

r-:,:jction

yield. This simulation is done for knowing

--.

.;rfluence

of

the increment

of

V

1895

S

on the

-::.ment

of

unsaturated content

in

V

1895 S. The

':,

_{-.:s rvithin Table} 5 proved the prediction above. See

..

Figure

8

below.The higher possible production

..:

can be achieved but at the same time unsaturated

- t:,3nt is closer to the maximum point of unsaturated : _--,ent and finally of specs on

9l

Vo,93 % and 95 Vo

:: -,:.rction

yield

(Table

5

above

and

Figure

8

:t.:.r').The in specs one ofV 1895 S should be made in ,-

:

research.

How

many

percentthe maximum

:::'r.rction

yield

has

to

be

achieved?

How

many

:r::ent

the safest production yield?

It

has to be met.

-::

rend

in

this Figure 9 can be used to predict the

,

--"ble _{production yield of}

V

_{1895 S to provide}

.:.

rodine value and unsaturated content of

V

1895 S -- Table 5 above) came up to be higher. This is cause

:.

*nsaturated component is evaporated more together

, :.

\/

1895 S as the impact

of

the increment

of

V

-.::

S production yield and/or decreasing

of

reflux

:r,:

see Figure 8 above). The composition

of

C20 is

: :-ler

also, caused

of

the

same reasons.

This

is .: - :rding to the distillation principles t5l t I 1l I171.

i.3.

Actual

versus

predicted operating conditions

-:.:

reduction of

V

1895 S production yield mean the

-:

:3mperature of the fractionation column is adjusted

.-.rer.

This

temperature

could

be

determined and

::::rct

practicallyby

Roult's

Law but

have

to

be

:

_=l-red actually through this research. The predicted

11

The

off

specs one stearic acid

V

1895 S

in

Table 5 [image:7.612.299.502.415.536.2]

above is sent back the other feed tank as described in Figure 5 above to avoid the higher unsaturated content in the same feed tank and in the next

V

1895 S will be produced.Based on data in this table,

it

is so clear the influence of the higher production yield

V

1895 S to

the higher it unsaturated content. See Figure 8 below, Base

on

this figure,

V

1895

S

production yield is predicted 89.5 Vo

to

achieve

O.l5

7o unsaturated

content

in V

1895

S

(point

A).

So the

safest

production yield should be under 89.5 Vo. Based on this

predictionv

1895

S

production

yield

should be adjusted to be lower than 89.5 % (see Figure 9 below).

It

could be 88 Vo or 89 Vo. Whyit can be happened?

It

has to be considered strongly the unsaturated content should be achieved first lower than 0.15 Vo.

lt

is very important

to

meet the specs

first.

If

the production yield is kept constantly as is (89.5 Vo), therc is a big possibility that

V

1895 S will be off specs.

Beside

this

reason

the

stability

of

this

process is considered strongly.

It is

not

guaranteed

all

the instru:mentations

have

the

straight

line

response,

according to the experience it's normally has the small fluctuate on the same amplitude.

,5, 80 *5 90 9' t00

lro&rtionyi{d of Y lS95 S G6)

Figure 9. The influence of

V

1895 S production yield on unsaturated content in

V

1895 S

The actual average production yield is achieved 85.0

Vo. Why is it different? The production yields in Table 5 are not straight since the increment is done, It is done slowly, step by step.It so logic the actual production yield is lower than the predicted one.

one

is

used as a main guide and very important to conduct this research. This prediction was limited by unsaturated content

or

double bond

of

C13-1

in

the quality standard.

If

the consideration was based only of C18 purity (see Table 3 above),

V

1895 S can be draw

0.45

3 0.1

; 0 35

6

o.r

6 0?5

6 ^-i n r{

:

0.r

5

o.o5

B (91, 0.19 !

a{s9.i,0.ri)

lnternirtional Journal of Engineering & Technology IJET-IJENS Vol: I

I

No: 04 t2

off 98 Vo or

it

production yield 98 70 as

it

composition in the feed but actually unsaturated content is off specs

when

it

production yield achieved 93 7o and95 Vo. So

it

must belower because

of

timited

by

unsaturated content

in

the quality standard.

It's

mean also the

actual operating conditions

are

different

with

the predicted operating conditions. See Table 6 until Table

9 below.

The average conditions for the production yields 80 7o,

87 Vo and 93 Va (Table

6)

were the average

of

the

simulation data on the same yields from Table 7 below. The data for 93 7o and 95 Vo production yield didn't take more because

of

the

conditions were

up

set

already.

