SCHEDULE A TO THE LNG SALES AND PURCHASE CONTRACT (KOREA II FOB) between PERUSAHAAN PERTAMBANGAN MINYAK DAN GAS BUMI NEGARA (PERTAMINA) as Seller and KOREA GAS CORPORATION as Buyer SCHEDULE A TESTING AND METHODS This Schedule A, entitled "Testing and Methods", is attached to and forms a part of the LNG Sales and Purchase Contract ("Contract") between Pertamina, as Seller, and Korea Gas Corporation, as Buyer, and sets forth, pursuant to Article 13 of the Contract, detailed procedures for sampling and analysing LNG and for gauging and calculating the density and heating value of LNG. SECTION I - DEFINITIONS Terms defined in the Contract and appearing in this Schedule A shall, when used herein, have the meanings set forth in the Contract. SECTION II - TANK GAUGE TABLES II.1 Calibration of LNG Tanks During or immediately following the completion of construction of each vessel which Buyer intends to use as an LNG Tanker, Buyer shall arrange for each LNG tank of each such vessel to be calibrated by a qualified surveyor mutually agreed upon by Buyer and Seller. II.2 Preparation of Tank Gauge Tables Buyer shall have a qualified surveyor prepare tank gauge tables for each LNG tank of each vessel which Buyer intends to use as an LNG Tanker from the results of the calibration referred to in Section II.1 above. Such tank gauge tables shall include sounding tables, correction tables for list (heel) and trim, volume corrections to tank service temperature, and other corrections if necessary. The tank gauge tables prepared by such surveyor shall be verified for use by the authorized agency of the Republic of Korea and the Republic of Indonesia. II.3 Accuracy of Tank Gauge Tables The tank gauge tables prepared pursuant to Section II.2 above shall indicate volumes in Cubic Meters expressed to the nearest thousandth, with tank depths expressed in meters to the nearest hundredth. II.4 Witnessing of Tank Calibration Seller shall have the right to have its representative witness the tank calibrations referred to in Section II.1 above. Buyer shall give adequate advance notice to Seller of the timing of such tank calibrations. II.5 Recalibration of LNG Tanks in Case of Distortion In the event that any LNG tank of any LNG Tanker suffers distortion of such a nature as to cause any party reasonably to question the validity of the tank gauge tables referred to in Section II.2 above, Buyer, subject to Seller's consent, shall arrange for such LNG tank to be recalibrated in the same manner as set forth in Sections II.1 and II.2 hereof during any period when such is out of service for inspection and/or repairs. Buyer shall bear the costs of recalibration unless such recalibration was done at Seller's request and did not demonstrate any inaccuracy in the tank gauge tables, in which case Seller shall pay the costs of recalibration. Except as provided in this Section II.5, no other recalibration of any LNG tank of any LNG Tanker shall be required. SECTION III - SELECTION OF GAUGING DEVICES III.1 Liquid Level Gauging Devices III.1.1 Each LNG tank of each LNG Tanker shall be equipped with a main and an auxiliary liquid level gauging device. III.1.2 The measurement error of the liquid level gauging devices shall be no greater than +10 millimeters. The expected accuracy for the main gauging device shall be +7.5 millimeters and for the auxiliary gauging device shall be +10 millimeters. III.1.3 The level in each LNG tank shall be logged or printed. III.2 Temperature Gauging Devices III.2.1 Each LNG tank of each LNG Tanker shall be equipped with a minimum of four (4) temperature gauging devices located on or near the vertical axis of such LNG tank. III.2.2 Such temperature gauging devices shall be installed near the bottom, at approximately fifty percent (50%) of the height, at approximately eighty-five percent (85%) of the height and at approximately one hundred percent (100%) of the height of such LNG tank. III.2.3 The measurement error of the temperature gauging devices shall be no greater than +2C. The expected accuracy shall be +0.2oC when in liquid and +0.4oC when in vapor. III.2.4 The temperatures