1975Z-1-TBT-1011-0001-B1

TECHNIP TIANCHEN CHEMICAL ENGINEERING (TIANJIN) CO., LTD.
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SLIC HCL Recycle Project
Pages modified under this revision:
B1 2015/07/01 Issued for CBT CHEAH CangTo WANG XinCong WANG XinCong RAO HongLing
A1 2015/06/26 Issued for comment CHEAH CangTo WANG XinCong WANG XinCong RAO HongLing
Rev. Date
YYYY/MM/DD
STATUS WRITTEN BY (name & visa) CHECKED BY (name & visa) REVIEWED BY
(name & visa)
APPROVED BY
(name & visa)
DOCUMENT REVISIONS
Sections changed in last revision are identified by a vertical line in the right margin
Proprietary and Confidential information belonging to Shanghai Lianheng Isocyanate Co., Ltd
Document class B: Confidential (Not to be disclosed without authorization)
Technical Bid Tabulation for Chlorine
Compressor Package
CangTo Cheah
2015.07.01
17:20:16 +08'00'
XinCong Wang
2015.07.01 17:30:34
+08'00'
XinCong Wang
2015.07.01
17:30:54 +08'00'
HongLing Rao
2015.07.01
17:31:18 +08'00'

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CONTENTS
EVALUATION BASED ON MAN DIESEL & TURBO’S TECHNICAL PROPOSAL ..........................4
1.1 MDT’s compressor train arrangement ......................................................................................4
1.2 MDT’s compressor shaft seals.................................................................................................5
1.3 MDT’s compressor casing........................................................................................................6
1.4 MDT’s compressor performance ..............................................................................................7
1.5 MDT’s thermodynamic model...................................................................................................8
EVALUATION BASED ON SIEMENS’ TECHNICAL PROPOSAL...................................................9
2.1 Siemens’ compressor train arrangement..................................................................................9
2.2 Siemens’ compressor shaft seals........................................................................................... 10
2.3 Siemens’ compressor casing ................................................................................................. 12
2.4 Siemens’ compressor performance........................................................................................ 14
2.5 Siemens’ thermodynamic model ............................................................................................ 15
Appendix 1: Technical bid tabulation............................................................................................. 16
Appendix 2: Dew point margin upstream of compressor inlet flanges ........................................... 17
Appendix 3: Evaluation of compressor final stage discharge temperature when inter-stage chilled
water supply fails .......................................................................................................................... 18
Appendix 4: Evaluation of compression stage discharge temperature when first stage inlet
temperature increases to 23.5 deg. C ........................................................................................... 19
Appendix 5: Minutes of meeting for MAN Diesel & Turbo.............................................................. 20
Appendix 6: Minutes of meeting for Siemens ................................................................................ 21
Note: Electronic bookmarks are implemented in PDF copy of this document.

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This write-up and associated technical bid tabulation (Appendix 1) contain detailed technical
review for the bids of SLIC project chlorine compressor package. Material requisition for chlorine
compressor package (1975Z-1-MR-1011-0001-B3) was sent out to three compressor suppliers,
namely:-
1) MAN Diesel & Turbo (MDT)
2) Siemens
3) Kobelco
Technical bids from all three compressor suppliers were received on mid April 2015, noting that
multi-shaft integrally-geared centrifugal compressor was proposed by Kobelco, on the other hand
single shaft centrifugal compressors were proposed by MDT and Siemens.
Kobelco had declined to continue their further involvement with SLIC chlorine compressor package
at the first round of technical clarification in 4th May 2015 (see below).

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EVALUATION BASED ON MAN DIESEL & TURBO’S TECHNICAL PROPOSAL
1.1 MDT’s compressor train arrangement
API 617 single shaft centrifugal compressor is indirectly-coupled to HV induction motor (fixed
speed) via an API 613 double helical speed increaser.
Inlet of each compression stage is provided with a knock-out pot, which is in compliance with
project LOPA / HAZOP requirement.
MDT’s machine comprises two compression stages with one inter-stage cooling. Inter-stage
cooling comprises of two shell and tube heat exchangers (TEMA Class R) configured in series.
First cooler utilises cooling water (supply temperature 33 deg. C & maximum return temperature 43
deg. C) as coolant and second cooler uses chilled water as cooling medium (supply temperature 5
deg. C & return temperature 10 deg. C).
Capacity control is realized (in MDT’s compressor PLC) via suction throttling valve (supplied by
MDT with associated pre-fabricated process piping). Whereas anti-surge protection is taken care
by anti-surge valve (loose-supplied by MDT) and integrated with MDT’s compressor PLC.

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1.2 MDT’s compressor shaft seals
Double oppose self-acting dry gas seals with segmented carbon rings (separation seals) are
offered by MDT, in compliance with project requirement.
Nitrogen leakage that commingles with process gas in process chamber is guaranteed at 2.4 kg/hr
(total value for drive & non-drive end dry gas seals). Note that process mixture (51.04 kg/kmol)
contains nitrogen gas of 15.37 mol% (equivalent to 8.44 weight %) at total weight flow 31090 kg/hr
consists 2624 kg/hr of nitrogen stream. This leakage rate (i.e. 2.4 kg/hr of nitrogen) is insignificant
(in comparison with 2624 kg/hr of nitrogen in main process stream) and therefore deemed
acceptable from process perspective as nitrogen gas is allowed in process gas mixture.

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1.3 MDT’s compressor casing
Compressor casing offered by MDT is barrel type, see above (typical barrel casing construction).
Plant down time due to compressor internal change-out can be greatly reduced as the spare
internal bundle (to be supplied by MDT as capital spare) is pre-assembled with rotor, bearings, dry
gas seals, static diaphragm and return channels. Note that spare internal bundle will undergo 4-
hour mechanical running test and performance test in the contract barrel casing at MDT’s
workshop.

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1.4 MDT’s compressor performance
Generic compressor performance curve (polytropic efficiency vs. flow coefficient) shown above is
extracted from Process Centrifugal Compressor: Basics, Function, Operation, Design,
Application (by Klaus Ludtke, Springer 2004).
The generic curve provides rough guideline for basic value of polytropic efficiency vs. flow
coefficient for impellers with backward curved blades, medium Mach and Reynolds numbers and
medium impeller diameters. This curve needs to be corrected for size, shroud leakage, Mach
number, Reynolds number, surface roughness, diffuser ratio, inlet loss, exit loss and geometry
variants.
Lacking of correction factors (as stipulated above), the generic curve however can still be utilized
as a reliable guideline to select impeller stages with good performance aiming at optimum flow
coefficient region. Flow coefficient is to a great extent an independent tool for compressor designer
to determine the size (e.g. number of impellers, impeller diameter, shaft diameter, shaft length, etc)
and speed of the machine and is indubitably the most influencing parameter for the efficiency and
associated head coefficient.
Flow coefficient at each compressor stage inlet is calculated based on impeller diameter, rotational
speed and actual inlet volume flow rate provided in MDT’s compressor data sheet. It can be seen
that flow coefficients (for certified point) yielded from MDT’s compressor selection (first stage
0.1027 & second stage 0.0503) are scattered at the optimum efficiency plateau, i.e. good overall
impeller stage efficiency.
0.65
0.67
0.69
0.71
0.73
0.75
0.77
0.79
0.81
0.83
0.85
0 0.02 0.04 0.06 0.08 0.1 0.12 0.14 0.16
Polytropic efficiency vs. flow coefficient
Ludtke generic curve
MDT stage 1 per Ludtke generic curve
MDT stage 2 per Ludtke generic curve
MDT stage 1 per MDT curve
MDT stage 2 per MDT curve
Optimum efficiency plateau

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1.5 MDT’s thermodynamic model
Process temperatures are one of the crucial thermodynamic factors in chlorine gas compressions
(condensate would occur if temperature too low; risk of run-away reaction with compressor internal
when temperature gets high), thermodynamic models used by compressor supplier shall therefore
be disclosed to Purchaser. As informed by MDT, thermodynamic models used are:-
(a) Lee-Kesler-Plocker (LKP) corresponding state for calculations of isentropic / polytropic
exponents, compressibility factor, density, etc based on project specific process gas
mixture.
(b) Redlich-Kwong-Soave (RKS) cubic equation of state to develop vapour dew point of project
specific process gas mixture.
Both LKP and RKS are recommended for chlorine gas compression according to Ludtke’s
compressor literature.
Minimum dew point margin at compressor inlet flange required by MDT is 10 deg. C. According to
inlet conditions stated in MDT’s data sheet for certified case, it is confirmed that minimum dew
point margin is fulfilled with MDT’s selection.
0
2
4
6
8
10
12
14
16
18
20
-50 -40 -30 -20 -10 0 10 20 30
Pressure(barA)
Temperature (deg. C)
Vapor saturation curve for SLIC chlorine gas mixture
Vapor saturation curve_Redlich Kwong Soave
MDT stage 1 inlet
MDT stage 2 inlet
41.35 deg. C
17.38 deg. C

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EVALUATION BASED ON SIEMENS’ TECHNICAL PROPOSAL
2.1 Siemens’ compressor train arrangement
API 617 single shaft centrifugal compressor is indirectly-coupled to HV induction motor (fixed
speed) via an API 613 double helical speed increaser.
Only one suction knock-out pot is provided by Siemens, whereas the LOPA / HAZOP require inlet
of each compression stage needs to be fitted with a knock-out pot.
Siemens’ machine consists three compression stages with two inter-stage cooling. Each inter-
stage cooling itself is made up of a shell and tube heat exchanger (TEMA Class R) with cooling
water (supply temperature 33 deg. C, maximum return temperature 43 deg. C) being the coolant.
Both capacity control and anti-surge protection are realized (in Siemens’ compressor PLC) via
cooled bypass / anti-surge valve loose-shipped by Siemens.

