sngs pofessional opinion

8/8/2019 Sngs Pofessional Opinion

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Professional EngiTender C

1. INTRODUCTION:

This document relates tdocument. The major coapparently does not suproposed by the Business

It is quite clear that duringnetwork, the Engineeringstage, it was based on asdemands. Hence by definaccurate at the stage of s

2. THE ENGINEERING PL

The engineering plan presurvey that was well-knengineering plan presentwere checked in depth.

In the Tender Documentataken in regard to the exeavailability of the "Lapidquantitative) solution to awas presented and entmentioned previously. Itthat "the subject will be di

The basic postulates ofconservative and took intconditions into the distriaccepted flow velocitiesbased on the worst gassupplied by Israeli suppliensure an increased gas

up to 87,162 Sm3/hr or e

The consequence of thethe Tender would permit

eering Opinion Regarding the ClaimLetter Dated 14/11/2010inmmittee

o the engineering issues raised in thecern is the discrepancy between the Engiport the prediction of 1BCM per year iPlan.

the time of preparation of the Tender for tPlan is assumed to be a conceptual de

sumptions derived from a survey with theition from an engineering point of view, thebmission of the Tender.

N IN THE TENDER DOCUMENT

sented in the Tender documents was basown at the time of the preparation ofd was the preferred alternative between

tion at the end of Section 1.1.1 "Design",cution of the proposed network over a 5-yot" PRMS. The assumptions proposedpossible problem. The principle of the

ailed the implementation of one of theas evident that they are more expensivecussed separately with the Manager, if ne

the engineering plan presented in theo consideration an extremely poor gas qubution network, low pressure drops andin distribution networks were assumed.ualities presented by INGL. It is known thrs is better and in the future will be evenflow from 77,682 Sm3/hr as written in the

en 99,506 Sm3/hr as described in Section

e assumptions is that the distribution netas flows in excess of those shown in the c

7/12/2010

of the

above-mentionedineering Plan thatin 25 years time

he NG distributionsign only. At thisstimations for NGdesign cannot be

d on a consumerthe Tender. The

alternatives that

ssumptions werear period and the

a qualitative (notualitative solutionsix alternatives,

and it was statedessary".

Tender are verylity. Inferior entrythe low end of

he calculation isat the gas qualityhigher, which willEngineering Plan

3 & 5 later.

ork presented innsumer survey.


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3. COMENTS to the CHECKING of the ENGINEERING PLAN by GL CONSULTANT

In the documents of the Tender Committee it is written that the grid of Ashdod areahas been sent to an expert from GL as a test case, distinct from the whole grid of theSouthern District. The combination of isolating Ashdod together with the method bywhich the design data have been transferred to GL, created a distortion in the GL

expert's professional opinion and lead him to a wrong conclusion, as described below.The GL expert's conclusion is that it is impossible to transfer the 64,000 Sm3/hr basedon the fact the Ashdod local PRS will not operate, i.e. the system will see an upperpressure lower than 7.5 barg. We claim this is an incorrect finding as the local PRS willoperate only during the initial stage and later, when the consumption will reach themaximum, it will be either 100% open during its natural aspiration to compensate thedownstream pressure, or it will be by-passed.

Regarding the calculation, the process team carried out the Ashdod PRMS (ASD1) -local PRS (ASD8) section simulation by Aspen Plus (see Appendix D), which isconsidered to be the most accurate way to evaluate the compressible flows.

The following are the inherent assumptions:

1) The gas consumption was evaluated based on the future heat demand forecastbased on the lowest HHV reported by INGL (see Appendix C) as 0.0346MMBTU/Sm3. The 64,000 Sm3/hr is equivalent to 64,000 x 0.0346 = 2214.4MMBTU/hr.

2) Two extreme cases were checked:a) The lower gas quality (92 vol. % CH4) featuring 0.78 kg/Sm3 gas density. (SeeAppendix A)b) The higher gas quality (100% CH4) (see Appendix B), as was simulated in

PIPENET. During simulation the Joule-Thomson gas cooling effect was consideredin both cases assuming an adiabatic process (soil has poor thermal conductivityand the pipe flow can be approximated as adiabatic). As can be seen, both casestransfer 2214.4 MMBTU/hr and are both feasible.

