Pressure Base 14.65 psia
Mole %
Hydrogen 0.000
Helium 0.030
Nitrogen 0.320
Oxygen 0.000
Hydrogen Sulfide 0.000 Carbon Dioxide 2.020
Methane 83.020
Ethane 7.450
Propane 4.390
I-Butane 0.830
N-Butane 1.080
I-Pentane 0.310 N-Pentane 0.250
C6+ 0.300
Total 100.000
Z = 0.99682 = 1 + (PressureBase * Sum of (xi * xj * Bij) / 1000)
First compound Second compound
Second Virial Coefficient
Bij, 103 psia–1 at 60 °F xi * xj * Bij
Hydrogen Hydrogen 0.04100 0.000000000000000 Hydrogen Helium 0.04600 0.000000000000000 Hydrogen Nitrogen 0.03500 0.000000000000000 Hydrogen Oxygen 0.03200 0.000000000000000 Hydrogen Hydrogen Sulfide 0.00200 0.000000000000000 Hydrogen Carbon Dioxide –0.06600 0.000000000000000 Hydrogen Methane 0.02200 0.000000000000000 Hydrogen Ethane 0.03200 0.000000000000000 Hydrogen Propane 0.01600 0.000000000000000 Hydrogen I-Butane 0.00000 0.000000000000000 Hydrogen N-Butane 0.02600 0.000000000000000 Hydrogen I-Pentane 0.06900 0.000000000000000 Hydrogen N-Pentane –0.01200 0.000000000000000
Hydrogen C6+ (n-C6) –0.01000 0.000000000000000 Helium Helium 0.03400 0.000000003060000
Helium Nitrogen 0.06000 0.000000115200000 Helium Oxygen 0.06300 0.000000000000000 Helium Hydrogen Sulfide 0.04300 0.000000000000000 Helium Carbon Dioxide 0.05100 0.000000618120000 Helium Methane 0.07000 0.000034868400000 Helium Ethane 0.05700 0.000002547900000 Helium Propane 0.09800 0.000002581320000 Helium I-Butane 0.07500 0.000000373500000 Helium N-Butane 0.12800 0.000000829440000 Helium I-Pentane 0.07500 0.000000139500000 Helium N-Pentane 0.07500 0.000000112500000
Helium C6+ (n-C6) 0.08000 0.000000144000000 Nitrogen Nitrogen –0.01900 –0.000000194560000
Nitrogen Oxygen –0.03700 0.000000000000000 Nitrogen Hydrogen Sulfide –0.13500 0.000000000000000 Nitrogen Carbon Dioxide –0.14400 –0.000018616320000
Nitrogen Methane –0.06000 –0.000318796800000 Nitrogen Ethane –0.15200 –0.000072473600000 Nitrogen Propane –0.23700 –0.000066587520000 Nitrogen I-Butane –0.21300 –0.000011314560000 Nitrogen N-Butane –0.25000 –0.000017280000000 Nitrogen I-Pentane –0.32600 –0.000006467840000
Nitrogen N-Pentane –0.28000 –0.000004480000000
Nitrogen C6+ (n-C6) –0.37300 –0.000007161600000
Copyright American Petroleum Institute Provided by IHS under license with API
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Oxygen Oxygen –0.05300 0.000000000000000 Oxygen Hydrogen Sulfide –0.16100 0.000000000000000 Oxygen Carbon Dioxide –0.11800 0.000000000000000 Oxygen Methane –0.05200 0.000000000000000 Oxygen Ethane –0.12400 0.000000000000000 Oxygen Propane –0.20100 0.000000000000000 Oxygen I-Butane –0.27000 0.000000000000000 Oxygen N-Butane –0.29300 0.000000000000000 Oxygen I-Pentane –0.39100 0.000000000000000 Oxygen N-Pentane –0.47400 0.000000000000000
Oxygen C6+ (n-C6) –0.50800 0.000000000000000 Hydrogen Sulfide Hydrogen Sulfide –0.64100 0.000000000000000 Hydrogen Sulfide Carbon Dioxide –0.41600 0.000000000000000