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2.2 Siemens’ compressor shaft seals
Despite the mandatory requirements for dry gas seals as stated in clause 2.8.1.3 of GEN4-0-
ROTE-SP-0012-B1 and item 1.6 of 1975Z-1-SR-1011-0001-B3 (as well as technical bid
clarifications and email correspondence), 3-chamber labyrinth compressor shaft seals were offered
by Siemens. Labyrinth seal is made up of a number of evenly spaced thin strips or teeth, the
diametral clearance between each of the seal teeth and the rotating shaft is equivalent to a series
of orifices; leakage rate is proportional to this clearance.
Labyrinth seals have higher leakage rate (clearance of labyrinth seals with rotating shaft increases
when rubbing occurs due to high vibration, known as mushrooming effect. High vibration amplitude
“Ac1” is expected when the compressor passes through first lateral critical speed as shown in rotor
response plot below, at both start-up and coast down) compared to self-acting dry gas seals; the
seal faces of the latter technology are mechanically-controlled by springs which are evenly
distributed around the circumference of stationary rings, i.e. leakages through self-acting dry gas
seal are therefore minimized.
Siemens 3-chamber labyrinth seal design has a vent line that continuously emitting process gas
mixture (Chlorine mixture in this case) outside the process boundary (i.e. from chamber II as
depicted in schematic above), where additional process treatment may be envisaged in order to
neutralise the toxic or hazardous nature of process gas before it can be safely discharged to
atmosphere.
When seal gas supply (nitrogen gas in this application) fails, process gas will likely flow into
atmosphere or bearing compartment (depending on the design of bearing housing) as there is no
positive mechanical mechanism (e.g. spring force in self-acting dry gas seals) to seal up the
diametral clearance between labyrinths and shaft.

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New and clean labyrinth seal Rubbed labyrinth seal (i.e. mushrooming effect)
Rotor response plot (extracted from API 617, 7th
edition)

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2.3 Siemens’ compressor casing
Compressor casing offered by Siemens is horizontal split type.
Duration required for main overhaul is relatively longer (compared to barrel casing) as rotor,
bearings, seals, static diaphragm, return channels need to be dealt with and dismantled as
individual parts (i.e. not modularised).
Ensuring proper sealing between top and bottom halves of horizontal split casing is a challenging
task; as the entire area of mating planes needs to be properly cleaned and matched prior to re-
assembly. Pictures below are provided by Siemens (newly supplied chlorine compressor for other
project), where compressor casings were dismantled due to unsuccessful performance tests at
Siemens’ workshop. It can be seen that the sealing cords fitted by Siemens’ specialists were
installed in false position and out of groove.

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2.4 Siemens’ compressor performance
Flow coefficient at each compressor stage inlet is calculated based on impeller diameter, rotational
speed and actual inlet volume flow rate provided in Siemens compressor data sheet.
Flow coefficients (for certified point) derived from Siemens compressor selection (first stage
0.0435, second stage 0.0323 & third stage 0.0223) are scattered towards the left end of efficiency
curve with falling efficiencies.
Siemens compressor selection can be improved with smaller impellers diameter (at the expense of
additional impeller to compensate polytropic head loss due to reduced impeller diameter), to
increase flow coefficients (flow coefficient is inversely proportional to the product of impeller tip
speed and squared of impeller diameter).
Note that compressor rotor-dynamics (e.g. lateral critical speeds) likely be impacted if aero-
dynamics (efficiencies) were to be optimized, i.e. slimmer shaft diameter (reduced impeller
diameter) and wider bearing span (additional impeller).
Siemens compressor design is therefore non-optimum in term of compressor aero-dynamics, i.e.
poor efficiency.
0.65
0.67
0.69
0.71
0.73
0.75
0.77
0.79
0.81
0.83
0.85
0 0.02 0.04 0.06 0.08 0.1 0.12 0.14 0.16
Polytropic efficiency vs. flow coefficient
Ludtke generic curve
Siemens stage 1 per Ludtke generic curve
Siemens stage 1 per Siemens curve
Falling efficiency

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2.5 Siemens’ thermodynamic model
It is unclear which equation of state is used by Siemens as the basis for thermodynamic model,
despite several clarifications (both formally and verbally).
Minimum dew point margin required by Siemens is 20 deg. C; note the available dew point
margins according to Siemens’ design are more than twice of the required value (for certified
case).
0
2
4
6
8
10
12
14
16
18
20
-50 -40 -30 -20 -10 0 10 20 30 40
Pressure(barA)
Vapor saturation curve_Redlich Kwong Soave
Siemens stage 1 inlet
41.32 deg. C
51.2 deg. C
40.94 deg. C

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Appendix 1: Technical bid tabulation

Technip Tianchen Chemical Engineering (Tianjin) Co., Ltd.
Client: Shanghai Lianheng Isocyanate Co., Ltd.
Site: Shanghai Chemical Industrial Park, Shanghai, China
MDT Acceptability Siemens Acceptability
Minutes of meeting & technical clarifications
Minutes of meeting & technical clarifications Refer to Appendix 5 Noted. Refer to Appendix 6 Noted.
Scope of supply
API 617 single shaft centrifugal compressor preferable with barrel type outer casing. Comply. Accepted API 617 single shaft with horizontal‐split casing. Accepted
Suction throttling valve with anti surge valve both valves will be controlled by compressor Cooled bypass valve for machine anti surge protection and capacity control only Valve will
SLIC HCL Recycle Project Material Requisition No: 1975Z‐1‐MR‐1011‐0001
TECHNICAL BID TABULATION: 1975Z‐1‐TBT‐1011‐0001
Means of compressor control (supplier to propose). Variable inlet guide vanes not to be used.
Suction throttling valve with anti‐surge valve, both valves will be controlled by compressor
PLC. Note that:‐
a) suction throttling valve will be used to regulate suction pressure.
b) anti‐surge valve serves surge protection and capacity control (for bypass operation).
Accepted
Cooled bypass valve for machine anti‐surge protection and capacity control only. Valve will
be controlled by compressor PLC.
Independent process‐bypass valve needs to be provided by Purchaser in order to regulate
suction pressure.
Accepted
Skid mounted lube oil console with:‐
a) Stainless steel 304L reservoir as minimum
b) 2 x 100% AC motor driven screw‐type oil pumps
c) 2 x 100% shell and tube TEMA class C lube oil coolers
d) 2 x 100% lube oil strainers
e) 2 x 100% lube oil filters
f) Temperature control valve (3 port valve with internal thermostat)
g) Lube oil pump discharge lines pressure relief valves
h) Electric lube oil heater
Provided. Accepted
Skid mounted lube oil console with:‐
a) Stainless steel 304L reservoir as minimum
b) 1 x AC motor driven screw‐type oil pump, and 1 x gearbox driven screw‐type pump.
c) 2 x 100% shell and tube TEMA class C lube oil coolers
d) 2 x 100% lube oil strainers
e) 2 x 100% lube oil filters
f) Temperature control valve (3 port valve with internal thermostat)
g) Lube oil pump discharge lines pressure relief valves
h) Electric lube oil heater
Accepted
Oil mist eliminator unit consists of:‐
a) Oil reservoir of 304L stainless steel as minimum
b) 1 x 100% AC motor driven blower
) Fl t
Provided. Accepted
Oil mist eliminator unit consists of:‐
a) Oil reservoir of 304L stainless steel as minimum
b) no motor driven blower required
) Fl t t li bl
Accepted
c) Flame arrestor c) Flame arrestor not applicable.
Non‐pressurized lube oil rundown tank of 304L stainless steel, as minimum. Provided. Accepted Not applicable. Accepted
Inter‐stage process coolers.
Total of two compression stages, one inter‐stage cooling required. Inter‐stage cooling
consists one cooling water cooler and one chilled water cooler configured in series.
Accepted
Total of three compression stages, two inter‐stage cooling required. Each inter‐stage
cooling consists one cooling water cooler.
Accepted
Process suction and inter‐stage knock‐out pots. Comply. One suction knock‐out pot and one inter‐stage knock‐out pot will be provided. Accepted
Not comply.
Only one suction knock‐out pot will be provided, i.e. inter‐stage knock‐out pots will not be
provided.
Not accepted
Dry gas seal panel (to be mounted on compressor skid) to cater for self‐acting dry gas seal
cartridges. Shaft seals shall consist of double opposed dry gas seals with segmented carbon ring
separation seals.
Dry gas seal panel provided on compressor skid. Compressor shaft seals are double
opposed self‐acting dry gas seal, with segmented carbon rings as separation seals.
Accepted 3‐chamber labyrinth seals will be provided. Not accepted
Compressor suction strainer (pipe spool and strainer internal element) for each compression
stage, to be used during commissioning.
Each compression stage will be fitted with a suction strainer. Accepted Only suction strainer before first stage offered. Not accepted
One anti‐surge valve per compression stage. One anti‐surge valve sufficient for both stages. Accepted One anti‐surge valve after the last stage offered. Accepted
Process check valve. One inter‐stage check valve will be provided. Accepted One discharge check valve will be provided. Accepted
Inter‐connecting piping for lube oil system.
Provoded.
Note that inter‐connecting piping from oil reservoir to rundown tank will be excluded from
Supplier's scope, as the elevated location of rundown tank will be determined by
Accepted Provided. Accepted
Purchaser in view of available space in the plant.
Inter‐connecting piping for process piping.
Note: anti‐surge piping be excluded from Supplier's scope.
Provided. Accepted Provided. Accepted
All gaskets, bolts and nuts within the equipment package. Provided. Accepted Provided. Accepted
Equipment allowable nozzle loads:‐
a) Centrifugal compressor process connections nozzle loads shall be minimum 2 times API 617,
i.e. 3.7 times NEMA 23.
b) Alllowable nozzle loads for all auxiliary connections on compressor (e.g. balancing line, lube
oil connections on bearing housing, seal gas and buffer gas connections on dry gas seal module,
etc), auxiliary equipment (e.g. seal gas filter, nitrogen filter, lube oil connections on oil console /
rundown tank / oil mist eliminator / lube oil headers) and process equipment (e.g. inter‐stage
coolers, suction scrubber, inter‐stage scrubber, etc) shall be in accordance with Appendix 3 of
GEN4‐0‐VESS‐SP‐0001.
c) Allowable nozzle loads for shell and tube heat exchangers shall be in accordance with
Attachment 1 of GEN4‐0‐HEEX‐SP‐0001.
Comply. Accepted
a) 2 x API 617 nozzle loads & moments
b) manufacturer standard
c) manufacturer standard
a) Accepted
b) TBC post PO
c) TBC post PO
Equipment base plate Provided. Accepted Provided. Accepted
Lifting lugs on equipment / on‐skid. Provided. Accepted Provided. Accepted
This document is the property of TECHNIP and contains confidential information
Document class: B ‐ Confidential (Not to be disclosed without authorization) Page 1 of 7 Appendix 1: Technical bid tabulation

