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EUR 5103 e COMMISSION OF THE EUROPEAN COMMUNITIES HYDROGEN, OXYGEN AND NATURAL GAS BY PIPELINES: COMPARATIVE TRANSPORT COSTS by G. BEGHI, J. DEJACE (Euratom) Β. CIBORRA (Istituto di Macchine - Politecnico di Milano) C. MASSARO (SNAM Progetti - Milano) 1974 Joint Nuclear Research Centre Ispra Establishment - Italy
Transcript of HYDROGEN, OXYGEN AND NATURAL GAS BY PIPELINES: …aei.pitt.edu/91758/1/5103.pdf · Luxembourg,...
EUR 5103 e
COMMISSION OF THE EUROPEAN COMMUNITIES
HYDROGEN, OXYGEN AND NATURAL GAS BY PIPELINES:
COMPARATIVE TRANSPORT COSTS by
G. BEGHI, J. DEJACE (Euratom) Β. CIBORRA (Istituto di Macchine - Politecnico di Milano)
C. MASSARO (SNAM Progetti - Milano)
1974
Joint Nuclear Research Centre Ispra Establishment - Italy
LEGAL NOTICE
This document was prepared under the sponsorship of the Commission of the European Communities.
Neither the Commission of the European Communities, its contractors nor any person acting on their behalf ;
make any warranty or representation, express or implied, with respect to the accuracy, completeness, or usefulness of the information contained in this document, or that the use of any information, apparatus, method or process disclosed in this document may not infringe privately owned rights; or
assume any liability with respect to the use of, or for damages resulting from the use of any information, apparatus, method or process disclosed in this document.
This report is on sale at the addresses listed on cover page 4
at the price of B.Fr. 40.-
Commission of the European Communities D.G. XIII - C.I.D. 29, rue Aldringen L u x e m b o u r g August 1974
This document was reproduced on the basis of the best available copy.
EUR 5103 e HYDROGEN, OXYGEN AND NATURAL GAS BY PIPELINES: COMPARATIVE TRANSPORT COSTS by G. BEGHI, J. DEJ ACE (Euratom) Β. CIBORRA (Istituto di Macchine - Politecnico di Milano) C. MASSARO (SNAM Progetti - Milano) Commission of the European Communities Joint Nuclear Research Centre — Ispra Establishment (Italy) Luxembourg, August 1974 — 26 Pages — 11 Figures — B.Fr. 40.—
A technical-economical comparison was made between the transport by pipeline of natural gas, hydrogen and oxygen. Comparative costs were calculated for distances up to 2000 Km, and flows up to 4000 Gcal/ sec; the influence of transport pressure and intermediate compression stations was also taken into account.
EUR 5103 e HYDROGEN, OXYGEN AND NATURAL GAS BY PIPELINES: COMPARATIVE TRANSPORT COSTS by G. BEGHI, J. DE J ACE (Euratom) Β. CIBORRA (Istituto di Macchine - Politecnico di Milano) C. MASSARO (SNAM Progetti - Milano) Commission of the European Communities Joint Nuclear Research Centre — Ispra Establishment (Italy) Luxembourg, August 1974 — 26 Pages — 11 Figures — B.Fr. 40.—
A technical-economical comparison was made between the transport by pipeline of natural gas, hydrogen and oxygen. Comparative costs were calculated for distances up to 2000 Km, and flows up to 4000 Gcal/ sec; the influence of transport pressure and intermediate compression stations was also taken into account.
EUR 5103 e HYDROGEN, OXYGEN AND NATURAL GAS BY PIPELINES: COMPARATIVE TRANSPORT COSTS by G. BEGHI, J. DEJACE (Euratom) Β. CIBORRA (Istituto di Macchine - Politecnico di Milano) C. MASSARO (SNAM Progetti - Milano)
Commission of the European Communities Joint Nuclear Research Centre — Ispra Establishment (Italy) Luxembourg, August 1974 — 26 Pages — 11 Figures — B.Fr. 40.—
A technical-economical comparison was made between the transport by pipeline of natural gas, hydrogen and oxygen. Comparative costs were calculated for distances up to 2000 Km, and flows up to 4000 Gcal/ sec; the influence of transport pressure and intermediate compression stations was also taken into account.
EUR 5103 e
COMMISSION OF THE EUROPEAN COMMUNITIES
HYDROGEN, OXYGEN AND NATURAL GAS BY PIPELINES:
COMPARATIVE TRANSPORT COSTS by
G. BEGHI, J. DEJACE (Euratom) Β. CIBORRA (Istituto di Macchine - Politecnico di Milano)
C. MASSARO (SNAM Progetti - Milano)
1974
Joint Nuclear Research Centre Ispra Establishment - Italy
ABSTRACT A technical-economical comparison was made between the transport
by pipeline of natural gas, hydrogen and oxygen. Comparative costs were calculated for distances up to 2000 Km, and flows up to 4000 Gcal/ sec; the influence of transport pressure and intermediate compression stations was also taken into account.
KEYWORDS
I N D E X
1. Introduction 5
2. General Data and Basic Hypotheses 5
3. Technical-Economic Evaluation 6
4. Results *
References $
1. INTRODUCTION
Hydrogen is mentioned with increasing frequency in energy market forecasts for its potential in various fields D. 2I, 3), 4)
Since one of the most important elements in the development of a fuel is ease of transport, it is important to have some information on this subject.
The technical fesibility of hydrogen pipelines has already been demonstrated; we can mention, amongst others, the several hundreds of kilometers of ducts which link petrochemical centres and chemical industries in Western Germany 5>.
This study makes a preliminary attempt, within
the limits set by assumptions, to make technico — economical comparisons between hydrogen and an already existing conventional energy source, such as the widely employed natural gas. For the purposes of this comparison we have taken into consideration only transport over long distances with or without intermediate compressor stations.
The transport cost for oxygen has also been calculated, due to the fact that a chemical plant for hydrogen production by water decomposition gives oxygen as a byproduct; this gas may have interesting applications.
2. GENERAL DATA AND BASIC HYPOTHESES
2.1 Characteristics of Gas 2.3 Utilization Factor
We are considering the transport of 100% pure hydrogen and oxygen, and natural gas composed of 100% methane. The principal characteristics are as follows:
For these preliminary calculations we will consider the case of regular operation, without peak period, equal to 8000 hours/per year, with a resulting utilization factor of approximately 91%.
— Chemical formula
— Specific gravity at 0°C and 700 mm Hg
— Molecular weight
- R = ^ 8 m / ° M
-Cp(Cal/°Kg)
-C v (Cal /°Kg)
- κ - Cp/Cv
ψ κ — P j = Heat of combustion (net)
KCal/m3(0°C, 760mm Hg)
— Zm, average compressibility
coefficient in transport
conditions
Hydrogen
H,
.08987
2.016
420.6
3.408
2.420
1.407
.289
2600
1.02
1.03
1.042
Methane
CH4
.7168
16.032
52.9
.531
.406
1.31
.237
8600
.94
.90
.86
Oxygen
0,
1.42904
32.
