Philosophy of Control for Complex Logics

8/20/2019 Philosophy of Control for Complex Logics

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MUMBAI REFINERY Rev. Date: 20/01/2010

LOBS QUALITY UPGRADATIONPROJECT

D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

C'APTER ( &

P'ILOSOP'Y OF CONTROL

PREPARED BY C'EC)ED BY C*a+te, ( &

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TABLE OF CONTENT

1.0 PREFACE............................................................................................................&

S!+e................................................................................................................................&

Le-e..............................................................................................................................&

2.0 OERALL PLANT CONTROL P'ILOSOP'Y...................................................

$.0 COMPLE3 CONTROL SYSTEMS.....................................................................11

$.1 Fee S4,-e D,45 6%%#D#027 P,e884,e Ct,9 6PIC#120&7.................................11

$.2 Fee S4,-e D,45 Leve9 Ct,9 6LIC#120 'S#120;7.......................................1$

$.$ Ma7.......................................................................................................1"

$. 'DT Rea!t, E94et St,=++e, Fee Te5+e,at4,e Ct,9 6TIC#1>107.............21

$.; 'DF Rea!t, E94et Te5+e,at4,e Ct,9 6TIC#1>027.....................................2&

$.> 'DT Rea!t, C*a,-e 'eate, O4t9et Te5+e,at4,e Ct,9 6TIC#1"0>7..............2;

$." 'DT Rea!t, Te5+e,at4,e Ct,9 6TIC#201%/2012/201&/201;7........................2"

$.% MSD? Fee D=e,et=a9 P,e884,e Ct,9 6PDIC#21027....................................$1

$.10 Rea!t, L+ P,e884,e Ct,9 6PIC#$20"/'S#$212/FIC#$202/FIC#210;7.........$2

$.11 Lea A5=e Te5+e,at4,e Ct,9 6DTIC#2$0"7..................................................$

$.12 ?a8* ?ate, S4,-e D,45 6%%#D#1$7 P,e884,e Ct,9 6PIC#2&017.....................$>

$.1$ 'DF Fee Te5+e,at4,e Ct,9 6TIC#2027........................................................$%

$.1& MSD? C*a,-e 'eate, O4t9et Te5+e,at4,e Ct,9 6TIC#2;0>7.........................&1

$.1 MSD? Rea!t, Te5+e,at4,e Ct,9 6TIC#2"0"/2"11/2"1&7.............................&$$.1; 'DF Rea!t, Te5+e,at4,e Ct,9 6TIC#2%0$/2%027..........................................&;

$.1> 'TS O'D/Re!@!9e Ga8 E!*a-e, 6%%#E#0>7 Re!@!9e Ga8 O4t9et

Te5+e,at4,e Ct,9 6TIC#$0027.........................................................................&%

$.1" 'TS L=4=/F,a!. Btt5 E!*a-e, 6%%#E#1&A/B7 P,4!t St,=++e, Fee

Te5+e,at4,e Ct,9 6TIC#$0017.........................................................................1

$.1% P,4!t St,=++e, 9eve9 Ct,9/F9 Ct,9 t a!. F,a!. C*a,-e 'eate, %%#F#

0$ LIC#$$0$/FIC#$$02/FIC#$$0&7..........................................................................$

$.20 a!. F,a!. C*a,-e 'eate, O4t9et Te5+e,at4,e Ct,9 6TIC#$07...................


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$.21 Fee/F,a!. Btt5 E!*a-e, 6%%#E#01A/B7 Ra=ate Fee Te5+e,at4,e

Ct,9 6TIC#&10$7..............................................................................................."

$.22 ?a,5 Fee/F,a!. Btt5 E!*a-e, 6%%#E#1>A/B7 Deae O=9 O4t9et

Te5+e,at4,e Ct,9 6TIC#&1017.........................................................................;0

$.2$ a!445 F,a!. P45+a,4 Ret4, Te5+e,at4,e Ct,9 6TIC#&2017..............;2

$.2& A5=e De-a88=- D,45 6%%#D#1&7 P,e884,e Ct,9 6PIC#&>0%7......................;&

$.2 S4, ?ate, De-a88=- D,45 6%%#D#17 P,e884,e Ct,9 6PIC#&>0&7..............;;

$.2; 'eate, 6%%#F#017 Da5+e, Ct,9 6PIC#1"0/'IC#1"0/'S#1"107......................;"

$.2> Deae O=9 P,4!t C9e, 6%%#AFC#0;7 Te5+e,at4,e Ct,9 6TIC#&10&7....>1

$.2" P,4!t St,=++e, Ove,*ea A!!4549at, 6%%#D#107 Leve9 Ct,9 6LIC#

$&10/FIC#$&0&A/FIC#$&0&B7................................................................................>$

$.2% a!445 F,a!. Ove,*ea A!!4549at, 6%%#D#117 Leve9 Ct,9 6LIC#$%02/FIC#

&10&A/FIC#&10&B7................................................................................................>

$.$0 a!445 F,a!. Ove,*ea Te5+ Ct,9 6%%#T#07 Re94 Ct,9 6TIC#$>02/FIC#

$>0$7.....................................................................................................................>"

$.$1 'eav@ D=8t=99ate St,=++e, 6%%#T#0>7 Leve9 Ct,9 6LIC#$"017............................"0

$.$2 LPG a+,=e, 6%%#D#2;7 Leve9 Ct,9 6LIC#%017 / P,e884,e !t,9 6PIC#

%0&7....................................................................................................................."2

$.$$ S4, ?ate, De-a88=- D,45 6%%#D#17 Leve9 Ct,9 6LIC#&>017...................."&

$.$& ?a8* ?ate, F9 Ct,9 6FIC#2&01 / FIC#21017 , ?a8* ate, C945 6%%#T#

0$7 a 't St,=++e, O'D C9e, 6%%#AFC#017................................................";

&.0 PUMP AUTO START/STOP CONTROL SYSTEM............................................"%

&.1 A4t Sta,t /St+ S@8te5 6I#&%7 , C98e B9 S@8te5 P45+ 6%%#P#

1"A/B7...................................................................................................................%0

&.2 A4t Sta,t /St+ S@8te5 6I#2017 , Ba!


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1.0 PREFACE

S!+e

This narrative describes the plant control systems by instrumentation.

The purposes of this document are as follows:

(1) To explain control systems to those who are not familiar with instrumentation

symbols or functional logic diagrams.

(2) To define purpose and algorithm of each control system.

Complex control include split range control cascade control and dual range control.