Access stairs / ladders / platforms / walkways / handrails Where necessary at skid. Accepted Not necessary. Accepted
Flow element, pressure and temperature instruments required for the anti‐surge system.
Provided. However these anti‐surge instruments will be loose‐supplied and be installed on
Purchaser‐supplied recycle loop.
Accepted
Provided. However these anti‐surge instruments will be loose‐supplied and be installed on
Purchaser‐supplied recycle loop.
Accepted
All local instrumentation required for operation. Provided. Accepted Provided. Accepted
On‐skid inter‐connecting instrument wiring. Provided. Accepted Provided. Accepted
On‐skid instrument junction boxes. Provided. Accepted Provided. Accepted
On‐skid instrument pneumatic tubing. Provided. Accepted Provided. Accepted
On‐skid instrument wiring and tubing supports. Provided. Accepted Provided. AcceptedOn skid instrument wiring and tubing supports. Provided. Accepted Provided. Accepted
Calibration certificates for all instrumentation in Supplier's scope shall be supplied. Provided. Accepted Provided. Accepted
Console gauge board (un‐enclosed bracket or plate to support and display gauges, switches and
other instruments).
Provided. Accepted Gauge board will not be provided. Not preferred
Self‐standing local panel with button, lamps and horn for start, stop, ESD, lamp test,
local/remote selector, start permission and alarm.
Self‐standing remote control panel (PLC‐based), located in rack room. HMI to be integrated as
part of remote control panel. Serial link communication required from compressor PLC to Owner
DCS.
High voltage induction motor as compressor main drive. Provided. Accepted Provided. Accepted
Two LV inducation motors for lube oil pumps. Provided. Accepted One LV induction motor for standby oil pump. Accepted
One LV induction motor for oil mist eliminator blower. Provided. Accepted Not applicable. Noted.
Earthing / continuity:‐
a) Electrical continuity between equipment / pipe work / skid earthing termination points.
b) Minimum one earthing connection per equipment item.
c) Minimum two earthing termination connections shall be provided, fitted at apposite corners
or sides of the package skid.
Provided. Accepted
Main equipment (main motor, gearbox, compressor, lube oil reservoir) will have dedicated
earthing. Equipment on piping (valve, PSV, instrument) will be metal‐to‐metal connections
to ensure earthing continuity, earthing will be provided on piping.
Accepted
All on‐skid electrical cabling and wiring Provided Accepted Provided AcceptedAll on‐skid electrical cabling and wiring. Provided. Accepted Provided. Accepted
All on‐skid cable supports and clamping facilities. Provided. Accepted Provided. Accepted
All on‐skid interface junction boxes supplied on the edge of skid in a safe and convenient
location.
All cable glands for cable on‐skid up to the interface junction boxes. Provided. Accepted Provided. Accepted
All on‐skid local lighting required for instrumentation, controls, panel, etc. Provided. Accepted Only lighting fixture inside unit control panel considered. Accepted
Main equipment (compressor, gearbox, electrical motors, knock‐out pots, coolers, anti‐surge
valves, flow elements, etc) nameplates in English.
Tags / labels for instrument wiring and tubing in English. Provided. Accepted Provided. Accepted
Tags / labels for instrument junction boxes in English. Provided. Accepted Provided. Accepted
Tags / labels for piping, valves and fittings in English. Provided. Accepted Provided. Accepted
Full painting and coating system as per project specification.
Supplier painting specification subject to Purchaser approval at detailed engineering. Final
coating will be provided in accordance with project requirement.
Accepted
Supplier painting specification subject to Purchaser approval at detailed engineering. Final
coating will be provided in accordance with project requirement.
Accepted

Optional quotations
Optional price for the supply of suction shutdown valve and discharge shutdown valve. Quoted as optional items. TBC post PO Quoted as optional items. TBC post PO
Operator station to be located at central control room. Fiber optic cable of 500 meters to be
included in the optional price.
Option to be considered. CBT to be updated accordingly. Accepted. Option to be considered. CBT to be updated accordingly. Accepted.
Optional price for PLC to be SIL3‐rated. SIL3 certificates shall be provided for PLC, and SIL loop
calculation to be included in the optional price.
Option to be considered. CBT to be updated accordingly. Accepted. Option to be considered. CBT to be updated accordingly. Accepted.
Some instruments within the chlorine compressor package may subject to SIL requirement and
SIL tifi t b d SIF l l ti i d t il d i i O ti l i t b id d A ti ft l ifi ti f l t d l TBC t PO O ti l i ill b id d b d th lt f SIL t d TBC t POSIL certificate based on SIF calculation in detailed engineering. Optinal price to be provided
accordingly.
As option after clarification of related loops. TBC post PO Optional price will be provided based on the result of SIL study. TBC post PO
Optional price for all noise attenuation equipment in order to meet 82 dBA at 1 meter from main
skid edge.
To be confirmed based on optional price on noise attenuation system. TBC prior to PO To be confirmed based on optional price on noise attenuation system. TBC prior to PO
Optional price for compressor package that is suitable for start‐up with oxygen concentration
from 35 mol% to 40 mol%.
Optional price to be provided by MDT. TBC prior to PO Not applicable for Siemens. NA
Optional price for compressor package that is suitable for start‐up with oxygen concentration
above 40 mol%.
Optional price to be provided by MDT. TBC prior to PO Not applicable for Siemens. NA
Exclusions
Limit of supply and terminal points as follows.
1. Main and auxiliary unit / skid interfaces:‐
(a) Skid / supports / structural: top of concrete (or structural)
(b) Connections at battery limits: with flanges, according to Purchaser's piping class.
(c) Vents: vents piped, valved, flanged to a single connection per type of fluid at battery limit of
each base plate / sub‐system. An additional blind is required if the vent is not connected.
(d) Drains: drains piped, valved, flanged to a single connection per type of fluid at battery limit of
each base plate / sub‐system. An additional blind is required if the drain is not connected.
1. (a) Okay, (b) Okay, (c) Okay, (d) drain for process coolers will not be manifolded.
Instrument air for bypass / ASV will not be manifolded with separation gas supply. (e) Single p / y q
(e) Utility distribution: manifolded to a single flanged connection at battery limit of each base
plate / sub‐system for supply and return, and including block valves. Gas supply manifold shall
include any required pressure regulator, lubricator or filter.
2. Instrumentation and electrical equipment:‐
(a) Instrumentation: instrument junction box including cable gland.
(b) Main and auxiliary drive electrical motor power supply: motor terminal box including cable
gland (if applicable)
(c) Panels / cubicles: wired terminal strips with cable glands for all signals and power supply.
(d) Earthng: 2 skid earthing connections or motor terminals.
Comply. Accepted.
yp / p g pp y ( ) g
line manifolded is applied to: cooling water supply for oil cooler, cooling water supply for
process cooler.
2) (a) to (d): Okay.
Accepted.
Foundations and foundation bolts. Not in scope. Accepted. Not in scope. Accepted.
Gaskets and bolting for battery limit terminal points. Not in scope. Accepted. Not in scope. Accepted.
Piping beyong battery limit terminal points. Not in scope. Accepted. Not in scope. Accepted.
Instrument wiring / cabling outside the package battery limit. Not in scope. Accepted. Not in scope. Accepted.
General area lighting for access and safety around the equipment package. Not in scope. Accepted. Not in scope. Accepted.
Site installation / erection.
Not in scope. However site supervision for installation and erection to be quoted
separately.
Accepted.
Not in scope. However site supervision for installation and erection to be quoted
separately.
Accepted.
First fill of commonly used lube oil Not in scope Accepted Not in scope AcceptedFirst fill of commonly used lube oil. Not in scope. Accepted. Not in scope. Accepted.
Motor local start / stop stations. Not in scope. Accepted. Not in scope. Accepted.
Thermal insulations.
Not in scope. Lines / equipment require thermal insulation will be indicated in supplier's
drawing.
Accepted.
Not in scope. Lines / equipment require thermal insulation will be indicated in supplier's
drawing.
Accepted.

Factory inspection and testing
Inspection and testing per project data sheets, material requisition, referenced specifications,
codes and standards.
Supplier's exceptions / comments to 1975Z‐1‐ITP‐1011‐0001‐B1 were received on 26th
June 2015. Reviewed and under separate discussion.
Accepted.
Supplier will review 1975Z‐1‐ITP‐1011‐0001‐B1 and incorporate in supplier ITP, any
comments or deviations shall be informed to Purchaser.
Pending
Puchaser's inpsection ‐ free access to Supplier's works and their sub‐supplier's works for
Purchaser's representatives.
Comply. Accepted. Comply. Accepted.
Third party inspection (as required to satisfy relevant Chinese National Design Codes and
C l A d C l A d
p y p ( q y g
Regulations).
Site acceptance test for chlorine compressor package. Comply. Accepted. Comply. Accepted.
Protection / packing / preparation for shipment
Corrosion protection and surface finish. All equipment and materials shall be supplied suitably
protected from corrosion during transit, storage, after installation and during operation.
Preservation and protection ‐ Supplier shall advise any requirements for preservation of plant
and materials should they require long term storage after delivery. Supplier shall provide all
preservation and protection required for shipment and storage on site prior to installation.
Packing and shipping ‐ Supplier shall ensure that all deliverables are designed and packed for
transit to site.
Scope of services
Project coordinator: After purchase order placement Supplier shall assign a project engineerProject coordinator: After purchase order placement, Supplier shall assign a project engineer
responsible for the following activities:‐
a) Act as a single point of contact for all communication between Supplier and Purchaser.
b) Monitor and expedite all Supplier and sub‐supplier activities to ensure compliance with the
agreed schedule and the requirements stated in this material requisition and referenced
documents.
c) Monitor and expedite responses to Purchaser's communications with Supplier.
d) Attend an order kick‐off meeting at Supplier's / Purchaser's office.
e) Attend technical and progress meetings at Purchaser's office, these may include HAZOP,
layout, constructability, operability, maintenance and safety reviews.
Field services: Supplier shal quote for provision of suitably qualified and experienced personnel
for the supervision of field services. Rates, manpower requirements and durations shall be
quoted for the following services:‐
a) installation
b) commissioning
Supplier shall recommend the scope of field services they consider necessary, specifically
detailing any mandatory field services required for warranty.