Hydrogen Sulfide Methane –0.24100 0.000000000000000 Hydrogen Sulfide Ethane –0.44500 0.000000000000000 Hydrogen Sulfide Propane –0.84200 0.000000000000000 Hydrogen Sulfide I-Butane –1.11200 0.000000000000000 Hydrogen Sulfide N-Butane –1.15200 0.000000000000000 Hydrogen Sulfide I-Pentane –1.43600 0.000000000000000 Hydrogen Sulfide N-Pentane –1.47600 0.000000000000000
Hydrogen Sulfide C6+ (n-C6) –1.87600 0.000000000000000 Carbon Dioxide Carbon Dioxide –0.38800 –0.000158319520000
Carbon Dioxide Methane –0.18100 –0.006070754480000 Carbon Dioxide Ethane –0.38500 –0.001158773000000 Carbon Dioxide Propane –0.61800 –0.001096060080000 Carbon Dioxide I-Butane –0.81900 –0.000274627080000 Carbon Dioxide N-Butane –0.86200 –0.000376107840000 Carbon Dioxide I-Pentane –1.06300 –0.000133130120000 Carbon Dioxide N-Pentane –1.09100 –0.000110191000000
Carbon Dioxide C6+ (n-C6) –1.37900 –0.000167134800000 Methane Methane –0.13500 –0.093046325400000
Methane Ethane –0.28100 –0.034759643800000 Methane Propane –0.42500 –0.030978913000000 Methane I-Butane –0.45700 –0.006298063240000 Methane N-Butane –0.56000 –0.010042099200000 Methane I-Pentane –0.63200 –0.003253055680000
Methane N-Pentane –0.67500 –0.002801925000000
Methane C6+ (n-C6) –0.79300 –0.003950091600000 Ethane Ethane –0.56900 –0.003158092250000
Ethane Propane –0.83300 –0.005448736300000 Ethane I-Butane –1.00500 –0.001242883500000 Ethane N-Butane –1.10600 –0.001779775200000 Ethane I-Pentane –1.29300 –0.000597236700000
Ethane N-Pentane –1.37900 –0.000513677500000
Ethane C6+ (n-C6) –1.65200 –0.000738444000000 Propane Propane –1.18300 –0.002279889430000
Propane I-Butane –1.52200 –0.001109142280000 Propane N-Butane –1.66600 –0.001579767840000 Propane I-Pentane –1.95300 –0.000531567540000 Propane N-Pentane –2.06800 –0.000453926000000
Propane C6+ (n-C6) –2.54200 –0.000669562800000 I-Butane I-Butane –2.09700 –0.000144462330000
I-Butane N-Butane –1.98200 –0.000355332960000 I-Butane I-Pentane –2.55600 –0.000131531760000
I-Butane N-Pentane –2.61400 –0.000108481000000
I-Butane C6+ (n-C6) –3.31700 –0.000165186600000 N-Butane N-Butane –2.28900 –0.000266988960000
N-Butane I-Pentane –2.67100 –0.000178850160000 N-Butane N-Pentane –2.91500 –0.000157410000000
N-Butane C6+ (n-C6) –3.40400 –0.000220579200000 I-Pentane I-Pentane –3.37500 –0.000032433750000
I-Pentane N-Pentane –3.50400 –0.000054312000000
I-Pentane C--`,,```,,,,````-`-`,,`,,`,`,,`---6+ (n-C6) –4.45200 –0.000082807200000
N-Pentane N-Pentane –3.97800 –0.000024862500000
N-Pentane C6+ (n-C6) –4.73900 –0.000071085000000 C6+ (n-C6) C6+ (n-C6) –6.43400 –0.000057906000000 Total Bij –0.217311185460000 NOTES
C6+ virial coefficient values are for n-C6.
Virial coefficient values are from Orifice Metering of Natural Gas AGA Report No. 3, 1985.
Copyright American Petroleum Institute Provided by IHS under license with API
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33
Water Content Example Calculations
The examples used in this annex are merely examples for illustration purposes only (each company should develop its own approach). They are not to be considered exclusive or exhaustive in nature. API/GPA make no warranties, express or implied for reliance on or any omissions from the information contained in this document.
