CONCORD TEXTILE CORPORATION VIETNAM
Nhon Trach 2 industry park, Nhon Trach District, Dong Nai Province
TRAINING REPORT

Name: Nguyen Huynh Thoa
Code: 12117
Position: Poly staff
Day of submit: 21-12-2015

Content
1.
2.

Page

Theory basis....................................................................................................
Process technology of POLY plant description..............................................
2.1 Preparing catalyst and PTA.......................................................................
2.2 Preparing TiO2...........................................................................................
2.3 Esterification stage 1 and 2.......................................................................
2.3.1 Esterification stage 1.......................................................................
2.3.2 Esterification stage 2........................................................................
2.4 Rectification column 1401........................................................................
2.5 Prepolycondensation stage 1 and 2...........................................................
2.5.1 Prepolycondensation stage 1............................................................
2.5.2 Prepolycondensation stage 2............................................................
2.6 Vapour noncondensation of prepolycondensation....................................
2.7 Final polycondensation.............................................................................
2.8 Vapour noncondensation of final polycondensation................................
2.9 EG evaporator jet ejector 2218.................................................................

1 Theory basis
Polyethylene terephthalate (PETP) is made by reacting pure terephthalate acid PTA
and ethylene glycol EG to form diglycol terephthalate DGT which is the monomer of
PETP. The reaction to form PETP is result both of esterification and polycondensation
reaction.
This reaction process include 5 reaction stage:


•
•
•

Two esterification reaction.
Two prepolycondensation reaction.
One final polycondensation reaction.

Physical parameters of raw materials will participate into the process production as:
Ethylene glycol (EG)
Molecular formula

OHCH2CH2OH

Mass molecular

62 g/mol

Boiling heat (at 101.3 kPa)

197.60 0C


Melting temperature (at 101.3kPa) -13 0C
Density (at 200C)

1.1135 g/cm3

Heat of vaporization (at 101.3 52.24 kJ/mol
kpa)
Heat of combustion

19.07 MJ/kg

Ignition temperature

410 0C

Viscosity (at 200C)

19.83 Ns/m

Pure terephthalic acid (PTA)
Molecular formula

C6H4(COOH)2

Mass molecular

166 g/mol

Melting temperature (at 101.3kPa) 402 0C
Density (at 200C)


1.14318 g/cm3

Evaporation (at 200C, 101.3kPa)

5.74

Antimon acetate
Molecular formula

Sb(CH3COO)3

Mass molecular

298 g/mol

Melting temperature (at 101.3kPa) 128.5 0C
Density ( at 200C)

1.22 g/cm3

Titanium dioxide
Molecular formula

TiO2

Mass molecular

80 g/mol


Boiling heat (at 101.3 kPa)

2972 0C


Melting temperature (at 101.3kPa) 1843 0C
Density ( at 200C)

4.23 g/cm3

Esterification
2HO-CH2-CH2-OH + HOOCOH + 2*H2O

-COOH

HO-CH2-CH2-OOC-

-COO-CH2-CH2-

Polycondensation
n*(HO-CH2-CH2-OOC- -COO-CH2-CH2-OH)
CH2-CH2-OH + (n-1)* HO-CH2-CH2-OH

H-(O-CH2-CH2-OOC-

-CO)n-O-

Balance of chemical equation:
PTA + 2EG = DET + 2H2O
DET = PETP + EG

PTA + EG = PETP + 2H2O
Molecular weight:

166

62

X

2*18

X = 166 + 62 – 2*18 = 192
Raw materials wanted to create 1kg Chip:
+ 2H2O
Molecular weight:

166

62

Amount raw material (kg):

0.846 0.32

PTA + EG = PETP
192

36

1


0.187

Since, the capacity of the polycondensation plant calculated to create how much chip
tons per day. Theoretically, there would be 2 mol EG required 1 mol PTA but the process
reaction is actually requires a mol ratio 1.7 – 1.8 only.
2 Process technology of POLY plant description
2.1 Preparing catalyst and PTA
Catalyst