This document does not cover simple control loops.

Le-e

!C" !istributed Control "ystem

#$ #rocess $alue (%nput) to !C" controller

"# "et #oint of Controller


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2.0 OERALL PLANT CONTROL P'ILOSOP'Y

O=9 C*a,-e a Fee S4,-e D,45

&il charge is received at the battery limits from tan'age. n offsite pump provides

sufficient pressure to pass through low temperature heat exchanger (**+,1-)

filtration (**/%0,1) Coalescer (**!2,) and enter the /eed "urge !rum (**!,1).

&il charge flow to the unit is controlled by **!,1 level which is cascaded to a flow

controller. handswitch ("12,) is provided to allow selection of flow control to either

the normal unit charge controller (/%C12,1) or the special startup feed (wetting and

sulfiding stoc') control valve (0$12,3). /rom the /eed "urge !rum the feed is

boosted to high pressure by the ooster pump (**#45-) /eed Charge #ump (**#

,2-) and sent to the 6arm /eed - /ractionator ottom +xchanger (**+17-) and

the /eed - !T 8eactor +ffluent +xchangers (**+,5--C). The oil charge to the

!T is on straight flow control.

Mauench flow rates. The !T 8eactor consists of four beds of catalyst

to limit the overall exotherm in the !T. Two thirds of the expected exotherm is

eliminated by means of >uench to the outlet of the first second and third beds. The

>uench gas enters on flow control reset by bed inlet and-or outlet temperature. nadditional >uench gas connection is provided to the inlet of the reactor for fast trim


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temperature control if re>uired during an upset condition and for use in controlling the

wetting exotherm on startup. oth Treat ;as and ?uench ;as to the !T 8eactor is

supplied from the 8ecycle ;as Compressor (**C,2-).

'DT E94et St,=++e,

The !T +ffluent "tripper (**T,1) removes 2" and =5 from the !T effluent

stream with fresh incoming ma'eup hydrogen. The stripper can function through a

reasonable temperature range but will operate close to 1


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(**+5*). 0ean amine and wash water flow rates to their respective towers are both on

simple flow control.

MSD? a 'DF Rea!t, Te5+e,at4,e Ct,9

The control philosophy for the 9"!6 8eactor is identical to that of the !T 8eactor.

The 9"!6 reactor temperature is controlled by adusting the furnace firing rate. The

9"!6 8eactor (**8,2) consists of three bed of catalyst to control the overall

exotherm. The maority of the expected (gross) exotherm is eliminated by means of

8ecycle ;as >uench to the outlet of the first and second beds. The >uench gas enters

on flow control (reset by bed inlet - outlet temperature). n additional >uench gasconnection is provided to the inlet of the reactor for fast trim temperature control during

an upset condition and for use in controlling the wetting exotherm on startup.

The !/ 8eactor (**8,5) exotherm is expected to be negligible in normal operation.

The !/ inlet temperature is controlled through bypassing of 9"!6 /eed around the

**+,--C. The !/ 8eactor consists of two beds of catalyst. The inlet to each bed

is e>uipped with hydrogen >uench connections. The >uench hydrogen to the first bed

enters the reactor inlet line on flow control (reset by either reactor inlet temperature) andprovides trim temperature control and for the bed wetting exotherm during the initial

startup. n additional >uench inection point is provided at the inlet to the second bed

for similar reasons.

P,4!t Se+a,at, Te5+e,at4,e Ct,9

!/ 8eactor effluent is sent to the 9"!6 8eactor /eed-!/ +ffluent +xchanger (**

+,2--C). This exchanger will be in use during endofrun (+&8) conditionsB but at

startofrun ("&8) the duty is expected to be near Dero. The !/ 8eactor effluent

temperature leaving the exchanger is controlled by bypassing oil feed around the

exchanger. The intent of this is to provide a controlled temperature to the igh

Temperature "eparator ET"F (**!,4). "eparator li>uid product is discharged on flow

control reset by drum level to the T" 0i>uid - /ractionator ottoms +xchanger (**+

14-) and then to the #roduct "tripper tower (**T,4). T" vapor is cooled by

exchange with the Treated ;as (**+,7) then aircooled (**/C,2) then water

cooled (**+,


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;as purity. n additional amount of light hydrocarbon will be condensed in this drum

which is sent on flow control reset by level where it combines with the light

hydrocarbons condensed in the !T 0ow Temperature separator (**!,2) and the

combined stream is heated by exchange with !ewaxed 0ube #roduct (**+13) before

entering **T,4.

%n order to protect against a highpressure blowthrough of gas from the separators to

the fractionation section both **!,4 and **!,3 separators are e>uipped with low

level switch interloc's. These interloc's operate a chopper valve and act to close the

product flow control valves by means of airactivated solenoids located on the air supply

to the valves.

Re!@!9e Ga8 a U=t P,e884,e Ct,9

9a'ep ydrogen ;as is inected into the unit at the !T +ffluent "tripper as

described above. %n order to maintain 8ecycle ;as hydrogen purity it is necessary to

continuously purge a small portion of gas from the unit. The purge gas stream is ta'en

from the 8ecycle Compressor "uction A& !rum (**!,) overhead line. The unit

pressure controller is also located on the 8ecycle Compressor "uction A& !rum. The

pressure control signal from #%C52,< goes to a hand switch (**"5212) to control

either the 9a'ep ;as rate or the unit purge gas rate. &nce selected the other

remains left on straight flow control. The unit was designed with a purge allowance of

2G of the 8ecycle ;as 8ate. The ma'eup hydrogen re>uirements are minimiDed when

setting the purge gas rate at some minimum value. This allows the pressure controller to

bring in ma'eup hydrogen as re>uired to maintain unit pressure.

/or stable operation of 9"!6 reactor it is necessary to have stable !T effluentstripper operation. ence it is preferred to have constant ma'eup as flow rate to **T

,1 and reactor section pressure is controlled by varying purge rate.

'P St,=++e, Se!t=

The igh #ressure "tripper is a steam stripped column designed to remove naphtha

and lighter boiling components from the li>uid product stream. There is no external heat

source for this column. $apor traffic is generated solely from the sensible heat of the

feed. "tripping steam is introduced on flow control to the bottom of the # "tripper.


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The amount of naphtha product produced is small. The endpoint of the naphtha is

controlled by the tower top temperature which resets the reflux rate. #ressure control

of the tower is accomplished by throttling the vapor product which is sent to 8efinery

/uel ;as eader. The amount of reflux can be controlled somewhat by regulating the

igh Temperature "eparator Temperature as described earlier. The =aphtha endpoint

and degree of stripping will in turn influence the flashpoint of the distillate product in the

$acuum /ractionator.

