CL2 compression SOP report_26 May 2016

1 | P a g e
Author: CangTo Cheah Date: 26th
May 2016
Document title: Estimation of settle out pressure of chlorine compression system during an ESD & normal shutdown
Disclaimer: This technical note is written in the interest of personal development & learning and for the sake of
posterity for those who appreciates the contributions of thermodynamics and mathematics in the detailed
engineering phase of turbo‐machinery system. This technical note reflects the author's best judgment and knowledge
(i.e. fundamental law of physics, thermodynamics and engineering mathematics) in light of the information and
resources available to him at the time of its preparation. Any use which any party makes of this technical note, on
any reliance on or decision to be made based on it, are the responsibility of such parties. The author accepts no
responsibility for damages, if any, suffered by any party as a result of decisions made or actions based on this
technical note.

Documents in referenced
Technip PID: CMDI‐5‐PROJ‐25‐6570 revision R1, CMDI‐5‐PROJ‐25‐6560 revision R1, CMDI‐5‐PROJ‐25‐6585 revision
R1.
Technip piping isometric drawings (not in MDT’s scope of supply): Refer to appendix 1
MDT’s piping volume data: Refer to appendix 2
MDT’s PID: 1975Z‐1‐A0103‐1011‐0001‐0001 revision 3
Static equipment supplier drawings (not in MDT’s scope of supply): 1975Z‐1‐A1109‐0841‐0001‐0004 revision 0
(Filters F6570 A/B), 1975Z‐1‐A1109‐0610‐0001‐0006 revision 1 (compressor suction cooler E6570) and 1975Z‐1‐
A1109‐0610‐0001‐0007 revision 1 (compressor discharge cooler E6571).
Project utility specification: GEN4‐1‐PROJ‐SP‐0001 revision B2
Thermodynamic literatures: (1) The properties of gases and liquids – 5th
edition, Bruce E. Poling, John M. Prausnitz
and John P. O’Connell. (2) Thermo‐physical properties of fluids – 1996, Marc J. Assael, J. P. Martin Trusler and
Thomas F. Tsolakis.

Introduction
The main purpose of this note is to calculate settle out pressure (SOP) of process medium trapped in between
suction isolation valve H656010 (CMDI‐5‐PROJ‐25‐6560), discharge isolation valve H657008 (CMDI‐5‐PROJ‐25‐6570),
depressurizing valve H657005 (CMDI‐5‐PROJ‐25‐6570) and sampling stream isolation valve H658501 (CMDI‐5‐PROJ‐
25‐6585). Per MDT’s requirement, nitrogen supply pressure 4 bar above the SOP (refer to page 6 of MDT’s PID) is
needed to ensure positive flow from dry gas seal to compressor (this will prevent process gas leaks into compressor
lube oil system).
Sub‐studies (related to SOP) that deemed beneficial to the compressor system which included in this study are listed
below:‐
a) Calculate mass of chlorine trapped in between the same envelope as described above. If total mass of
chlorine trapped in between the compression system exceeds 850 kg, suction and discharge isolation valves
shall be added near the compressor skid.
b) Determine dew point margin at various settle‐out temperatures (both initial phase and lowest ambient
temperature ‐10 deg. C scenario), so that the compression system will be depressurized to ensure no liquid
entrainment in the centrifugal compressor.
c) Gas temperature drop due to Joule‐Thomson effect during blowdown of process gas following an SOP.

2 | P a g e
Break‐down of piping volumes

Estimation of process mass trapped in the compression system
Process mass for each sections are calculated according to the following formula: PV = ZmRT
Where: P = pressure in Pascal, V = volume in m3
, Z = compressibility factor, m = mass in kg, R = specific gas constant
in J/kg‐K and T = temperature in Kelvin.
Note that compressibility factor is calculated from Lee‐Kesler‐Plocker law of corresponding state, with binary
interaction parameters dedicated for SLIC chlorine gas mixture extracted from HYSYS (commercially‐available
process simulation software).