1302
1102

1114

1303

1701


1103

2203A/B

1101

2202A/B
1201

The process line starts with continouns preparation of mix paste of pure EG and PTA

powder.
The pure EG go through the filter 1302A/B then enter the catalyst preparation vessel
1102 together the catalyst is poured into by handmade through a feed funnel. A amount of
EG have calculated with the pre-set of FQI01-02. A certain amount of EG prepare batch
with the right amount of catalyst in a concentration of 2% weight.
The catalyst use for this process is antimon acetate – Sb(CH 3COO)3, which is used as
a polycondensation reaction catalyst. Level in the vessel 1102 give signal to the inventer
LSL01-04 control the agitator 2302.
On the other side, the vessel 1102 is equipped with the coils system as a HTM heated
jacket. The vessel 1102 is supplied the heat by pump 2230 and adjust temperature about 60
– 650C by the inventer TSH01-05 control valve TV01-05.
After the paste of EG and catalyst which homogenised in the vessel 1102 and
conveyed down the filter 1303 to the storage vessel 1103.
After the mass of PTA powder transferred the stored silo 1701, the nitrogen is
charged in 1701 combinate with PTA powder generated a fluidize phenomenon to avoid
obstruction in here. PTA powder is discharged down continously by gravimetric of PTA
powder into the paste preparation tank 1101.
Nitrogen as carrier of the PTA is fed back to the conveying area by passing the filter
1301 at the top 1701.
The quantity of PTA powder is continously calculated and rechecked by the pre-set
value. A quantity of PTA is fed into the tank 1101 by the inventer LRC02-09 will interlock
WQRC02-07 to control valve WV02-07.
At the same, the inventer WRC02-07 will interlock for both FQRC01-13 and
FQRC01-15.
The inventer FQRC01-13 will control the speed of pump 2203A/B to discharge the
mix of EG and catalyst of the storge vessel 1103 feed into the tank 1101.


The inventer FQRC01-15 will control the valve FV01-15 to adjust a amount of EG
feed into the tank 1101. In the case star up, the flow of pure EG feed into vessel 1101 will

be provided by the filter 1302A/B and when the plant is normal stable operation, the flow
of EG will be provided by the amount of EG generate in the process reaction collected and
contained in the vessel 1114.
This process controller how to ensure the feed of mol ratio must exactly.
The mix of PTA, EG and catalyst will be stirred by the agitator to become a
homogeneous paste of PTA, EG and catalyst. Then the paste is discharged by the pump
2202A/B to go into the esterification stage 1 reactor 1201. The inventer FRC02-15 will
control SIK02-11 and SIK02-12 to adjust the speed of pump 2202A/B have how much
amount the paste must provide to the reactor 1201. In the case one pump fail, the
remaining pump must run automatically full capasity of plant.
1118A

1118B

2.2

1104

1105A

1105B

1116

Preparing TiO2
The Ti2O fed into the preparation vessel 1118A from the TiO 2 feed hopper 1702
where EG has already resided before. At here, the mix of TiO 2 and EG are stirred by
agitator to form a suspension. The concentration is about 50% weight in EG. Amount of
TiO2 prepare batch with a certain quantity.
The suspension discharge through the filter and pumped to the pearl mill 2702 by

pump 2710A then enter 1118B. The pearl mill is operating at certain rate given by its feed
pump and disperse the suspension with a certain particle size distribution.
After the suspension passed the pearl mill for the first time and ressided in 1118B.
The suspension will continously pass the pearl mill again then enter the dilution vessel
1104 where a certain amount of EG has already waited before. At here, the suspension will
be agitated and diluted with a concentration about 10.5% weight in EG.

1304

1702

2402

1308


2702
2701A

1401

1202

1501

1602
2204A/B

2701B


1108
The suspension continued pump 2701B
convey to the centrifuge 2402
make the suspension become more
homogeneous and charge into
the intermediate vessel 1105. In the case centrifuge have the problem, the suspension go
into 1105 that it do not go through centrifuge 2402. After passing the centrifuge, the
concentration of TiO2 particles became less about 10% weight in EG.
After centrifugation, the residue of TiO2 bigger particles will be cleaned by supply of
a small flow EG and discharged back into the preparation vessel 1118A.
The suspension resides in the intermediate vessel 1105 in a certain time and passed
throught the filter system 1304/1308 transferred into the suspension feed vessel 1106 by
air pressure. The agitator of vessel 1106 is stirred continuously with a low speed.
One of both dosing pump 2204A/B are normal in operation and will change if meet
problem. The suspension is fed in the esterification stage 2 reactor 1202 by pump
2204A/B. the inventer FRC02-15 will interlock SFRC03-17 and SFRC03-18 to control the
speed of pump 2204A/B how to provide enough a mol ratio and amount TiO 2 feed into the
reactor 1202 already calculate before.
2.3