"tripped li>uid product from the bottom of the # "tripper is sent on flow control (reset

by level) to the $acuum /ractionator Charge eater (**/,5). The stripper contains a

large li>uid inventory to ensure stable operation of the eater. s **/,5 is two pass

furnace flow is e>ually divided between two passes by individual flow controllers which

are reset by column level.

a!445 F,a!t=at= Se!t=

The $acuum /ractionation "ection consists of four vessels the $acuum /ractionator

(**T,3) the !ewaxed &il $acuum !ryer (**T,) the eavy !istillate "tripper (**T

,7) and the eavy !istillate $acuum !ryer (**T,


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for **/,5. ny hydrocarbon li>uid from the Condensate 8eceiver is pumped to **!

11 inlet. ny sour water is pumped to the "our water !egassing !rum (**!13).

The hydrocarbons that have condensed in **!11 are pumped (**#,* -) under

level control and the stream split into two parts. The first is returned to the $acuum

/ractionator as top reflux under flow control that is cascaded to overhead temperature.

The second part is watercooled (**+15) and leaves the unit as 0ight !istillate product

under flow control that is cascaded to the **!11 level.

heavy distillate product is withdrawn from below the second pac'ed section and

pressured to the eavy !istillate "tripper (**T,7). /low to **T,7 is set by **T,7

bottoms level control. The distillate product is steam stripped to remove lighter distillate

and sent to the eavy !istillate $acuum !ryer (**T,


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$.0 COMPLE3 CONTROL SYSTEMS

$.1 Fee S4,-e D,45 6%%#D#027 P,e884,e Ct,9 6PIC#120&7

This specification should be read in conunction with the following:

(1) #H%! =o.: 1


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T & / 0 8 +

/ : + 0 ; "

# $

1 2 , 4

# $

1 2 , 4

# % C

1 2 , 4

# 0

( , 4 7 . 3 G )

( 3 2 . 3 1 , , G )

" # 0 % T 8 = ; +

/ 8 &

9 + ! + 8

" % 9 # 0 % / % + ! 0 & C A ! % ; 8 9

/ % ; . 1

C & = T 8 & 0 ( # % C 1 2 , 4 )

/ C

/ ,

* * !

, 1

1 , , G

1 , , G

, G

# % C 1 2 , 4

" # 0 % T 8 = ; + C & = / % ; : 8 T % & =

# $ ) 1 2

, 4 (

/ + + !

T & * *

+ 1 7

$ % *

* # 4 5 - H * * # , 2 -

# $ ) 1 2

, 4 .

C&=T8&0 $(0$+ +=%=; G

C & = T 8 & 0 0 + 8 & : T # : T G

3 , G

4 7 . 3 G

3 2 . 3 G

# 8 + " " : 8 + % = C 8 + " +

/ 8 & 9 * * ! 2 ,

/ + + !

/ + + ! " : 8 ; + ! 8 : 9 ( * * ! , 1 ) # 8

+ " " : 8 +

$.2 Fee S4,-e D,45 Leve9 Ct,9 6LIC#120 'S#120;7


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(1) #H%! =o.: 1uid (startup) oil flow to be controlled.


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" T 8 T : #

" % 9 # 0 % / % + ! 0 & C A ! % ; 8 9

/ % ; 2

/ + + ! " : 8 ; + ! 8 : 9 ( * * ! , 1 ) 0 + $ + 0

C & = T 8 & 0 ( 0 % C 1 2 , 3 " 1 2 , )

T & * * + 1 7

$ % * * # 4 5 -

H * * # , 2 -

/ + + !

/ $

/ % C

1 2 , 1

/ 0

/ 8 & 9 " T & 8 ; +

/ C

* * ! , 1

/ + + !

"

1 2 ,

* * + , 1 -

* * / % 0 , 1

* * ! 2 ,

0 % C

1 2 , 3

0

0 0

1 2 , 1

/ 0 : " % = ; & % 0 H

# 8 + " : 0 / % ! % = ;

0 % ? : % !

/ 8 & 9 " T & 8 ; +

0 $

/ C

1 2 , 3

= & 8 9 0 & # + 8 T % & =

" #

/ T 1 2 , 1


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$.$ Ma


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control spill bac' flow. This configuration always ensures suction pressure at the

compressor H thereby avoid serious trips while ensuring constant discharge pressure.

%n addition to that pressure controller will give high-low alarm (#152


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9 9 - D - 0 7 A

9 9 - C - 0 1 A

9 9 - C - 0 1 A

9 9 - E - 0 9 A

9 9 - D - 0 8 A

1 S T S T A G E

2 N D S T A G E

9 9 - E - 1 1 A

9 9 - C - 0 1 A

3 R D S

T A G E

9 9 - E - 1 0 A

9 9 - D - 0 9 A

T O 9 9 - T - 0 1

M

A K E U P G A S F R O M O S B L

S W R

S W S

S W S

S W R

S W R

S W S

P V 1 4 0 2

F O

P I C

1 4 0 2

P Y

1 3 2 8

P I C

1 3 2 8

P A

P A L

M

N C

N C

N C

" % 9 # 0 % / % + ! 0 & C A !

% ; 8 9

9 A + : # ; " C & 9 #

8 + " " & 8 ( * * C , 1 ) " : C T % &

=

/ % ; . 5

# 8 + " " : 8 + C & = T 8 &

0 ( # % C 1 4 , 2 - 1 5 2 < - # I 1 5 2 < )

P V 1 3 8 1

P I C

1 3 8 1


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$.& Ma/PY#12>7


(1) #H%! =o.: 1


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the compressor H thereby avoid serious trips while ensuring constant discharge

pressure.

%n addition to that pressure controller will give high-low alarm (#1327-#01327)

as applicable on !C".


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9 9 - D - 0 7 B

9 9 - C - 0 1 B

9 9 - C - 0 1 B

9 9 - E - 0 9 B

9 9 - D - 0 8 B

1 S T S T A G E

2 N D S T A G E

9 9 - E - 1 1 B

9 9 - C - 0 1 B

3 R D S

T A G E

9 9 - E - 1 0 B

9 9 - D - 0 9 B

T O 9 9 - T - 0 1

M A K E U P G A S F R O M O S B L

S W R

S W S

S W S

S W R

S W R

S W S

P V 1 ! 0 2

F O

P I C

1 ! 0 2

P Y

1 " 2 7

P I C

1 " 2 7

P A

P A L

M

N C

N C

N C

" % 9 # 0 % / % + ! 0 & C A !