in each LNG tank shall be logged or printed. III.3 Pressure Gauging Devices III.3.1 Each LNG tank of each LNG Tanker shall have one absolute pressure gauging device. III.3.2 The measurement error of the pressure gauging device shall be no greater than + one percent (1%) of full-scale. The expected accuracy shall be +0.01 kg/cm2. III.3.3 The pressure in each LNG tank shall be logged or printed. III.4 Verification of Accuracy of Gauging Devices Gauging devices shall be verified for accuracy and corrected for error in accordance with the terms of Subarticle 13.10 of the Contract. SECTION IV - MEASUREMENT PROCEDURES IV.1 Liquid Level IV.1.1 Measurement of the liquid level in each LNG tank of each LNG Tanker shall be made to the nearest millimeter by using the main liquid level gauging device referred to in Section III.1 hereof. Should the main device fail, the auxiliary device shall be used. IV.1.2 Three (3) readings shall be made in as rapid succession as possible. The arithmetic average of the readings shall be deemed the liquid level. IV.1.3 Such arithmetic average shall be calculated to the nearest 0.1 millimeter and shall be rounded to the nearest millimeter. IV.2 Temperature IV.2.1 At the same time liquid level is measured, temperature shall be measured to the nearest 0.1oC by using the temperature gauging devices referred to in Section III.2 hereof. IV.2.2 In order to determine the temperature of liquid and vapor in the LNG tanks of an LNG Tanker one (1) reading shall be taken at each temperature gauging device in each LNG tank. An arithmetic average of such readings with respect to vapor and liquid in all LNG tanks shall be deemed the final temperature of vapor and liquid. IV.2.3 Such arithmetic average shall be calculated to the nearest 0.01oC and shall be rounded to the nearest 0.1oC. IV.3 Pressure IV.3.1 At the same time liquid level is measured, the absolute pressure in each LNG tank shall be measured to the nearest 0.01 kg/cm2 by using the pressure gauging device referred to in Section III.3 hereof. IV.3.2 The determination of the absolute pressure in the LNG tanks of each LNG Tanker shall be made by taking one (1) reading of the pressure gauging device in each LNG tank, and then by taking an arithmetic average of all such readings. IV.3.3 Such arithmetic average shall be calculated to the nearest 0.001 kg/cm2 and shall be rounded to the nearest 0.01 kg/cm2. IV.4 Procedures in Case of Gauging Device Failure Should the measurements referred to in Sections IV.l, IV.2 and IV.3 hereof become impossible to perform due to a failure of gauging devices, alternate gauging procedures shall be determined by mutual agreement between Buyer and Seller. IV.5 Determination of Volume of LNG Loaded IV.5.1 The list (heel) and trim of the LNG Tanker shall be measured at the same time as the liquid level and temperature of LNG in each LNG tank are measured. Such measurements shall be made immediately before loading commences and immediately after loading is completed. The volume of LNG, stated in Cubic Meters to the nearest 0.001 Cubic Meters, shall be determined by using the tank gauge tables referred to in Section II hereof and by applying the volume corrections set forth therein. IV.5.2 The volume of LNG loaded shall be determined by deducting the total volume of LNG in all tanks immediately before loading commences from the total volume in all tanks immediately after loading is completed. This volume of LNG loaded is then rounded to the nearest Cubic Meter. SECTION V - DETERMINATION OF COMPOSITION OF LNG V.1 Sampling Procedures V.1.1 Representative samples of LNG shall be obtained continuously and at an even rate during the period starting immediately after continuous loading has commenced and ending immediately prior to the suspension of continuous loading. V.1.2 A composite gaseous sample shall be collected in a suitable gas holder using a continuous gasification/collection method agreed upon by Seller and Buyers. V.1.3 Three (3) samples shall be transferred from the gas holder to sample bottles after completion of loading. Such sample bottles shall be sealed by