Training: Supplier shall provide a separate quote for providing suitably experienced and qualified
personnel to train the Owner's personnel in:‐
a) maintenance
b) operation
of the equipment offered. Training shall be carried out at Supplier's shop and a site and shall
include the provision of suppor documentation. The training and support documentation shall
be in English.
i i l i f h i l (b d i i i i d i h ill bDynamic simulation for the compression loop (based on piping isomteric drawings that will be
provided by Purchaser at detailed engineering), to study the following items as minimum:‐
a) To ensure the sizing of anti‐surge valve (i.e. Cv values and stroke time) is adequate.
b) To check the requirement of hot gas bypass valve. If hot gas bypass valve is needed as
suggested by dynamic simulation, Supplier shall furnish hot gas bypass valve data sheet and it
will then be procured by the Purchaser. Necessary controls of hot gas bypass valve shall be
integrated within Supplier's PLC.
c) To confirm settling out pressure of compression loop.
If hot gas bypass valve is required, the dynamic simulation shall be re‐performed with revised
piping isomterics (reflecting the change / additional piping due to hot gas bypass loop). Revised
piping isomterics will be provided by Purchaser once hot gas bypass valve data sheet is provided
by Supplier.
Lifting beams and special tools
Lifting beams: Supplier shall include for and price separately, any special lifting beams or lifting
equipment required to lift the equipment during transportation to site or during installation.
Comply. Accepted. Not applicable. Noted.
Special tools: Supplier shall include for and price separately, any special tools required for
installation, field testing, operation or maintenance of the equipment.
Comply. Accepted. Price included in total price. Noted.
Spare parts
Capital / insurance spares as optional price. Comply. Accepted. Comply. Accepted.
Construction spares as optional price, i.e. 5% minimum spare fasteners for site‐made joints,
gaskets for all joints opened during testing including pressure testing.
Comply. Accepted. Not applicable. Noted.
Commissioning and start‐up spares as optional price. Comply. Accepted. Comply. Accepted.
Two years operational spares. Comply. Accepted. Comply. Accepted.
Consumables
First fill: Supplier shall only indicate equivalent grade, quantity and schedule for commonly used
lube oil in the lubricant list provided in this material requisition. The first fill of such lubricants
will be provided by Purchaser. Supplier shall confirm details of any supply of first fill of all
lubricants, chemical, etc, of not commonly available in the industry.
Operational consumables: Supplier shall provide Purchaser with a list stating the specification,
quantities, and replacement frequency of all operational consumables required for the
equipment.
Documentation
Supplier data / documentation as per Part II and III of 1975Z‐1‐SR‐1011‐0001‐B3. Per agreed document list, refer to Attachment 2 of MOM‐1975Z‐C349‐011. Accepted. Per agreed document list, refer to Attachment 3 of MOM‐1975Z‐C349‐010. Accepted.

Compressor design / selection
Casing construction Barrel type Accepted. Horizontal split Not preferred.
Main nozzles facing Upward facing (main skid on solid foundation) Accepted. Down nozzles (main skid on elevated concrete table top) Accepted.
Main nozzles rating / standard 300 # per ASME B16.5 (in compliance with project piping class) Accepted.
150# (for low pressure nozzles), all nozzles will be supplied per DIN standard (not complied
with project piping class) due to casting limitation.
Not accepted.
Main nozzles size (inches) Stage 1 inlet = 14"; Stage 1 discharge = 10"; Stage 2 inlet = 10"; Stage 2 discharge = 8" Accepted. Not available. Pending
C h ft l D bl d d l ith t d b i A t d 3 h b l b i th l ( j d i ti t j t i t) N t t dCompressor shaft seals Double opposed dry gas seals with segmented carbon rings. Accepted. 3‐chamber labyrinth seals (major deviation to project requirement). Not accepted.
Number of inter‐stage coolings One inter‐stage cooling (with two coolers in series) Accepted. Two inter‐stage coolings (one cooler each) Accepted.
Inter‐stage cooling water consumption (kg/hr)
21000 kg/hr based on supply water temperature 33 deg. C and return water temperature
43 deg. C.
Accepted.
30367 kg/hr for inter‐stage cooler # 1 (suppply temperature 33 deg. C, return temperature
39 deg. C).
37525 kg/hr for inter‐stage cooler # 2 (supply temperature 33 deg. C, return temperature 40
deg. C).
Accepted.
Inter‐stage chilled water consumption (kg/hr)
49000 kg/hr based on supply water temperature 5 deg. C and return water temperature 10
deg. C.
Accepted. Not applicable Noted.
Impellers arrangement Back‐to‐back Accepted. Back‐to‐back Accepted.
Number of impellers & associated diameter (mm) Four impellers (290 mm, 290 mm, 285 mm & 275 mm) Accepted. Three impellers (406 mm, 380 mm & 370 mm) Accepted.
Number of process stages Two Accepted. Three Accepted.
Inlet flow coefficient of certified case "Normal" Stage 1 = 0.1027; Stage 2 = 0.0503 Accepted. Stage 1 = 0.0435; Stage 2 = 0.0323; Stage 3 = 0.0223 Not preferred.
Polytropic efficiency of certified case "Normal" (%) Stage 1 = 83.6%; Stage 2 = 82.5% Accepted. Stage 1 = 81.2%; Stage 2 = 80.1%; Stage 3 = 76.2% Not preferred.
Compression power required at motor output shaft (inclusive both mechanical losses of
compressor and gearbox) for certified case "Normal"
849 kW Accepted. 990 kW Not preferred.
Compressor operating speed (rpm) 13103 rpm Accepted. 11264 rpm Accepted.
Impeller tip speed (m/s)
Impeller # 1 = 199.0 m/s, Impeller # 2 = 199.0 m/s; Impeller # 3 = 195.5 m/s; Impeller # 4 =
188.7 m/s
Accepted. Impeller # 1 = 239.5 m/s, Impeller # 2 = 224.1 m/s, Impeller # 3 = 218.2 m/s Accepted.
Polytropic head for certified case "Normal" (kJ/kg) Stage 1 = 39.3 kJ/kg; Stage 2 = 36.5 kJ/kg Accepted. Stage 1 = 30 kJ/kg; Stage 2 = 24.1 kJ/kg; Stage 3 = 22 kJ/kg Accepted.
Process gas discharge temperature for certified case "Normal" (deg. C) Stage 1 = 90 deg. C; Stage 2 = 82 deg. C Accepted. Stage 1 = 73.5 deg. C; Stage 2 = 88.1 deg. C; Stage 3 = 86.7 deg. C Accepted.
Process gas dew point margin at compressor inlet flanges for certified case "Normal".
Stage 1 = 41.35 deg. C; Stage 2 = 17.38 deg. C. Refer to Appendix 2 for details.
Note: Minimum dew point margin required by MDT is 10 deg. C
Accepted.
Stage 1 = 40.94 deg. C; Stage 2 = 51.2 deg. C; Stage 3 = 41.32 deg. C. Refer to Appendix 2 for
details.
Note: Minimum dew point margin required by Siemens is 20 deg. C
Accepted.
Seal gas leakage rate (kg/hr)
Inner leakage (to process chamber): Guaranteed total 2.4 kg/hr of nitrogen gas, expected
1.2 kg/hr of nitrogen gas.
Primary vent (to atmosphere): Guaranteed total 76.4 kg/hr of nitrogen gas, expected 38.2
kg/hr of nitrogen gas.
Vent to bearing compartment: Guranteed total 72.2 kg/hr of nitrogen gas, expected 36.1
kg/hr of nitrogen.
Accepted. Not available. Pending
Compressor design that can cope with high oxygen concentration during start‐up
a) From 0 mol% to 23.5 mol% of oxygen concentration: no special compressor materials
required, and no cleaning requirement.
b) From 23.5 mol% to 35 mol% of oxygen concentration: measures implemented for
chlorine service (material of construction) with cleaning of the rotor (already considered
for project specific chlorine mixture) TBC prior to PO
Siemens response email 22nd June 2015:
Based on your description of start‐up point 2 and 4 are not acceptable for the offered PendingCompressor design that can cope with high oxygen concentration during start up. for project specific chlorine mixture).
c) From 35 mol% to 40 mol% of oxygen concentration: small design changes required, with
cleaning of rotor.
d) Above 40 mol% of oxygen concentration: all material and design changes per EIGA
guideline need to be implemented, plus clean room conditions for compressor assembly.
TBC prior to PO Based on your description of start up, point 2 and 4 are not acceptable for the offered
compressor. We have to discuss these two points in details.
Pending
Experience list 8 chlorine gas compression duties with similar discharge pressure and power. Accepted. 7 chlorine gas compression duties with similar discharge pressure and power. Accepted.