The average conditions for the production yields 88 7o,

89 Vo

in

Table 10 were the average of the simulation

data on the same yields from Table 11 below.

Table 6. The actual operating conditions to produce V 1895 S of l't test

IJroductron TP"

mbar

TT. {

C

SPTT.

FT, o

C

_BT, o

C

_RR,

U:t&

_E},

mbar

_Remarks

v'ipld l9,ir\ o _fl

80.0

19.3

.I3X.S

l4j{.4 231"4 ?66"6 1.1-1.1 50-J4

Cg-1<015 9',;

sl-o

:J.8

ll4-i

t43"S 136.8 :6S.0 1.09-1.1

50_Jf

93.0

27.2 :03"8 ?45.1 138-9 t?4.0 0.Sl-0.9

50-51

c8-1< 0-15 f.i C8-l> 0"15 o;';

fl8-1> 0"15 o]$

95-0

?5.5 lBl,I ?44.: ?t8.9

I

?-1.$

0.7S,0"S3

50"0

Source:

ffara {6g;ffi

_C*s#i11&" JOU

j

Notes: TP

:

top _PreB$uE; TT = top temperatlue;

SITT:

aide product tlsy temFerature;

FT:

f*ed temperstue;

ET:

fo1t1g;g1 tenlperature; RR

-

reflus mte ; BP

:

bottom pres$ure

Table 7. The actual simulation ofthe operating conditions to produce

V

1895 S of

l't

test

Production

TP,mbar

TT,DC

SPTT,

FI,{C

BT,sC

}-R,E*r,h

Bp,mh4r

Iroduction TP,mbar TT,DC SPTT, FI,{C BT,sC RR,E*iih BP,mhar

Remzrks

yietlf"..t) ,..

oc

80.0 l9J

t32_S

:44.4 :3?.4

256"6

1.1-11 5g:54

Cts-l< 015 0/6

s0-0 80,0

The actual operating conditions on 80.0 7o production yield has a small different than the predicted one (see

Figure 5). The actual suitable prediction of production

yield

was 89.5 Vo (discussion

3.2

above).

It's

so

different also than the prediction was done only base

on the C18 composition in the feed. Feed temperature can't be reached because of the limitation Oil Thermal Heater system capacity

(on

850-900 kgs/trour feed rate), to conduct heating

in

a heater and a reboiler of fractionation column.

Reducing of TT and SPTT trends that almost constant are according

to

the simulation

of

Roult's Law (not shown here)

I5l.

SPTT trend

as

is

due

to

Cl8

concentration

is

almost constant around 98 Vo on the same pressure

27

mbat. Reducing

of TT is

due to increasing

Cl6

or

reducing C18 composition

in

the

c.8-1{O-t5 9d

c.8-1{8-15 9/a

cB-:{

*-15 9t *8-:{0-1"5 *6 c*-14 0.1,J % c8-1> 0-15 $6

cg-1> 0"15 BL

tr8-1> 0.15

}t

total reflux of light end on the same pressure, around 25 mbar, as affect

of

V

1895

S

production yield increment

or

decreasing

of

total reflux into

the column,

This

increment

is

cause

of

reducing C15 composition in

V

1895 S that is added major from light end and also C18 composition increment that is added major from bottom product. This increment

is

also cause of the increment of BT that is effect to the higher C18 evaporation so

it

composition

is

higher

at

the production

yield

87

Vo (see Figure

8 in

the next discussion 3.4). [ncrement of production yield (priority 93 Vo and 95 Vo) is cause of the increment of BT that is so effect

to

the higher content

of

Cl8-1,

C20 and

unknown components, unsaturated content is off specs

(0.36 and 0.38 Vo). This is also so affect to the lower C18 content in

V

1895 S. That is why both the last 2

actual operating conditions in Table 6 can't be applied

19"5

]]J

-0 344,2 13?.6 ?67.0 1-1-1.:

51_54

19-1 23t.6 :.{.1.6 ?3?3 266.2 1.1-1.19

49-54

87,0

25.8 ?14.5 f,43.6 :36.S 268"0 i.g9_1"1

5S-53

s7.0

21"6

X14-7

?44.0 J37.0

?68..+

1.0S-1.11

51_51

B?"0

?6.0 214-3 t4t.I 236.6 ?67.6 1.09,1.1

49-52

93,0

:?.:

203.$ 145.1 :38"9

2?4-1

0.8.1_0.9

50_51

93,0

27.25 ?03"7 :44.9 :38.9

??3.9

0.8$_0"39

50-51

9t"0

ts.l

:04-5 J44-5 :38"9

]?i

.83

50-51

Soruce: SIora _{SqU*;g SftS4i*f{k} 3

I'{ote: IP

-

top prersurs;

TT:

tcp t€nlperaturB; SPTT = side pro'duct ua}'trr.$erertue;

r-I:

feed iemperaft$e;

ET:

Itltgm

terRperature ; RR = r,eflux ret* ; BF = boitorn pre*:,r:re

International Journal _{of Engineering & Technology UET-IJENS 11 No: 04}

,he next test, but the higher yield should be pointed

.,

shown as discussion 3.2, based on Figure 7. The

:

,"iuction yield 88 and 89 Vo are met graphically and

89.0 ?3

J6

:1?- ?44-

246_

ll& 145

24"7

the

operating conditions

Roult's Law, next

has

compared how precise it.

have

to

be

predicted by

to

be

tested actually, and

-

":le

8. The predicted operating conditions to produce V lg95 S of l,ttest

ion

TP,

mbar

TT, o

C

_SPTT,

BT,{C

_RR,

,

mbar

R

r{d*lT)

==

..

,

,

oc

ss.0 2336 217-

?44

118 ?45 ?47

264 9t (beee on

ligure

9

of

I st tes$ C8-1= 0.14 +6

{

CI"15

flo, (base on Frgule

I

?s3-

:.01-1.s.1+ 264

cflsttest

\ote:T}=tgpPr*sure;TT:toFtempi[etue;S}T:=*i*uperEtue;BT=

hSffnS

tenper*true

; RR = reflti:r rate ; EP = bottompre:ssire ;

;

base on the highest agtual 1.ecu11111Irregflrre

l:ble

9" The predicted of

V

I 895 S quality on l,t tesr

-i

c:6

18-1

C?S Reflux rate, ductio* yield s

.

?

0,76

99.6? 0,06

0"32

0.30* -

1.0I-1.04+

89$

In

specs

Table 10. The actual operating conditions to produce

V

1895 S of 2nd test

Production

TP,mbar

TT,oC

SPTT,

m

rield (Va)

25.8

214.5 243.6

236.9

268.2

LOg_Lts C8-1= 0 < 0.15 7p (base

on Table 12)

23.2

229.5 242.7

242.5

265.5

1.03-1.1 CS-l= 0.02 <0.15 Vo,

base on Table 12

\ote: TP = top pressure ; TT = toP temperature; SPTT ₌ side product tray temperature ; _{FT =} feed temperature; _{BT =} bottom temperature; RR _{= reflux rate ; Bp = bottom} pressure

Table I L The actual simulation of the operating conditions to produce

v

1 g95 S of 2nd test 5A-52

50-52

16-0

t14-S :44-0 :37,O :69-5

1.09_1-ld

51-53

16l

I14.2 243.8 :36,8 t6?.9

1.O9-1,14

49-i1

88.0 83.0

89.O

89.0 s9.0

?3-l

iJ .J

C8-1:0

<0.15 9.5

C8-1:O<O.15li)

2?9.i Xtr3-7 342"5 265,5

t

-O3-1"1 50-it

CB_l:

O"0-?

<fi_l5

9.6.

:t$.g f4"?-: 24?"3 :65.8

t-03-1

,l

50-11

CS-t:

0-01 < 0.15 9.a

?3fr-1

t41"9

2.7 t65-3

1"03-

J0-t3

CS-1: O.01 < 0-15 9n

Souree; Floro _{fi4ggiitg "G&emUgdg} ,OOJ

Note: ?P

:

_{toP Pre$u.re; TT}

:

_{top ternperehne; $PTT}

:

side product tra!' ternperature;

FI:

fe.ed ternperature; BT

:

l:ottomtemuer*ttre: RtrL: Teflux rete :

}lp

: hcttomorsr.*.|

S ource: F lo ra S awit aChemindo, 2 00 5

1 I 0r10.+^J737 UEI'-IJENS @ Augusr 201 I LIE^-S

@

l3

50*

Remarks 88.0

89.0

vield

(%,)

o _C [image:9.612.52.508.552.674.2]