C.1 Dry and Water Saturated Conditions (Non-rigorous)
To convert from dry to water saturated at base conditions or from water saturated at base conditions to dry basis using the law of partial pressures.
partial pressure water fraction water vapor =
total pressure (C.1)
The partial pressure of water equals its vapor pressure, which at 60 °F is 0.25640 psia196. Thus,
60
0.25640 fraction water vapor F Fwv
° = P = (C.2)
where
P is the pressure, absolute;
Fwv is the water vapor fraction.
To convert from dry to water saturated determine the fraction of gas other than water vapor, the dry gas fraction, by subtracting Fwv from unity. At base pressure and 60 °F this is:
fraction gas60°F = − 1 Fwv (C.3)
To convert from water saturated to dry at base pressure and 60 °F, multiply by the reciprocal of the fraction of gas other than water vapor, fraction gas 60 °F.
Convert saturated to dry 1
1 Fwv
= − (C.4)
The total pressure at base conditions is the base pressure. Conversion factors for common base pressures appear in the Table C.1.
Table C.1⎯Conversion Factors
Base pressure in psia 14.65 14.696 14.73 15.025
Dry to water saturated 0.9825 0.9826 0.9826 0.9829 Water saturated to dry 1.0178 1.0178 1.0177 1.0174
6 Wagner, W. and Pruss, A., "The IAPWS Formulation 1995 for the Thermodynamic Properties of Ordinary Water Substance for General and Scientific Use”, J. Phys. Chem. Ref. Data, 31(2):387 – 535, 2002
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EXAMPLE⎯Convert Water Saturated Heating Value to Dry
For example, convert a 1015 Btu/scf water saturated heating value at 14.73 psia and 60 °F to dry at the same base conditions. The water saturated to dry conversion value from Table C.1 at 14.73 psia base pressure is 1.0177. Therefore the calculation is:
Dry Heating Value = Water Saturated Heating Value Conversion Factor thus:
Dry Heating Value = 1015 × 1.0177=1033.0 Btu/scf at14.73 psia and 60 °F
×
EXAMPLE⎯Convert Dry Heating Value to Water Saturated
To convert a 1033 Btu/scf dry at 14.73 psia and 60 °F heating value to water saturated at the same base conditions requires a similar procedure. The dry to water saturated conversion value from Table C.1 at 14.73 psia base pressure is 0.9826. Therefore the calculation is:
Water Saturated Heating Value = Dry Heating Value × Conversion Factor thus:
Water Saturated Value = 1033 × 0.9826 = 1015.0 Btu/scf at14.73 psia and 60°F
C.2 Dry to Partially Water Saturated (non-rigorous)
The water content in a natural gas stream may be obtained by determining the dew point using a suitable tester, such as the chilled mirror device (Bureau of Mines dew point tester), then converting the dew point to a water vapor content to appropriate units such as Ib/MMSCF using industry accepted methods, such as those in the dehydration section of the Gas Processors Suppliers Association (GPSA) Engineering Data Book or tables such as those published by the International School of Hydrocarbon Measurement.
Acceptable test instruments are available that display the mass of water vapor per unit volume of gas directly using an indicating or recording meter. The test instruments should be carefully calibrated and used with caution if the gas being measured may contain substances known to interfere with water vapor content measurement.
To calculate the volume of vapor occupied by water at the measured water content in lb/MMCF:
Mwater= 18.0153 lb (GPA 2145) = 1 Mol Water
1 Mol Ideal Gas = V = RT P
where
Mwater is the molar mass (molecular weight) of water;
R is 10.7316 psia ft3 (lbmol ˚R)-1; T is 60 °F = 519.67 °R;
V is the volume in ft3 at pressure and temperature;
P is the pressure, absolute.
Copyright American Petroleum Institute Provided by IHS under license with API
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Pressure, psia 14.65 14.696 14.73 15.025
Volume, ft3 380.675 379.484 378.608 371.174
Table C.2⎯Mole Volume of Water Vapor at 60 °F
Volume Water Vapor
water
Measured Water Content
Mol Volume Vwv
= M × (C.5)
C.2.1 Volume Ratio of Dry to Partially Saturated Gas
Where the dry volume is large relative to the amount of water vapor such as is usually the case for water content measured in pounds per million cubic feet of gas, the ratio of dry to partially saturated gas can be calculated as:
ratio
1, 000, 000 1,000,000 wv
V = V
± (C.6)
NOTE In Equation (C.6), use plus (+Vwv) for dry to partially saturated and use minus (–Vwv) for partially saturated to dry.