Esterification stage 1 and 2
1110

TiO2


1101
1203

DEG

2208A/B

2207A/B

1114

Beside the esterification reaction of two reactor 1201 and 1202, the polycondensation
reaction is occur at the same time with a low molecular product. In all control parameter
influence to the esterification reaction, only two temperature and residennce time profiles
influence
direction and decied effective
of both the esterification
1202 temperature. If it is
reaction
1201 but the most important is
raised, the
esterification will increase
and conversely.
2.3.1 Esterification stage 1
After prepare the paste of EG, PTA and catalyst in the tank 1101. The paste is
conveyed into the esterification stage 1 reactor 1201 depend on the speed of pump
2202A/B discharge from the tank 1101.
At the same, the amount EG circulation from the rectification column 1401 also enter
the reactor 1201. The inventer FRC02-15 interlock FQRC04-01 control valve FV04-01
adjust how much amount EG circulation from 1401 required reflux rate back 1201 to
maintain the feed mol ratio.
LIRC04-06 will measure level in 1201 then give signal command to FRC02-15
control the speed of pump 2202A/B will provide a certain amount of the paste from 1101.
Moreover, LIRC04-06 will also control the agitator 2703 in the condition safety.
The temperature in 1201 is provided by the HTM circulation pump 2206A/B with

form the coils system put at the bottom reactor 1201. TRC04-03 will measure the
temperature in 1201 then give signal command to TRC04-07 control valve TV04-07 adjust
the amount heating oil of the feed HTM into the HTM circulation pump 2206A/B. The
flow of HTM to 1201 is liquid HTM.
The temperature of jacket 1201 and 1202 is provided by the HTM evaporator 1601
and TRC04-44 measure the temperature outlet of 1601 control valve TV04-44 adjust
amount heating oil of the feed HTM into 1601. The flow of HTM to the jacket of 1201 is
vapour HTM.


The temperature of vapour pipe outlet 1201 is provided by the HTM evaporator 1611
and TRC11-11 measure the temperature outlet of 1611 control valve TV11-11 adjust
amount heating oil of the feed HTM into 1611. The flow of HTM to the vapour pipe of
1201 is vapour HTM.
PRC04-10 control valve PV04-10 to adjust the pressure in 1201. The reactor 1201 is
protected by rupture discs in order to against overpressure and blowed into the chamber.
At this mechanism, the esterification reaction stage 1 achieved high effection about
86%, required temperature about 2530C, pressure about 0.5 bar, level about 36%, residence
time about 4.5 hours.
The esterification reactor 1201 happen the esterification consists of two main
components is EG and PTA form Diethylglycol terephthalate – DGT and Water. Besides,
the reaction also generated some secondary reaction to creacte agent unexpected.
After performed the esterification, the evaporating EG and water are fed into the
rectification column 1401 and the liquid product is discharged by pump 2208A/B feed into
the esterification stage 2 reactor 1202. If on pipe go from pump 2208A/B to 1202 is
protected against overpressure, the other pipe refluxed back to 1201. The pipe of flow
product from 1201 to 1202 is also jacketed heated by pump 2205A/B which provide
heated liquid.
2.3.2 Esterification stage 2
After completed the esterification stage 1 reaction, the product fed into the reactor

1202 to continue the esterification stage 2. LRC04-24 measure level in 1202 to control
valve LV04-24 and also control the agitator in the condition safety.
At the same, the suspesion TiO 2 – EG and Diethylene glycol – DEG are also fed into
1202. The purpose of TiO2 is make the color for PETP, DEG is make PETP keep the stable
color of PETP and adjust the melting temperature of PETP. The amount EG in the
suspension TiO2 –EG and DEG are fed into 1202 to maintain the real mol ratio.
FQRC04-20 control valve FV04-20 to adjust amount DEG feed into 1202. The flow
feed of suspension TiO2 – EG is adjusted by SFRC03-17 and SFRC03-18 control the speed
of pump 2204A/B.
The temperature in 1202 is provided by the HTM circulation pump 2209A/B with
form the coils system put at the bottom reactor 1202. TRC04-22 will measure the
temperature in 1202 to control valve TV04-22. The flow of HTM to 1201 is liquid HTM.
The jacket 1202 is provided by the HTM evaporator 1601 with vapour HTM.
At this mechanism, the esterification reaction is optimised complete more than about
96%, require temperature limited about 258oC, pressure about 108 mbar, level about 41%,
residence time about 1.5 hour.