Where:

Newton‐Raphson root‐finding method (https://en.wikipedia.org/wiki/Newton%27s_method) is used tackle the
above LKP equation, i.e. to solve for reduced volume (ν). Note: ν = [Pc / (R x Tc)] x Vm

Total mass of process medium (chlorine mixture) trapped in the compression system is 263.19 kg with molecular
weight 51.04 kg/kmol. This is equivalent to 5.1565 kmol of chlorine mixture, which yields 5.1565 kmol x 0.4817 =
2.4839 kmol of chlorine (process medium consists 48.17 mol% chlorine).
In term of conventional mass, chlorine in the system is 2.4839 kmol x 70.91 kg/kmol = 176.13 kg (note: molecular
weight of chlorine is 70.91 kg/kmol).
to

3 | P a g e
Estimation of settle out pressure and associated temperature in the
compression system
Total mass and total volume obtained in previous step are then used to estimate the SOP. Energy balance (i.e. mass
multiplied by enthalpy) is used to estimate the settle‐out temperature when the compression system is at SOP.

The idea is based upon the law of conservation of energy (total energy of an isolated system remains constant), i.e.
energy can neither be created nor destroyed; rather, it transforms from one form to another
(https://en.wikipedia.org/wiki/Conservation_of_energy).
Enthalpy is a measurement of energy in a thermodynamic system, it includes the internal energy (which is the
energy required to create a system, and the amount of energy required to make room for it by displacing its
environment and establishing its volume and pressure (https://en.wikipedia.org/wiki/Enthalpy).
Total energy at initial stage (assuming insignificant heat dissipation to environment via convection) of SOP shall
equal to the sum of energies at various locations of compression path based on steady‐state operating conditions
(i.e. various pressures and temperatures at different components, e.g. LP compression inlet, LP compression outlet,
inter‐stage cooler # 1 discharge, inter‐stage cooler # 2 discharge, HP compression inlet, HP compression outlet, and
after‐cooler discharge).
Side notes regarding the calculation of enthalpy with LKP law of corresponding state: Residual enthalpy is calculated
with 4th
order Gaussian numerical integration method at 200 density discrete at the vertical axis, and each density
row is further divided into 4 slots according to Gauss’ coefficients. Ideal gas enthalpy for the chlorine mixture is
converted from property data bank of “The Properties of Gases and Liquids – 5th
edition by Bruce E. Poling, John M.
Prausnitz and John P. O’Connell”. Formula for calculating enthalpy is in accordance with AGA report no. 10 (15th

November 2002).

In LKP law of corresponding state, compressibility factor is defined as (per Thermo‐physical properties of fluids –
1996, Marc J. Assael, J. P. Martin Trusler and Thomas F. Tsolakis):

And the partial derivative of compressibility factor with respect to temperature is derived as follows:‐

4 | P a g e
Calculated settle‐out pressures and enthalpies at various temperatures:‐

A guestimate algorithm is used to calculate the temperature which yields an energy level of 46.23 MJ at settle‐out
pressure. Settle‐out pressure is calculated to be 5.88 barA at 32.07 deg. C with compressibility factor 0.9777.

5 | P a g e
The following graph shows the trend of energy level (J) with respect to SOP (barA), i.e. energy level decays with
reduction in SOP:‐

The following graph shows the trend of SOP (barA) with respect to equilibrium temperature (deg. C), i.e. settle‐out
temperature increases with SOP:‐

6 | P a g e
Estimation of dew point margin with respect to SOP

The curve on the left represents the vapor dew point curve for process gas, the line on the right is the SOP curve
calculated at various temperatures. We can see that dew point margin reduces when SOP reduces.

Vapor saturation curve is calculated with Vapor‐Liquid Equilibrium (VLE) technique based on partial fugacity
coefficients according to the literature “Thermo‐physical properties of fluids – 1996”.

Equation of state used in the VLE calculation is Redlich‐Kwong‐Soave (RKS) cubic type equation of state (RKS and LKP
are recommended by Mr. Klaus Lüdtke for chlorine gas in his compressor literature; to be more precise clause 2.2.6
of Process Centrifugal Compressors) with binary interaction parameters (BIP) extracted from HYSYS software. BIP for
RKS is tabulated below:‐

Note: RKS equation of state is used for VLE calculation due to its simplicity in arriving the departure function for
partial fugacity coefficients.
Vapor saturation curve
based upon RKS EoS
SOP curve
Vapor + liquid region Full vapor region

7 | P a g e
Validation of vapor saturation curve with compressor OEM’s information

There is a need to verify the validity of vapor saturation curve which is used as reference in the interest of dew point
margin throughout this study.