EXAMPLE⎯Convert Dry Heating Value to Partially Saturated
As an example, correct a dry heating value of 1050 Btu/ft3 at 14.73 psia and 60 °F for the effect of 30 lb of water per MMCF of gas.
30 3
378.608 630.5 ft 18.0153
Vwv = × =
ratio
1, 000, 000
0.9994 (1,000,000 630.5)
V = =
+
3
partially sat dry ratio 1050 0 9994 1049 3 Btu ft
Hv = Hv × V = × . = . /
EXAMPLE⎯Convert Partially Saturated Heating Value to Dry
As an example, a gas has a heating value of 1075 Btu/ft3 @ 15.025 psia and 60 °F when it contains 35 lb of water per MMCF. Determine the heating value of the same gas containing no water.
35 3
371.174 721.1 ft 18.0153
Vwv = X =
ratio
1,000,000
1.0007 (1,000,000 721.1)
V = =
−
3
dry partially sat ratio 1075 1.0007 1075.8 Btu / ft
Hv = Hv × V = × =
C.3 Water Content Correlation⎯IGT RB 8
The water vapor content Equation (C.7) is based on the IGT RB 8. This further references seventeen other works. As presented in IGT RB 8, the fundamental equation for W is:
f
W A B
= P + (C.7)
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where
W is the water vapor content (lb water / MMSCF gas at 14.7 psia and 60 °F);
Pf is the flowing pressure, psia;
A and B are the variables contained within IGT RB 8 Tables as function of Tf; Tf is the flowing temperature, °F.
Since the IGT RB 8, Table B values of constants A and B are non-linear a simple table look up is not appropriate as linear interpolation between table entries would result in error. Therefore, non-linear equations that replicate the table and interpolate between the table entries are used to solve for A and B. These equations and their constants are:
(K1 (K 2 / (Tf K3 )))
A = e − + (C.8)
(K4 (K5 / (Tf K6 )))
B = e − + (C.9)
where
e is the Naperian constant;
K1 is 25.36794227;
K2 is 7170.42747964;
K3 is 389.5293906;
K4 is 15.97666211;
K5 is 7737.37631961;
K6 is 483.28778105;
Tf is the water dew point temperature, °F.
Table C.3, Values of Constants A and B, from IGT RB 8 is reproduced in Table C.3.
Copyright American Petroleum Institute Provided by IHS under license with API
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Table C.3⎯Values of Constants A and B Base conditions = 14.7 psia and 60 °F
To correct A and B to other base conditions, multiply each by:
(Pb/14.7) [519.6/(459.6 + Tb)] (0.998/zb)
°F A B °F A B °F A B °F A B –40 131 0.22 42 6240 3.54 124 89700 25.8 206 619000 115 –38 147 0.24 44 6740 3.74 126 94700 26.9 208 644000 119 –36 165 0.26 46 7280 3.96 128 100000 28.0 210 671000 122 –34 184 0.28 48 7850 4.18 130 106000 29.1 212 698000 126 –32 206 0.30 50 8460 4.42 132 111000 30.3 214 725000 130 –30 230 0.33 52 9110 4.66 134 117000 31.6 216 754000 134 –28 256 0.36 54 9800 4.92 136 124000 32.9 218 785000 139 –26 285 0.39 56 10500 5.19 138 130000 34.2 220 816000 143 –24 317 0.42 58 11300 5.48 140 137000 35.6 222 848000 148 –22 352 0.45 60 12200 5.77 142 144000 37.0 224 881000 152 –20 390 0.48 62 13100 6.08 144 152000 38.5 226 915000 157 –18 434 0.52 64 14000 6.41 146 160000 40.0 228 950000 162 –16 479 0.56 66 15000 6.74 148 168000 41.6 230 987000 166 –14 530 0.60 68 16100 7.10 150 177000 43.2 232 1020000 171 –12 586 0.64 70 17200 7.47 152 186000 44.9 234 1060000 177 –10 648 0.69 72 18500 7.85 154 195000 46.6 236 1100000 182 –8 714 0.74 74 19700 8.25 156 205000 48.4 238 1140000 187 –6 786 0.79 76 21100 8.67 158 215000 50.2 240 1190000 192 –4 866 0.85 78 22500 9.11 160 225000 52.1 242 1230000 198 –2 950 0.91 80 24100 9.57 162 236000 54.1 