Compressor off‐design sensitivity check / study
Note that inter‐stage cooling consists of cooling water cooler and chilled water cooler
configured in series.
Cooling water cooler data sheet dated 11‐May‐2015 was sized based on 55 deg. C
discharge gas temperature, and it gets further cooled down to 10 deg. C across chilled
water cooler.
Investigate the effect on compressor final stage discharge temperature if there is a failure on
chilled water supply to inter‐stage chilled water cooler.
A study was therefore conducted to check the effect on final stage discharge temperature
when suction gas temperature entering final stage compression is 55 deg. C (i.e. failure of
chilled water supply). It reveals that suction temperature entering final stage compression
shall be reduced to 50 deg. C, in order to control final stage discharge temperature within
120 deg. C. Refer to Appendix 3 for details.
Both cooling and chilled water cooler data sheets were revised (3‐June‐2015) to re‐
distribute heat duty of each cooler, i.e. cooling water cooler discharge gas temperature is
revised to 50 deg. C, inlet gas temperature to chilled water cooler is revised to 50 deg. C.
Accepted. Not applicable. Noted.
Effect on discharge temperatures when suction temperature increases to 23.5 deg. C (from 15
deg. C and 5 deg. C).
Both compression stages discharge temperature will be below 110 deg. C for all
compression duties identified in compressor data sheet. Refer to Appendix 4 for details.
Accepted.
All three compression stages discharge temperature will be below 110 deg. C for all
compression duties identified in compressor data sheet. Refer to Appendix 4 for details.
Accepted.
Technical acceptability
Technically not acceptable, major deviations / concerns are:‐
Technical acceptability Technically acceptable. Accepted.
a) Compressor shaft seals. Double opposed dry gas seal with segmented carbon rings are
required, but 3‐chamber labyrinth seals are offered. When nitrogen supply (seal gas) fails,
springs fitted around the perimeter of seal rings (of dry gas seal) will positively seal up the
sealing gap; therefore minimise the potential leakage of process gas to lube oil system.
Positive sealing mechanism is not available with labyrinth seals.
b) Compressor main nozzle rating. 300# ASME B16.5 flanges are needed according to
project requirement (chlorine containment philosophy), however 150# flanges on low
pressure nozzles are offered. And all nozzles are provided in accordance with DIN standard,
not ASME B16.5.
c) Low efficiency. Siemens' compressor requires an extra of 141 kW (compared with MDT)
for the certified case (i.e. case Normal). This would result in higher OPEX in view of
electricity consumption. Which also lead to higher fossil fuel rate usage (less environmental
friendly).
d) Inter‐stage scrubber. Inter‐stage scrubbers not provided by Siemens. This is a major
Not accepted.
deviation to LOPA / HAZOP conducted in previous stage.
e) Horizontal split casing. Compressor internal change‐out is much more challenging (and
most likely requires longer plant down time) as the idea of internal bundle (rotor, static
diaphragm, bearings, seals) cannot be implemented for horizontal split casing.

PLANT N°
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21
Appendix 2: Dew point margin upstream of compressor inlet flanges

Appendix 2
10
12
14
16
18
20
Pressure (barA)
Vapor saturation curve per Redlich Kwong Soave EoS
MDT Stage 1
MDT Stage 2
Siemens Stage 1
Siemens Stage 2
Siemens Stage 3
Vapor & liquid mixture Full vapor region
0
2
4
6
8
10
‐50 ‐40 ‐30 ‐20 ‐10 0 10 20 30 40 50
Pres
Vapor & liquid mixture Full vapor region

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1975Z 1 TBT 1011 0001 B1 18 /
21
Appendix 3: Evaluation of compressor final stage discharge temperature when
inter-stage chilled water supply fails

Page | 1 Appendix 3
By: CangTo CHEAH (29th
June 2015), Senior Rotating Equipment Engineer (Technip)
Project: SLIC HCL recycle project
Equipment / type: Chlorine gas compressor / centrifugal
Document title: Evaluation of compressor discharge temperatures when chilled water supply fails at inter-stage
cooler, based on MDT’s proposal.
Introduction
The chlorine compressor proposed by MDT consists of two process stages; and inter-stage coolers will be supplied
by MDT. The inter-stage cooling itself consists of two shell-and-tube coolers configured in series, note that coolant
for 1st
cooler is cooling water (supply & return temperatures are 33 deg. C and 43 deg. C, respectively) and coolant
for 2nd
cooler is chilled water (supply & return temperatures are 5 deg. C and 10 deg. C, respectively). 1st
cooler
discharge temperature for process gas is 55 deg. C per MDT’s preliminary proposal. The LOPA (layer of protection
analysis) performed in the earlier stage of SLIC HCL recycle project places an action item for EPC contractor to look
at mitigation measures to limit compressor discharge temperature below 120 deg. C, during failure of chilled water
supply. There are various ways to reduce discharge temperature for centrifugal compressor, namely:
a) Improved efficiency b) Reduced head c) Reduced inlet temperature
Noting that item a) can be realized in two ways. Efficiency can either be improved by varying suction volume flow
rate along the x-axis of performance curve “efficiency vs. inlet volume flow rate”, or in case if inlet volume flow
rates cannot be varied (due to process restrictions), then re-selection of impeller family may be considered. This
study is based on the former (with combinations of b and c), as maintaining inlet volume flow rate at abnormal
process conditions (e.g. failure of chilled water supply) is not a mandatory requirement.
Basis of compressor performance calculation
1) Thermodynamic model
Lee-Kesler-Plocker corresponding state is used, with binary interaction coefficients extracted from HYSYS.
Polytropic temperature and polytropic volume exponents are used to calculate discharge temperature and
discharge pressure, respectively.
2) Aerodynamic model
MDT’s performance curves (polytropic head vs. actual inlet volume flow rate and polytropic efficiency vs. actual
inlet volume flow rate) are modeled with 4th
order polynomial curve-fitting technique (i.e. least square method).
Inputs are: Inlet volume flow rate & inlet pressure for LP stage, suction temperature for both LP and HP stages,
inter-stage pressure loss (assumed 0.15 bar, per MDT’s data sheet), and project specific gas mixture.
Calculated outputs are: Polytropic head, polytropic efficiency, discharge temperature, discharge pressure,
compression power, polytropic exponents, compressibility factor, and mass flow rate.
Conclusion: On page 9

Page | 2 Appendix 3
Normal: 55 deg. C cooling water cooler discharge temperature
Remark: Final stage discharge temperature approx 116 deg. C. Okay

Page | 3 Appendix 3
Maximum: 55 deg. C cooling water cooler discharge temperature

Page | 4 Appendix 3
Case A: 55 deg. C cooling water cooler discharge temperature

Page | 5 Appendix 3
Case B: 55 deg. C cooling water cooler discharge temperature
Remark: Final stage discharge temperature approx 123 deg. C. Not okay.

Page | 6 Appendix 3
Case B: 50 deg. C cooling water cooling discharge temperature

Page | 7 Appendix 3
Case C: 55 deg. C cooling water cooler discharge temperature
Remark: Final stage discharge temperature approx 129 deg. C. Not okay
According to MDT’s response on 2nd
June 2015, anti-surge valve (ASV) would need to be opened if compressor
discharge temperatures approach alarm limit (~105 deg. C) due to low flow. When ASV opens, flow that goes into
compressor suction flanges will increase and hence reduce discharge temperature & discharge pressure (due to
reduced polytropic head).

Page | 8 Appendix 3
Case C: 50 deg. C cooling water cooler discharge temperature
Remark: Final stage discharge temperature approx 119 deg. C. Note that inlet volume flow rate 4191 m^3/hr (per
MDT’s Q_inlet) on LP stage would yield final stage discharge temperature 124.7 deg. C (based on 50 deg. C inter-
stage temperature); Therefore a larger Inlet volume flow rate, i.e. 4550 m^3/hr is used to estimate HP stage T2.
With Q_inlet 4550 m^3/hr, discharge temperatures on both LP and HP stages are reduced (LP stage T2 is reduced
with improved efficiency (from 82.58% to 83.60%) & reduced head; HP stage: even though efficiency is reduced
(from 82.65% to 81.60%), low T2 is however compensated by reduced head, as T2 is directly proportional to
compression ratio). See Appendix A for more details (page 10 to 15).

Page | 9 Appendix 3
Case D: 55 deg. C cooling water cooler discharge temperature
Remark: Final stage discharge temperature approx 115 deg. C
Conclusion: It is proposed to reduce 1st
cooler discharge temperature (from 55 deg. C down to 50 deg. C), so that
HP stage discharge temperature can be controlled below 120 deg. C during a chilled water supply failure, and
chlorine compressor train can be coast-down in a safe manner.

Page | 10 Appendix 3
Appendix A (page 10 to 15)
Case C with Q_inlet 4191 m^3/hr and inter-stage temperature 50 deg. C
Performance curves: Refer to page 11 and 12 for LP and HP stages, respectively.

LP stage performance curves

HP stage performance curves

Case C with Q_inlet 4550 m^3/hr and inter-stage temperature 50 deg. C
Performance curves: Refer to page 14 and 15 for LP and HP stages, respectively.

LP stage performance curves

HP stage performance curves

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N° REV. PAGE
1975Z 1 TBT 1011 0001 B1 19 /
21
Appendix 4: Evaluation of compression stage discharge temperature when first
stage inlet temperature increases to 23.5 deg. C

Page | 1 Appendix 4
By: CangTo CHEAH (16th
June 2015), Senior Rotating Equipment Engineer (Technip)
Project: SLIC HCL recycle project
Equipment / type: Chlorine gas compressor / centrifugal
Purpose: Study the effects of compressor discharge temperatures when suction gas temperature
increases to 23.5 deg. C (from 15 deg. C and 5 deg. C) for all compression cases (except nitrogen
start-up case, note that suction gas temperature for nitrogen gas during start-up had been specified
as 25 deg. C; which is already higher than 23.5 deg. C) identified in compressor data sheet.
Assumptions:-
1. Additional heat energy incurs from increased suction temperature is assumed to remain within
compressed gas stream (i.e. extra heat will not be removed by inter-stage coolers).
2. Lee-Kesler-Plocker (LKP) corresponding state as the basis of thermodynamic model. Polytropic
exponents derived from LKP to be used for calculation of discharge pressure and discharge
temperature of each compression stage.
3. Supplier-supplied performance curves for each process stages will be used to calculate polytropic
head and polytropic efficiency based on suction volume flow rate for each compression cases.
Observations:-
(a) MAN Diesel & Turbo: Highest discharge temperature is predicted at first stage compression for
Case C at 106 deg. C.
(b) Siemens: Highest discharge temperature is predicted at second stage compression for Case D at
106.4 deg. C.
All these temperatures are well within allowable temperature limit 120 deg. C, therefore run-away
reaction with compressor internal will not occur.