Project specific (chlorine gas mixture) vapor saturation curves from compressor OEM and author’s calculation are
overlapped on the same scale (with background of compressor OEM’s curve being set to transparent), i.e. vapor
saturation calculation based upon VLE technique is justified (within the ranges of pressure and temperature
presented above).

8 | P a g e
The following curve shows the relationship between dew point margins (deg. C) and SOP (barA).

Dew point margin at initial stage of SOP is approximately 40.71 deg. C, it declines with the reduction of SOP (due to
gradual heat rejection from the metal surface of chlorine compression system to ambient air); dew point margin
when process medium decays to lowest ambient temperature (‐10 deg. C) is 2.92 deg. C at 5.02 barA.

At initial SOP
condition
SOP at lowest
ambient temperature

9 | P a g e
Gas temperature drop due to Joule‐Thomson effect during blowdown of
process gas following an SOP
Joule‐Thomson coefficient at SOP condition (P = 5.88 barA, T = 32.07 deg. C) is estimated as 0.0000101878 Kelvin /
Pascal. Expected temperature drop when the process gas is relieved to atmospheric pressure (1.01325 barA) is
approximately 4.96 Kelvin, which means process gas temperature is reduced to 27.11 deg. C.

It can be seen that:‐
a) Gas temperature during blow down following an SOP is not the governing case to determine minimum
design metal temperature (MDMT) of compressor gas path / casing. Current MDMT is ‐10 deg. C which is
due to lowest ambient temperature.

b) No liquid formation in process gas during blowdown (from 5.88 barA) following an SOP event, refer to
graphical presentation below.

Note: Joule‐Thomson coefficient used in this study note is in accordance with the formula provided in Perry’s
chemical engineers’ handbook (7th
edition), as defined below:‐

Blowdown line from
SOP 5.88 barA
based upon RKS EoS
Vapor + liquid region Full vapor region
Adequate dew point margin, i.e. > 15 Kelvin

10 | P a g e
(dV/dT) at constant pressure in LKP law of corresponding state is derived as follows (author’s hand‐written
derivations in the olden days):‐

Where: Ru = universal gas constant, Tc = critical temperature, Pc = critical pressure, Vm = m3
/mol., T = temperature.

11 | P a g e
Conclusions
Settle‐out pressure is estimated at 5.88 barA with settle‐out temperature 32.07 deg. C, this fulfils MDT’s
requirement on minimum 4 bar differential pressure on N2 supply pressure to dry gas seal system. The available
margin of N2 supply pressure is 4.62 barD (i.e. subtracting 5.88 barA from 10.5 barA). Note that minimum nitrogen
supply pressure is 10.5 barA according to clause 15.1 of project utility specification GEN4‐1‐PROJ‐SP‐0001 revision
B2:‐

Total chlorine trapped in the compression system is estimated at 176.13 kg, below the limitation of 850 kg i.e.
Category 4 release event per Client’s LOPA matrix. This implies suction and discharge isolation valves near
compressor skid are unnecessary, refer to item 8 of 1975Z‐C349‐MOM‐049‐F1 (29‐30th
Oct 2015):‐

The compression system shall be depressurized at standstill condition when gas condition approaches vapor
saturation point. From machinery protection perspective or perhaps in the interest of equipment warranty, dew
point margin at standstill condition should be determined by MDT. Preliminary response from MDT dated 24th
March
2016, quoted as follows “We have to avoid any liquid in the compressor, in special because of the design with the
compressor nozzle up direction. Therefore the system should be prepared for depressurization during standstill. MDT
PLC will deliver the required signal for your depressurization device, probably valve shown on the P&ID.”.

12 | P a g e
Further email correspondence from MDT (29th
March 2016) requires minimum dew point margin of 15 K.
It is convenient to view dew point margin with respect to settle‐out pressure. With the information of vapor
saturation curve and SOP curve; dew point margin vs. SOP is obtained, as tabulated below:‐
Subtracting temperatures of saturation curve from temperatures of SOP
curve yields

The following discrete data sets (2.92, 5.02; 11.85, 5.23, 20.81, 5.43; 29.81, 5.63; 38.84, 5.84; 40.71, 5.88) are
transformed into an equation which allows us to interpolate SOP values (in between 5.02 barA to 5.88 barA) based
on dew point margin in a precise manner.