the surveyor who witnessed such sampling in accordance with Subarticle 13.8 of the Contract and shall be delivered to Seller. Seller shall use one (1) such sample for analysis to determine the composition. V.1.4 Distribution of Samples The gaseous samples shall be distributed as follows: First sample: for analysis by Seller. Second sample: for analysis by Buyer. Third sample: for retention by Seller for at least twenty-five (25) days. In case any dispute as to the accuracy of any analysis is raised, the sample shall be further retained until Buyer and Seller agree to retain it no longer. V.1.5 Failure in Collecting Samples and in Determining the Composition of LNG - If sampling and/or analysis fails for some reason, the arithmetic average of the analysis results of the five (5) immediately preceding cargoes (or of the total cargoes delivered is less than five) under this Contract from the applicable Loading Port shall be deemed to be the composition of the LNG. The loaded BTUs and metric tons are calculated as follows: E5 (BTU/m3) X Vm3 loaded = BTU E5 (Kg/m3) X Vm3 = Metric Tons V.2 Analysis Procedures V.2.1 Hydrocarbons, Carbon Dioxide and Nitrogen - Seller's sample shall be analysed immediately by Seller to determine, by gas chromatography, the mol fraction of hydrocarbons, carbon dioxide and nitrogen in the sample. The method used shall be the method described in the latest version of the Gas Processors Association (GPA) Publication 2261 current at the time of analysis or any other method agreed upon by Buyer and Seller. Duplicate runs shall be made on each sample to determine that the repeatabilities of peak heights or peak areas are within acceptable limits. The calculated results of such duplicate runs shall be averaged. V.2.2 Hydrogen Sulfide - The ASTM D 2725-70, Standard Method of Test for Hydrogen Sulfide in Natural Gas (Methylene Blue Method), shall be used to determine the hydrogen sulfide content of Seller's sample, unless Seller and Buyer mutually agree that some other method should be used. V.2.3 Total Sulfur - The ASTM D 3246-76, Standard Method of Test for Sulfur in Petroleum Gas by Oxidative Microcoulometry, shall be used to determine the total sulfur content of Seller's sample, unless Seller and Buyer mutually agree that some other method should be used. If the total sulfur content is less than 0.25 grains per 100 Standard Cubic Feet, it is not necessary to analyze the sample for H2S. V.3 Correlation Test of Analytical Equipment and Devices Buyer and Seller shall, prior to use and during periods of use, perform a correlation test using standard gas in order properly to maintain the accuracy of Seller's and Buyer's equipment and devices. Such correlation tests are subject to the following conditions: (a) Mutual agreement of Seller and Buyer as to timing of a test; (b) The standard gas sample shall be obtained by Buyer; (c) The standard gas sample shall be transported to the applicable Loading Port on an LNG Tanker; (d) Seller shall analyze the sample and return it to Buyer on an LNG Tanker; (e) Buyer shall analyze the sample; and (f) The results of these tests shall be made available to all Parties. SECTION VI - DETERMINATION OF BTU QUANTITY OF LNG SOLD VI.1 Calculation of Density The density of LNG shall be calculated by use of the formula: E (Xi x Mi) D = ___________________ E (Xi x Vi) - Xm x C where: D is the density to four (4) significant figures of the LNG loaded, stated in kilograms per Cubic Meter at temperature TL; TL is the temperature of the LNG in the tanks of the LNG Tanker after loading, stated in degrees Centigrade to the nearest 0.1oC; Xi is the mol fraction, to the nearest fourth (4th) decimal place, of component (i) from the composition obtained in accordance with Section V hereof; Mi is the molecular weight of component (i) as set forth in Table 1 attached hereto; Vi is the molar volume, to the nearest sixth (6th) decimal place, of component (i), stated in Cubic Meters per kilogram-mol at temperature TL and obtained by linear interpolation of the data set forth in Table 2 attached hereto; Xm is the mol fraction, to the