244 1270000 204 0 1050 0.97 82 25700 10.0 164 248000 56.1 246 1320000 210 2 1150 1.04 84 27400 10.5 166 259000 58.2 248 1370000 216 4 1260 1.11 86 29200 11.1 168 272000 60.3 250 1420000 222 6 1380 1.19 88 31100 11.6 170 285000 62.5 252 1470000 229 8 1510 1.27 90 33200 12.2 172 298000 64.8 254 1520000 235 10 1650 1.35 92 35300 12.7 174 312000 67.1 256 1570000 242 12 1810 1.44 94 37500 13.3 176 326000 69.5 258 1630000 248 14 1970 1.54 96 39900 14.0 178 341000 72.0 260 1680000 255 16 2150 1.64 98 42400 14.6 180 357000 74.5 280 2340000 333 18 2350 1.74 100 45100 15.3 182 372000 77.2 300 3180000 430 20 2560 1.85 102 47900 16.0 184 390000 79.9 320 4260000 548 22 2780 1.97 104 50800 16.7 186 407000 82.7 340 5610000 692 24 3030 2.09 106 53900 17.5 188 425000 85.5 360 7270000 869 26 3290 2.22 108 57100 18.3 190 443000 88.4 380 9300000 1090 28 3570 2.36 110 60500 19.1 192 463000 91.4 400 11700000 1360 30 3880 2.50 112 64100 20.0 194 483000 94.5 420 14700000 1700 32 4210 2.65 114 67900 20.9 196 504000 97.7 440 18100000 2130 34 4560 2.81 116 71800 21.8 198 525000 101 460 22200000 2550 36 4940 2.98 118 76000 22.7 200 547000 104
38 5350 3.16 120 80400 23.7 202 570000 108 40 5780 3.34 122 84900 24.7 204 594000 111
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38
Annex D
(informative)
Calculation of NGL Energy Content from Volume
The examples used in this annex are merely examples for illustration purposes only (each company should develop its own approach). They are not to be considered exclusive or exhaustive in nature. API/GPA make no warranties, express or implied for reliance on or any omissions from the information contained in this document.
D.1 Scope
This method includes procedures to convert natural gas liquid (NGL) volumes to energy units (such as Btu) to meet the need for system balances, plant shrinkage calculations or a situation that requires a consistency in energy units between natural gas and the liquids extracted as a result of processing. The NGL volumes may be expressed in mass, liquid volume or equivalent vapor volumes. Equivalent vapor volumes calculated from liquid volumes using GPA volume factors may be converted directly to Btu using GPA component heating values. Vapor volumes measured by conventional methods and corrected for deviation from ideal gas behavior must use a corrected Btu factor for accuracy. NGL volumes measured by conventional methods and expressed as liquid volume shall be converted to component volume or mass in accordance with GPA 8173.
D.2 Procedure
Given either component mass, component liquid volume or component gas volume, convert the quantity to energy using the appropriate physical constant from the latest version of GPA 2145. Component mass, component liquid volumes and component gas volumes should be determined according to the latest version of GPA 8173.
D.2.1 Mass
i i i
Q = m Hm × (D.1)
where
Q is the energy;
m is the mass;
Hm is the component heating value represented as energy per unit mass, fuel as an ideal gas; and
i is the (subscript) component i.
An example calculation follows to illustrate the determination of component and total energy in MMBtu (million Btu) for component mass from an NGL quantity of 29,604,847 lb.
D.2.2 Liquid Volume
i i i
Q = LV Hl × (D.2)
where
Q is the energy;
LV is the liquid volume;
Hl is the component heating value represented as energy per unit liquid volume, fuel as an ideal gas; and
i is the (subscript) component i.