The best fit (applying least squares method) of the above data sets is found to be 3rd
order polynomial function, see
comparison tabulated below (of course 4th
order can also be used, at the expense of additional coefficient):‐

Note the first column contains dew point margins (i.e. x‐values or input variable).
The SOP values (y‐values or output variable) calculated with 3rd
order polynomial function (fifth column) are very
close to the input data (second column) compared to linear (third column) and quadratic (fourth column) functions.

13 | P a g e
Coefficients for 3rd
order polynomial function are given below (valid for pressure range in between 5.02 barA to 5.88
barA):‐

Note that SOP = a0 + (a1 x DPM) + (a2 x DPM2
) + (a3 x DPM3
)
Where: DPM = dew point margin

Settle‐out pressure at dew point margin 15 Kelvin is approximately 5.30 barA. Associated settle‐out temperature at
SOP 5.30 barA is reverse‐calculated, around 3.60 deg. C, as tabulated below:‐

14 | P a g e
Information obtained above is consolidated and transferred into graphical form for clearer visual understanding.

The curve on the left represents vapor saturation limit (liquid / vapor mixture on its left, full vapor on its right) for
project specific gas composition (chlorine mixture).
The relatively straight line on the right end represents SOP curve calculated at various temperatures (from 85 deg. C
down to ‐10 deg. C) to cover various scenarios that might be encountered by the compression system during
pressurized hold.
The compression system will initially be experiencing an SOP value of 5.88 barA (32 deg. C), due to energy balance
(mass times enthalpy) from various parts of the compression system i.e. LP [3.013 barA, 15 deg. C], HPHT [12.7 barA,
85.7 deg. C], HPLT [12.1 barA, 40 deg. C], MPHT [6.303 barA, 93 deg. C], MPMT [6.138 barA, 43 deg. C] and MPLT
[5.973 barA, 10 deg. C].
It is assumed that most parts of the compression system (piping, valves, static equipment, compressor) are not
thermally‐insulated, heat transfer will occur from hot‐to‐cold medium (fundamental thermodynamics teaching) and
lead to reduced internally energy of process medium where both pressure and temperature decrease accordingly.

15 Kelvin
SOP curve
Full vapor regionLiquid + vapor region
Initial SOP conditions
SOP decay due to heat
dissipation to ambient air

15 | P a g e
The compression system will be depressurized once dew point margin reaches the minimum threshold 15 Kelvin. It is
crucial to ensure no liquid formation occurs during the depressurization process, Joule‐Thomson effect is therefore
considered; based on initial conditions prior to depressurization, i.e. 5.30 barA at 3.6 deg. C.
Joule‐Thomson effect due to blow down of process gas from 5.30 barA (at 3.60 deg. C) to atmospheric pressure:‐

Joule‐Thomson coefficient is approximately 0.0000116586 K/Pa. With a pressure differential of 4.29 bar,
temperature drop is 5 Kelvin. Blowdown line (from 5.30 barA down to 1.01 barA) is plotted together with vapor
saturation curve, as shown below.

It can be seen that blowing‐down the process gas from 5.30 barA to atmospheric pressure will maintain a positive
dew point margin; i.e. no liquid formation throughout the entire blow down sequence.

End of note CT Cheah (26th
May 2016)
15 Kelvin
Blowdown line from
SOP 5.30 barA
Liquid + vapor region Full vapor region

178 mm
110 mm
381 mm
241 mm
381 mm
381 mm
1246 mm
740 mm
30 mm
284 mm
180 mm
381 mm
381 mm
1379 mm
381 mm
381 mm
5083 mm
381 mm
381 mm
1735 mm
381 mm
117 mm
740 mm
284 mm
30 mm
137 mm
See page 14
Appendix 1 - Technip's isometric drawings
To after-cooler
(E6571) inlet nozzle
To compressor
discharge PSV