nearest fourth (4th) decimal place, of methane from the composition obtained in accordance with Section V hereof; and C is the volume correction, to the nearest sixth (6th) decimal place, stated in Cubic Meters per kilogram-mol at temperature TL and obtained by linear interpolation of the data set forth in Table 3 attached hereto. An example of an LNG density calculation is shown in Table 4 attached hereto. VI.2 Calculation of Gross Heating Value VI.2.1 The Gross Heating Value (mass basis) of LNG shall be calculated by use of the formula: Xi x Mi P = E Hi x ____________ E (Xi x Mi) where: P is the Gross Heating Value of LNG, stated in BTU's per kilogram; Hi is the Gross Heating Value of component (i), stated in BTU's per kilogram as set forth in Table 1 attached hereto; Xi is the mol fraction, to the nearest fourth (4th) decimal place, of component (i) from the composition obtained pursuant to Section V hereof; and Mi is the molecular weight of component (i) as set forth in Table 1 attached hereto. An example of a Gross Heating Value (mass basis) calculation is shown in Table 5 attached hereto. VI.2.2 The Gross Heating Value (volume basis) for purposes of Subarticle 11.1 of the Contract shall be calculated by use of the formula: Hv = E (Xi x Hvi) where: Hv is the Gross Heating Value, stated in BTU's per Standard Cubic Foot; Xi is the mol fraction, to the nearest fourth (4th) decimal place, of component (i) from the composition obtained pursuant to Section V hereof; and Hvi is the Gross Heating Value of component (i), stated in BTU's per Standard Cubic Foot, as set forth in Table 1 attached hereto. An example of a Gross Heating Value (volume basis) calculation is shown in Table 6 attached hereto. VI.3 Calculation of BTU Quantity of LNG Delivered The BTU quantity of LNG sold shall be computed by use of the formula: Q = V x D x P where: Q is the BTU quantity sold; V is the volume of the LNG loaded, stated in Cubic Meters, obtained pursuant to Section IV.5 hereof; D is the density of the LNG, stated in kilograms per Cubic Meter, as calculated in accordance with Section VI.1 hereof; and P is the Gross Heating Value of the LNG, stated in BTU's per kilogram, as calculated in accordance with Section VI.2.1 hereof. VI.4 Method of Rounding Numbers VI.4.1 General - If the first of the figures to be discarded is five (5) or more, the last of the figures to be retained is increased by one (1). If the first of the figures to be discarded is four (4) or less, the last of the figures to be retained is unaltered. For the purpose of rounding to a zero (0), the last of the figures to be retained shall have the same value as a ten (10). The following example is given to illustrate how a number is to be established in accordance with the above: Number after being rounded to first Number to be rounded decimal place 2.24 2.2 2.249 2.2 2.25 2.3 2.35 2.4 2.97 3.0 VI.4.2 Determination of BTU Quantity of LNG delivered - The BTU quantity of LNG delivered is computed by the use of the formula: Q = V x D x P where: Q is the BTU quantity delivered. The BTU quantity shall be rounded to the nearest ten (10) million BTU's; V is the volume of the LNG loaded, stated in Cubic Meters. The volume shall be rounded to the nearest Cubic Meter; D is the density of the LNG, stated in kilograms per Cubic Meter at temperature TL. The density shall be rounded to the nearest tenth (0.1) of a kg/m3; TL is the temperature of the LNG in the tanks of the LNG Tanker after loading, stated in degrees Centigrade to the nearest tenth (0.1) degree C; and P is the Gross Heating Value of the LNG, stated in BTU's per kilogram. The Gross Heating Value shall be rounded to the nearest BTU/kg. VI.4.3 Determination of LNG Density - The density of the LNG is calculated by use of the formula: E(Xi x Mi) D = ___________________ E(Xi x Vi) - Xm x C where: D is the density of the LNG, stated in kilograms per Cubic Meter at temperature TL. The density shall be rounded to the nearest tenth (0.1) of a kg/m3; TL is the temperature of the LNG in the tanks of the LNG Tanker after loading, stated in degrees Centigrade to the nearest tenth (0.1) degree C; Xi is the mol fraction, to the nearest fourth (4th) decimal place, of component (i) from the composition obtained in accordance with Section V hereof. The mol fraction of methane shall be adjusted so as to make the total mol fraction equal to 1.0000; Mi is the molecular weight of component (i) as set forth in Table 1 attached hereto; E(Xi x Mi): The result of the calculation of "Xi x Mi" of component (i) shall be rounded to the nearest third (3rd) decimal place, and then, "E(Xi x Mi)" shall be calculated to the nearest third (3rd) decimal place; Vi is the molar volume, to the nearest sixth (6th) decimal place, of component (i), stated in Cubic Meters per kilogram-mol at temperature TL, and shall be obtained by linear interpolation of the data set forth in Table 2 attached hereto; E(Xi x Vi): The result of the calculation of "Xi x Vi" of component (i) shall be rounded to the nearest sixth (6th) decimal place, and then "E(Xi x Vi)" shall be calculated to the nearest sixth (6th) decimal place; Xm is the mol fraction, to the nearest fourth (4th) decimal place, of methane from the composition obtained in accordance with Section V hereof; C is the volume correction, to the nearest sixth (6th) decimal place, stated in Cubic Meters per kilogram-mol at temperature TL, and shall be obtained by linear interpolation of the data set forth in Table 3 attached hereto; Xm x C: "Xm x C" shall be calculated to the nearest sixth (6th) decimal place; and E(Xi x Vi) - Xm x C: "E(Xi x Vi) - Xm x C" shall be calculated to the nearest sixth (6th) decimal place. VI.4.4 Determination of Gross Heating Value VI.4.4.1 The Gross Heating Value (mass basis) of the LNG is calculated by use of the formula: Xi x Mi P = E Hi x ___________ E(Xi x Mi) where: P is the Gross Heating Value of the LNG, stated in BTU's per kilogram. Each term of the above equation shall first be calculated and rounded to the nearest BTU/kg, and then all terms shall be summed to obtain the Gross Heating Value "P"; Hi is the Gross Heating Value of component (i), stated in BTU's per kilogram, as set forth in Table 1 attached hereto; Xi is the mol fraction, to the nearest fourth (4th) decimal place, of component (i) from the composition obtained in accordance with Section V hereof; Mi is the molecular weight of component (i) as set forth in Table 1 attached hereto; Xi x Mi: "Xi x Mi" of component (i) shall be calculated to the nearest third (3rd) decimal place; E(Xi x Mi): "E(Xi x Mi)" shall be calculated to the nearest third (3rd) decimal place by summing all "Xi x Mi" obtained as above; Xi x Mi __________ : E(Xi x Mi) Xi x Mi " __________ " shall be E(Xi x Mi) calculated for component (i) to the nearest fifth (5th) decimal place by dividing " Xi x Mi" by " E(Xi x Mi)"; Xi x Mi Hi x __________ : E(Xi x Mi) Xi x Mi "Hi x __________ " shall E (Xi x Mi) be calculated for component (i) to the nearest whole number by multiplying "Hi" by Xi x Mi " __________ " ; and E (Xi x Mi) Xi x Mi E Hi x _________ : E(Xi x Mi) Xi x Mi " E Hi x __________ " E(Xi x Mi) shall be calculated to the nearest whole number by summing all " Xi x Mi " Hi x _________ E(Xi x Mi) obtained as above. VI.4.4.2 The Gross Heating Value (volume basis) of the LNG shall be calculated by use of the formula: Hv = E(Xi x Hvi) where: Hv is the Gross Heating Value of LNG, stated in BTU's per Standard Cubic Foot. Each term of the above equation shall first be calculated and rounded to the nearest tenth (0.1) of a BTU/scf, and then all terms shall be summed and rounded to the nearest BTU/scf to obtain the Gross Heating Value "Hv"; Xi is the mol fraction, to the nearest fourth (4th) decimal place, of component (i) from the composition obtained pursuant to Section V hereof; and Hvi is the Gross Heating Value of component (i), stated in BTU's per Standard Cubic Foot, as set forth in Table 1 attached hereto. TABLE 1 PHYSICAL CONSTANTS Gross Heating Gross Heating Molecular Value (BTU/kg) Value (BTU/scf) Weight at 60oF, at 60oF Component Mi Hi Hvi Methane (CH ) 16.043 52671 1010.0 4 Ethane (C H ) 30.070 49236 1769.6 2 6 Propane (C H ) 44.097 47737 2516.1 3 8 