26.5
.218
.156
1.401
.285
.975 (40 Kg/cm2)
.96 (65 Kg/cm2 )
.95 (90 Kg/cm2 )
2.2 Average Temperature for Transport
We have assumed for transport in the ducts an average temperature equal to 10°C = 283° K.
2.4 Pressure in the Pipeline
We have assumed three values for the pressure in the pipeline: 90 Kg/cm2; 65 Kg/cm2; 40 Kg/cm2
65 Kg/cm2 is a value which is normally utiiized for
methane. For the other gases it will be possible to
have information on the best values for the pressure.
2.6 Material·
We consider to use API 5LXX60 steel or an
equivalent (yield point 42 Kg/mm2).
Calculations of the wall thickness of the pipes
were carried out according to DIN 2413 norms.
During this preliminary phase no special atten
tion was paid to any particular safety measures re
lating, for instance, to the materials of the duct
itself, which might be required for hydrogen trans
port.
2.6 Terminal Station
We assumed two cases:
— production pressure equal to transport pressure.
In this case we do not have to calculate the cost
of constructing and operating a special terminal
station for comoresslng the gases.
— a production pressure equal to 10 Kg/cm2 (for
hydrogen and oxygen only).
In this case, a terminal station is necessary
between production plantand the duct
2.7 Gas Flow
In order to have a term for comparison purpo
ses, for methane and hydrogen, the flow has been
expressed in heat quantity, the calculations have
been made on the basis of an equal number of KCal
transported In a unit of time, combustion efficiency
being assumed equal. In the case of oxygen, only
volume units have been considered.
3. TECHNICAL ECONOMIC EVALUATION
3.1 Calculation of Pipe Diameter
For a determination of the pressure drop the
general formula of gases has been taken into consi
deration, together with the expression of the fric
tion coefficient as proposed by Weymouth.
We have referred to this formula of Weymouth,
both because of its simplicity and because of the
lack of semiempirical formulae for hydrogen and
oxygen gas as accurate and as experimentally tested
as those at present available for natural gas.
This equation becomes:
0 = 13θ7(Ρ
*'Ρ'2>°
T.«XTZm
(D
where:
Q gas f low, Nm3 /sec (0°C 760 mm Hg)
Pi PJ pressures at the beginning and at the end of
the section of gasduct under consideration,
Kg/cm2
diameter of the pipe, m,
specific gravity of the gas, Kg/Nm3 (0°C e
760 mm Hg)
length of the section of gasduct under consi
deration, Km
friction coefficient according to Weymouth =
0,00941 D_1 Λ
(D ¡n m)
average transport temperature, °K
compressibility factor of the gas
D
7o
Τ
Zm
Substituting the value of λ using the compres
sion ratio ρ = (Pi /P3 ) and setting yQ Τ Zm = a (con
stant depending only of gas and temperature) we
find:
D= [5.56· ΐ σ ' Q2 a fi 3/16
Ρ2, (1 ] (2)
D diameter of pipeline as function of the flow Q, of the length of the pipeline's section, of pressure Pi of transport and of compression ratio p.
3.2 The Cost of the Pipe
The cost per unit of length of the pipe has been calculated as a function of the diameter D, taking into consideration the thicknesses and the materials mentioned in § 2.5, the cost of the steel, the costs of the protective coatings, the assembly, the transport, and also the various indirect costs which must be added.
In these estimates we have considered average european costs (for year 1970) and have left out eventual special safety devices arising out of the transport of hydrogen. Part of the cost (essentially the price of steel) is taken as proportional to the thickness (i.e. proportional to the pressure) through the following formula:
CT u = (0.985· 103 P, +127 · 103 )D' ·6
7
where:
C j u is the cost of the pipe (Lit/m), Ρχ the transport
pressure (Kg/cm2) and D the diameter of the pipe
im). For the particular case of Pi »65 Kg/cm2 we
obtain a formula for methane which is in good
agreement with experience.
C T u = 191 · 103 · D
1'6
By substituting the value of D from formula (2) and
setting fi = (L/t), where L is the total length of the
pipe (in Km) and t the number of sections, we have:
CT = (1.308· 104 P, +1 .688 · 10
6)
. a Q2 L ° ·
3
Γ.) tP2, o A )
P
(3)
3.3 The Cost of Compression Stations
The power absorbed by each station is given by
T . Û H N = .
V where
T? is the compression efficiency (assumed equal to
.8)
Η is the adiabatic work given by
If we express Ν in HP, substitute the value of R and
let (70 Z m T)/(m φ) ■ b (constant depending only
on gas and temperature) we obtain:
Ν = 14.13 b Q ( p ^ 1 ) (4)
Allowing for an increase of 25% for obtaining the
installed power, we obtain for the cost of one
compression station
< CS = 1,25· N 'Pçy
where P w is the price of the installed HP
(5)
3.4 Economical Evaluation
The price of transport was calculated under the
following assumptions:
Devaluation allowance (15 years at 8%)
for pipeline ,12 CT/year
for stations . 12 CS/year
Maintenance costs
for pipeline .005 CT/year
for stations .035 CS/year
Energy costs per year for one station
CE = .736 · Ν
where
P|cvv is the price of Kwh
kw (6)
n n is the number of operating hours per year.
Personnel costs
C per year for one station
As the flow Q is given in m3/sec the price of trans
port of one cubic meter is given by
C=1
Q · Sec. [.125 CT+ .155 CS· ( t 1 ) + C E
• ( t D + Cp^Mt DJ + a
where
Sec= 3600 · n p is the operating time per year
expressed in seconds
Ci takes in account the cost of eventual initial
compression
Substituting the values of CT, CS, CE from
formulae (3), (5), (6) and grouping into coefficients
all quantities not dependent on p, we find
C = a(1-p-2r°-3+/3p^ + 7
where
α = ( . 1 6 3 · 104 · P} + .2115 · 10
6)
, ' j Q2 Up.» L
P2i t Q· sec
0=(i
S^Pcv
+ 2
8 8'
1 ö"
3 pk w >
b< t
1>
C ^ J t 1 ) pers
Q · Sec + C¡
It is now possible to calculate the value of the
compression ratio p which minimizes the price C.
For this value of p, the first derivative (dc)/(dp)
will vanish
— =-Ο.6α(1 -ρ - 2 Γ 1 · 3 ρ- 3 +0 φ p^> =0 dp
After some calculation and setting
0.6 φ
1.3 and
0.6 α
we obtain an equation in ρ easily solved by the
Newton method
p"(p2-1) = B (7)
It should be noted that, in the case of t = 1,
which means a duct without intermediate compres
sion station, β vanishes and equation (7) no longer
makes sense. In this case we have assumed for the
compression ratio a value of ρ = 1.5 (average value
encountered in the majority of cases).
- 8 -
3.6 Initial Compression
The initial compression ratio is calculated by:
P\ PD
where Pi is the pressure In the duct Pp is the production pressure
The energy of compression was calculated with the formula (4) used in § 3.3. With some simplified assumptions the cost of initial compression was evaluated In the various cases. Exemples of the obtained results are given in the diagrams of Fig. 4.
3.6 Numerical Calculations
A computer program has been written In Fortran IV language. The input consists of:
- gas data: specific gravity, molecular weight, φ, heat of combustion, compressibility coefficient.