% ; 8 9

9 A + : # ; " C & 9 #

8 + " " & 8 ( * * C , 1 ) " : C T % &

=

/ % ; . 4

# 8 + " " : 8 + C & = T 8 &

0 ( # % C 1 , 2 - 1 3 2 7 - # I 1 3 2 7 )

P I C

1 3 8 1

P V 1 3 8 1


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$. 'DT Rea!t, E94et St,=++e, Fee Te5+e,at4,e Ct,9 6TIC#1>107


(1) #H%! =o.: 1


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to close H the inlet valve T$171,C will start to open allowing more recycle gas flow to

pass through the exchanger thereby increasing heat transfer. %nlet valve T$171,C is

provided with mechanical min. stop (4,G) to avoid exchanger running dry H thereby

preventing damage to it. %n this range oil feed valve T$171, is fully open allowing the

max. oil flow through the exchanger H no bypass is there.

%n addition to that temperature controller will give high alarm (T171,) as applicable

on !C".


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! T 8 + C T & 8 + / / 0 : + = T

/ 8 & 9 * * 8 , 1

T % C

1 7 1 ,

/ + + !

/ 8 & 9 * * + 1 7 -

! : 0 C T % = ;

T & * * / , 1

T & * * T , 1

T $

1 7 1 ,

" % 9 # 0 % / % + ! 0 & C A ! % ; 8 9

T + 9 # + 8 T : 8 + C & = T 8 & 0 ( T % C 1 7 1 , )

T $ ) 1 7

1 , (

T $ ) 1 7

1 , .

1 , , G

1 , , G

( 4 , G )

T % C 1 7 1 ,

" # 0 % T 8 = ; + C & = / % ; : 8

T % & =

/ % ; . J 3

! T 8 + C T & 8 + / / 0 : + = T " T 8 % # # + 8 / + + !

/ &

/ C

* *

+ , 5 - - C

C&=T8&0 $(0$+ +=%=; G

C & = T 8 & 0 0 + 8 & : T # : T G

! T 8 + C T & 8 + / / 0 : + = T

9 % = . " T & # ,

G

T

9 % = .

" T & #

8 + C I C 0 + ; "

/ 8 & 9 * * + , 7

T $

1 7 1 , C

/ &

9

% = .

" T

& #

T $

1 7 1 ,

/ C

T $

1 7 1 , !

/ + + !

T $ ) 1 7 1

, C

T $ ) 1 7

1 , !

3 , G

T + 9 # + 8 T : 8 + % = C 8 + " +

! :

0 C T % = ;

( 3 , 1 , , G

)

( , 3 , G )

& T % =

& T & : T

C & 0

! % =

C & 0 ! & : T

& % 0

; "


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$.; 'DF Rea!t, E94et Te5+e,at4,e Ct,9 6TIC#1>027


(1) #H%! =o.: 1


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D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

! / 8 + C T & 8 + / / 0 : + = T

/ 8 & 9 * * 8 , 5

T % C

1 7 , 2

" T 8 % # # + 8 9 " ! 6 / + + !

/ 8 & 9 * * T , 1

! : 0 C T % = ;

T & * * + , - - C

T & * * ! , 4

T $

T $

1 7 , 2

" % 9 # 0 % / % + ! 0 & C A ! % ; 8 9

T + 9 # + 8 T : 8 + C & = T 8 & 0 ( T % C 1 7 , 2 )

T $ ) 1

7 , 2 (

T $ ) 1 7 , 2 .

1 , , G

1 , , G

( 4 , G )

T % C 1 7 , 2

! : 0 8 = ; + C & = / % ; : 8

T % & =

/

% ; . J

! / 8 + C T & 8 + / / 0 : + = T

/ &

/ C

* *

+ , 2 - - C

C&=T8&0 $(0$+ +=%=; G

C & = T 8 & 0 0 + 8 & : T # : T

G

1 7 , 2

! / 8 + C T & 8 + / / 0 : + = T

" T 8 % # # + 8 9 " ! 6 / + + !

9 % = . " T & # ,

G

T

9 % = .

" T & #

T + 9 # + 8 T : 8 + % = C 8 + " +

& T % =

& T & : T

C & 0 ! % =

C & 0 ! & : T


RMB R'D Pa-e 2 %


26/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

$.> 'DT Rea!t, C*a,-e 'eate, O4t9et Te5+e,at4,e Ct,9 6TIC#1"0>7


(1) #H%! =o.: 1


27/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

* * / , 1

/

+ + !

T

& * * 8 , 1

/ :

+ 0 ; "

/ 8 & 9 * * ! 1 2

# % C

1 * , 1

# $

1 * , 1

#

T % C

1 < , 7

T

* * / , 1

: 8 = + 8

" % 9 # 0 % / % + ! 0 & C A ! % ; 8 9

/ % ; . J 7

! T 8 + C T & 8 C 8 ; + + T

+ 8 & : T 0 + T

" #

/ C

T 0

# 0

T + 9 # + 8 T : 8 + C & = T 8 & 0 ( T % C

1 < , 7 )

/ : 8 = C + & : T 0 + T


RMB R'D Pa-e 2> %


28/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

$." 'DT Rea!t, Te5+e,at4,e Ct,9 6TIC#201%/2012/201&/201;7


(1) #H%! =o.: 1


29/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

$.".$ De8!,=+t=

/or each catalyst bed inlet ( eight thermocouples in total) and outlet ( eight

thermocouples in total) temperatures are measured. ed %nlet (except top bed) and

&utlet (except bottom bed) Tis are averaged in a calculation (TI) bloc'. The target bed

outlet temperature is entered by operator based on the operating case and catalyst run

length. veraged out bed outlet temperature is compared to the operator entered set

point and this difference is used to reset the bed inlet target temperature with a time

delay of 3 min. (adustable). The bed inlet target temperature is compared to the actual

average inlet temperature (every 1 min. adustable). The difference between these two

values is used to reset >uench flow.