The vapour leave at the top reactor 1202 to go into 1401. When low pressure, a
amount vapour of reactor 1202 is not go into 1401, the nitrogen is pressed into 1202 to
push up amount vapour move to 1401. The vapour pipe outlet 1202 is heated by the HTM
evaporator 1611. The flow of HTM to the vapour pipe of 1202 is vapour HTM.
The flow from 1202 to 1203 is transferred by the difference of pressure and height
between the two reactor. The jacket of this pipe is heated, too.
2.4 Rectification column 1401
The vapours left the esterification reactors and a amount EG of vessel
into the bottom of the process column 1401. The column 1401 is
2211
separate between low and high boiling components, the main
is glycol and water. 1401 have 16 trays, on each tray have many

type. Damage pressure on each tray about 5 mbar.

1110 are fed
used
to
component
bubble cap

The temparature in the column 1401 is heated at the bottom of column with a coil
system. Pump 2205A/B provide heat with liquid HTM. TRC05-30 receive temperature at
outlet of pump 2205A/B then control TV05-30 adjust flow feed HTM.
The vapours leave overheads of the process column 1401 are passed through the
condenser 1602 where is cooled by cooling water, the excess vapour will move to the
chiller 1501 system. The liquid of 1602 flow down the reflux vessel 1108 with the help of
gravimetric flow. Continuously, the liquid is fed back to 1401 as reflux to maintain
temperature of 1401. TRC05-26 receive temperature of 1401 and interlock FRC05-14
control LV05-14 to adjust reflux flow fed back to 1401.The remaining water of 1108 is
discharged the overhead of vessel into the waste water system.
The bottom product is discharged through the filter system by pump 2207A/B feed
into 1201 to maintain a mol ratio. The level of 1401 maintain a certain level. When the
level of 1401 is high, the inventer LRC05-12 control valve LV05-12 to feed into the vessel
1114 to against overlevel in 1401.
Besides, the reflux product pipe return 1401 to increase the matabolism. It also protect
the pump 2207A/B against overpressure when flow product discharge from 1401 to 1201
ensure a mol ratio.
The pressure in column is protected against the overpressure to avoid break disc,
which will have a vent to blow down the chamber.
2.5 Prepolycondensation stage 1 and 2

2218



1202

1205

2214

1603A

1603B
2210A/B/C

1401

2211A/B

1114
After

the

esterification

reaction
complete,
the
1204
1203
prepolycondensation

reaction
take
place
under a certain
vacumn pressure and high
temperature.
At
this
prepolycondensation stage, the catalyst will
participated in the process
The
chains
of
polyethylene
1604 reaction.
terephthalate
are
formed by split-off of EG. The
product
is 1109A
in
two
1109B formed
1110
prepolycondensation stage with low viscosity.
2.5.1 Prepolycondensation stage 1
The inlet product of precondensation stage 1 reactor 1203 is fed from 1202 and level
in the reactor is maintained by LRC06-05 control valve LV06-05 to adjust the flow feed
into.
The teparature in 1203 is controlled by TRC06-06 control valve TV06-06 on heated

pipe outlet. The HTM circulation pump 2209A/B provide heat for the reactor with the coil
system put at the bottom of reactor, heated by liquid HTM.
The jacket of 1203 is provided by the HTM evaporator 1605 and TRC06-17 control
valve TV06-17 to adjust temperature of jacket 1203, heated by vapour HTM.