From after-cooler
(E6571) discharge
nozzle
Newly added
non-return valve
Compressor anti-surge valve
upstream tapping point.
External recycle valve
upstream tapping point
See page 4
See page 5
See page 7
Page 3
137 mm
137 mm
66 mm
381 mm
117 mm
381 mm
381 mm
137 mm
181 mm
1334 mm
381 mm
381 mm
1818 mm
381 mm
137 mm
66 mm 381 mm
2392 mm
381 mm
381 mm
1238 mm
381 mm
381 mm
2338 mm
381 mm
381 mm
238 mm
381 mm
22338 mm
76 mm
76 mm
188 mm
303 mm
Straight pipe or equivalent (inches) Schedule Length (mm)
10 40 117+1334+1818+2392+1238+2338+238+22338
2 80 188+303
1.5 80 181
8 40 66+66
Pressure = 12.1 barA
Temperature = 40 deg. C

To blow down
(depressurizing) valve
Compressor discharge
isolation valve
See page 3
See page 6
Page 4
381 mm
381 mm
5238 mm
381 mm
381 mm
6588 mm
381 mm
178 mm
63 mm
216 mm
500 mm
137 mm
457 mm
2246 mm
10 40 5238+6588+2235+2246
4 40 500
2235 mm

See page 3
Page 5
See page 12
ASV upstream
ASV return
Compressor ASV
8"
8"
8"
6"
6"
6"
457 mm
457 mm
457 mm
457 mm
457 mm
3119 mm
457 mm
1591 mm
1646 mm
203 mm
152 mm
101 mm
84 mm
291 mm
1861 mm
8 40 511+559+111
6 40 101+998+(473/2)
1 80 291
6 40 (473/2)+1598
12 40 1861+1646+3119+1591
3.013 bara
3.013 bara
12.1 bara

See page 4
Discharge blow down valve
Page 6
152 mm
152 mm
152 mm
3058 mm
3746 mm
152 mm
152 mm
1796 mm
152 mm
86 mm
178 mm
4 40 3058+3746+1796+86+178

See page 3
Page 7
External recycle valve
Upstream
Recycle valve return
See page 8
305 mm
305 mm
305 mm
305 mm
3192 mm
963 mm
2877 mm
3064 mm
110 mm
290 mm
8 40 3192+963+2877
1 80 290
8 40 3064
12.1 bara

See page 7
See page 9
See page 10
Page 8
457 mm
457 mm
986 mm
457 mm
178 mm
4699 mm
203 mm
111 mm
330 mm
457 mm
8004 mm
457 mm
457 mm
3286 mm
457 mm
9924 mm
8 40 111
12 40 986+4699+8004+3286+9924
14 40 280+279

See page 8
Suction isolation valve
457 mm
162 mm
114 mm 114 mm
114 mm
114 mm
269 mm
1122 mm
286 mm
457 mm
457 mm
457 mm
457 mm
14736 mm
1786 mm
1448 mm
162 mm
76 mm
230 mm
12 40 14736+1786+1448
3 40 286+1122+269
2 80 230+70
76 mm
70 mm
3
See page 16
From chlorine sampling return line

Compressor
suction filter inlet
Compressor
suction filter inlet
Page 10
See page 11
533 mm
533 mm
898 mm
533 mm
2998 mm
533 mm
898 mm
279 mm
533 mm
533 mm
533 mm 533 mm
2134 mm
1417 mm
178 mm
840 mm
30 mm
284 mm
14 40 1417+2134+1604+2998+898
2 80 840
1 80 284
1604 mm
524 mm
Assumed unit offline (standby);
i.e. isolation valve shut.
3
See page 8

Compressor suction
filter outlet
Compressor suction
filter outlet
Page 11
See page 12
533 mm
143 mm
533 mm
533 mm
219 mm
533 mm
533 mm
1239 mm
533 mm
533 mm
533 mm
2997 mm
533 mm
1239 mm
533 mm
533 mm
219 mm
533 mm
143 mm
178 mm
472 mm
178 mm
840 mm
30 mm
284 mm
14 40 143+219+1239+2997+472
2 80 840
1 80 284
524 mm
Assumed unit offline (standby);
i.e. isolation valve shut.
3

Compressor suction
cooler inlet
See page 11
See page 5
533 mm
533 mm
533 mm
280 mm
1570 mm
533 mm
533 mm
355 mm
533 mm
143 mm
417 mm
178 mm
840 mm
30 mm
284 mm
14 40 417+1570+355+143
2 80 840
1 80 284
12 40 92
178 mm
92 mm