/or top bed reactor inlet temperature (T%2,1*) is used instead of bed top temperature

(T%2,1, ). /or bottom bed the reactor outlet temperature (T%2,1


30/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

BED-3

99-R-01

TO 99-E-03 A#B#C

FROM 99-F-01

SP

SP

PV

SP

FROM 99-C-02A#B

SP

BED TOP

BED BOTTOM

BED TOP

BED

BED TOP

BED TOP

PV

PV

PV

PV

PV

PV

TAL

TO 99-F-01

TO 99-F-01

TO 99-F-01

#F-02 TRIP

TO 99-F-01

#F-02 TRIP

#F-02 TRIP

BOTTOM

BED

BOTTOM

BED

BOTTOM

#F-02 TRIP

TIC

2013

TIC

201"

TIC

2018

TIC

2011

TY

2014

#$

#$

TY

2012

TI

2013

TA

TA

A-

FT

2004

FT

2003A#B

FT

2002

FV

2004

FV

2003

FV

2002

FV

2001

FO

FO

FO

FO

#$

FIC

2003

FT

2001

TI

2011

TA

TA

A-

TI

2010

TA

TA

A-

TI

2012

TA

TA

A-

TI

2014

TA

TA

A-

TY

201!

TIC

201! TAL

PV

TI

2017

TA

TA

A-

TI

201!

TA

TA

A-

TI

201"

TA

TA

A-

FIC

2004

TY

201"

TIC

2014

TA

TA

TY

2013

TIC

2012

TA

TA

TAL

FIC

2002

TY

2011

TIC

2019

TA

TA

TAL

FIC

2001

TI

2018

TA

TA

TI

2019

BED-1

BED-2

BED-4

I

3

#$

#$

#$

I

3

I

3

I

3

" % 9 # 0 % / % + ! 0 & C A !

% ; 8 9

! T 8 + C T & 8 ( * * 8

, 1 ) T + 9 # + 8 T : 8 +

/ % ; . <

C & = T 8 & 0 ( T % C 2 , 1 * - 2 , 1 2 - 2 , 1 4 - 2 , 1 )


RMB R'D Pa-e $0 %


31/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

$.% MSD? Fee D=e,et=a9 P,e884,e Ct,9 6PDIC#21027


(1) #H%! =o.: 1uired to maintain a high enough differential

pressure between **T,1 and treated recycle hydrogen from the wash water tower (**

T,5) to ensure that li>uid flows to **+,--C.

$.%.2 S=5+9==e B9!< D=a-,a5 MSD? Fee D=e,et=a9 P,e884,e Ct,9 6PDIC#21027

8efer /%;. * on "heet =o 54.

$.%.$ De8!,=+t=

The #ressure !ifferential Controller #!%C21,2 receives signal from #T21,2 which

measure pressure of **T,1 &verhead. This signal is then compared with signal from

#T21,2 which measures the pressure of treated gas from wash water tower (**T,5)

to upstream of shell side inlet of !T stripper &verhead-Treat ;as +xchanger (**+

,4-). ased on these values the controller will then act to manipulate the control

valve located at the treated gas stream to ensure a pressure gradient is maintained

between **T,1 and **+,--C. y maintaining this the bottoms stream will be

able to flow to **+,--C and 9"!6 8eactor (**8,2).


RMB R'D Pa-e $1 %


32/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

$.10 Rea!t, L+ P,e884,e Ct,9 6PIC#$20"/'S#$212/FIC#$202/FIC#210;7


(1) #H%! =o.: 1


33/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

by operator and the #ressure Controller #%C52,< controls the flow of purge gas

out of the unit via cascade control of /%C52,2-/$52,2.

/ixed #urge ;as (/%C52,2 set by operator) and variable 9a'eup ;as (#%C

52,< cascade with /%C21,):

!C" operator shall select the destination of the signal from #%C52,< to /%C21,

with the help of and "witch "5212.The output of the controller /%C21, shall

be used by computation bloc' (/I21,2 and /I21,) to give the set point to the

flow controllers (/%C21,2 and /$21, respectively). %n ,3,G output range all

the ma'eup 2 is directed towards **T,1 H used as stripping gas. %f the

re>uirement of 2 is higher (i.e. /%C21, output is LM 3,G) to maintain reaction

operating pressure then bypass valves /$21, will be opened. This is done to

avoid overloading of the stripper. The stripping ydrogen valve is provided with a

soft higher limiter to limit opening of valve H avoid excess stripping 2 in **T,1.

lso the bypass valve /$21, is provided with low limiter (2G adustable) to

'eep the system live with small 2 flow through bypass loop. 8ecycle ;as can

also be used for stripping the !T +ffluent in **T,1 which is on a separate flow

controller /%C211,. The output of the controller /%C21,2 and /%C211, shall be

used by computation bloc' (/I211,) to calculate the total amount of stripping gas

flow to the stripper (/%212,).


RMB R'D Pa-e $$ %


34/95


35/95


36/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

" % 9 #

0 % / % + ! 0 & C A ! % ; 8 9

0 + =

9 % = + T + 9 # + 8 T : 8 +

/ % ; . 1 ,

C & =

T 8 & 0 ( ! T % C 2 5 , < )

T O

9 9 - D - 0

3

T O

9 9 - D - 1

4

T O

T - 0

4

9 9 - T - 0

2

L E A N A M I N E F R O M

A R U

D T L T S O V D

V A P O U R

F R O M

9 9 - D - 0

2

9 9 - P - 1

1 A # B

9 9 - D - 2

3

2 0

1 3 2

L P C O N D E N S A T E

L P S T E A M

9 9 - E - 1

!

F C

T I

2 3 2 1

T A

T A L

D T I C

2 3 0 8

D T A L

T I

2 3 0 2

T A

T A L

T V

2 3 0 8

T T

2 3 0 8 A

T T

2 3 0 8


RMB R'D Pa-e $; %


37/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

$.12 ?a8* ?ate, S4,-e D,45 6%%#D#1$7 P,e884,e Ct,9 6PIC#2&017


(1) #H%! =o.: 1


38/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

T & / 0 8 +

/ : + 0 ; "

# $

2 4 , 1

# $

2 4 , 1

2 4 , 1

( , 4 7 . 3 G )

( 3 2 . 3 1 , , G )

" # 0 % T 8 = ; +

/ 8 & 9 + !

+ 8

" % 9

# 0 % / % + ! 0 & C A ! % ; 8 9

/ % ; . 1 1

# 8 +

" " : 8 + C & = T 8 & 0 ( # % C 2 4 , 1 )

/ C

/ ,

* * ! 1 5

1 , , G

1 , , G

, G

# % C 2 4 , 1

" # 0 % T 8 = ; + C & = / % ; : 8 T % & =

# $ ) 2 4

, 1 .