Iso-butane (i-C H ) 58.123 46809 3251.9 4 10 Normal Butane (n-C H ) 58.123 46959 3262.3 4 10 Iso-pentane (i-C H ) 72.150 46392 4000.9 5 12 Normal Pentane (n-C H ) 72.150 46485 4008.9 5 12 Normal Hexane (n-C H ) 86.177 46172 4755.9 6 14 Nitrogen (N ) 28.013 0 0 2 Oxygen (O ) 31.999 0 0 2 Carbon Dioxide (CO ) 44.010 0 0 2 The above table of Physical Constants, developed from GPA Publication 2145-88, shall be used for all density and heating value calculations associated with this Contract. This table of Physical Constants shall be revised to conform to any subsequent officially published revision of GPA Publication 2145. The values for the Gross Heating Value in BTU/kg as shown above have been obtained by multiplying the GPA 2145 values for "BTU/lbm fuel as ideal gas" from GPA 2145 by 2.20462. TABLE 2 MOLAR VOLUMES OF INDIVIDUAL COMPONENTS Molar Volumes (m3/kg-mol) at Various Temperatures x 103 ______________________________________________________ -162oC -160oC -158oC -156oC _______ ______ ______ ______ CH 37.95 38.21 38.48 38.76 4 C H 47.84 48.00 48.16 48.33 2 6 C H 62.34 62.52 62.70 62.89 3 8 i-C H 76.90 77.11 77.33 77.54 4 10 n-C H 76.63 76.82 77.01 77.20 4 10 i-C H 90.92 91.13 91.35 91.56 5 12 n-C H 90.26 90.47 90.67 90.88 5 12 n-C H 104.67 104.89 105.11 105.34 6 14 N 45.64 46.83 48.11 49.47 2 O 31.14 31.51 31.90 32.30 2 CO 29.73 29.83 29.93 30.03 2 Reference : Density calculations and method from Proceedings of the First International Conference of LNG, April 1968, Paper No. 22, Densities of Liquefied Natural Gas and of Low Molecular Weight Hydrocarbons, J. Klosek and C. McKinley. Note: Molar volumes for CO2 were developed by mutual agreement between Buyer and Seller. /TABLE TABLE 3 CORRECTION C FOR VOLUME REDUCTION OF MIXTURE Molecular Weight C (m /kg-mol) at Various Temperatures x 10 3 of Mixture ___________________________________________ o o o o E(Xi x Mi) -162 C -160 C -158 C -156 C _______ ______ ______ ______ ______ 17.00 0.240 0.240 0.250 0.260 17.50 0.360 0.370 0.380 0.390 18.00 0.470 0.490 0.500 0.520 18.50 0.580 0.600 0.620 0.640 19.00 0.690 0.710 0.730 0.750 19.50 0.790 0.810 0.840 0.860 20.00 0.890 0.910 0.940 0.970 Reference : Density calculations and method from Proceedings of the First International Conference of LNG, April 1968, Paper No. 22, Densities of Liquefied Natural Gas and of Low Molecular Weight Hydrocarbons, J. Klosek and C. McKinley. /TABLE TABLE 4 EXAMPLE OF LNG DENSITY CALCULATION Molar Volume Mol Molecular Vi x 103 Fraction Weight (m3/kg-mol) at TL-158.9oC Xi Mi Xi x Mi Vi (Xi x Vi)x103 CH 0.9128 16.043 14.644 38.359 35.014 4 C H 0.0539 30.070 1.621 48.088 2.592 2 6 C H 0.0241 44.097 1.063 62.619 1.509 3 8 i-C H 0.0043 58.123 0.250 77.231 0.332 4 10 n-C H 0.0044 58.123 0.256 76.925 0.338 4 10 i-C H 0.0001 72.150 0.007 91.251 0.009 5 12 N2 0.0004 28.013 0.011 47.534 0.019 _______ ______ _______ Total 1.0000 17.852 39.813 Average Molecular Weight = 17.852 Average Molar Volume = 39.813 -3 C = 0.460 x 10 17.852 D = ________________________________________ -3 -3 39.813 x 10 - 0.9128 x 0.460 x 10 17.852 = _______________________________ -3 -3 39.813 x 10 - 0.420 x 10 3 = 0.453177 x 10 3 D = 453.2 kg/m /TABLE TABLE 5 EXAMPLE OF GROSS HEATING VALUE (MASS BASIS) CALCULATION Gross Mol Heating Value Molecular Heating Value Fraction (BTU/kg) Weight Hi x Xi x Mi * Xi Hi Mi (Xi x Mi) E(Xi x Mi) _______ ______ _______ _________ ___________ CH 0.9128 52671 16.043 14.644 43206 4 C H 0.0539 49236 30.070 1.621 4471 2 6 C H 0.0241 47737 44.097 1.063 2843 3 8 i-C H 0.0043 46809 58.123 0.250 655 4 10 n-C H 0.0044 46959 58.123 0.256 673 4 10 i-C H 0.0001 46392 72.150 0.007 18 5 12 N2 0.0004 0 28.013 0.011 Total 1.0000 17.852 51866 * Rounded to the fifth (5th) decimal place P = 51866 BTU/kg /TABLE TABLE 6 EXAMPLE OF GROSS HEATING VALUE (VOLUME BASIS) CALCULATION Component Mol Fraction Gross Heating Value, Hvi (BTU/scf) Xi Hvi (Xi x Hvi) CH 0.9128 1010.0 921.9 4 C H 0.0539 1769.6 95.4 2 6 C H 0.0241 2516.1 60.6 3 8 i-C H 0.0043 3251.9 14.0 4 10 n-C H 0.0044 3262.3 14.4 4 10 i-C H 0.0001 4000.9 0.4 5 12 N 0.0004 0 0 2 Total 1.0000 1106.7 Hv = 1107 BTU/scf