International Journal of Engineering & Technoiogy IJET-IJENS Vol: 1

I

No: 04

Table 12. The acrual V 1895 S quality of 2nd test

cls

_rate,

1.09-1"15

TS

9S"9,7 _1,CI3-1"I

3'4' Mechanism of

the

changing of

the

main temperature in

the

manufacturing of

V

_{1g95 S}

C1

Ifuk

89 CI$0

0,ff1

180

,2

zta

EE

260

t-E

250

is

:ro t c 2i0

T* rrn .e e :10

1 E roi:

ig

rco

-

_lso

The changing of the top, side product hay and bottom temperatwe

versus

reflux

rate

in the

single fractionation column (in this research) can be seen-in [image:10.612.118.566.140.192.2]

8qs

9*0

100& u!9

,!a00

13oo Reflq ntekE/hfl(

Figure _{10. Mechanism of} the changing of the main temperature to produce

V

lg95 S in a single

fractionation column

4. Conclusions

Unsaturated _{content of}

V

_{1895 S is higher than0.l5 Vo} 11"_a

ft"

producrion yield of

V

l89ts

is higher than 90 Vo.

Based on the actual operating conditions to meet the safest unsaturated _{content (lower than O.l5 Vo)}

in

y

1895 S finally is found graphically on g9.5 Zo V iB95 S

production yield. Practically is found gg _ g9 _Vo

V

_lg95

S production yield. The light end has to be total reflux and unsaturated content of

V

lg95 S is controlled by the adjustmenr

of

V

1895 S production yield on rhe

found practical or actual operating conditio;s

4.

Suggestions

[image:10.612.117.316.285.409.2]

It's

suggested _{strongly to improve the OTHS capacity} tg q:t

tlg

higher FT/capacity and

V

1895 S production yield. The increment

of

FT

will

be cause

of

tfre Rn increment

that

can

reduce

the lower

unsaturated content.

Figure

l0

below. The changing temperature above happen whtle total reflux of lisht end

in

_{the single fractionation column as Figure 3} above.

Reducing ofreflux rate or increment ofthe production yield

V

1895 S is cause

of

the top temperature (TT) decreasing, _{relatively no changing of the side product} ffay temperature (SPTT) and the bottom temperature

(BT)

increment

of

the single column,

on

the same

heating in the reboiler.

This mechanism

is

so different with the temperature mechanism

offatty

_{acid blended fractional disiillation}

as

Figure

4

above. According

to

the

experience practically, the total reflux of light end is cauje of TT and BT decreasing

in

lst column and the increment of production

leld

distillate product

in

2nd column is cause

of TT

and BT increment

in

2nd _{column on} the

same heating in _{the reboiler. This is according also to}

the reference

Il

l].

The actual operating conditions are found atTp (23.2 _ 25.8 mbar

), TT

(214.5

-

229.5 "C), SPTT (242.7 _ 243.6

"C),

FT

(236.9

_

242.7

.C), BT

(265.5 _ 268.2"C), RR (1.03

-

l.I5

mt/hou0,

Bp

(

'50

_

52 mbar) and feed rate 850

-

900 kg/hour. It is found base

on the predicted operating conditions

at

W

(23.36 mbar ), T T

Qfi -

218 "C), SPTT (244 -245 .C),

FI

(246

-

247"C),

BT

(263 _{-264C), RR}

(

l.0l

_

1.09 mVhour),

BP

(50

_{mbar) and feed rare g50}

_

900 kg/hour.

Feed temperature

is

actually found lower than the predicted one because

of

the limitation

of

the oil thermal heater system (OTHS) capacity.

It's

suggested strongly

to

improve vacuum system capacity so

it

can be achieved 3 -5 mbar Tp in of the single column to improve the total performance of the single column

for

this

special product. The highest vacuum pressure _{2 mbar is also stated by [9] to get the} better results

of

fractionation/distillation products.

110i104-37-]7 III:1,IJINS @i Augusr 20lt IfjNS

@

International Journal of Engineering & Technology IJET-IJENS Vo1: I

I

No: 04 15

-

!";I.rences

:::-:--:.::.

E.,

1985.,

"Oii

Seeds Oils and Fats",

-

l'd

Edition"

B.E

Oil

Publishing House,

-. ::-.:r

R and McPherson, W", 1979., "Fractional

- -

.:-on", JAOCS,

Vol.

56

:743A-

745A :

-:,::--.nn,

R."

