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This book is designed to provide a convenient source of vital information for anyone who works with or
studies industrial gases. It is published by Air Liquide America Corporation, a subsidiary of Air Liquide,
the world's largest industrial gas organization. Through Air Liquide America Corporation, Air Liquide
markets virtually every industrial gas to industrial, commercial, and public facilities throughout North
America. Air Liquide is active in more than 60 countries around the world.
The data contained here is based on sources using standard industry references. It is believed to beaccurate, but is recommended for use as a guideline only.
INTRODUCTION TO THE INDUSTRIAL GAS DATA BOOK
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1.
2.
3.
4.
5.
6.
7.8.
9.
10.
11.
12.
13.
14.
15.
16.
17.
18.
19.20.
21.
22.
23.
24.
25.
26.
27.
28.
30.
31.
32.
33.
34.
35.
36.
37.
38.
39.
40.
41.
42.
43.
44.
45.
Safe Storage Distances for LPG and Liquid Oxygen
Nitrogen Refrigeration
Physical Properties of Gases - USA units
Physical Properties of Gases - Metric units
Customer Cryogenic Tank
VGL Parts
Pressure, Temperature and Density Relationships for Liquid Oxygen, Nitrogen, & Argon
Saturated Steam Tables - Pressure Basis
Saturated Steam Tables - Temperature Basis
Superheated Steam Tables
Gas Flammability
Saturated Liquid Flashing
Gas Turbine Capacity
Liquid Hydrogen Vapor Release
Pressure Drop of Compressed Air in Piping
Minimum Safe Distance for Liquid Hydrogen Storage
Liquid CO2 Storage Vessel Dimensions and Foot Prints
Tube Trailers' and Generic Cryogenic Vessels' Capacities
High Pressure Steel & Aluminum Gas Cylinders' Specifications
Saturated Densities
Nitrogen Purging
Nitrogen Purging Efficiency
Electric, Steam, and Ambient Vaporizers' Specifications
Dissociated MeOH & NH3 Conversion Data
Absolute Temperatures ChartCO2 Cylinder Specifications
CO & Ozone Conversion Factors
CGA Gas Cylinder Valves and Specifications
Length and Weight Conversion Factors
Liquid Oxygen, Liquid Nitrogen, & Liquid Hydrogen mass conversions to Volume
Liquid Oxygen & Liquid Nitrogen Tonnage Rate Conversion to Volumetric Rate
Dew Point Conversion to Parts per Million (Volume)
Metered Gas Conversion Factors
Combustion Requirements for Boiler Fossil Fuels
Helium and Hydrogen Conversion Data
Krypton and Xenon Conversion Data
Velocity and Miscellaneous Conversion FactorsDensity and Pressure Conversion Factors
Energy and Power Conversion Factors
Area and Volume Conversion Factors
TABLE OF WORKSHEET CONTENTS
Introduction (This Worksheet)
Oxygen and Nitrogen Conversion Data
Argon and Neon Conversion Data
Carbon Dioxide, Propane, and Propylene Conversion Data
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pounds
(lb)
kilograms
(kg)
cubic feet
(scf)
cu
meters
(nm3)
gallons
(gal)liters (l)
1 pound 1.0 0.4536 12.076 0.3174 0.105 0.3977
1 kilogram 2.205 1.0 26.62 0.6998 0.2316 0.8767
1 scf gas 0.08281 0.03756 1.0 0.02628 0.008691 0.0329
1 nm3
gas 3.151 1.4291 38.04 1.0 0.331 1.2528
1 gallon liquid 9.527 4.322 115.1 3.025 1.0 3.785
1 liter liquid 2.517 1.1417 30.38 0.7983 0.2642 1.01 ton 2,000 907.2 24.16 635 209.9 794.5
pounds
(lb)
kilograms
(kg)
cubic feet
(scf)
cu
meters
(nm3)
gallons
(gal) liters (l)
1 pound 1.0 0.4536 13.803 0.3627 0.1481 0.5606
1 kilogram 2.205 1.0 30.42 0.7996 0.3262 1.2349
1 scf gas 0.07245 0.03286 1.0 0.02628 0.01074 0.04065
1 nm3
gas 2.757 1.2506 38.04 1.0 0.408 1.5443
1 gallon liquid 6.745 3.06 93.11 2.447 1.0 3.785
1 liter liquid 1.782 0.8083 24.6 0.6464 0.2642 1.0
1 ton 2,000 907.2 27.605 725.4 296.2 1,121
A Scf (standard cubic foot) is gas measured at 1 atmosphere and 70 F.