- transport parameters: temperature, production pressure, maximum transport pressure, Pj, cost of installed horse-power, P^, cost of kwh, P|cw, cost of personnel C p ^ , number of hours of exercise per year, nh.
— quantity of gas with an option for the units (volume or energy)
— total length of the duct and minimum and maximum number of sections.
The following prices valid for year 1970 ' were assumed
Price of Kilowat-hour Pk w = 10 Lit (Italian lire) 2)
Price of Installed horse-power P^ = 180 000 Lit Coat of personnel per station and year C__r. · 100 · 10' Lit.
The flow for methane and hydrogen was made to vary between 500 and 4000 MCal/sec; which correspond to flow between 200 000 and 1 6 0 0 000 Nm 3 / h for methane and between 700 000 and 5 600 000 Nm3/h for hydrogen.
For oxygen, flow varying between 500 m3/tec (1 8 0 0 0 0 0 N i n ' / h ) and 1 5 0 0 m3 /sec (5,400,000 Nm3/h) were considered.
The total length of the pipe varies between 500 and 2000 Km. Three transport pressures, as previously mentioned, were used: 40, 65 and 90 Kg/cm2.
For each pair of Q and L and for different values of t, the value of compression ratio p, which minimizes the cost, was calculated. Other quantities which may be Interesting were also calculated; an example of output is given in Table 11 for methane at 65 Kg/cm2.
1) All the utilized prices are 1970 prices: this does not influence the main objective of the work, which Is e comparative ratio of costs.
2) The Influence of the price of the KWh has been verified: an Increate or e reduction of this price by e fector 2 will Influence the total transport cost by lees than 6%.
4. RE8ULTS
4.1 General Considerations
A synthesis of results is given in Figs. 1, 2, 3 which for a different flows (.5, 1,2,3, 4 GCal/sec), different distances (500, 1000, 1500, 200 Km) and different transport pressures (40, 65, 90 Kg/cm2) give the optimized cost of transportation.
Table I a) gives the detailed results for pressure of 90 Kg/cm2 (which gives the minimum cost); only the line corresponding to the number of sections t which minimizes the cost has been printed.
In Table I b) the results are reported for 65 Kg/cm1, which is the pressure currently utilized for natural gas.
The influence of eventual initial compression is illustrated in Figure 4. It is clear that this initial compression becomes, specially over short distances, an important factor in the total cost. This may influence the choice of pressure in the pipe; in a practical calculation, the utilization pressure needed, at: the end of the pipeline should also be considered.1
Influence of pressure P-j is illustrated in Table-Ill; for the three gases (without taking account of
initial compression) the optimized price is decreasing with pressure in the duct.
We must underline that all the evaluations are based on simplified assumptions.
4.2 Comparisons of Costs for Methane and Hydrogen
The widely diverse physical characteristics of the two gases, methane and hydrogen, give rise to different consequences.
First of all, the lower heating value in the case of hydrogen gives the result that, according to the thermal energy transported, much higher volumes of gas are needed.
But other factors, such as the much lower specific gravity, are involved, and as a consequence, we have a nearly compensating (increase of ' the flow est-pacity. One less favourable aspect, is the pumping energy for transmission^ in> view, of ι the greater volumes to be handtedj
- 9
Indicative data for comparison of transport costs are given in Table IV referring to a pressure P̂ in the pipe of 90 Kg/cm2.
We may consider for hydrogen calorie an increase of costs of transport varying from 30% to 50% when compared to natural gas. The ratio of costs increases with distance and diminishes (slowly) with flow.
It appears also from Table IV that the optimum distance between intermediate compression stations is higher for hydrogen than for methane.
Similar results were also obtained for other working pressures. Nevertheless it should be emphasized that the total costs vary very slowly with the number of sections. For instance one can see from Table II that for methane (2GCal/sec and 2000 Km) varying t from 9 to 15 (minimum) (distance from 220 Km to 133 Km) changes the price by only .6%.
The ratio of investment costs in costructing a gas pipeline is also about 45% to 60% higher for hydrogen, due to the larger diameter of the pipe used.
4.3 Oxygen
It might be interesting to see if it is worthwile to transport oxygen from the production plant to a utilization plant. One of the uses could be to substi
tute air for the combustion of hydrogen, thus increasing the efficiency because the gross heat of combustion (3100 KCal/m3) can be considered.
So starting with a production price of hydrogen of 12 mills/m3 and assuming an increased efficiency for combustion in pure oxygen of 20%, a first estimation shows that for transporting 4.106 Nm3/hr of hydrogen the breakeven distance is about 1000 Km. This distance will of course be longer if hydrogen prices increase.
References 1) 7th Intersociety Energy Conversion Engineering Con
ference, San Diego California, September 26-29, 1Θ72. Conference Proceedings, 14 papers presented at the two sessions on Hydrogen Energy Systems.
2) D.P. GREGORY The Hydrogen Economy. Scientific American, January 1973, p. 13.
3) C. MARCHETTI Hydrogen end Energy Chemical Economy and Engineering Review, January 1973, p.7.
4) W.E. WINSCHE, K.C. HOFFMAN, F.J. SALZANO Hydrogen: its future role in the netion's Energy Economy. Science, June 1973, p. 1326.
5) C. ISTING Pipelines now play Important role in petrochemical transport. World Petroleum, April 1970, p. 38; May 1970, p. 36.
- 10 -
CAPTION TO TABLES I AND II
Column .} 3
4
:} 9
10
11
12
13
14 15 16 J
" ) 18 J
Flow in m3/sec
Flow In GCal/sec
Total length in Km
Number o f section
Compression ratio
Diameter of tube in m
Absorbed power for transport (thousand of HP)
Absorbed power for Initial compression (thousand of HP)
Cost of installation tubes stations
total
in 109 Lit
Partial costs in % of total costs for
- depreciation of tubes
- transport compression: degradation of stations + energy (column 15 is included)
- initial compression
- energy for intermediate compression stations
- energy for initial compression
Total costs 'in 1(Γ3 Lit/m3 mLIT
in 1CT6 Lit/KCal pLIT
8υ » Μ Τ ' T V n i S T . NR
κκ s: ητ « M
M A B S . P O H F P I K H P » cnsT ( T N B l u m s ) ρ » » τ ι » ι r o s T s « I N P F P TPSP ΙΝ.Γ. TUPFS STAT. T.*S. Τ. Τ.Γ. ».Γ. T.F.
58. 58. 88. 58.
116. lift, lift. IIA. 73?. 73?. ?33. 73?.
!*<-. »4o. 3*9. ■»49. 465. 4*8. 465. 465.
0. "0
o.*o 0.50 0.50 1.00 1.00 1.00 '.00 7.00 '.00 '.00 7.00 ■».oo '.00 3.00 3.00 *-00 4.00 4.00 4.00
?UA1TTTY . 8 . Γ,Γ·1
1 9 ? . 1 9 ? . 1 9 ? . 1 9 ? . 3 8 5 . 3 8 5 . 3 8 5 . 3 8 5 . 7 6 9 . 7 6 9 . 7 6 9 . 7 6 9 .