6 " 6 T + 8

T & * * T , 5

$ % * * # 1 , -

# $ ) 2 4

, 1 (

C&=T8&0 $(0$+ +=%=; G

C & = T 8 & 0 0 + 8 & : T # : T G

3 , G

4 7 . 3 G

3 2 . 3 G

# 8 + " " : 8 + % = C 8 + " +

/ 8 & 9 * * +

1 <

/ 6

6 "

6 T + 8 " : 8 ; + ! 8 : 9 ( * * ! 1 5 )

# % C


RMB R'D Pa-e $" %


39/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

$.1$ 'DF Fee Te5+e,at4,e Ct,9 6TIC#2027


(1) #H%! =o.: 1


40/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

9 " ! 6

8 + C T & 8 + / / 0 : + = T

/ 8 & 9 * * 8 , 2

T % C

2 3 , 2

9 " ! 6

8 + C T & 8 0 % ? . / + + !

/ 8 & 9 * * + , 2 - - C

! : 0 C T % = ;

T & * * / , 2

T & * * 8 , 5

T $

T $

2 3 , 2

" % 9

# 0 % / % + ! 0 & C A ! % ; 8 9

C &

= T 8 & 0 ( T % C 2 3 , 2 )

T $ ) 2

3 , 2 (

T $ ) 2 3 , 2 .

1 , , G

1 , , G

( 4 , G )

T % C 2 3 , 2

! : 0 8 = ; + C & = / % ; : 8

T % & =

/ % ;

. J 1 2

!

/ / + + ! T + 9 # + 8 T : 8 +

/ &

/ C

* * + , - - C

C&=T8&0 $(0$+ +=%=; G

C & = T 8 & 0 0 + 8 & : T # : T G

2 3 , 2

9 % = . " T & # ,

G

T

9 " ! 6

8 + C T & 8 + / / 0 : + = T

9 " ! 6

8 + C T & 8 C 8 ; +

9 % = .

" T & #

T + 9 # + 8 T : 8 + % = C 8 + " +

& T % =

& T & : T

C & 0 !

% =

C & 0 ! & : T


RMB R'D Pa-e &0 %


41/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

$.1& MSD? C*a,-e 'eate, O4t9et Te5+e,at4,e Ct,9 6TIC#2;0>7


(1) #H%! =o.: 1


42/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

9 " ! 6 8 + C T & 8

C 8 ; +

T

& * * 8 , 2

/ :

+ 0 ; "

/ 8 & 9 * * ! 1 2

# % C

2 7 , 5

# $

2 7 , 5

#

T % C

2 , 7

T

: 8 = + 8

" % 9 # 0 % / % + ! 0 & C A ! % ; 8 9

/ % ; . J 1 5

9 " ! 6 C 8 ; + + T + 8 & : T

0 + T T + 9 # + 8 T : 8 +

" #

/ C

T 0

# 0

* * / , 2

* * / , 2

C & = T 8 & 0 ( T % C 2 , 7 )

/ : 8 = C + & : T 0 + T


RMB R'D Pa-e &2 %


43/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

$.1 MSD? Rea!t, Te5+e,at4,e Ct,9 6TIC#2"0"/2"11/2"1&7


(1) #H%! =o.: 1uire interbed >uenching. Temperature re>uired tocarry out the dewaxing reactions which increases gradually throughout the run as the

catalyst ages is controlled by adusting **8,2 feed inlet temperature through

manipulation of **/,2 firing rate and by the inlet and inter bed >uench flow rates. The

9"!6 8eactor consists of three beds of catalyst. To limit the overall exotherm in the

9"!6 two thirds of the expected exotherm is eliminated by means of >uench to the

outlet of the first and second beds. The >uench gas enters on flow control reset by

averaged bed inlet and averaged bed outlet temperature. n additional >uench gas

connection is provided to the inlet of the reactor for fast trim temperature control if

re>uired during an upset condition and for use in controlling the wetting exotherm on

startup.

8eactor temperature control is vital to good catalyst performance and should be

controlled to K - ,.3,C. !epending upon the age of the catalyst feed >uality feed rate

and the desired conversion a target 6eighted verage ed Temperature (6T) must

be maintained for each bed. /urther the temperature rise across each bed must be

'ept below a set targetB this is especially important during runaway reaction.

$.1.2 S=5+9==e B9!< D=a-,a5 MSD? Rea!t, Te5+e,at4,e Ct,9 6TIC#2"0"/2"11/2"1&7

8efer /%;. 14 on "heet =o 43.

$.1.$ De8!,=+t=

/or each catalyst bed inlet ( eight thermocouples in total) and outlet ( eight

thermocouples in total) temperatures are measured. ed %nlet (except top bed) and


RMB R'D Pa-e &$ %


44/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

&utlet (except bottom bed) Tis are averaged in a calculation (TI) bloc'. The target bed

outlet temperature is entered by operator based on the operating case and catalyst run

length. veraged out bed outlet temperature is compared to the operator entered set

point and this difference is used to reset the bed inlet target temperature with a time

delay of 3 min. (adustable). The bed inlet target temperature is compared to the actual

average inlet temperature (every 1 min. adustable). The difference between these two

values is used to reset >uench flow.

/or top bed reactor inlet temperature (T%2


45/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

99-R-02

TO 99-E-0! A#B#C

FROM 99-F-02

SP

PV

SP

FROM 99-C-02A#B

SP

BED TOP

BED BOTTOM

BED TOP

BED TOP

PV

PV

PV

PV

TO 99-F-01

TO 99-F-01

#F-02 TRIP

TO 99-F-01

#F-02 TRIP

BED

BOTTOM

BED

BOTTOM

#F-02 TRIP

TIC

2803

TIC

281"

TIC

2807

#$

TY

2811

TI

2803

TA TA

A-

FT

2803

FT

2802A#B

FV

2803

FV

2802

FV

2801

FO

FO

FO

#$

FT

2801

TI

2807

TA TA

A-

TI

2820

TA TA

A-

TI

2811

TA TA

A-

TY

2814

TIC

2814 TAL

PV

TI

2812

TA

TA

A-

TI

2814

TA TA

A-

FIC

2803

TY

2803

TIC

2811

TA TA

TAL

FIC

2802 TY

2807

TIC

2808

TA

TA

TAL

FIC

2801

TI

281"

TA TA

TI

2808

BED-1

BED-2

BED-3

I

8

#$

#$

I

8

I8

" % 9 #

0 % / % + ! 0 & C A ! % ; 8

9

9 " ! 6

8 + C T & 8 ( * * 8 , 2 ) T + 9 # + 8 T : 8 +

/ % ; . 1 4

C & =

T 8 & 0 ( T % C 2 < , < - 2 < 1 1 - 2 < 1 4 )


RMB R'D Pa-e & %


46/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

$.1; 'DF Rea!t, Te5+e,at4,e Ct,9 6TIC#2%0$/2%027


(1) #H%! =o.: 1uench flow to the !/ 8eactor. The !/ 8eactor consists of two beds of

catalyst. The !/ 8eactor (**8,5) exotherm is expected to be negligible in normal

operation. The !/ inlet temperature is controlled through bypassing of 9"!6 /eed

around the **+,. The >uench gas enters on flow control reset by averaged bed inlet

temperature. n additional >uench gas connection is provided to the inlet of the reactor

for fast trim temperature control if re>uired during an upset condition and for use in

controlling the wetting exotherm on startup.