An example calculation follows to illustrate the determination of component and total energy in MMBtu (million Btu) for component volume from an NGL quantity of 7,432,671 gal.
Copyright American Petroleum Institute Provided by IHS under license with API
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Table D.1⎯Calculate Energy Content from Liquid Mass
Component Mass
(lb)
GPA 2145 Btu/lbm, fuel as
ideal gas 725 Energy (MMBtu) Carbon Dioxide 760,845 0 0
Methane 5,921 23,892 141
Ethane 9,754,797 22,334 217,864 Propane 7,836,403 21,654 169,689 i-Butane 2,871,670 21,232 60,971 n- Butane 2,569,701 21,300 54,735 i-Pentane 1,204,917 21,044 25,356 n-Pentane 716,437 21,085 15,106 Hexane Plus 826 3,884,156 20,839 80,942 Total 29,604,847 624,805
Table D.2⎯Calculate Energy Content from Liquid Volume Component
Volume (gallons)
GPA 2145 Btu/gal, fuel as
ideal gas 725
Energy (MMBtu) Carbon Dioxide 111,017 0 0
Methane 2,368 59,729 141
Ethane 3,282,675 66,340 217,773 Propane 1,852,534 91,563 169,624 i-Butane 611,853 99,630 60,959 n- Butane 527,703 103,740 54,744
i-Pentane 231,386 109,680 25,378 n-Pentane 136,158 110,870 15,096 Hexane Plus 826 676,977 119,570 80,946
7,432,671 624,661
D.2.3 Gas Volume
i i i
Q = GV Hv × (D.3)
where
Q is the energy;
GV is the gas volume;
Hv is the component heating value represented as energy per unit gas volume, fuel as an ideal gas;
i is the (subscript) component i.
An example calculation follows to illustrate the determination of component and total energy in MMBtu (million Btu) for component volume from an equivalent gas volume of 257,594 MCF (thousand cubic feet) at 14.696 psia and 60 °F.
7 GPA 2145-09, use latest version.
8 This example uses the heating value for normal heptane for hexanes plus. Use the results of an extended analysis, engineering evaluation or other method--`,,```,,,,````-`-`,,`,,`,`,,`---.
Table D.3⎯Calculate Energy Content from Equivalent Gas Volume
Component
Volume (MCF @ 14.696
psia)
GPA 2145 Btu/ft3, fuel as
ideal gas 7
Energy (MMBtu) Carbon Dioxide 6,561 0.0 0
Methane 140 1010.0 141
Ethane 123,110 1769.7 217,868 Propane 67,440 2516.1 169,686 i-Butane 18,750 3251.9 60,973 n- Butane 16,778 3263.3 54,752
i-Pentane 6,338 4000.9 25,358 n-Pentane 3,768 4008.7 15,105 Hexane Plus 8 14,710 5502.6 80,943
257,594 624,815
Copyright American Petroleum Institute Provided by IHS under license with API
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41
Annex E (informati ve) Determination of Gas Energy Content per Unit Mass Table E.1⎯Calculations for Btu per Pound for Water Saturated Gas at Base Conditions Dry Basis Wet BasisMolecular Weight Dry Basis Wet BasisDry Basis Wet BasisBtu / lb.- Mass Dry Basis Wet Basis Mole FractionMole Fraction GPA 2145-09Molecular Weight Molecular Weight Weight FractionWeight FractionGPA 2145- 09 Hv (mass) Hv ( Mole Percent xixiwM xi* Mxiw* Mxi / Σxxiw / ΣxHv-mass Wt Fractioni * Btu/lbWt Fra Btu/lb 0.000 H2O 0.000000.0174418.01530.0000.314 0.00000 0.015530 0 0.030 Helium0.000300.000294.00260.0010.001 0.00006 0.000060 0 0.000 H2S 0.00000 0.0000034.08090.0000.000 0.00000 0.000000 0 2.020 CO20.02020 0.0198544.00950.8890.873 0.04386 0.043180 0 0.320 N20.00320 0.0031428.01340.0900.088 0.00442 0.004350 0 0.000 O20.00000 0.0000031.99880.0000.000 0.00000 0.000000 0 83.020 C10.83020 0.8157216.042513.31813.086 0.65712 0.6469123,89215,700 7.450 C20.07450 0.0732030.06902.2402.201 0.11053 0.1088122,3342,468 4.390 C30.04390 0.0431344.09561.9361.902 0.09551 0.0940321,6542,068 0.830 IC40.00830 0.0081658.12220.4820.474 0.02380 0.0234321,232505 1.080 NC40.01080 0.0106158.12220.6280.617 0.03097 0.0304921,300660 0.310 IC50.00310 0.0030572.14880.2240.220 0.01104 0.0108621,044232 0.250 NC50.00250 0.0024672.14880.1800.177 0.00890 0.0087621,085188 0.300 C6+ (NOTE 1) 0.00300 0.0029593.18870.2800.275 0.01379 0.0135820,894288 100.000 Summation 1.000001.00000 20.26920.2291.000001.00000 22,110
NOTE 1 Molecular weight of C6+ is an arbitrary value derived from a 60-30-10 nC6-nC7-nC8 split. NOTE 2 Mass and energy are not pressure dependent. Do not adjust the sample Btu/lbm for pressure base.