3) The 40,000 Sm3/hr case for the lower quality gas (the worst hydraulic case) isattached as well and shows the necessity of the local PRS as the ASD8 pressure ishigher than 7.5 barg. Hence the conclusion, made by GL's expert, that the max flowwill be around 27,000 Sm3/hr is wrong.

Furthermore, as the original customers' gas demand forecast at the end of the 1stoperation decade was estimated at 77,700 Sm3/hr, the proposed network delivers the

60,595 kg/hr of pure CH4 at the temperature of 38o

C that actually is equivalent to:a) 60,595 kg/hr / 0.675 kg/Sm3 (100% CH4, 101325 Pa and 15oC) =89,770 Sm3/hr of

100% CH4. The gas temperature decrease to 15oC has a potential to increase thiscapacity to 89,770 x (273.15+38K)/(273.15+15K) = 96,936 Sm3/hr of pure CH4.

b) 60,595 kg/hr x 0.526 MMBTU/kg/[0.03460.0395 MMBTU/Sm3 taken from INGL]= [80,71992,150] Sm3/hr. As in the item (a), the gas temperature decrease to15oC has a potential to increase this capacity to[80,71992,150] x (273.15+38K)/ (273.15+15K) = [87,16299,506] Sm3/hr


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Considering the average annual operating hours as 7,650 hours / year, the proposednetwork can transfer 7,650 hr/year x [87,16299,506] Sm3/hr = [0.6670.761] BCMof gas annually.

Considering the higher Gas Quality, releasing the velocity limit from 20 m/s to 40 m/sand the lowest end-user pressure from 2 barg to 250 mbarg, the network actualcapacity will be even higher.

4. COMMENTS TO INGL's LETTER RELATED to the PRMSs

The tariff for PRMS with the capacity of 40,000 Sm3/hr, which is mentioned in INGL'sletter, amounts to MNIS 10 while the present tariff is MNIS 8.9 and very similar to thevalue which is presented in the Tender documentation as (M$ 2.38 x 3.75 )= MNIS8.925.

According the price breakdown for the design, purchasing and construction of PRMS,

as published on the NGA's internet web, this price includes all the additional costs thatare mentioned in INGL's letter. Hence the additional amount of MNIS 11-12, as writtenin paragraph 2 of that letter, is not clear and seems unnecessary.

It is correct that the PRMS for the distribution network, should be designed andordered from the beginning for the largest capacity, while in practice, during the firstperiod of operation it will be partially erected.

Only in the last few months has the characterization of PRMS for the distributionnetwork become clear to all parties in the Natural Gas market. However, the effects oncost considerations are relatively small.

5. COMPATIBILITY BETWEEN BUSINESS & ENGINEERING PLANS

In the afore-mentioned letter from the Tender Committee it was assumed that thegrowth of the demands would be uniform for all the sub-regions. Because of thisincorrect assumption a demand of 64,000 Sm3/hr has been taken for the Ashdod sub-region.

The growth of the demands is a function of the industrial development of a region. It ismore realistic than that because of many reasons, such as governmentalencouragement policy which will ensure that the industrial development ofundeveloped area will be more rapid than the established areas. Hence we canassume with reasonable certainty that the development rate of Ashdod will be more

moderate compared to the other regions.

For example, flow rate of 40,000 Sm3/hr in Ashdod reflects an annual demand of 0.3BCM after 25 years, which corresponds to a total growth of about 150% above theannual demand after 10 years, as had been calculated in the Engineering plan of theTender. Those figures are very reasonable for a well-developed area and are basedon assumptions which are not less reliable than the others.


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In the letter of Super NG South dated 5/10/2010 to the Tender Committee, it wasstated that the accumulative flow rate would be 130,870 Sm3/hr for all the 5 sub-regions connected to 4 PRMSs.

As mentioned in section 2 above, the hydraulic calculations presented for thedistribution system are very conservative, based on low quality NG at 380C and withinlet pressure of 2 barg into the yard of the furthest end users from the PRMS.