Page | 2 Appendix 4
MDT: Case Normal with suction temperature 23.5 deg. C
Remark: Maximum discharge gas temperature is 98.8 deg. C from first stage.

Page | 3 Appendix 4
MDT: Case Maximum with suction temperature 23.5 deg. C

Page | 4 Appendix 4
MDT: Case B with suction temperature 23.5 deg. C

Page | 5 Appendix 4
MDT: Case C with suction temperature 23.5 deg. C
Remark: Maximum discharge gas temperature is 106 deg. C from first stage.

Page | 6 Appendix 4
MDT: Case D with suction temperature 23.5 deg. C

Page | 7 Appendix 4
Siemens: Case Normal with suction temperature 23.5 deg. C
Remark: Maximum discharge gas temperature is 96.4 deg. C from second stage.

Page | 8 Appendix 4
Siemens: Case Maximum with suction temperature 23.5 deg. C

Page | 9 Appendix 4
Siemens: Case B with suction temperature 23.5 deg. C

Siemens: Case C with suction temperature 23.5 deg. C

Siemens: Case D with suction temperature 23.5 deg. C

PLANT N°
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N° REV. PAGE
1975Z 1 TBT 1011 0001 B1 20 /
21
Appendix 5: Minutes of meeting for MAN Diesel & Turbo

MINUTES OF MEETING
Document Class B : Confidential
Technip Tianchen Chemical Engineering Co. Ltd
Activity Discipline Chrono
MOM 1975Z C349 007
Page 1 of 3
Date of meeting or visit 2015/06/10 Report issued on 2015/06/10
Place of meeting or visit Meeting Room 1302 By CangTo CHEAH
Subject SLIC HCL Recycle Project – Technical bid clarification face-to-face meeting
with MAN Diesel & Turbo for Chlorine Compressor Package
Attended by Technip SLIC MAN Diesel & Turbo
CangTo CHEAH (CTC) Neil Collins (NC) Robert Strube (RS)
JingYu PAN (JYP) Frank Qin (FQ) Heaven Zeng (HZ)
Jack Yang (JY)
Jordan Han (JH)
011
Appendix 5

MINUTES OF MEETING
MOM 1975Z C349 007
Page 2 of 3
No. Description Action by Due date
1
Regarding P&ID legend, Supplier to check if it is feasible to implement Project specific legend
(CMDI-8-PROJ-25-0001 to 0006) in detailed engineering.
MDT 19-June-2015
2 API 614 (chapter 2 and 4) will be provided on 24-June-2015. MDT 24-June-2015
3
Lubricant charts need to be provided at detailed engineering in accordance with project template,
GEN4-1-ROTE-IN-1005-B1.
For info NA
4 MDT to check if dry gas seal drawings can be provided at detailed engineering. MDT 24-June-2015
5
All connections in contact with Chlorine gas shall be minimum 300#.
ASME B16.5 (or B16.47 if 26” or larger) will be implemented for all customer connections
(including main process nozzles on compressor).
For info. NA
6
Supplier’s scope of process-related inter-connecting piping:-
a) base scope: to be purchased in Europe
b) optional quote: to be purchaser in China
For info. NA
7 Duplex 2205 to be used for tube side of chilled water cooler. For info. NA
8
Concentration of oxygen within the chlorine mixture may be higher than the contract value during
start-up. MDT to check if this will lead to special requirement on the compressor.
Client to inform oxygen level that may be seen during start-up.
MDT
SLIC
19-June-2015
16-June-2015
9 There will be connection point on Supplier’s Bentley Nevada 3500 to link with Owner’s System 1. For info. NA
10
Process PSV and blow down valve will now be excluded from MDT’s scope. Commercial
quotation to be updated accordingly. PSV for lube oil system shall be in MDT’s scope.
For info. NA
11
NPT connections shall not be used in chlorine gas service, flanges shall be used (including tubing
application for dry gas seal system) for process gas line.
For info. NA
12 Suction and discharge shutdown valves to be quoted as optional items. For info. NA
13 Dry gas seal failure will lead to compressor trip. For info. NA
14
Spare parts for start-up and commissioning (if applicable):-
a) gaskets
b) dry gas seals
c) bearings
d) filters
e) rupture discs
f) instrumentation (such as vibration, special cabling, pressure, temperature sensors, etc)
g) electrical equipment (such as RTDs in HV induction motor)
h) coupling
i) blinds
j) bolting
For info. NA
011
Appendix 5
MDT response email 19th June 2015:
For higher oxygen concentrations than specified for the normal
operating conditions (as in the newly specified start-up cases),
necessary measures are the application of special materials for the
labyrinth strips and stator parts. The compressor also needs to be
assembled in clean room conditions. The measures lead to longer
delivery time and higher cost, which will be informed later.
MDT confirmed.

MINUTES OF MEETING
MOM 1975Z C349 007
Page 3 of 3
No. Description Action by Due date
k) complete unit spare gearbox
MDT to update proposal
15
Capital spares as follow (if applicable):-
a) compressor bundle (with rotor, static diaphragm / return channel, dry gas seals, journal
bearings, thrust bearing and casing covers)
b) scrubber packing
MDT to update proposal
For info. NA
16
Supplier to check if the following items can be supplied from China:-
a) process scrubbers
b) process coolers
c) lube oil console / system
d) process inter-connecting piping
e) auxiliary inter-connecting piping
MDT 24-June-2015
17
Regarding complete unit test, the following equipment shall be included as minimum:-
a) compressor
b) gearbox
c) HV induction motor
e) high and low speed flexible diaphragm couplings
Shop lube oil system can be used in lieu of contract lube oil system.
Mechanical test and functional test of contract lube oil system will be conducted at sub-supplier’s
work.
For info. NA
18
Instrument data sheet. MDT to check if instrument data sheets can be provided in isf format in
detailed engineering.
Template and software will be provided by Technip.
MDT
Technip
24-June-2015
10-June-2015
19
Compressor test procedure consists the following:-
a) mechanical running test (4 hours)
b) Air comparison test (performance test)
c) unit string test (job compressor, job gearbox, job HV induction motor and job high & low speed
couplings).
For info. NA
20
Instrument hard-wired signal between DCS and UCP should be power-free. Control signals
from/to MCC are via UCP.
For info. NA
21
MDT to review project ITP (1975Z-1-ITP-1011-0001-B1), and provide feedback / exception (if
any) to Purchaser.
MDT 24-June-2015
22
Accumulator is not specified by Purchaser, it is to be removed from MDT’s scope if not required
from MDT’s perspective (in view of rundown tank). P&ID to be updated accordingly.
MDT 24-June-2015
23
Current P&ID shows tilting-pad thrust bearings for gearbox. It was agreed (in previous tele-
conference) that tapered-land axial + radial bearing can be used for gearbox.
MDT to update P&ID data sheets accordingly.
MDT 24-June-2015
Attachment 1: SLIC CL2 MDT TC table_10th
June 2015
Attachment 2: SLIC CL2 MDT document schedule_10th
June 2015
End of Meeting Minutes
011
Appendix 5
MDT confirmed with price adder (will be offered as option)

Issue Date: 10th June 2015
Return Date:
Prepared by: CangTo
1.0 Remark All answers shall be 'Yes' for full compliance, if the answer is ‘No’, then give the explanations to be exception taken. noted Technip 4th June 2015: Noted. Closed
2.0
TP/OWNER Technical Requirement /Clarification Bidder reply TP/OWNER Response
Bidder Name
Requisition Name
Requisition Ref No.
Bidder Offer Ref No.
Revision No.
StatusSN
TECHNICAL CLARIFICATION No. 1
Project: SLIC HCL Recycle Project
Bidder Proposal
Page No./Clause
Technical Clarification
Table
General
MAN Diesel & Turbo
Chlorine compressor package
1975Z-1-MR-1011-0001
3614111
May 14, 2015. Rev. 01
Subject
2.1 MR documentation
Bidder to confirm all the inquiry documents listed in 1975Z-1-MR-1011-0001-B3 are received. And if any additional documents is expected
by bidder, please inform.
noted Technip 4th June 2015: Noted. Closed
2.2 Conformity declaration / deviation
Bidder’s quotation shall satisfy all technical specifications and documents attached in the Requisition 1975Z-1-MR-1011-0001-B3 . Any
deviation by bidder not listed in the Technical Deviation/Exception List during bidding shall not be considered as valid reason for any cost
impact after P.O. Only deviations agreed by Purchaser in writing shall be considered valid.
confirmed Technip 4th June 2015: Okay. Closed
3.0
4.0 Documents requirement at bid stage
To further consolidate your bid, please submit the following documents/information specified in enquiry package before 14-May-
2015.
A0001: List of Supplier's documents and drawings after order
Supplier's document list had been submitted for
Purchaser review.
Closed
Deviation and exception list (in Microsoft Word format) in Word format only for final offer.
Deviations / exceptions in Excel format will be
id d
Closed
Not used
p ( ) y
provided.
A0101: Equipment / Process descriptions after order Okay Closed
A0102: Process flow diagrams with heat and material balance P&ID only Okay Closed
A0103: Piping and instrument diagrams (shall be in accordance with project specific legends). Equipment numbering shall be in
accordance with 1975Z-1-PP-104.
P&ID only Refer to MoM 10th June item 1. Closed
A0104: Equipment list after order Okay Closed
A1001: Equipment filled-in data sheets:
a. API 617 data sheet
b. API 613 data sheet
API 617 data sheet provided. Comments will be incoporated after
Clarification meeting. API 613 data sheet will be sent before clarification
meeting.
Preliminary API 613 (from RENK and Voith) received.
Will be reviewed separately.
Closed
A1002: Centrifugal compressor performance curves (both stage-wise and overall performances to be submitted) confirmed but not stage-wise, only for each stage group What I meant is process stage (not impeller stage). Closed
A1005: Performance curves of auxiliaries equipment (e.g. drivers for lube oil pumps and oil mist eliminator blower). will not be provided
Okay. Supplier confirmd that data sheets for LV
induction motors (of lube oil system) will be provided
in detailed engineering.
Closed
A1006: Auxiliaries data sheets:
a. API 614 data sheet (both lube oil and dry gas seal system)
b. API 671 data sheet
c. Inter-stage coolers (enthalpy curves and cooling curves to be included)
d. Suction scrubber
e. Inter-stage scrubber
a. after clarification meeting
b. before clarification meeting
c. lower pressure drop after revised quotation from cooler suppliers
d. will not be provided
e. see d.
API 614 pending (for chapter 2 and 4). See MOM
10th June item 2.
Closed
A1015: Completed lubricant charts after order Okay. See MOM 10th June item 3. Closed
A1101: Cross sectional and assembly drawings (with part list) for compressor gearbox, main driver and auxiliary drivers. cross sectional sketch only
Okay. Cross-sectional drawings of main components,
i.e. compressor, gearbox and HV induction motor will
be provided in detailed engineering.
Closed
Attachment 1: SLIC CL2 MDT TC table_10th June 2015
Appendix 5