The vapour product go outlet on top reactor into the scraper condenser 1603A and
heated with jacket by the HTM evaporator 1611, heated by vapour HTM. On the vapour
pipe outlet have instal PRC06-03A/B to control valve PV06-03A/B to adjust the vacumn
pump 2211A/B create vacumn pressure for 1203.
The liquid product is transfered to the prepolycondensation stage 2 reactor 1204 by
different vacumn pressure between the two reactor. The jacket of discharge pipe is also
heated by the HTM circulation pump 2209A/B.
The reactor 1203 is not have the agitator.
2.5.2 Prepolycondensation stage 2
The product is continuously removed to the prepolycondensation 2 reactor 1204 with
purpose in order to increase the converts of prepolycondensation reaction.
The level of reactor is maintained by the inventer LRC06-13 control valve LV06-13
will open how much allow more or less product feed into 1204.
The temperature of reactor is provided by the pump 2213A/B after go through the
HTM heat exchanger 1613 and is maintained by the inventer TRC06-30 control valve
TV06-30.
The product is agitated by the discs installed on a through shaft of reactor, in order to
generate a large surface and combinate with vacumn pressure, it allows a amount EG form
in the process reaction.
The speed agitator has a great influence to the process reaction but it is not use to
control, because only have a small change of the speed agitator will change the prepolymer
product, too.
The shaft of agitator is operated by around change motors with connected gearbox
and inventer speed SIK06-18. It is lubricated by oil circulation system and sealed by

sealing system with silicon oil.
The vapours formed in the process reaction are removed into the scraper condenser
1603B by suction of vacumn. The vacumn is formed by the EG vapour jet ejector 2218
and is maintained by PRC06-11 control PV06-11.
The liquid product is discharged by pump 2214A/B to fed into the final
polycondensation 1205.
2.6 Vapour noncondensation of prepolycondensation
The vapours of reactor 1203 are sucked into the scraper condenser 1603A together the
flow EG condensate circulation is adjusted by FAL07-08 in order to condense vapour EG.
In the scraper condenser 1603A have a agitator form horizontal tye with low speed
agitator. The rotating bars of the agitator keep the oligomer floated together the EG


condensation move down 1109A. The vessel 1109A have a building weir. The EG
condensate go over the building weir and filted by a pair of mesh sieve instal on the weir.
Continue pulled through the filter
1309A/B by the pump 2210A/B and
1606
cooled by the cooler 1604A/B system
then enter 1603A to ensure the flow
reflux of EG circulation.
The level of 1109A is
in order to open valve allow a
level of 1109A still high, a
1109A.

1607

maintained by LIC07-01 control valve LV07-01
amount EG go to the vessel 1110. In the case

amount EG will enter the small pipe instal in

The vapour noncondensation of 1603A is sucked off by the vacumn pump 2211A/B.
Then go to the vessel 1115A/B and move down the cooler 1615A/B. A part go back pump
2211A/B to sealing and remain part go down the vessel 1110.
A amount EG in the vessel 1110 contain rather more water, so it will transfer to 1401
in order to separate again. The inventer LRC07-23 control valve LV07-23 to open valve
allow the flow EG remove to the collecting vessel 1114 to maintain the level of 1110.
The vapours of reactor 1204 are sucked into the scraper condenser 1603B together the
flow EG condensate circulation is adjusted by FAL07-18.
The constructing principle of 1603B and 1109B operate similar 1603A and 1109A.
Only have two different thing as:
The first, the vapour of 1603B is pulled to the EG vapour jet ejector 2218.
The remain, the inventer LIC07-11 control valve LV07-11 allow a mount EG move to
the vessel 1115 after cooled by the cooler 1604B/C system to maitain level in the vessel
1109B.
2.7 Final polycondensation
After the prepolycondensation complete, the prepolymer product is discharged by
pump 2214A/B and transferred to the disc ring reactor 1205. The final polycondensation
will take place.
The gear pump 2214A/B is driven by around change motors with reduction gear and
inventer speed control.
2218


Cutting
1305
2215
1205


1204
2214

Spinning

2217
The level of 1205 is maintained by

1111

inventer LIC09-07.

The inventer LIC09-07 give signal
command to SFYIK08-01 which
interlock SFRC08-01. Then SFRC08-01 will control SIK08-13 and SIK08-14 to adjust the
speed of pump 2214A/B.
The prepolymer product is pumped continuously through the filter 1305A/B. The
inventer PRC08-04 control valve PV08-04 to adjust pressure of flow product passed the
filter 1305A/B.
The purpose of reactor 1205 is to increase the expected viscosity of polymer product.
The viscosity of product is decided by two pressure and speed of agitator parameters.
The product is agitated by the disc rings, in order to generate a large surface and
combinate with deep pressure vacumn to splip off a amount vapour EG generate in the
polycondensation reaction.
The disc rings, which are arranged on each of these chambers and are installed on a
through shaft.
The shaft is driven by an around change motor with connected reduction gear and
inventer speed control SIK09-02. It is lubricated by oil circulation system and sealed by
sealing system with silicon oil.
The temperature of reactor 1205 is provided by the pump 2219A/B after go through

the HTM heat exchanger 1608 and is maintained by the inventer TRC09-40 control valve
TV09-40, heated by liquid HTM.
The vapours of reactor 1205 are removed into the scraper condenser 1606 by suction
of vacumn. The vacumn is formed in by the EG vapour jet ejector 2218 and is maintained
by PRC09-08 control PV09-08. The HTM evaporator 1611 provide heating for the vapour
pipe.


