philosophy of control for complex logics
TRANSCRIPT
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C'APTER ( &
P'ILOSOP'Y OF CONTROL
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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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This specification should be read in conunction with the following:
(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
This specification should be read in conunction with the following:
(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
This specification should be read in conunction with the following:
(1) #H%! =o.: 1
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LOBS QUALITY UPGRADATIONPROJECT
D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1
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".
PREPARED BY C'EC)ED BY C*a+te, ( &
RMB R'D Pa-e 22 %
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LOBS QUALITY UPGRADATIONPROJECT
D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1
! 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
; "
PREPARED BY C'EC)ED BY C*a+te, ( &
RMB R'D Pa-e 2$ %
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MUMBAI REFINERY Rev. Date: 20/01/2010
LOBS QUALITY UPGRADATIONPROJECT
D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1
$.; 'DF Rea!t, E94et Te5+e,at4,e Ct,9 6TIC#1>027
This specification should be read in conunction with the following:
(1) #H%! =o.: 1
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LOBS QUALITY UPGRADATIONPROJECT
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
PREPARED BY C'EC)ED BY C*a+te, ( &
RMB R'D Pa-e 2 %
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MUMBAI REFINERY Rev. Date: 20/01/2010
LOBS QUALITY UPGRADATIONPROJECT
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
This specification should be read in conunction with the following:
(1) #H%! =o.: 1
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LOBS QUALITY UPGRADATIONPROJECT
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
PREPARED BY C'EC)ED BY C*a+te, ( &
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LOBS QUALITY UPGRADATIONPROJECT
D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1
$." 'DT Rea!t, Te5+e,at4,e Ct,9 6TIC#201%/2012/201&/201;7
This specification should be read in conunction with the following:
(1) #H%! =o.: 1
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LOBS QUALITY UPGRADATIONPROJECT
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
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LOBS QUALITY UPGRADATIONPROJECT
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 )
PREPARED BY C'EC)ED BY C*a+te, ( &
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D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1
$.% MSD? Fee D=e,et=a9 P,e884,e Ct,9 6PDIC#21027
This specification should be read in conunction with the following:
(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).
PREPARED BY C'EC)ED BY C*a+te, ( &
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LOBS QUALITY UPGRADATIONPROJECT
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
This specification should be read in conunction with the following:
(1) #H%! =o.: 1
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LOBS QUALITY UPGRADATIONPROJECT
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,).
PREPARED BY C'EC)ED BY C*a+te, ( &
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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
PREPARED BY C'EC)ED BY C*a+te, ( &
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LOBS QUALITY UPGRADATIONPROJECT
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
This specification should be read in conunction with the following:
(1) #H%! =o.: 1
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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
PREPARED BY C'EC)ED BY C*a+te, ( &
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D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1
$.1$ 'DF Fee Te5+e,at4,e Ct,9 6TIC#2027
This specification should be read in conunction with the following:
(1) #H%! =o.: 1
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LOBS QUALITY UPGRADATIONPROJECT
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
PREPARED BY C'EC)ED BY C*a+te, ( &
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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
This specification should be read in conunction with the following:
(1) #H%! =o.: 1
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LOBS QUALITY UPGRADATIONPROJECT
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
PREPARED BY C'EC)ED BY C*a+te, ( &
RMB R'D Pa-e &2 %
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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
This specification should be read in conunction with the following:
(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
PREPARED BY C'EC)ED BY C*a+te, ( &
RMB R'D Pa-e &$ %
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LOBS QUALITY UPGRADATIONPROJECT
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
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LOBS QUALITY UPGRADATIONPROJECT
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 )
PREPARED BY C'EC)ED BY C*a+te, ( &
RMB R'D Pa-e & %
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MUMBAI REFINERY Rev. Date: 20/01/2010
LOBS QUALITY UPGRADATIONPROJECT
D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1
$.1; 'DF Rea!t, Te5+e,at4,e Ct,9 6TIC#2%0$/2%027
This specification should be read in conunction with the following:
(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
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LOBS QUALITY UPGRADATIONPROJECT
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 %
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MUMBAI REFINERY Rev. Date: 20/01/2010
LOBS QUALITY UPGRADATIONPROJECT
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 )
PREPARED BY C'EC)ED BY C*a+te, ( &
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LOBS QUALITY UPGRADATIONPROJECT
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
This specification should be read in conunction with the following:
(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.
PREPARED BY C'EC)ED BY C*a+te, ( &
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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
PREPARED BY C'EC)ED BY C*a+te, ( &
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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
This specification should be read in conunction with the following:
(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.
PREPARED BY C'EC)ED BY C*a+te, ( &
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MUMBAI REFINERY Rev. Date: 20/01/2010
LOBS QUALITY UPGRADATIONPROJECT
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
This specification should be read in conunction with the following:
(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".
PREPARED BY C'EC)ED BY C*a+te, ( &
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LOBS QUALITY UPGRADATIONPROJECT
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
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 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
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 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
PREPARED BY C'EC)ED BY C*a+te, ( &
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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
This specification should be read in conunction with the following:
(1) #H%! =o.: 1
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MUMBAI REFINERY Rev. Date: 20/01/2010
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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".
PREPARED BY C'EC)ED BY C*a+te, ( &
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MUMBAI REFINERY Rev. Date: 20/01/2010
LOBS QUALITY UPGRADATIONPROJECT
D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1
$.21 Fee/F,a!. Btt5 E!*a-e, 6%%#E#01A/B7 Ra=ate Fee Te5+e,at4,e Ct,96TIC#&10$7
This specification should be read in conunction with the following:
(1) #H%! =o.: 1
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MUMBAI REFINERY Rev. Date: 20/01/2010
LOBS QUALITY UPGRADATIONPROJECT
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
PREPARED BY C'EC)ED BY C*a+te, ( &
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MUMBAI REFINERY Rev. Date: 20/01/2010
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D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1
$.22 ?a,5 Fee/F,a!. Btt5 E!*a-e, 6%%#E#1>A/B7 Deae O=9 O4t9etTe5+e,at4,e Ct,9 6TIC#&1017
This specification should be read in conunction with the following:
(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
PREPARED BY C'EC)ED BY C*a+te, ( &
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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
This specification should be read in conunction with the following:
(1) #H%! =o.: 1
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D!. N. 1"#$1""#M#%%#01#&&00Rev. N. 1