$.1;.2 S=5+9==e B9!< D=a-,a5 'DF Rea!t, Te5+e,at4,e Ct,9 6TIC#2%0$/2%027

8efer /%;. 13 on "heet =o 4


47/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

$.1;.& De==t=8

/or the 9"!6 8eactor **8,5 there are 2 >uench gas flows:

ed %nleted

Temp.

verageCalculation

&utleted

Temp.

verageCalculation

ed&utletTemp.

Controller

ed%nlet

Temp.Controller

/lowController

1 T%2*15()

T%2*,<()

T%C2 %


48/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

99-R-03

TO 99-E-02 A#B#C

FROM 99-E-0! A#B#C

PV

SP

FROM 99-C-02A#B

SP

BED TOP

BED TOP

TO 99-F-01

BED BOTTOM

#F-02 TRIP

BED BOTTOM

TO 99-F-01

#F-02 TRIP

FT

2901FV

2901

FV

2902

FO

FO

FT

2902

TI

2908

TA TA

A-

TI

2913

TA TA

A-

TY

2902

TIC

2902 TAL

PV

TI

290"

TA TA

A-

TI

2902

TA TA

A-

FIC

2901

TIC

2903

TA

TA

TAL

FIC

2902

TI

2901

TA

TA

TI

2903

BED-1

BED-2

I

9

#$

I

9

" % 9 #

0 % / % + ! 0 & C A ! % ; 8

9

! /

8 + C T & 8 ( * * 8 , 5 ) T +

9 # + 8 T : 8 +

/ % ; .

1 3

C & =

T 8 & 0 ( T % C 2 * , 5 - 2 * , 2 )


RMB R'D Pa-e &" %


49/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

$.1> 'TS O'D/Re!@!9e Ga8 E!*a-e, 6%%#E#0>7 Re!@!9e Ga8 O4t9et Te5+e,at4,eCt,9 6TIC#$0027


(1) #H%! =o.: 1.2 S=5+9==e B9!< D=a-,a5 'TS O'D/Re!@!9e Ga8 E!*a-e, 6%%#E#0>7Re!@!9e Ga8 O4t9et Te5+e,at4,e Ct,9 6TIC#$0027

8efer /%;. 1 on "heet =o 3,.

$.1>.$ De8!,=+t=

8ecycle ;as outlet temperature controller T%C5,,2 is dual acting controller. T%C5,,2

controls 8ecycle ;as outlet temperature from **+,7 through control valves T$5,,2

and T$5,,2 by controlling the relative flows through exchanger **+,7 and its

bypass.

6hen the 8ecycle ;as outlet temperature from **+,7 increases than the set point

T%C5,,2 will pass less flow through the **+,7 i.e. bypass valve T$5,,2 starts to

open and %nlet valve T$5,,2 will start to close. 8everse action will be followed when

the 8ecycle ;as outlet temperature from **+,7 decreases i. e. start to close **+,7

bypass valve T$5,,2 and start to open the inlet valve T$5,,2. %n addition inlet

valve T$5,,2 is provided with min. stop to prevent exchanger running dry.


RMB R'D Pa-e &% %


50/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

T " " + # 8 T & 8 & $ !

/ 8 & 9 * * ! , 4

T % C

5 , , 2

8 + C I C 0 + ; "

/ 8 & 9 * * C , 2 -

T & * * + , 5 - - C

T & * * / C , 2

T $

T $

5 , , 2

" % 9 # 0 % / % + ! 0 & C A ! % ; 8 9

8 +

C I C 0 + ; " & : T 0 + T T + 9 # + 8

T : 8 + C & = T 8 & 0 ( T % C 5 , , 2 ) T $

) 5 , ,

2 .

T $ ) 5 , , 2 (

1 , , G

1 , , G

T % C 5 , , 2

! : 0 8 = ; + C & = / % ; : 8

T % & =

/ % ; . J 1

T " & $ ! - 8 + C I C 0 + ; " + N C

= ; + 8 ( * * + , 7 )

/ & /

C

* * + , 7

C&=T8&0 $(0$+ +=%=; G

C & = T 8 & 0 0 + 8 & : T # : T

G

5 , , 2

, G

! : 0 C T % = ;

T " " + # 8 T & 8 & $ !

8 + C I C 0 + ; "

4 , G

9 % = . " T & #

9 % = .

" T & #

T + 9 # + 8 T : 8 + % = C 8 + " +

& T % =

& T & : T

C & 0

! % =

C & 0 ! & : T


RMB R'D Pa-e 0 %


51/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

$.1" 'TS L=4=/F,a!. Btt5 E!*a-e, 6%%#E#1&A/B7 P,4!t St,=++e, FeeTe5+e,at4,e Ct,9 6TIC#$0017


(1) #H%! =o.: 1uid from **!,4 exchange heat with !ewaxed &il from $acuum !ryer (**T,) in

T" 0i>uid-/rac. ottom +xchanger (**+14-) and then routed to the #roduct

"tripper (**T,4). Control of the #roduct stripper feed temperature is accomplished by

T%C5,,1 by bypassing !ewaxed &il around the exchanger.

$.1".2 S=5+9==e B9!< D=a-,a5 'TS L=4=/F,a!. Btt5 E!*a-e, 6%%#E#1&A/B7'TS L=4= O4t9et Te5+e,at4,e Ct,9 6TIC#$0017

8efer /%;. 17 on "heet =o 32.

$.1".$ De8!,=+t=

#roduct stripper feed temperature controller T%C5,,1 is dual acting controller. T%C5,,1

controls #roduct stripper feed temperature from **+14- through control valves T$

5,,1 and T$5,,1 by controlling the relative flows through exchanger **+14-

and its bypass.