After the product reached viscosity as expect, the product is discharged by pump
2215A/B with heated by the HTM pump 2219A/B. The gear pump 2215A/B is driven by
around change motors with reduction gear and inventer speed control SIK12-02 and
SIK12-03.
The
polymer
down
2.8

1610

polymer pumped throught the POY plant to textile and excess
transfer to the cutter chip system to form the chips production then go
the chip vessel 1703A/B.
Vapour noncondensation of final polycondensation

The vapours of reactor 1205 are sucked into the scraper condenser 1606 together the
flow EG condensate circulation go down in order to condensate the vapour, which adjust
by preset inventer FAL10-11.
The scraper condenser 1603A have a agitator form horizontal tye with low speed
agitator. The rotating bars of the agitator keep the oligomer floated together the EG
condensation move down 1111. The vessel 1111 have a building weir. The EG condensate

go over the building weir and filted by a pair of mesh sieve instal on the weir. Continue
pulled through the filter 1311A/B by the pump 2217A/B and cooled by the cooler
1607A/B system then enter 1606 to ensure the flow reflux of EG circulation.
The level of 1111 is maintained by LRC10-14 control valve LV10-14 in order to open
valve allow a amount EG go to the vessel 1114. In the case level of 1111 still high, a
amount EG will enter the small pipe instal in 1114.
The vapour noncondensation of 1606 is pulled through the EG vapour jet ejector 2218
by the vacumn pump 2221A/B.
2.9 EG evaporator jet ejector 2218
The vapour leave the scraper 1606 is pulled into the ejector 2218 by the flow vapour
EG of 1610 provide into spray nozzle of the ejector 2218 with high pressure. The deep
vacumn pressure is formed in here by the suction of pump 2221A/B combinate with the
flow evaporate EG of 1610. The vapour of scraper 1603B is also pulled to 2218 by
vacumn.
Each stage of three stage EG ejector 2218 also have the jet ejector.

1603B
1606


2221

2218

1609
1101
1112
2227A/B

1114

2225A/B

Each stage of three stage EG ejector 2218 is distributed by three flow EG condensate
circulation entered at the top of ejector 2218 to condensate vapours and adjusted by preset
of three flowmeter.
The condenser remove down the vessel 1112. Continue pulled through the filter by
the pump 2227A/B convey the EG condensation to the individual spray nozzle condenser
while only the flow to the first stage is passed the cooler 1609 in order to receive the
required temperature profile enter the ejector 2218 to separate the low boilers.
After ensure the flow reflux of EG circulation. Level of 1112 is maintained by LIC1124 control valve LV11-24 to adjust a amount EG move to pump 2221A/B.
The part noncondensation is sucked through the vacumn pump 2221A/B. The vacumn
is maintained in the ejector 2218 by the inventer PRC11-17A/B control valve PV1117A/B. Then go to the vessel 1117A/B and move down the cooler 1616A/B. A part go
back pump 2211A/B to sealing and remain part go down the collecting vessel 1114.
The amount EG is provided to the evaporator 1610 to be discharged from the vessel
1112. The amount of glycol leave the evaporator is compensated by the flow liquid glycol
branched off from the flow EG circulation loop of ejector 2218 system. Level of
evaporator 1606 is maintained by LRC11-55 control valve LV11-55 to adjust a amount
EG feed into evaporator.
The heat of 1610 is provided by pump 2223 with a removable heating coil. The
inventer TRC11-70 control valve TV11-70 to adjust temperature in the evaporator, heated
by liquid HTM.
The collecting vessel 1114 have function collect the split off of EG of the process.
The amount EG contain water is almost less, so it is transferred back to the tank 1101 by
pump 2225A/B as raw material.