1 1 5 4 . 1 J 5 4 . 1 1 5 4 . 1 1 5 4 . 1 5 3 8 . 1 5 3 8 . 1 5 3 8 . 1 5 3 8 .
0 . 5 0 0 . 5 0 0 . 5 0 0 . 5 0 1 . 0 0 ' . 0 0 1 . 0 0 1 . 0 0 ? . 0 0 ' . 0 0 7 . 0 0 ? . 0 0 3 . 0 0 3 . 0 0 » . 0 0 » . 0 0 4 . 0 0 4 . 0 0 4 . 0 0 4 . 0 0
5 0 0 . 1 0 0 0 . 1 5 0 0 . 7 0 0 0 .
5 0 0 . 1 0 0 0 . 1 5 0 0 . ? 0 0 0 .
5 0 0 . 1 0 0 0 . 1 5 0 0 . 7 0 0 0 .
5 0 0 . 1 0 0 0 . 1 5 0 0 . 7 0 0 0 .
5 0 0 . 1 0 0 0 . 1 5 0 0 . 7 0 0 0 .
m ST. KM
5 0 0 . 1 0 0 0 . 1 5 0 0 . 7 0 0 0 .
5 0 0 . 1 0 0 0 . 1 5 0 0 . 7 0 0 0 .
5 0 0 . 1 0 0 0 . 1 5 0 0 . 7 0 0 0 .
5 0 0 . 1 0 0 0 . 1 5 0 0 . 7 0 0 0 .
8 0 0 . 1 0 0 0 . 1 5 0 0 . 7 0 0 0 .
? 5 8
1? ? 5 Ρ
13 ? 6
1 0 1 5
? 5
n 1 6 7 5
11 1ft
NR ST
1 ? 4
8 1 ? ? 8 1 ? ? 7
i ? ? 1 1 ? ?
1 . 8 7 0 1 . 4 9 5 1 . 4 3 8 1 . 3 81 1 . 6 8 9 1 . 4 0 7 1 . 3 Í 9 1 . 7 8 8 1 . 5 7 0 1 . 7 7 4 1 . 7 3 4 l . ? 0 * 1 . 5 1 0 1 . 7 9 8 1 . 1 88 1 . 1 6 9 1 . 4 7 1 1 . 7 74 1 . 1 7 3 1 . 1 5 6
en
1 . 5 0 0 1 . 6 5 ? 1 . 3 8 7 1 . ? 3 5 1 . 5 0 0 1 . 5 4 1 1 . T 7 0 1 . 1 9 ? 1 . 5 0 0 1 . 4 4 7 1 . 6 4 0 1 . 1 8 0 1 . 5 0 0 1 . 5 0 0 1 . 5 7 4 1 . 7 3 7 1 . 5 0 0
ϊ:Λ 1 . 6 8 3
0 . 4 5 ? 0 . 4Ç? 0 . 4 5 3 0 . 4 5 0 0 . 5 9 5 0 . 6 0 0 0 . 5 9 6 0 . 5 9 5 0 . 7 8 4 0 . 7 8 9 0 . 7 8 9 0 . 7 8 7 0 . 9 7 7 0 . 9 4 0 0 . 9 3 1 0 . 9 3 3 1 . 0 3 6 1 . 0 5 8 1 . 0 5 0 1 . 0 4 »
OTAN «1
0 . 5 9 1 0 . 5 7 7 0 . 5 7 7 0 . 5 6 8 0 . 7 6 7 0 . 7 6 ! 0 . 7 9 6 0 . 7 5 8 0 . 9 9 4 1 . 0 0 6 1 . 0 4 8 1 . 0 1 7 1 . 1 5 8 1 . 3 1 8 1 . 2 3 3 1 . 7 7 3 1 . 7 9 0 1 . 4 6 9 1 . 3 8 3 1 . 4 7 7
METHANE 6 .
1 5 . 7 4 . 3 3 . 1 0 . ? 5 . 4 1 . 5 6 . 1 7 . 4 5 . 6 9 . 9 5 .
2 3 · 8 8 . 9 5 .
1 ? 8 .
??: 1 1 6 . 1 5 8 .
0 . 3 . 9 . 3 . 3 . 3 . 3 . 3 . 3 . 3 . 0 . 3 . 0 . 0 . 3 . 0 .
| : 3 . 9 .
H: ' 1 .
1 ? 0 . 4 7 .
ï ? . 1 4 1 . 1 3 8 .
7 3 . 1 4 7 . ? ? ! . ? 9 4 .
9 5 . 1 9 5 . ? 9 8 . » 3 4 . 1 1 4 . ? 3 6 . » 4 9 . 4 6 5 .
1 .
». 5 . 7 . ? . 6 .
«. 1 » .
4 . 1 0 . 1 6 . ? 1 .
5 .
'?· λ ί . 7 9 .
6 . 1 6 .
» :
» ? . 6 4 . 9 7 .
1 ? 8 . 4 0 .
1 0 1 . 1 5 1 . 7 0 0 .
7 7 . 1 5 7 . ' 3 7 . 3 1 3 . ; » : in-. ? $ ? : 3 7 5 . 8 0 1 .
8 5 . 8 1 . 8 0 . 7 8 . 8 3 . 8 1 . 7 9 . 7 8 . 8 4 .
Λ 7 8 . 8 4 . 8 1 . 7 9 . 7 8 . 8 4 . 8 1 . 7 9 . 7 8 .
1 5 . i o . 7 0 . 7 ? . 1 5 . 1 9 . ? 1 . ? ? . 1 6 .
??: ? ? . 1 6 . 1 9 . 7 1 . ' ? . 1 6 . 1 9 . ? 1 . ? ? .
0 . 0 . 0 . 0 .
8: 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 .
fc 0 . 0 .
8 . o .
1 0 . ' 0 .
9 . 1 0 . 1 1 . 1 1 .
9 . 1 1 . 1 ? . 1 ? . ι α. i l . ι ? . 1 ? .
;?: 1 ? . ι ? .
: F N T S I ' . = .
o. o. o. o.
o. o. o. o. o. o. o. o. o. 0 . 0 . 0 . 0 . 0 .
ΤΠΤ. CPST " I t Τ ««ILT Τ ft.Η. / Κ Γ · 1
» B S . PPHFB.IKHP» COST t TN B I L L T 3 N S I P » » T T A l COSTS J I M PFP CFNTSI T " S P T N . C . TJBFS S T A T . T . * S . T . T . f . f . : . T . e . f . e .
HYDROGEN 0 .
1 9 . 3 6 . 5 4 .
0 . 3 » . 4 4 . 9 0 .
0 . 5 6 . T S .
1 4 6 . 0 . 0 .
1 0 4 . 1 7 8 .
0 . 0 .
1 3 0 . 1 6 1 .
) . 3 . 9 . 3 . 9 . 9 . 3 . 3 .
9 . 0 . 0 . 3 . 0 . 9 . 9 . 9 . 9 . 9 .
4 6 . 3 9 .
ili: 7 0 .