6hen the #roduct stripper feed temperature from **+14- increases than the set

point T%C5,,1 will pass less flow through the **+14- i.e. bypass valve T$5,,1

starts to open and %nlet valve T$5,,1 will start to close. 8everse action will be

followed when the #roduct stripper feed temperature from **+14- decreases i. e.

start to close **+14- bypass valve T$5,,1 and start to open the inlet valve T$

5,,1.


RMB R'D Pa-e 1 %


52/95


53/95



D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

$.1% P,4!t St,=++e, 9eve9 Ct,9/F9 Ct,9 t a!. F,a!. C*a,-e 'eate, %%#F#0$LIC#$$0$/FIC#$$02/FIC#$$0&7


(1) #H%! =o.: 1uid product flow to the $ac. /rac.

Charge eater (**/,5). lso the middle value of above /Ts shall be used by

computation bloc' (/I55,4) to calculate the difference between two flows and it will

give high difference alarm (/!) as applicable on !C".

%n addition to that level controller will give high-low alarm (055,5-0055,5) asapplicable on !C".


RMB R'D Pa-e $ %


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D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

" % 9

# 0 % / % + ! 0 & C A ! % ; 8 9

# 8 & ! : C T " T 8 % # # + 8 0 + $ + 0 C & = T

8 & 0 - / 0 & 6 C & = T 8 & 0 T & $ C .

/ % ;

. 1 <

/ 8 C . C 8 ; + + T + 8 * * / , 5 ( 0

% C 5 5 , 5 - / % C 5 5 , 2 - / % C 5 5 , 4 )

9 9 - T - 0 4

T O V A C U U M F R A C T I O N A T O R

C A R G E E A T

E R S U T D O W N

9 9 - F - 0 3


C A R G E E A T

E R 9 9 - F - 0 3

L I ' U I D F R O M 9 9 - D - 2 3 *

2 + + 3

9 9 - E - 1 4 * 9 9 - E - 1 "

M I D D L E V A L U E


C A R G E E A T

E R 9 9 - F - 0 3

2 + + 3

F D I

3 3 0 4

F D A

F Y 3 3 0 4

F I

3 3 0 "

F Y 3 3 0 2

F C

I 3 7

F T 3 3 0

4

A * B * C

F V 3 3 0 4

F I C 3 3 0 4

S E T P T

F A

F A L

P V

F C

I 3 7

L I C 3 3 0 3

L A

L A L

F T 3 3 0 2

A * B * C

F V 3 3 0 2

L T 3 3 0 3

F I C 3 3 0 2 S

E T P T

F A

F A L

P V

M I D D L E

V A L U E


RMB R'D Pa-e & %


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D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

$.20 a!. F,a!. C*a,-e 'eate, O4t9et Te5+e,at4,e Ct,9 6TIC#$07


(1) #H%! =o.: 1


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D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

more opening of /$5,1 H corresponding high flow of fuel oil to the burner. %f the

outlet temperature increases the actions will be vice versa.

"5,1 will be on /uel ;as mode controlling fuel gas flow rate with /ixed /uel

&il /low rate to maintain the furnace outlet temperature when furnace is run in

dual fired mode:

%n addition to that temperature controller will give high and low temperature alarm (T

53,3 H T053,3) pressure controller will give high and low flow alarm (#5,1 H

#05,1) and flow controller will give high and low flow alarm (/5,1 H /05,1)

as applicable on !C".


RMB R'D Pa-e ; %


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$.21 Fee/F,a!. Btt5 E!*a-e, 6%%#E#01A/B7 Ra=ate Fee Te5+e,at4,e Ct,96TIC#&10$7


(1) #H%! =o.: 1


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D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

: = % T / + + !

/ 8 & 9 " T & 8 ; +

T % C

4 1 , 5

! + 6 N + ! & % 0

/ 8 & 9 * * + 1 7 -

! : 0 C T % = ;

T & * * / C , -

T & * * / % 0 , 1

T $

" % 9 # 0 % / % + ! 0 & C A ! % ; 8 9

8 / / % = T + / + + ! T + 9 # + 8 T : 8 +

C & = T 8 & 0 ( T % C 4 1 , 5 )

T $ ) 4

1 , 5 .

T $ ) 4 1 , 5 (

1 , , G

1 , , G

T % C 4 1 , 5

! : 0 8 = ; + C & = / % ; : 8

T % & =

/ % ; . J 2 ,

/ +

+ ! - / 8 C . & T T & 9 + N C = ; +

8 ( * * + , 1 - )

/ C

*

* + , 1 -

C&=T8&0 $(0$+ +=%=; G

C & = T 8 & 0 0 + 8 & : T # : T

G

4 1 , 5

, G

T

! + 6 N + ! & % 0

T $

4 1 , 5

/ &

: = % T / + + !

T + 9 # + 8 T : 8 + % = C 8 + " +

& T

% =

& T & : T

C & 0 ! % =

C & 0 ! & : T


RMB R'D Pa-e % %


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D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

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(1) #H%! =o.: 1


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D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

/ + + !

/ 8 & 9 * * # , 2 -

T % C

4 1 , 1

! + 6 N + ! & % 0

/ 8 & 9 * * + 1 3 -

T & * * + , 1 -

T & * * + , 5 - - C

T $

T $

4 1 , 1

" % 9 # 0 % / % + ! 0 & C A ! % ; 8 9

! +

6 N + ! & % 0 & : T 0 + T T + 9 # + 8 T : 8 + C & = T 8 & 0 ( T % C 5 , , 2 ) T

$ ) 4

1 , 1 (

T $ ) 4 1 , 1 .

1 , , G

1 , , G

T % C 4 1 , 1

! : 0 8 = ; + C & = / % ; : 8

T % & =

/ % ; . J 2 1

6 8 9 / + + ! - / 8 C . & T T & 9 + N C = ; + 8 ( * * + 1 7 - )

/ & /

C

*

* + 1 7 -

C&=T8&0 $(0$+ +=%=; G

C & = T 8 & 0 0 + 8 & : T # : T

G

4 1 , 1

, G

! : 0 C T % = ;

! + 6 N + ! & % 0

/ + + !

T + 9 # + 8 T : 8 + % = C 8 +

" +

& T

% =

& T & : T

C & 0 ! % =

C & 0 ! & : T


RMB R'D Pa-e ;1 %


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D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

$.2$ a!445 F,a!. P45+a,4 Ret4, Te5+e,at4,e Ct,9 6TIC#&2017


(1) #H%! =o.: 1


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D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1

Date post:	07-Aug-2018
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Philosophy of Control for Complex Logics

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