The hydraulic calculations of the same pipe network but based on high quality NG,pure CH4 at 15oC, corresponding to the 0.676 kg/Sm3 standard density, withreference conditions of 101325 Pa, 15.5555oC (60oF) and with inlet pressure of500mbarg to the same end users, gives the following results:

PRMS-Ashdod: can deliver 40,000 Sm3/hr NG without any piping changes. PRMS-Ashkelon: can deliver 10,870 Sm3/hr NG without any piping changes. PRMS-Lapidot: can deliver 40,000 Sm3/hr NG but with increasing the diameter

of 3.3 km piping from 150mm to 200mm. (One commercial size)

PRMS-Qiryat Gat: can deliver 40,000 Sm3/hr NG but with increasing the diameterof 5 km piping from 200mm to 250mm. (One commercial size)

All the data for the above information is presented in the attached PDF file which is theoutput of the PIPNET Appendix E.

The total additional cost of the above changes in the piping is NIS 567,000. Thisbudgetary deviation of ~0.5% is negligible and can be compensated by thecontingency. It should be remembered that the distribution system cost estimationsbased on conceptual design only. It is very common that during the detailed designthere are large changes in the sizes of the pipes. Changing one commercial size in 8.3km out of about 158 km in total is trivial and acceptable.


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APPENDIX A


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Low Quality NG

1 2 4 5 6 7 8 11 13 ASD1 ASD8

P2 ASD7 ASD32 P3 P1

ASD32 ASD32 ASD32 P2 P1 ASD7 ASD7 ASD7 ASD32 P3

VAPOR VAPOR VAPOR VAPOR VAPOR VAPOR VAPOR VAPOR VAPOR VAPOR VAPOR

Substream: MIXED

Mole Frac

C1 0.92 0.92 0.92 0.92 0.92 0.92 0.92 0.92 0.92 0.92 0.92

C2 0.02 0.02 0.02 0.02 0.02 0.02 0.02 0.02 0.02 0.02 0.02

C3 0.01 0.01 0.01 0.01 0.01 0.01 0.01 0.01 0.01 0.01 0.01

I-C4 5.00E-03 5.00E-03 5.00E-03 5.00E-03 5.00E-03 5.00E-03 5.00E-03 5.00E-03 5.00E-03 5.00E-03 5.00E-03

N-C4 5.00E-03 5.00E-03 5.00E-03 5.00E-03 5.00E-03 5.00E-03 5.00E-03 5.00E-03 5.00E-03 5.00E-03 5.00E-03

I-C5 0.01 0.01 0.01 0.01 0.01 0.01 0.01 0.01 0.01 0.01 0.01

N-C5 1.36E-03 1.36E-03 1.36E-03 1.36E-03 1.36E-03 1.36E-03 1.36E-03 1.36E-03 1.36E-03 1.36E-03 1.36E-03

N-C6 1.00E-03 1.00E-03 1.00E-03 1.00E-03 1.00E-03 1.00E-03 1.00E-03 1.00E-03 1.00E-03 1.00E-03 1.00E-03

N-C7 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05

N-C8 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05

N-C9 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05

N-C10 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05 1.00E-05

CO2 0.0266 0.0266 0.0266 0.0266 0.0266 0.0266 0.0266 0.0266 0.0266 0.0266 0.0266

N2 0 0 0 0 0 0 0 0 0 0 0

H2O 1.00E-03 1.00E-03 1.00E-03 1.00E-03 1.00E-03 1.00E-03 1.00E-03 1.00E-03 1.00E-03 1.00E-03 1.00E-03Mass Frac