1 » 9 . ? ? 5 . ? 7 6 . 1 0 7 . ? 1 3 . » 4 9 . 4 4 ? . 1 3 6 . 3 8 5 . 4 5 ? . 6 8 4 . 1 6 ? . » 9 8 . 5 4 3 , 7 6 1 .
0 . 4 . 8 .
1 ? .
4 6 . 9 4 .
1 4 ? . 1 8 7 .
?: il?: 1 0 . 7 0 .
ï?: 1 7 . 3 ? .
0 .
??: ? 9 .
1 0 0 . 0 . 8 5 . 1 5 . β ? . 1 8 . 7 9 . ? 1 .
1 0 0 . 0 . 8 5 . 1 5 .
3 f .
7 3 5 . 7 9 7 . 1 0 7 . ?fO. 3 6 6 . 4 7 3 .
\l%: 4 7 5 . 6 6 3 . 1 6 ? . 3 9 8 . 5 7 ? . 7 β β .
8 7 . 7 9 .
Ίΐ: 3 f t . 7 9 .
Ì88: 8 5 . 8 7 .
1 0 0 .
'k 8 6 .
'??: ι?: 1 4 . ? ! .
8: 1 3 . 1 3 .
0 .
ι?: 1 4 .
? » 4 1 . 541 3 . • 3 3 5 .
1 1 4 3 4 . ' 0 5 ° . 4 * 3 » . 5 5 S 4 . 3 9 1 8 . »S I 5 . » 4 * 9 . 5 > 3 9 . T 0 » 3 . I » 3 3 . » 0 9 6 . M 4 T . 4 1 7 1 . 1 ? T » . » T 3 0 . 4 1 4 9 . 8 3 3 9 .
»οτ. 65». 9 9 5 .
1 » » 5 . 7 * 9 . 5 1 3 . 7 7 5 .
1 0 » 9 . 1 3 9 . 4 3 1 . 6 0 9 . B I T .
3 5 0 . 5 3 1 . 7 1 ? . 1 4 8 . 3 1 7 . 4 3 ? . 6 4 6 .
T O T . COST ni l τ NULI τ
/KCl /e.«.
0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 .
8: 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 .
0 . 9 .
îfc 0 . 9 . β .
1 ? .
.fc 9 .
1 ? . 0 . 0 . 9 . β . 0 . 0 .
1 0 . 9 .
0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 .
8: 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 .
1 3 4 9 . » 1 4 ? . » 4 9 ? .
4 » · ' . 7 9 5 .
1 · 3 8 . 7 9 1 9 . 3 9 * 5 .
5 0 ? . 1 * 4 8 . > > 9 4 . » 1 4 0 .
5 1 ? . 1 »ft* . 1 » » 3 . ? Τ 5 ? .
4 3 Τ . Μ » * . 1 3 3 9 . » » » 0 .
»ι
4 3 * . 9 3 » .
1 4 7 3 . 1 0 ( 3 .
335 . T I S .
1 1 » 3 . 131 Τ .
? * ? . 5 4 5 . 3 1 ? .
1 7 3 3 . 1 9 Τ . 4 * 5 . Τ 5 Τ .
1 0 5 3 . 1 7 4 . 4 3 » . 3 9 » . 9 5 8 .
0UA1T1TY
C.8. G:»L
?88: 500. 5 0 0 .
1 0 0 0 . 1 0 0 0 . 1 0 0 0 . 1 0 0 0 . 1 5 0 0 .
iflfc 1500.
0 . 0 0 . 0 0 . 0 0 . 0 0 . 0 0 . 0 0 . 0 0 . 0 0 . 0 0 . 0 0 . 0 0 . 0
n i S T . NP κ3 sr
lOõífc T 1 5 0 0 . 1 4 2 0 0 0 . 7 0
5 0 0 . 1 1 0 0 0 . 5 1 5 0 0 . 1 4 7 0 0 0 . ??
5 0 0 . 1 ïgoo. ? 1500. 14 7000. 73
8 0
,:?'8i 1 . 1 4 6 1 . 1 3 4
î:?4°? 1 . 1 1 9 ! . 0 9 9
hlîî 1 . 1 0 3 1 . 0 8 4
0 1 »Ν M
1 . 7 7 6 ! . ? ! ? 1 . ? ? 7 1 . 7 7 6 1 . 8 1 1
1:81 1 . A 3 9 7 . 1 0 9 7 . 0 4 9 1 . 9 5 0 1 . 9 4 6
Î S f i rowFJiKHPi çnsT U N e i u t y m P A R T I A L C O S T S t i Ν P F P J F N T S ) TBSP T N . C . TUBES S T A T . T . » S . T . T . C . f . : . T . e . » . F .
OXYGEN 3 T . 9 7 .
1 5 3 . » 0 * .
. , ? : » 5 1 . 3 4 1 .
.4?: 3 3 5 . » 5 3 .
i: 0 . 3 . 9 . 9 . 0 . 9 . 9 . 0 . 3 . 9 .
1 4 9 . 3 3 1 . 4 4 8 . 39 T . ? T 9 . 4 * 6 . T 1 5 . 9 5 1 . » 5 6 . 6 T 9 . 0 4 1 .
1 7 5 9 .
3 . ? ? . 3 4 . 4 * .
»2: 3 « . 7 7 .
? ? : 7 5 .
1 0 ? .
m: 483, 644 . J79. 3 ? 0 . 7 7 1 .
1 0 7 7 , 3 5 6 . 7 1 1 .
1 0 1 6 , 1 3 3 ? .
8 4 . 8 0 . 7 8 . 7 8 .
78 . 78 .
100. • f t . 78. 78 .
Ik 8: !?: 8: 7 ? . 0 . ' 3 . 0 7 ? . 0 . 1 3 . 0
ift 8: i£ 8 ? ? . 0 . 1 3 . 0 ? ? . 0 . 1 3 . 0 . 0 . 0 . 0 . 0 1 4 . 0 . 9 . 0 ? ? . 0 . 1 3 . 0 ? ? . 0 . ' 3 . 0
TOT. COST NIT Τ NUI I T ft.Ν. / K f » t
I SVI. 3»85.
49T6. 444?. I»10. »61 6. 394ft. 5193. »0»o. >>TB. »4T0. 4436.
TABLE la
QUANTI TV C . N .
5 8 . 58 . 5 8 . 5 8 .
116. 116. 116 . 116. 233 . 2 3 3 . 233. 233 . 349 . 3 4 9 . 3 4 9 . 3 4 9 . 4 6 5 . 465 . 465 . 465 .
GCAL
0 . 5 0 C 5 0 0 . 5 0 0 . 5 0 1 .00 1.00 1.00 1 .00 2 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 3 . 0 0 3 .00 3 .00 3 . 0 0 4 . 0 0 4 . 0 0 4 . 0 0 4 . 0 0
QUANTITY C . « .
19?. 192. 192 . 192 . 3 8 5 . 385 . 385 . 3 8 5 . 769. 769 . 769 . 769.
1154. 1154 . 1154. 1154 . 1538. 1538. 15 38. 1538.