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Shipping (International Orders) –Standard international shipping is by air express courier service. Subscription updates are sent by World Mail. Normal delivery is 3-4 days from shipping date.
Rush Shipping Fee –Next Day Delivery orders charge is $20 in addition to the carrier charges. Next Day Delivery orders must be placed by 2:00 p.m. MST to ensure overnight delivery.
Returns –All returns must be pre-approved by calling the IHS Customer Service Department at 1-800-624-3974 for information and assistance. There may be a 15% restocking fee.
Special order items, electronic documents, and age-dated materials are non-returnable.
or for incorporation into commercial products, training courses, workshops, or other commercial enterprises.
Available through IHS:
Phone Orders: 1-800-854-7179 (Toll-free in the U.S. and Canada) 303-397-7956 (Local and International) Fax Orders: 303-397-2740
Online Orders: global.ihs.com
2009
Publications Order Form
Copyright American Petroleum Institute Provided by IHS under license with API
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MPMS Chapter 14.1, Collecting and Handling of Natural Gas Samples for Custody Transfer MPMS Chapter 14.4, Converting Mass of Natural Gas Liquids and Vapors to Equivalent Liquid Volumes
$175.00
$57.00
API provides additional resources and programs to the oil and natural gas industry which are based on API Standards. For more information, contact:
API MONOGRAM® LICENSING PROGRAM
Phone: 202-962-4791 Fax: 202-682-8070
Email: certification@api.org API QUALITY REGISTRAR (APIQR®)
> ISO 9001 Registration
> ISO/TS 29001 Registration
> ISO 14001 Registration
> API Spec Q1®Registration Phone: 202-962-4791
Fax: 202-682-8070
Email: certification@api.org API PERFORATOR DESIGN REGISTRATION PROGRAM Phone: 202-682-8490
Fax: 202-682-8070 Email: perfdesign@api.org API TRAINING PROVIDER CERTIFICATION PROGRAM (API TPCPTM)
Phone: 202-682-8490 Fax: 202-682-8070 Email: tpcp@api.org
API INDIVIDUAL CERTIFICATION PROGRAMS (ICP®)
Phone: 202-682-8064 Fax: 202-682-8348 Email: icp@api.org
API ENGINE OIL LICENSING AND CERTIFICATION SYSTEM (EOLCS) Phone: 202-682-8516
Fax: 202-962-4739 Email: eolcs@api.org
API PETROTEAM (TRAINING, EDUCATION AND MEETINGS) Phone: 202-682-8195
Fax: 202-682-8222 Email: petroteam@api.org API UNIVERSITYTM Phone: 202-682-8195 Fax: 202-682-8222 Email: training@api.org
Check out the API Publications, Programs, and Services Catalog online at www.api.org.
Copyright 2008 – API, all rights reserved. API, API monogram, APIQR, API Spec Q1, API TPCP, ICP, API University and the API logo are either trademarks or registered trademarks of API in the United States and/or other countries.
THERE’S MORE
WHERE THIS CAME FROM.
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Copyright American Petroleum Institute Provided by IHS under license with API