C1 0.798568 0.798568 0.798568 0.798568 0.798568 0.798568 0.798568 0.798568 0.798568 0.798568 0.798568

C2 0.032539 0.032539 0.032539 0.032539 0.032539 0.032539 0.032539 0.032539 0.032539 0.032539 0.032539

C3 0.023859 0.023859 0.023859 0.023859 0.023859 0.023859 0.023859 0.023859 0.023859 0.023859 0.023859

I-C4 0.015724 0.015724 0.015724 0.015724 0.015724 0.015724 0.015724 0.015724 0.015724 0.015724 0.015724

N-C4 0.015724 0.015724 0.015724 0.015724 0.015724 0.015724 0.015724 0.015724 0.015724 0.015724 0.015724

I-C5 0.039038 0.039038 0.039038 0.039038 0.039038 0.039038 0.039038 0.039038 0.039038 0.039038 0.039038

N-C5 5.31E-03 5.31E-03 5.31E-03 5.31E-03 5.31E-03 5.31E-03 5.31E-03 5.31E-03 5.31E-03 5.31E-03 5.31E-03

N-C6 4.66E-03 4.66E-03 4.66E-03 4.66E-03 4.66E-03 4.66E-03 4.66E-03 4.66E-03 4.66E-03 4.66E-03 4.66E-03

N-C7 5.42E-05 5.42E-05 5.42E-05 5.42E-05 5.42E-05 5.42E-05 5.42E-05 5.42E-05 5.42E-05 5.42E-05 5.42E-05

N-C8 6.18E-05 6.18E-05 6.18E-05 6.18E-05 6.18E-05 6.18E-05 6.18E-05 6.18E-05 6.18E-05 6.18E-05 6.18E-05

N-C9 6.94E-05 6.94E-05 6.94E-05 6.94E-05 6.94E-05 6.94E-05 6.94E-05 6.94E-05 6.94E-05 6.94E-05 6.94E-05

N-C10 7.70E-05 7.70E-05 7.70E-05 7.70E-05 7.70E-05 7.70E-05 7.70E-05 7.70E-05 7.70E-05 7.70E-05 7.70E-05

CO2 0.06334 0.06334 0.06334 0.06334 0.06334 0.06334 0.06334 0.06334 0.06334 0.06334 0.06334

N2 0 0 0 0 0 0 0 0 0 0 0

H2O 9.75E-04 9.75E-04 9.75E-04 9.75E-04 9.75E-04 9.75E-04 9.75E-04 9.75E-04 9.75E-04 9.75E-04 9.75E-04

Total Flow kmol/hr 59.13779 88.03035 1284.612 1284.612 2470.452 142.2445 113.3519 1029.016 1038.672 2470.452 1029.016

Total Flow kg/hr 1093 1627 23742.54 23742.54 45659.54 2629 2095 19018.54 19197 45659.54 19018.54Total Flow cum/hr 129.8874 193.3456 2821.46 4679.749 5425.98 518.1865 412.9329 3748.63 2281.288 3299.714 5331.818

Temperature C 10.99287 10.99287 10.99287 8.426937 10.99287 8.426937 8.426937 8.426937 10.99287 15 7.244853

Pressure barg 9.386808 9.386808 9.386808 5.280341 9.386808 5.280341 5.280341 5.280341 9.386808 16 3.419572

Vapor Frac 1 1 1 1 1 1 1 1 1 1 1

Liquid Frac 0 0 0 0 0 0 0 0 0 0 0

Solid Frac 0 0 0 0 0 0 0 0 0 0 0

Enthalpy kJ/kmol -85982.9 -85982.9 -85982.9 -85982.9 -85982.9 -85982.9 -85982.9 -85982.9 -85982.9 -85982.9 -85982.9

Enthalpy kJ/kg -4652.18 -4652.18 -4652.18 -4652.18 -4652.18 -4652.18 -4652.18 -4652.18 -4652.18 -4652.18 -4652.18

Enthalpy kW -1412.46 -2102.53 -30681.9 -30681.9 -59004.6 -3397.39 -2707.31 -24577.2 -24807.8 -59004.6 -24577.2

Entropy kJ/kmol-K -108.211 -108.211 -108.211 -104.145 -108.211 -104.145 -104.145 -104.145 -108.211 -112.132 -101.282

Entropy kJ/kg-K -5.85485 -5.85485 -5.85485 -5.63487 -5.85485 -5.63487 -5.63487 -5.63487 -5.85485 -6.06702 -5.47997

Density kmol/cum 0.455301 0.455301 0.455301 0.274505 0.455301 0.274505 0.274505 0.274505 0.455301 0.748687 0.192995

Density kg/cum 8.414984 8.414984 8.414984 5.073463 8.414984 5.073463 5.073463 5.073463 8.414984 13.83742 3.566989

Average MW 18.48226 18.48226 18.48226 18.48226 18.48226 18.48226 18.48226 18.48226 18.48226 18.48226 18.48226

Liq Vol 60F cum/hr 3.296862 4.907589 71.61561 71.61561 137.7248 7.929963 6.319237 57.36641 57.90472 137.7248 57.36641

*** ALL PHASES ***

QVALGRS MMBtu/lb 0.021998 0.021998 0.021998 0.021998 0.021998 0.021998 0.021998 0.021998 0.021998 0.021998 0.021998