GCAl
C.SJ 0 . 5 0 C 50 0 . 5 0 1 .00 1 .00 l .OC 1 .00 ?.oo 7 . 0 0 2 . 0 0 2 . 0 0 3 . 0 0 3 . 0 0 3 . 0 0 3 .00 4 . 0 0 4 . 0 0 4 . 0 0 4 . 0 0
QUANTITY C . N .
500 . 5 0 0 . 5 0 0 . 5 0 0 .
loco. loco. 1 0 0 0 . 1 0 0 0 . 1500 . 1 5 0 0 . 15C3. 1500 .
GCAL
0 . 0 C O 0 . 0 0 . 0
co co co 0 . 0 O.C 0 . 0
co 0 . 0
01 ST. KN
500. 1000. 1500. 2000 .
500. 1000. 1500. 2000.
500. 1000. 1500. 2000.
500 . 1000. 1500. 2 000.
500 . 1000. 1500. 2000 .
IT ST. KN
■»00. 1000. 1500. 2 000.
500. 1009. 1500. 2003 .
500 . 1003. ÌSOO. 2000 .
500. 1000. 1503. 2 000 .
500 . 1000. 1500. 2 000.
OTST. KN
500 . 1000. 1500. 2000 .
500 . 1000. 1500. 2000 .
500 . 1000. 1500. 2000 .
NP SC
2 5 9
12 2 6
IO 14 2 6
I I 16
2 b
12 17
2 6
1? 17
N" SC
7 5 a 1 2 4 8 1 2 2 8 1 1 2 7 1 1 2 2
NP SC
2 3
15 22
2 7
16 23
1 2
16 25
RO
1 .852 1 .510 1 .401 1 .392 1 .709 1 .345 1 .295 1.2 76 1 .587 1 .282 1 .219 1 .197 1 .525 1 .251 1 .178 1.164 1 .485 1 .231 1 .163 1 .151
p i
ι . soo 1.6 89 1 .315 1 .249 1 .500 1.572 1 .333 1.204 1 .500 1 .473 1 .677 1 .166 1 .500 1 .500 1 .607 1 .170 1 .500 1 .500 1 .561 1 .721
pn
1 .525 1 .185 1 .143 1 .128 1 .433 1 .174 1 .109 1 .099 1 .500 1 .716 1 .096 1.081
OTAN N
0 .514 0 .515 0 . 5 1 0 0 . 5 1 2 0 . 6 7 6 0 . 6 7 3 0 . 6 7 3 0 .673 0 . 8 9 1 0 .895 0 .892 0 . 8 9 0 1 .048 1 . 0 5 8 1.052 1.052 1 .177 1 .192 1 .187 1 .187
01 AN N
0 . 6 6 7 0 . 6 4 7 0 .638 0 .635 0 .864 0 . 8 5 3 0 . 8 5 7 0 . 3 4 7 1 .121 1 .127 1 .176 1 .131 1 .305 1 .486 1 .383 1 .346 1 .454 1 .656 1.551 1 .602
OTAN N
1 .382 1 .379 1.375 1 .374 1 .828 1 .850 1 .839 1 .839 2 . 3 8 7 2 . 3 1 1 2 . 1 8 3 2 . 1 8 1
A8S. TPS Ρ
6 . 14 . 2 6 . 3 5 . 1 1 . 2 9 . 4 5 . 6 1 . 1 8 . 4 8 . 7 6 .
1 0 3 . 2 5 . 6 5 .
1 0 3 . 1 3 9 .
3 1 . 8 0 .
1 2 7 . 1 7 1 .
Ans. TPsp
0 . 2 0 . 4 0 . 5 7 .
0 . 3 4 . 6 3 . 9 4 .
0 . 5 8 . 7 9 .
1 5 5 . 0 . 0 .
1 0 8 . 2 0 4 .
0 . 0 .
134 . 1 6 6 .
ABS. TPSP
3 8 . 105 . 163 . 2 2 1 .
6 5 . 1 6 9 . 2 6 9 . 3 6 2 .
0 . 1 5 0 . 3 5 9 . 4 8 6 .
' N . C . COST «TN RTL I I INS» PAOTIAl COSTS (TN PFP CFNTSI
TU8FS s t » ¥ . T . * s . T . T . c . T . : . T . F . f . F .
METHANE
TOT. COST N t i * » M I T T / C . N . /KCAL
3 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 .
3 3 . 6 6 . 9 8 .
1 3 1 . 5 } ·
1 0 1 . 1 5 2 . 2 0 2 .
7 9 . 1 6 0 . 2 3 8 . 3 1 7 . 1 0 3 . 2 0 9 . 3 1 1 . 4 1 4 .
HS: 3 7 7 . 5 0 3 .
1 . 4 . 6 . 8 . 2 . 6 .
10 . 14 . 4 .
}*: 2 3 .
6 . 1 5 . 2 3 . 3 1 .
7 . 18 . 2 9 . 3 9 .
7*0.' 1 0 3 . 1 3 9 .
5 3 . 1C8 . 1 6 2 . 2 1 6 .
8 3 . 1 7 1 . 2 5 5 . 3 4 0 . 1 0 8 . 2 2 4 . 3 3 4 . 4 4 6 . 1 3 1 . 2 7 1 . 4 0 5 . 5 4 1 .
86 . 8 1 . 79 . 79 . 85 . 8C. 7 9 . 7 8 . 85 . 80 . 7 9 . 7 8 . 84. 8C. 7 8 . 7 8 . 84 . 8 0 . 7 8 . 78 .
HYDROGEN
8 : 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 3 . 0 . 0 .
5 0 . 9 5 .
1 3 9 . 1 8 5 .
7 6 . 1 4 8 . 2 2 4 . 2 9 3 . 1 1 5 . 2 3 1 . 3 7 1 . 4 6 5 . 1 4 6 . 3 6 0 . 4 8 1 . 6 1 4 . 1 7 4 . 4 2 8 . 5 7 8 . 8 1 1 .
C . 4 . 9 .
1 3 . 0 . 8 .
1 4 . 2 1 .
0 .
il: 35 . 0 . 0 .
2 4 . 4 6 .
0 . C.
3 0 . 3 7 .
5 0 . 1 0 0 . 1 4 8 . 1 9 7 .
7 6 . 1 5 6 . 2 3 8 . 3 1 4 . 1 1 5 . 2 4 4 . 3 8 9 . 5 0 0 . 1 4 6 . 3 6 0 . 5 0 5 . 6 6 0 . 1 7 4 . 4 2 8 . 6 C 8 . 8 4 9 .
IOC. 86 . 8 1 . 79 .
IOC. 85 . 82 . 79 .
toc 8 4 . 36 . 79.
I O C 100 .
85 . BC.
I O C IOC.
8 5 . 8 7 .
!5: 2 1 . 2 1 . 15. 2 0 . 2 1 . 22. 15. 20 . 2 1 . 22 .
2 C 22. 22. 1 6 . 2 0 . 22. 22.
0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 .
c 0. 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 .
8 . 9.
I C 10.
8 . 1 1 . 1 1 . 1 1 .
9 . 1 1 . 1 2 . 1 2 . 1 0 . 1 2 . 1 2 . 1 2 . 1 0 . 1 2 . 1 2 . 1 3 .
0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 .