Demmering,

G.,

Kreutzer,

-

.-:3man,

M.,

Plachinka,

J.,

Steihrner, U., -:

-

Fatty

Acid",

Henkel KGaA, Dusseldorf,

;:=:-.

_{Republic of} German.

*

l

- .-. F.,

2006.,

"Official

Method

And

;.-,rmended

Practices

of

the

American Oi1

I-::--srs

Society",5th

Edition,

2nd

Printing,

-

-,-S Press, USA.

::-

..-

8.L,, 1989., "Applied Process Design for

-

-.

::;a1 and Petrochemical Plants", Volume -2,

-'-

::riion,

Gulf Publishing Company, Houston.

:. :

-nd

Hahn. GmbH,

1998.,

"Fatty

Acid

:-.:-onation",

_{Flora Sawita Chemindo,} Medan, : -:-:sia

-

-

-

r"

Sawita

Chemindo,

2005.,

"Production

:

-:::rg

Control", Medan, Indonesia

;-:.

E.. 1979., "Interrelationships

in

Fatty Acid -*-,::ssing", JAOCS, Vo1.56; 7 45A-746A"

:r:irnann, A.

E.

S.,

1990.,

::=:-:onation/Distillation

:

Improvement in

-.- .:).

Efficiency, Energy and Environment

-.::;ts",

Proceeding

World

Conference on

.

..

Chemical

into

21" Century, Kala Lumpur f.:.::3:'i. S., 1985., "Oils and Fats

of

Food", UI

:::...

Jakarta.

I

",::aphies

Muhammad Yuuf. Ritonga was bom in

Sipirok, Tapsel, North Sumatera province, lndonesia, on August 19,1962. He studied and graduate in North Sumatem University since 51 degree till obtaining his doctor.

He had being a lecture since 1989 in Chemical

Engineering Deptrtment, North Sumatera

University. He has 20 years of special field

;,ri::-.r: oleo chemical industry since l989in troubleshmting, u: : ;- : :i::i. start up, commissioning; oils and fats pretrcatment

;iL- :-:-:. glycerin purification, fatty acid dry fractionation,

' :-;::;:::. distillation md fractionation. His experiences related

"" : :l {ibhawana Utama (now called PT. Eco Green as a Fatty

[11] Muhammad.

Y. R.,

1996., "Practical Distillation

tr',

Study

Progam

of

Chemical Engineer, Faculty

of

Engineering, University

of

Sumatera Utara, Medan, Indonesia.

ll2l

Muhammad.

Y.

R., 2009., 'Fatty Acids

of

Oleo

Chemical Industry",

Proceeding

National Conference of Chemical Engineer, University of Sumatera Utara, Medan, Indonesia.

t13l

Peter,W. Faesler.,

Karl

Kolmezt.,

Wang SengKek., 2004., "Revamp Strategies

for

Fatty

Acid

Distillation

Section

In

Oleo-Chemical Plants", Sulzer Chemtech, Singapore.

[14]

SulzerChemtec. 2006., "Separation Technology for the Chemical Process Industry- Oleo chemical

Step

Into

a

Growing

Market

with

Sulzer Chemtech : 12".

ll5l

Thomas, H.W. 1985., "Bailey's Industrial Oil and

Fat Product", Volume

3.

Jhon

Wiley

&

Sons,

New Yorlc

[16]

Unichema lntemational. 1998., "Fatty Acid Data

Book"

2nd

Edition,

Unichema, Republic of German.

[17] Van Winkle. M., 1967., "Distillation", Mc. Graw -Hill Book Company, New

York

[8]

Yusuf Ritonga. M.,

2010.,

"Optimization of the Providing

of

Stearic

Acid

Based

on

Refined Bleached Deodorized

Palm

Stearin (RBDPS)

Which

is

Stable According

to

the

Quality Standard",

Doctor

Program,

FMIPA,

USU, Medan, Indonesia.

Alcohol and Glycerin Plant) md PT. Flora Sawita Chemido (as Fatty

Acid and Glycerin Plant), He had been done many resetrches relate

to oleo chemical industry ; fatty acid and glycerin products

diversification and modification and design and modification of

operating condition of the specific process in oleo chemical industry, on the plant scale. He also released many mmuscripts on the various science and technical journals relate to fatty acid and glycerin in the terrns splitting of various natural oils md fats, hydrogenation, distillation, fractionation and dry ftactionation of various fatty acid base on various natuml oils and fats. He is the author of book

Distillri Praktis. He planned to release two books (had being edited

till now on) ;"Practical Distillation Prirciples" and "Hydrolysis

Oik and Fats in Oleo Chemical Industy".