QVALNET MMBtu/lb 0.019884 0.019884 0.019884 0.019884 0.019884 0.019884 0.019884 0.019884 0.019884 0.019884 0.019884

Total Flow ncmh 1325.491 1973.078 28792.8 28792.8 55371.75 3188.213 2540.626 23063.96 23280.38 55371.75 23063.96

*** VAPOR PHASE ***

ZMX 0.966882 0.966882 0.966882 0.97932 0.966882 0.97932 0.97932 0.97932 0.966882 0.948509 0.985227

CPCVMX 1.326914 1.326914 1.326914 1.311627 1.326914 1.311627 1.311627 1.311627 1.326914 1.35157 1.304726

Density kg/cum 8.414984 8.414984 8.414984 5.073463 8.414984 5.073463 5.073463 5.073463 8.414984 13.83742 3.566989

MUMX cP 0.010859 0.010859 0.010859 0.0107 0.010859 0.0107 0.0107 0.0107 0.010859 0.011122 0.010628

CPMX kJ/kg-K 2.103173 2.103173 2.103173 2.066787 2.103173 2.066787 2.066787 2.066787 2.103173 2.162197 2.050405

KMX Watt/m-K 0.030162 0.030162 0.030162 0.029819 0.030162 0.029819 0.029819 0.029819 0.030162 0.030701 0.029661

TDEW C -4.39013 -4.39013 -4.39013 -10.4094 -4.39012 -10.4094 -10.4094 -10.4094 -4.39013 1.157764 -14.6077

THYDRATE C 0.103431 0.103431 0.103431 -7.63493 0.103431 -7.63493 -7.63493 -7.63493 0.103431 4.380542 -19.8053


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APPENDIX B


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High Quality NG

1 2 4 5 6 7 8 11 13 ASD1 ASD8

P2 ASD7 ASD32 P3 P1

ASD32 ASD32 ASD32 P2 P1 ASD7 ASD7 ASD7 ASD32 P3

VAPOR VAPOR VAPOR VAPOR VAPOR VAPOR VAPOR VAPOR VAPOR VAPOR VAPOR

Substream: MIXED

Mole Frac

C1 1 1 1 1 1 1 1 1 1 1 1

C2 0 0 0 0 0 0 0 0 0 0 0

C3 0 0 0 0 0 0 0 0 0 0 0

I-C4 0 0 0 0 0 0 0 0 0 0 0

N-C4 0 0 0 0 0 0 0 0 0 0 0

I-C5 0 0 0 0 0 0 0 0 0 0 0

N-C5 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00

N-C6 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00

N-C7 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00

N-C8 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00

N-C9 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00

N-C10 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00

CO2 0 0 0 0 0 0 0 0 0 0 0

N2 0 0 0 0 0 0 0 0 0 0 0

H2O 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00Mass Frac

C1 1 1 1 1 1 1 1 1 1 1 1

C2 0 0 0 0 0 0 0 0 0 0 0

C3 0 0 0 0 0 0 0 0 0 0 0

I-C4 0 0 0 0 0 0 0 0 0 0 0

N-C4 0 0 0 0 0 0 0 0 0 0 0

I-C5 0 0 0 0 0 0 0 0 0 0 0

N-C5 0 0 0 0 0 0 0 0 0 0 0

N-C6 0 0 0 0 0 0 0 0 0 0 0

N-C7 0 0 0 0 0 0 0 0 0 0 0

N-C8 0 0 0 0 0 0 0 0 0 0 0

N-C9 0 0 0 0 0 0 0 0 0 0 0

N-C10 0 0 0 0 0 0 0 0 0 0 0

CO2 0 0 0 0 0 0 0 0 0 0 0

N2 0 0 0 0 0 0 0 0 0 0 0

H2O 0 0 0 0 0 0 0 0 0 0 0

Total Flow kmol/hr 68.13042 101.4165 1257.097 1257.097 2623.258 163.8745 130.5885 962.6339 1196.615 2623.258 962.6339

Total Flow kg/hr 1093 1627 20167.3 20167.3 42084.3 2629 2095 15443.3 19197 42084.3 15443.3Total Flow cum/hr 149.6156 222.7123 2760.607 4007.136 5760.722 522.3683 416.2653 3068.502 2627.787 3541.919 3650.304