TP/OWNER Technical Requirement /Clarification Bidder reply TP/OWNER Response StatusSN
Bidder Proposal
Page No./Clause
Subject
A1106: Mechanical seal drawings (with material list) not applicable Refer to MoM 10th June item 4. Closed
A1310: Phase envelope (pressure vs. temperature) for all process gases as stated in compressor data sheet. for design point only Okay. Closed
A1311: Effluent and emission data summary (expected relieving flow, relieving fluid compositions and conditions, process / maintenance
drain's flow rate and nature of the drained liquids, process / maintenance vent's flow rate and nature of vented gases).
will not be provided
Okay. It is understood that primary (double oppose)
and separation (segmented carbon ring) vents of dry
gas seals are pure nitrogen, no process gas will
commingle with it.
Closed
A2502: Nozzle load data sheets / drawings. Nozzle loads only
Okay. Note that main process nozzle loads &
moments shall be minimum 2 x API. Refer to MOM
10th June item 5.
Closed
A3001: List of instruments (with manufacturer). after order Okay Closed
after order, if avaiblable for
Instrument data sheets / specification for the following items as
A3101: Instrument data sheets / specification for the following items as minimum: control valves, shutdown valves, blow down valves,
restriction orifices, on/off valves, level instruments, pressure instruments, temperature instruments, relieve valves, safety devices, flow
meters, etc.
Instrument data sheets / specification for the following items as
minimum: control valves, shutdown valves, blow down valves,
restriction orifices, on/off valves, level instruments, pressure
instruments, temperature instruments, relieve valves, safety devices,
flow meters
Okay Closed
A3501: Control system description, operating principles, functional design specification.
see block diagram, more information after order on Control system
description, operating principles only
Okay Closed
A4102: Electric motor data sheets (main driver and auxiliary drivers) for main driver only
Agreed that HV induction motor data sheet will be
provided along with technical bid. LV induction motor
data sheets will be provided in detailed engieering.
Closed
A5006: List of consumables for erection, commissioning and start-up. will not be provided Okay Closed
A5007: Filled-in spare parts and inter-changeability requirements (SPIR) form for capital / insurance spares, construction spares and
commissionng & start-up spares.
after order, spare parts shown in scope of supply sheets of quotation Okay Closed
A5016: Operation and maintenane manuals after delivery Okay Closed
A5021: Two years operational spare in SPIR form after delivery Okay Closed
5.0
6.0 Guarantee
6.1 Equipment Life
The equipment (including auxiliaries) shall be designed and constructed for a minimum service life of 25 years and at least 5 years of
uninterrupted operation. Maintenance activities envisaged during the period of 5 years uninterrupted operation shall not require the
shutdown of compressor package (e.g. instrument testing).
confirmed only if operated according to MDT recommendations Noted Closed
6.2 Mechanical Guarantee
For constant speed compressor, the capacity shall be as specified in 2-4.3.3.1.2 of API 617. The head shall be within the range of 100% -
105% of the normal head. The horse power, based on measured head at normal capacity, shall not exceed 104% of the value at the
specified normal operating condition inclusive of all tolerances.
API 617 applies Okay Closed
Not used
6.3 Process guarantee
Guarantee shall include, but not limited to the following:-
a) The installed scrubbers, compressor and inter-stage coolers shall be capable to handle the flow rate and operating condition as
specified in the data sheet. Performance guarantee shall be provided for 100% normal flow rate and corresponding operating conditions.
API 617 applies
It is agreed that scrubbers, compressor and inter-
stage coolers are capable to handle the flow rate and
operating condition as specified in the data sheet,
and performance gurantee will be provided for 100%
normal flow rate and corresponding conditions
(pressure, temperature).
Closed
Appendix 5

Bidder Proposal
Page No./Clause
Subject
6.4 Utility & power consumption Guarantee utility consumption (power, cooling water flow rate, chilled water flow rate, nitrogen, etc.) at 100% of normal flow rate.
Estimate already provided with quotation, deviations depend on revised
quotation from cooler suppliers.
Guarantees only for power, N2 consumption at guarantee point
It is agreed that utility consumptions for chlorine
compressor package will be guranteed at post PO
phase; it includes nitrogen gas (dry gas seals),
cooling water (lube oil cooler and process cooler) and
chilled water (process cooler). See MoM 21-May-
2015 item 12.
Closed
6.5 Noise level
82 dBA at 1 meter from main skid edge (compressor, gearbox and main driver). Noise limit for lube oil pumps and motors to be 80 dBA
(or less) at 1 meter from lube oil console.
Confirmed without additional noise control (Skid).
Process pipes need silencers for 82dBA in 1m
Noise limit for lube oil pumps and motors to be 80 dBA (or less) at 1
meter from lube oil console.
Supplier to provide technical information / data sheet
for the design of process piping silencer (upstream of
compressor suction flange) for review. Optional cost
to be quoted separately, when needed. See MoM 21-
May-2015 item 13.
Closed
7.0 Delivery
8.0 Technical clarfications based on bid
8.1 Process
Supplier shall provide each stage suction/discharge pressure, suction/discharge temperature, power and efficiency, utility duty (cooling
water or chilled water)
stage group performance data will not be supplied for suction/discharge
pressure, suction/discharge temperature, power and efficiency
What I meant is process stage (not impeller stage).
Guranteed power will be on gearbox input shaft (or
motor output).
Closed
Supplier shall consider below contents:
1) The design of the fire protection system and design of the lubrication system needs careful consideration. noted
High temperature protection on chlorine gas:-
a) 108 deg. C = alarm Closed
b) 120 deg. C = trip
2) The design must ensure that liquid cannot be trapped in or alternatively expansion pots (or similar) with bursting discs and pressure
measurements are installed. Since the review the location of E6571 has changed from the kickback line to the outlet of the compressor. If
pressure control valve is shut, blocking the kickback line, there will no longer be further cooling of the process fluid to cause condensation.
Flow will also continue to the purifying tower and expansion into the rest of the line will occur.
noted, not in MDT scope Noted Closed
3) The consequences of low pressure and surge with the compressor vendors. noted
Anti-surge valve and anti-surge controller is included
in Supplier's scope.
Closed
4) Consider the likelihood and consequence of the release of kinetic energy from the Compressor. noted Not in Supplier's scope. Closed
5) Review the design to consider how the risk of liquid flow to the compressor can be minimised. noted
Suction and inter-stage process scrubbers are in
Supplier's scope.
Closed
6) Basis of sizing through the relief valve needs to be supplied and the capacity of the compressor is known at discharge relief pressure. noted
Details (flow, P&T) for relief valve sizing to be
provided by Supplier at detailed engineering.
Closed
7) Confirm whether RV discharge can be routed to refrigeration compressor suction, taking into account the set pressure of the BD/RV
combination on the suction KO pot. See also related project action DYNA-PROJ-HCL-006-6510-055 from Hazard Study 2.
noted Not relevant to this machine. Closed
8) The maximum possible suction pressure for the maximum discharge pressure set by the compressor high pressure trip. noted Done, case C per Supplier's API 617 data sheet Closed
9) The compressor system volume depressurisation cannot exceed the design pressure of the overall reactor system. (i.e. discharge of
the compressor depressurises from say 12barg to 6, reactor system increases pressure from 5.5 to below 6.0)
noted
Preliminary SOP had been calculated by Supplier,
approx. 5 barA.
Closed
10) compressor package PLC contains a relevant alarm and a suitably designed interlock to shutdown compressor, independent of the
DCS.
noted Confirmed. Closed
11) The failure of a single interchanger (either the primary cooling water cooler or the chilled water cooler) can not lead to an high
temperature of the chlorine gas (T>120°C).
Failure of intercooler will lead to compressor trip due to high
temperature.
First stage process cooler discharge temperature is
now revised to 50 deg. C, which will limit the final
stage process gas temperature below 120 deg. C
when chilled water fails.
Closed
Appendix 5