Ans. PPWFRÍKMP) COST CTN B l l i r > N S ! ΡΑ4Τ1ΑΙ 1N.C. TUBFS STAT. T . 4 Î . τ .
COSTS Ι τ * PFP CFNTSI T .C . T . C . T . F . T . F .
C. 14. 19 . 2 1 .
0 . 15. 18. 2 1 .
0 . 16. 14. 2 1 .
C.
o. 15. 2 C.
0 . C
1 5 . 1 3 .
O. 0.' η. o. o. o. o. o. o. o. o. o. o. 0 .
o. 0 . 0 .
o. 0 . 0 .
0 . 8.
1 1 . 1 1 .
0. 9 .
I I . 1 2 .
0.^ 1 0 .
9 . 1 2 .
0 . 0 . 9 .
1 2 . 0 . 0 . 9 . 8 .
PPWFR(KHP) COST I TN B i l l I"»NS) PARTIAL COSTS | i | | DFP TN.C. TURFS STAT. T . * S . T . T . C . T . C . T . r .
OXYGEN 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 .
1 6 0 . 3 1 9 . 4 7 7 . 6 3 4 . 2 5 0 . 5 1 ! . 7 5 9 .
1 0 1 2 . 3 8 4 . 7 2 9 . 9 9 9 .
1 3 2 9 .
9 . 2 4 . » 7 . 5 0 . 15 . 3 8 . 6 1 . 8 2 .
0 . »4 . 8 1 .
109 .
1 6 9 . 3 4 3 . 5 1 3 . 6 R 4 . 2 6 5 . 5 4 9 . 8 1 9 .
1 0 9 3 . 3 8 4 . 7 6 3 .
1 0 7 9 . 1 4 3 8 .
84. 79. 78. 78. 83 . 79. 78 . 78 .
100. 87. 78 . 78.
16. 21 . 22. 22. 17. 21 . 2?. 72.
C. 13. 72. 22.
0 . 0 . 0 . 0 . 0 .
o. 0 . 0 . 0 . 0 . 0 . 0 .
1 0 . 1 2 . 1 3 . 1 3 . 1 0 . 1 2 . 1 3 . 1 3 .
0. 8 .
1 3 . 1 3 .
O. 0 . o. 0 . 0 . 0 .
o. 0 . 0 .
o. 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 .
o.
CFNTS1 l . F .
0 .
o. 0 . 0 .
o. 0 . 0 . 0 . 0 . 0 .
o. 0 .
2863. 6072. 9234.
12392. 2233. 4738. 7197. 9650. 1751. 3729. 5661. 7536. 1523. 3252. 4936. 6613. 1330. 2955. 4434. 6007.
333. 706. 1074, 1441. 260, 551. 837, 1122. 204. 434. 658. 882. 177. 378. 574, 769. 160. 344. 521. 699.
TOT. COST NI t T Nl l l lT
tr..^. /KCAi
1126. 7505. 3931. 5257. 853. 1949. 3037. 4163. 647. 1554. 7433. 3313. 550. 1354. ? U 6 . 7904.
4 9 0 . 1 7 0 6 . 1 9 1 7 . 2 6 4 3 .
433. 953. 1500. 2072. 378. 757. 1137. 1631. 249. 598. 936. 1274. 211. 521. 814. 1117. 183. 464. 737. 1016.
T° T . CO«T
NLTT MJI.TT ft.». /KCAI
1647. 3530. 5297. 7089. 1302. 2789. 4222. 5649. 1111. 2439. 3704. 4955.
CS)
ι
TABLE Ib
JUAN TI TY . . M . GCAL
DIST. KM
NR SC
Rn DIAM
M A B S . TRSP
POWFRtKHPl I N . C .
1 1 6 . 1 1 6 . 1 1 6 . 1 1 6 . 1 1 6 . 1 1 6 . 1 J 6 . 1 1 6 . 1 1 6 . 1 1 6 . 1 1 6 . 1 1 6 . 1 1 6 . 1 1 6 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 2 3 3 . 3 4 9 . 3 4 9 . 3 4 9 . 3 4 9 .
1 . 0 0 1 . 0 0 1 . 0 0 1 . 0 0 1 . 0 0 1 . 0 0 1 . 0 0 1 . 0 0 1 . 0 0 1 . 0 0 1 . 0 0 1 . 0 0 1 . 0 0 1 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 ? . 0 0 ? . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 7 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 2 . 0 0 3 . 0 0 3 . 0 0 3 . 0 0 3 . 0 0
1500. 1500. 1500. 2000. 2000. 2000. 2000. 2000. 2000. 2000. 2000. 2000. 2000. 2000. 500. 500. 500. 500.
1000. 1000. 1000. 1000. 1000. 1000. 1000. 1500. 1500. 1500. 1500. 15 00. 1500. 1500. 1500. 1500. 1500. 2000. 2000. 2000. 2000. 2000. 2000. 2000. 2000. 2000. 2000. 2000. 500. 500. 500. 500.
12 13 14 9 10 11 12 13 14 15 16 17 IR 19 1 2 3 4 2 3 4 5 6 7 8 5 6 7 θ 9
i? 12 13 14 9 10 11 12 13 14 15 16
n 19 1 2 3 4
1 . 2 4 5 1 . 2 2 6 1 . 2 1 0 1 . 4 2 9 1 . 3 8 6 1 . 3 5 1
Í . 3 2 2
1 . 2 5 8 1 . 2 4 1 1 . 2 2 7 1 . 2 1 5 1 . 2 0 3
\:W 1 . 3 3 1 1 . 2 3 2 2 . 0 6 7 1 . 6 2 3 1 . 4 4 3 1 . 3 4 5 1 . 2 8 2 1 . 2 3 9 1 . 2 0 7 1 . 5 0 0 1 . 4 1 ? 1 . 3 5 0 1 . 3 0 4 1 . 2 6 9 1 . 2 4 2 1 . 2 1 9 1 . 2 0 0 1 . 1 8 5 1 . 1 7 1 1 . 3 5 3 1 . 3 1 7 1 . 2 88 1 . 2 6 3
Í . 2 4 3
all 1 . 1 9 7
\:\K 1 . 1 6 6 Í . 5 0 0 1 1 . 5 2 5 1 1 . 2 9 5 1 . 2 0 6
0 . 6 6 6 0 . 6 6 3 0 . 6 6 1 0 . 6 9 3 0 .688 0 .683 0 .679 0 .676 0 .673 0 . 6 7 0 0 .668 0 .665 0 . 6 6 4 0 . 6 6 2
0 . 8 7 0 0 . 9 7 0 0 .935 0 .916 0 . 9 0 4 0 .895 0 . 8 8 9 0 . 8 8 4 0 .936 0 .923 0 . 9 1 4 0 .906 0 .901 0 .896 0 . 8 9 2 0 .888 0 .885 0 .883 0 .919 0 .913 0 .908 0 .903 0 .899 0 . 8 9 6 0 .893 0 . 8 9 0 0 . 8 8 8 0 . 8 8 6 0 . 8 8 4
. 1 9 9 _.Ü48 1 .036 1 .030
4 6 . 4 7 . 4 7 . 5 6 . 5 7 . 5 8 . 5 9 .