Compressor suction
cooler discharge
To compressor
suction KO pot
Page 13
533 mm
533 mm
143 mm 472 mm
533 mm
1595 mm
533 mm
533 mm
3734 mm
533 mm
3242 mm
222 mm
666 mm
222 mm
178 mm
230 mm
14 40 472+1595+3734+3242+666
1.5 80 230

229 mm
229 mm
229 mm
497 mm
229 mm
1304 mm
See page 2
Compressor
discharge PSV
Rupture disk
See page 15

See page 9
114 mm
79 mm
114 mm
114 mm
1322 mm
114 mm
114 mm
672 mm
114 mm
114 mm
114 mm
114 mm
114 mm
114 mm
114 mm
114 mm
1572 mm
3172 mm
372 mm
9947 mm
114 mm
777 mm
3 40 79+1322+672+9947+372+3172+1572+777

7
K6570
EN
00110001999795DRW
AFTER HAZOP
05.10.2015Schmitz05.10.2015Schrader
17.02.2016STZ17.02.201603 BPL
TRAIN
OF303
Lange
DOC. PARTDOCUMENT NO.DOC. TYPE
ORIGINAL
INDEX
REV. PAGE
LANG.SIZE
SHEET
RELEASED
CHANGE DESCRIPTIONCHANGE NO.
CHECKED
CHECKEDCHANGED
DATEDATE
DATEDATE
DATEISSUED
REV.
05.10.2015
P&I DIAGRAM CMDI-5-PROJ-25-657
PROCESS
CAOCHLOR
H.3600045.36
R
Q
N
M
L
K
G
E
D
C
B
A
1 2 3 4 5 6 7 8 9 10 11 12 13 16 17 18 20 21 2414 15 19 22 23
F
H
23 241 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22
P
J
R
Q
P
N
M
L
K
J
H
G
F
E
D
C
B
A
This document is the property of MAN Diesel & Turbo SE and is solely for the use of the party to which it is handed over.
2"
14"
2"
2"
2"
2"
2"
SET@= 18 bar(g)
4" 4"
F6570 A/B
3/4"
K6570
PROCESS GAS
PROCESS GAS
PI
657407
CR
P+
PI
657407
DCS P+
TI
657408
CR
TI
657408
DCS
FI
657409
CR
FI
657409
DCS
TI
657422B
CR
To+
TI
657422B
DCS
To+
TI
657422C
CR
To+
TI
657422C
DCS
To+
TS
657422
CR 2oo3
To+
TS
657422
DCS
To+
001
PI
657424
CR
P+
PI
657424
DCS
P+
TI
657423
CR
T+
TI
657423
DCS
T+
FO
FCV
657427
010
R10001 PIT
657407
PIT
657424
FIT
657409
E6571
V
D
TI
657422A
DCS
To+
TI
657422A
CR
To+
PDIT
657406
PDI
657406
CR
PD+
PDI
657406
DCS
PD+
LO
LO
LO
R14300
E6574
V
D
TI
657412A
CR
To+
TI
657412A
DCS
To+
TI
657412B
CR
To+
TI
657412B
DCS
To+
TI
657412C
CR
To+
TI
657412C
DCS
To+
TS
657412
CR2oo3
To+
TS
657412
DCS
To+
001
001
PIT
657414
PI
657414
CR
P+
PI
657414
DCS
P+
TI
657418
CR
T+
TI
657418
DCS
T+
PIT
657404
PIC
657404
CR
PI
657404
DCS
R22208
R22207
TE
657412A
TE
657412B
TE
657412C
TE
657418
TE
657422A
TE
657422B
TE
657422C
TE
657408
TE
657423
ZC
657427
S
PI
ZSH
657427
ZAH
657427
CR
ZAH
657427
DCS
ZSL
657427
ZAL
657427
CR
ZAL
657427
DCS
ZT
657427
ZI
657427
CR
ZI
657427
DCS
XY
657427
CR
405
FIC
657X
CR
400
R19445R19446
PIT
657410A
PI
657410A
CR
Po+
PI
657410A
DCS
Po+
PIT
657410B
PIT
657410C
PI
657410B