Bidder Proposal
Page No./Clause
Subject
12) The catastrophic failure rate of the compressor is not higher than the number used in initiating cause B. unclear requirement Not in Supplier's scope. Closed
13) Compressor manufacturer confirm the presence of a knock out drum with high level start up permissive/ compressor trip at the
required FRF.
unclear requirement
Liquid level on supplier's scrubbers will be considered
as permissive to start. And alarm / trip during
operation.
Closed
14) Compressor manufacturer confirm the presence of a high vibration trip at the required FRF. unclear requirement
Instrument probes local to machine will be in
supplier's scope, and will be monitored by MMS in
compressor PLC. Trip signals voting configuration to
be finalised at detailed engineering. Trip via PLC or
SIS to be confirmed at detailed engineering.
Closed
15) Upgrade compressor shutdown and isolation interlock from chlorine detectors specified in CMDI-5-PROS-PD-0219 to achieve the
FRF of 0.05 required by this hazan.
unclear requirement Not in Supplier's scope. Closed
16) The rating case for E6570 for the high temperature (60degC), not giving a high enough compressor inlet temperature. E6570 rating
case: process fluid inlet temperature is 60 oC, outlet temperature is 23.5 oC calculated by HTRI. Supplier shall consider 23.5 oC as
compressor inlet temperature effect.
??? To be discussed in a face to face meeting
Discharge of 1st stage will be below 110 deg. C with
23.5 deg. C suction temperature (for Normal case).
Closed
17)Confirm with compressor manufacturer that the operating point with the lowest efficiency can not lead to an high temperature of the
chlorine gas (T>120°C).
confirmed for 15 °C suction temperature Noted Closed
If the above requirement are not clear, we will clarify in face to face meeting. noted Noted Closed
8.2 Instrument
Page 39, Block
Diagram S7-400
1) Pls note the site is safe area, no explosion proof class requirement. noted Noted Closed
Page 39, Block
Diagram S7-400
2) Unit Control Pannel and local panel should be RAL 7035. confirmed Noted Closed
Page 39, Block
Diagram S7-400
3) Pls note that ESD(SIS) related loops require necessary reliability information for SIL calculation as GEN4-0-INST-SP-0005,section 6.3
mentioned and pls provide the solution for safe operation and automatic shutdown as per Vendor's Practice.
after order SIL data to be provided at detailed engineering. Closed
Page 39, Block
Diagram S7-400
4) Instruments is preferred to be with Hart,and pls consider the communication to AMS. Confirmed Noted Closed
Page 39, Block
Diagram S7-400
5) As per P&ID Machine, the TE/VT is hardwired to BENTLY NEVADA 3500 system.Pls update this information in the bock diagram.
TE/VT is already hardwired to BENTLY NEVADA 3500 system in the
block diagram.
Noted Closed
Page 16, 4.12 Pls provide SIL certification for systems(S7-400H, ET 200F I/O,ET 200 I/O) within proposal.
Please refer to 3138_201208210910519121.
Please note that SIL3 will only be considered for complete loops
including input instruments and outputs.
Max considered SIL level for MDT compressor package of this project
is SIL1.
Refer to item 4.12 and 4.13 of 1975Z-1-SR-1011-
0001-B3.
Closed
GEN4-0-INST-SP-0005, 9.2.14
Pls note that the datasheets format will be .isf file,and software for open/modify will be provided after P.O. Vendor is required to provide
all instrument datasheet in this Package with this format.
vendor format will be provided Refer to item 18 of MOM 10th June 2015. Closed
8.3 Mechanical
Stage-wise performance curves shall be furnished for all compression duties, in addition to overall performance curve.
Overall performance curves already provided. Single stage peformance
data will not be supplied.
What I meant is process stage (not impeller stage). Closed
data ot be supp ed
Equation of state and associated binary interaction parameters (in tabulated form) shall be furnished.
Equation of state: LKP
Binary interaction coefficients are considered within calculation program
but will not be supplied (internal data)
Noted. Closed
Supplier to advise minimum dew point margin required at compressor suction flange.
Safe operation of compressor is ensured due to suction scrubber D6570
behind cooler E6570 and suction srubber D6571 behind cooler E6574.
However, scrubbers are deemed not necessary (see provided dew point
curve)
Minimum 10K dew point margin according to Supplier
response 22-May-2015.
Closed
Supplier to advise leakage rate of primary seal vent.
Done. Please reconfirm the use of a labyrinth separation seal as per
2.8.4.1 of GEN4 0 ROTE SP 0012 B1. MDT normally uses carbon ring
separation seal. Seal leakage flows shown for both seal types in
separate documents
Segmented carbon ring separation seal to be used. Closed
Appendix 5

Bidder Proposal
Page No./Clause
Subject
High & low speed couplings shall be flexible diaphragm type, coupling guard shall be non-sparking type. Supplier to confirm. confirmed
Sparking-free coupling guard is not required
(equipment is located in safe area). Stainless steel
coupling guard can be considered. Note that copper,
copper alloy and aluminimum shall not be used.
Closed
Supplier to provide effluent data for oil mist eliminator discharge. discharge liquid flow is led back to oil reservoir Noted. Closed
Supplier shall peform torsional vibration analysis of the complete coupled train and shall be responsible for directing the modifications
necessary to meet the requirements of API 617 1-2.6.7.2 through 1-2.6.7.6. Supplier to confirm.
confirmed Noted. Closed
Mechanical running tests shall be provided for the following items:-
a) Main compressor rotor assembly
b) Spare compressor rotor assembly
c) Main gearbox rotors
d) Spare gearbox rotors
Supplier to confirm the above
confirmed Noted. Closed
Supplier to confirm the above.
Page 11, item 1.5
Supplier to advise:-
a) Whether or not suction throttling is sufficient to cater the needs of process control (for all compression duties mentioned in the API 617
data sheet), or capacity control valve is needed?
b) Supplier to advise whether or not the offered anti-surge valve serves both surge protection and capacity control (cooled bypass)
purposes?
a) Process control via suction throttling is sufficient for specified
operating point.
b) confirmed, anti-surge valve serves surge protection and capacity
control (for bypass operation).
Noted. Closed
Page 12, item 1.8 Supplier to advise Cv value and corresponding stroke time (of surge protection) for the anti-surge valve being offered.
Cv value and corresponding stroke time of anti surge valve are
dependent on valve manufacturer design.
Typical values are Cv of 70 or 80 and stroking times less than 5
seconds for opening and 10-20 seconds for closing and less than 2
seconds for fast opening via solenoid valve.
Detailed data can be provided during detail engineering.
Noted. Closed
Page 12, item 1.9
Page 41, note 4
Compressor blow down valve (with restriction orifice) to be included in scope of supply, Supplier to confirm compliance.
Confirmed with cost adder which will be informed after technical
clarification meeting
see line 120
Refer to MOM 10th June item 10. Process PSV and
BDV to be excluded from Supplier's scope.
Closed
Page 12 item 1 10
Supplier to advise additional heat duty that to be imposed on the Puchaser supplied after cooler (HEX X4002302, according to supplier's
No additional heat duty required Noted ClosedPage 12, item 1.10
pp y p pp ( g pp
tag number on page 41) due to recycle flow; to ensure the after cooler is not undersized.
No additional heat duty required. Noted. Closed
Page 13, item 2.5 Supplier to confirm that all information mentioned in item 2.5 can be provided at detailed engineering phase.
confirmed for MDT scope of supply. Most of the items are related to
EPC.
Noted. Closed
Page 23, item 16.1
Supplier data / documentation shall be provided in accordance with part II and III of 1975Z-1-SR-1011-0001-B3, Supplier to confirm
compliance.
refer to MDT proposed VDDR in separate document Noted. Closed
Page 25, API 617 dFull version (not just 1st page) of API 617 (7th edition) data sheet is needed at bid stage, Supplier to provide. confirmed - first round or comments started Noted. Closed
Page 25, API 617 d
Supplier to provide PTC 10 type 2 conditions (Gas composition, Z1, Cp/Cv, P1, P2, T1, T2, rpm, gas power, polytropic head & polytropic
efficiency) for Purchaser's review. Associated quadrant curves to convert into project specific duties shall be provided.
after order
Noted. Air comparison gas test will be conducted
(open loop type, stage-by-stage).
Closed
Page 41 Suction shutdwon valve shall be provided and controlled by compressor PLC, Supplier to confirm compliance. Confirmed with cost adder Refer to MOM 10th June item 12. Closed
Page 41 Discharge shutdown valve shall be provided and controlled by compressor PLC, Supplier to confirm compliance. Confirmed with cost adder Refer to MOM 10th June item 12. Closed
Page 41 Suction check valve shall be provided, Supplier to confirm compliance. will not be provided Suction check valve is not required. Closed
Page 41 Blow down valve shall be provided and controlled by compressor PLC, Supplier to confirm compliance.
Confirmed with cost adder
Please refer to line 111 for repitiion.
Refer to MOM 10th June item 10. Process PSV and
BDV to be excluded from Supplier's scope.
Closed
Page 41, note 6 Permanent / operating strainer (spool piece and internal) to be provided, Supplier to confirm compliance.
MB: With permanent strainer additional pressure loss has to be
considered in performance calculation.
Permanent strainers not required. Temporary
strainers will be provided by Supplier.
Closed
Page 41
Suction throttling valve or cooled bypass vavle shall be supplied and controlled by compressor PLC, as required. Supplier to confirm
compliance.
Confirmed Noted Closed
Page 43 Supplier to advise allowable back pressure of inter-connecting piping between air discharge of oil mist eliminator and flame arrestor inlet. after order
Supplier will check if there is requirement of allowable
back pressure on oil demister.
Closed
Page 46
What is this (between 006 and 007)? Not covered in legend / symbol sheet. What purpose it serves (it looks like ordinary pipe spool with
concentric reducer at both ends)?
Symbol was considered as kind of backup N2 source in case Nitrogen
supply loss. It is a piping arrangement which is not supplied by MDT.
MDT will remove the backup N2 source. Client please to confirm that
N2 source is always available.
Nitrogen back-up for seal gas supply (primary and
separation seals) is not required, as the plant nitrogen
supply (derived from nitrogen vaporizer) is reliable.
See MoM 21-May-2015 item 15.
Closed
Appendix 5

1975Z-1-TBT-1011-0001-B1

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