I?: 6 2 . 6 2 . 6 3 . 6 3 . 6 4 .
O. 1 8 . 2 2 . 2 4 . 3 0 . 3 8 . 4 3 . 4 6 . 4 8 . 4 9 . 5 0 . 6 4 . 6 7 . 7 0 . 7 2 . 7 3 . 7 5 . 7 6 . 7 7 . 7 8 . 7 8 . 9 4 . 9 6 . 9 7 . 9 9 .
1 0 0 . 1 0 1 . 1 0 2 . 1 0 3 . 1 0 4 . 1 0 5 . 1 0 5 .
0 . 2 5 . 3 0 . 3 2 .
0 . 0 . 0 . 0 . 0 . o. o. 0 . 0 .
o. 0 . 0 . 0 . 0 . 0 . o. 0 . o. 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 . 0 .
COST TUBFS
1 4 9 . 1 4 8 . 1 4 8 . 2 1 2 .
2 0 7 . 2 0 5 . 2 0 4 . 2 0 ? . 2 0 1 . 2 0 0 . 1 9 9 . 1 9 8 . 1 9 7 . 1 0 0 .
7 9 . 7 7 . 7 6 .
1 8 ? . 1 7 1 . 1 6 6 . 1 6 ? . 1 6 0 . 1 5 8 . 1 5 7 . ? 5 f i . ? 5 ? . 2 4 8 . ? 4 5 . 2 4 2 . ? 4 0 . ??P. 2 3 7 . ? 3 6 . ? » 5 . 3 3 4 . 3 » 0 . 3 ? 7 . 3 2 4 . 3 2 ? . 3 2 0 . 3 1 9 . 3 1 7 . 3 1 6 . 3 1 5 . 3 1 4 . 1?P . 1 0 3 . 101 . 1 0 0 .
U N BILLII TAT.
10. 11. 11.
lì: 13. 13. 14. 14. 14. 14. 14. 14. 14. 0. 4. 5. 5. 7. 9.
10. 10. 11. 11. 11. 14. 15. 16. 16. 17. 17. 17. 17. 17. IP. ?1. ??. ??. ??. ?3. ?3. ?3. ?3. ?3. ?4. 24. 0. 6. 7. 7.
DNSl T.*S.
160. 159. 158. 2?5. ??3. 2?1. 219. ?17. ?16. 215. 214. 213. 212. ?1?. 100. 83. 8?. 8?.
188. 180. 176. 173. 171 . 169. 168. ?7?. 267. 264. ?61. 259. ?57. ?55. ?54. ?53. ?5?. 3«5. 35?. »49. '47. »45. 3*3. »4?. 3*0. 339. »38. »»7. 1?P. 10P. 1 08. 107.
PARTIAL T.
77. 77. 76. 81. 81. 80. 79. 79. 78. 78. 77. 77. 76. 76.
100. 85. 81. 79. 89. 85. 83. 81. 80. 79. 78. 83. 8?. 81. 80. 80. 79. 79. 78. 7P. 77. PI. 81. 8 0. PO. 79. 79. 78. 78. 78. 77. 77.
100. 84. 81. 79.
COSTS T.C. I
?3. ?3. ?4. 19. 19. ?0. 21. ?1. 2?. 2?. ?3. ?3. ?4. ?4. 0.
15. 19. ?1. 11. 15. 17. 19. ?0. 21. ??. 17. IP. 19. ?0. ?0. 21.
???:
??. ?3. 19. io. ?0. ?0.
*!· 2i· 22. 2?. 22. 23. 23. 0.
16. 19. 21.
(IN .C.
0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0.
PFR T.F.
11. 11. 1?. 10. 10. 11. 11. 11. 11.
H: 11. 1?. 1?. 0. 9.
11. 1?. 7. 9.
10. 11. 11. 1?. 1?. 10. 10. 11. 11. 11. 1?. 12. 1?. 12. 12.
li: 11. 11.
li: 12. 12. 12. 12. 12. 0.
10.
If. 12.
CFNTS) I.F.
0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0. 0.
τπτ. cnsT ML T Τ /Γ.M.
7?06. 7?ι 6. 7??fl. 0730. 9697. 0675. 9661. 0653. 0650. 965?. 0657. 9664. 9674. 06Β6. 1868. 1751 . 1785. 183Ρ. 38?3. »768. »74». 373?. 37?ο. »731. »7»6. 575ο. 5710. 560». 5677. 5667. 566?. 5661. 566?. 5665. 5669. 7658. 7634. 7616. 7604. 7505. 7590. 7587. 7586. 7587. 7590. 7594. 158β. 15?3. 1556. 1576.
MULI Τ /KCAL
838 839 841
1131 1128 1175 1J23 11?? 112? 112? 11?3 1174 11?5 1126 ?17 ?04 ?08 ?10 445 438 435 434 434 434 434 670 66 5 66? 660 659 658 658 658 659 659 891 888 886 884 88» 883 83? 88? 8R? 8Ρ3 8Ρ» 185 177 1R1 18»
TABLE II
TABLE III Exemple of influence of pressure of transport
Flow
(GCal/sec)
2
2
2
2
2
2
(C.M./sec)
1000
1000
1000
Length
(km)
1000
1000
1000
1000
1000
1000
1000
1000
1000
Pressure
(ke/cm2)
40
65
90
40
65
90
40
65
90
G «
H,
H,
H2
CH4
CH4
CH»
0a
0 ,
0ï
! ' Cost
(Lit/MCal)
.678
.598
.565
.499
.434
.401
(Lit/C.M.)
3.171
2789
Z616
Mm»*ii of
sections
2
2
2
7
6
6
9
7
5
I
Fiow of energy
(Gcal/sec)
1
2
3
4
1
2
3
4
.5
TABLE IV Comparison of
Total length
(km)
1000
1000
1000
1000
2000
2000
2000
2000
500
Number of
sections
H,
2
2
1
1
8
7
2
2
1
CH«
5
6
5
5
13
15
16
16
2
costs foi
Optimal distance
between stations
H ,
500
500
1000
1000
250
285
1000
1000
500
CH«
200
167
200
200
154
133
125
125
250
hydrogen and
Wieimuin m m
(Lit/Meal)
Ha
.715
.565
.485
.432
1.517
1.208
1.058
.958
.403
CH*
.510
.401
.350
.317
1.039
.817
.712
.646
.307
methane.
H2/CH4
■ asemoit
cotti
1.40
1.41
1.38
1.36
1.46
1.48
1.48
1.48
1.31
H2/CH4
capita·
coati
1.46
1.46
1.61
1.58
1.48
1.51
1.59
1.59
1.43
maton
ratio
Ha
1.541
1.447
1.500
1.500
1.192
1.180
1.737
1.683
1.500
CH«
1.407
1.274
1.298
1.274
1.288
1.204
1.169
1.156
1.829
CO
í? CD O </> ty» (Λ r *
CD " * a O
^ I <0"
°S ο κ
o -π
Q .
ro 3
O
S C/ï
cu 3 Q.
et 3 O CD
CD CD
CD ι CD 3
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