Temperature C 11.53665 11.53665 11.53665 9.761019 11.53665 9.761019 9.761019 9.761019 11.53665 15 9.125069

Pressure barg 9.477722 9.477722 9.477722 6.22677 9.477722 6.22677 6.22677 6.22677 9. 477722 16 5.076836

Vapor Frac 1 1 1 1 1 1 1 1 1 1 1

Liquid Frac 0 0 0 0 0 0 0 0 0 0 0

Solid Frac 0 0 0 0 0 0 0 0 0 0 0

Enthalpy kJ/kmol -75202.4 -75202.4 -75202.4 -75202.4 -75202.4 -75202.4 -75202.4 -75202.4 -75202.4 -75202.4 -75202.4

Enthalpy kJ/kg -4687.62 -4687.62 -4687.62 -4687.62 -4687.62 -4687.62 -4687.62 -4687.62 -4687.62 -4687.62 -4687.62

Enthalpy kW -1423.21 -2118.54 -26260.2 -26260.2 -54798.7 -3423.26 -2727.93 -20109 -24996.7 -54798.7 -20109

Entropy kJ/kmol-K -102.166 -102.166 -102.166 -99.1515 -102.166 -99.1515 -99.1515 -99.1515 -102.166 -106.051 -97.7385

Entropy kJ/kg-K -6.36833 -6.36833 -6.36833 -6.18045 -6.36833 -6.18045 -6.18045 -6.18045 -6.36833 -6.61051 -6.09237

Density kmol /cum 0.45537 0.45537 0.45537 0.313715 0.45537 0.313715 0.313715 0.313715 0.45537 0.740632 0.263713

Density kg/cum 7.305388 7.305388 7.305388 5.032848 7.305388 5.032848 5.032848 5.032848 7.305388 11.88178 4.23069

Average MW 16.04276 16.04276 16.04276 16.04276 16.04276 16.04276 16.04276 16.04276 16.04276 16.04276 16.04276

Liq Vol 60F cum/hr 3.648915 5.431643 67.32735 67.32735 140.4959 8.77676 6.994033 51.55655 64.08804 140.4959 51.55655

*** ALL PHASES ***

QVALGRS MMBtu/lb 0.023867 0.023867 0.023867 0.023867 0.023867 0.023867 0.023867 0.023867 0.023867 0.023867 0.023867

QVALNET MMBtu/lb 0.021509 0.021509 0.021509 0.021509 0.021509 0.021509 0.021509 0.021509 0.021509 0.021509 0.021509

Total F low ncmh 1527.049 2273.109 28176.08 28176.08 58796.7 3673.021 2926.96 21576.1 26820.45 58796.7 21576.1

*** VAPOR PHASE ***

ZMX 0.973324 0.973324 0.973324 0.981133 0.973324 0.981133 0.981133 0.981133 0.973324 0.958824 0.983992

CPCVMX 1.346726 1.346726 1.346726 1.33593 1.346726 1.33593 1.33593 1.33593 1.346726 1.368221 1.332104

Density kg/cum 7.305388 7.305388 7.305388 5.032848 7.305388 5.032848 5.032848 5.032848 7.305388 11.88178 4.23069

MUMX cP 0.010917 0.010917 0.010917 0.010807 0.010917 0.010807 0.010807 0.010807 0.010917 0.01114 0.010768

CPMX kJ/kg-K 2.267308 2.267308 2.267308 2.240945 2.267308 2.240945 2.240945 2.240945 2.267308 2.320166 2.231628

KMX Watt/m-K 0.032309 0.032309 0.032309 0.032064 0.032309 0.032064 0.032064 0.032064 0.032309 0.032788 0.031977

TDEW C -123.186 -123.186 -123.186 -130.965 -123.186 -130.965 -130.965 -130.965 -123.186 -111.757 -134.331

THYDRATE C -3.15 -3.15 -3.15 -3.15 -3.15 -3.15 -3.15 -3.15 -3.15 -3.15 -19.6319


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APPENDIX C


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APPENDIX D


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40,000 Sm3/hr Low Quality NG


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64,000 Sm3/hr Low Quality NG


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64,000 Sm3/hr High Quality NG


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APPENDIX E


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sngs pofessional opinion

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