CR
Po+
PI
657410B
DCS
Po+
PI
657410C
CR
Po+
PI
657410C
DCS
Po+
PS
657410
CR2oo3
Po+
PS
657410
DCS
Po+
PIT
657411A
PI
657411A
CR
Po+
PI
657411A
DCS
Po+
PIT
657411B
PIT
657411C
PI
657411B
CR
Po+
PI
657411B
DCS
Po+
PI
657411C
CR
Po+
PI
657411C
DCS
Po+
PS
657411
CR2oo3
Po+
PS
657411
DCS
Po+
TI
657413
CR
T+
TI
657413
DCS
T+
TE
657413
PI
657417
CR
P+
PI
657417
DCS
P+
PIT
657417
PIT
657420A
PI
657420A
CR
Po+
PI
657420A
DCS
Po+
PIT
657420B
PIT
657420C
PI
657420B
CR
Po+
PI
657420B
DCS
Po+
PI
657420C
CR
Po+
PI
657420C
DCS
Po+
PS
657420
CR
2oo3
Po+
PS
657420
DCS
Po+
PIT
657421A
PIT
657421B
PIT
657421C
PI
657421A
CR
Po+
PI
657421A
DCS
Po+
PI
657421B
CR
Po+
PI
657421B
DCS
Po+
PI
657421C
CR
Po+
PI
657421C
DCS
Po+
P
657421
CR2oo3
Po+
P
657421
DCS
Po+
001
001
001
PDIT
657416
PDI
657416
CR
PD+
PDI
657416
DCS
PD+
E6573
V
D
R21208
R21207
D6570
E6570
V
D
R10607
LIT
657403
LI
657403
CR
L++
LI
657403
DCS
L++
001
010
D6571
LIT
657415
LI
657415
CR
L++
LI
657415
DCS
L++
PCV
657405
ZY
657405
ZSH
657405
ZSL
657405
ZAH
657405
CR
Z+
ZAH
657405
DCS
Z+
ZAL
657405
CR
Z-
ZAL
657405
DCS
Z-
010
R79485
R11617
PROCESSGAS
FLARE
ZSH
657425
ZSL
657425
S
657426
CR
ZSH
657401
ZSL
657401
S
657402
CR
010
ZAH
657401
DCS
ZAL
657401
DCS
ZAH
657425
DCS
ZAL
657425
DCS
INSTRUMENT AIR
001
010
010
R21206
R21205
R22206
R22205
COOLINGWATER
COOLINGWATER
CHILLEDWATER
CHILLEDWATER
FE
657409
LC
LC
ZT
657405
ZI
657405
CR
ZI
657405
DCS
03
REV 03
REV
H
656010
03
REV
TOSAFELOCATION
03
REV
R39007
TO SAFE LOCATION
03
REV
03
REV
PI
????
INSTRUMENT AIR
03
REV
TOSAFELOCATION
03
REV
03
REV
03
REV
H
657008
03
REV
NOTE 2NOTE 2
NOTE 5
NOTES:
CHECK VALVE AS CLOSE AS POSSIBLE TO THE ANTI SURGE LINE
STRAIGHT PIPE LENGTH UPSTREAM / DOWNSTREAM: 5D / 10D
MAXIMUM VOLUME BETWEEN COMPRESSOR DISCHARGE FLANGE, ANTISURGE VALVE
AND CHECK VALVE SHOULD BE LESS THAN EFFECTIVE VOLUME FLOW [m3/s] * 1s
COMPRESSOR BLOWDOWN IN CASE OF SEAL FAILURE
AS CLOSE AS POSSIBLE TO COMPRESSOR DISCHARGE FLANGE
TEMPORARY STRAINER, TO REMOVE AFTER START UP
MECHANICAL MINIMUM POSITION
1.
2.
3.
4.
5.
6.
7.
NOTE 6
NOTE 3
NOTE 5
NOTE 1
NOTE 5
NOTE 5
NOTE 6
NOTE 7
NOTE 4
NOTE 4
NOTE 4
DE NDE
4
NOTE 3
NOTE 3
NOTE 4
3421
FC
V = 3.2m³
V = 0.65m³
V = 0.5 m³
ETEYB/Marcel Poyda
11.03.16
V = 0.65m³
V = 3.5m³
Appendix 2 - MDT's piping volume

CL2 compression SOP report_26 May 2016

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CL2 compression SOP report_26 May 2016