/

LEMBAR

HASIL PENILAIAN SEJAWAT

SEBIDANG

ATAU

PEER

REWEW

KARYA

ILMIAH

:

JURNAL

ILMIAH

Judul Jurnal

Ilmiah

(Artikel)

:

Providing

Vegetable Stearic

Acid

Super

V

1895 S

From Hydrogenated

Of

Crude Vegetable Stearic

Acid

HCV

1895 S

With

A

Single

Fractional Distillation Column

:

Dr.Ir.

Muhammad Yusuf. Ritonga,

MT

:

a.

Nama

Jurnal

:

International

Journal

of

Engineering

&

Science

IJET/IJENS

Penulis Jurnal

Ilmiah

Identitas Jurnal

Ilmiah

(beri

/pada

kategori yang tepat)

Hasil

Penilaian Peer Review

:

b.

Nomor/Volume

c.

Edisi (bulanltahun)

d. Penerbit

e.

Jumlah halaman

04111

Agustus

201I

1JENS

Publisher

-

Pakistan

167

KategariPublikasi

Jumal

Ilmiah

, d

Jurnal

llmiah

Internasional

f]

Jurnal

Ilmiah Nasional Terakreditasi

I

Jurnal

Ilmiah Nasional Tidak

Terakreditasi

Komponen

Yang

Dinilai

Nilai

Maksimal

Jurnal llmiah

Nilai

Akhir

Yang

Diperoleh

Internasig/al

TE

Nasional

Terakreditasi

n

Nasional

Tidak

Terakreditasi

tl

a.

Kelenskapafl

unsur

isi buku (10%)

sF

ge

b.

Ruang

lingkup

dan kedalaman

pembahasan

{30%)

70

Jr,

/

c. Kecukupan

dan

kemutahiran

data/informasi

dan

metodolosi (30%)

s&

2t,

?

d.Kelengkapan unsur

dan

kualitas

penerbit

(30%)

te

Je,?

Total

=

(100o/o)

g/,9

Medan,

...(A.

:....!.*.:...*.Qf.*...

Nama

: Prof.

Dr. Harry

Agusnar.

M.

Sc.

Phil

NIP

:

19530817

i98303

1

002

tJnit

kerja

:

FMIPA

-

USU

i..i i1

Reviewer, _-

./

-A

g

Judul

Jumal Ilmiah

(Artikel)

Penulis Jurnal

Ilmiah

Identitas Jurnal

Ilmiah

Kategori Publikasi

Jurnal

Ilmiah

(beri

/pada

kategori yang

tepat)

Hasil

Penilaian Peer Review

:

LEMBAR

IIASIL

PEMLATAN SEJAWAT SEBIDANG

ATAU PEER

REYIEW

KARYA

ILMIAH

:

JURNALILMIAH

:

Providing

Vegetable Stearic

Acid

Super

V

1895 S

From Hydrogenated

of

Crude Vegetable Stearic

Acid

HCV

1895 S

V/ith

A

Single

Fractional Distillation

Colurnn

.

:

Dr.

h.

Muhammad

Yusuf. Ritonga,

MT

:

a.

Nama

Jurnal

b.

Nomor/Volume

c.

Edisi (bulariitahun)

d.

Penerbit

e.

Jumlah halaman

:

International

Journal

of Engineering

&.zc Science

IJET/IIENS

04/11

Agustus

20i

i

IJENS

Publisher

-

Pakistan

16'7

, lV

Jumal Ilmiah

Internasional

I--l

Jumal

Ilmiah Nasional Terakreditasi

t]

Jurnal

IlmiahNasional Tidak Terakreditasi

Medan,..4

Reviewer

2

Nama

NIP

,r,,%,s,auan.u.

si

:

19600618198703 1002

Unit

kerja

:

FMIPA

-

Guru Besar

Biokirnia

-Universitas

Negeri Medan

Nilai

Maksimal

Jurnal Ilmiah

Internasioual

d

Nasional

Tidak

Terakreditasi

E

unsur

isi buku (10%

b.

Ruang

lingkup

dan

kedalaman

pembahasan

c. Kecukupan

dan

kemutahiran

data/informasi

dan

d.Kelengkapan unsur

dan

kualitas penerbit

(30%)

:

l