A Nm3
(normal cubic meter) is gas measured at 1 atmosphere and 0 C.Liquid volume is measured at 1 atmosphere and its boiling temperature.
OXYGEN CONVERSION DATA
NITROGEN CONVERSION DATA
Weight Gas Liquid
Oxygen Quantity
Nitrogen
Quantity
Weight Gas Liquid
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pounds
(lb)
kilograms
(kg)
cubic feet
(scf)
cu
meters
(nm3)
gallons
(gal)liters (l)
1 pound 1.0 0.4536 9.671 0.2543 0.086 0.3255
1 kilogram 2.205 1.0 21.32 0.5605 0.18957 0.7176
1 scf gas 0.1034 0.0469 1.0 0.02628 0.008893 0.03366
1 nm3
gas 3.933 1.784 38.04 1.0 0.3382 1.2802
1 gallon liquid 11.63 5.276 112.5 2.957 1.0 3.785
1 liter liquid 3.072 1.3936 29.71 0.7812 0.2642 1.01 ton 2,000 907.2 19.342 508.6 172 651
pounds
(lb)
kilograms
(kg)
cubic feet
(scf)
cu
meters
(nm3)
gallons
(gal)liters (l)
1 pound 1.0 0.4536 19.18 0.504 0.09928 0.37581 kilogram 2.205 1.0 42.27 1.1112 0.2191 0.8292
1 scf gas 0.05215 0.02366 1.0 0.02628 0.005177 0.019594
1 nm3
gas 1.984 0.8999 38.04 1.0 0.1971 0.7462
1 gallon liquid 10.065 4.565 193.2 5.077 1.0 3.7851 liter liquid 2.661 1.207 51.03 1.341 0.2642 1.0
A Scf (standard cubic foot) is gas measured at 1 atmosphere and 70F.
A Nm3
(normal cubic meter) is gas measured at 1 atmosphere and 0 C.
Liquid volume is measured at 1 atmosphere and its boiling temperature.
All values are rounded to the nearest 4/5 significant numbers.
ARGON CONVERSION DATA
Argon Quantity
Weight Gas Liquid
NEON CONVERSION DATA
Neon Quantity
Weight Gas Liquid
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pounds (lb)kilograms
(kg)
cubic feet
(scf)
cu meters
(nm3
)
gallons
(gal)
liters (l)
1 pound 1.0 0.4536 8.06 0.2118 0.089 0.3355
1 kilogram 2.205 1.0 17.77 0.4671 0.1954 0.7397
1 scf gas 0.12406 0.05626 1.0 0.02628 0.011862 0.0449
1 nm gas 4.72 2.141 38.04 1.0 0.4525 1.7127
1 gallon liquid 11.283 5.117 84.3 2.21 1.0 3.785ter qu . . . . . 1.0
pounds (lb)kilograms
(kg)
cubic feet
(scf)
cu meters
(nm3)
gallons
(gal)liters (l)
1 pound 1.0 0.4536 13.793 0.3629 0.1475 0.5583
1 kilogram 2.2050 1.0 30.414 0.8001 0.3252 1.2309
1 scf gas 0.0725 0.0329 1.0 0.02628 0.0106 0.0401
1 nm3
gas 2.7500 1.2474 38.040 1.0 0.4056 1.5352
1 gallon liquid 6.7800 3.0750 93.516 2.4605 1.0 3.78501 liter liquid 1.7910 0.8125 24.703 0.6499 0.2642 1.0
A Scf (standard cubic foot) of gas is measured at 1 atmosphere absolute and 70 F.
A Nm3 (normal cubic meter) of gas is measured at 1 atmosphere absolute and 0 C.Liquid is measured at 1 atmosphere absolute and its boiling temperature.
All values are rounded to the nearest 4/5 significant numbers.
OZONE CONVERSION DATA
Weight Gas Liquid
Weight Gas LiquidOzone
Quantity
CarbonMonoxide
Quantity
CARBON MONOXIDE CONVERSION DATA
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pounds
(lb)
kilograms
(kg)
cubic feet
(scf)
cu
meters
(nm3)
gallons
(gal) liters (l)
1 pound 1.0 0.4536 96.71 2.542 0.9593 3.6311 kilogram 2.205 1.0 213.2 5.603 2.115 8.006
1 scf gas 0.01034 0.00469 1.0 0.02628 0.009919 0.03754
1 nm gas 0.3935 0.1785 38.04 1.0 0.3775 1.4289
1 gallon liquid 1.042 0.4728 100.8 2.649 1.0 3.785ter qu . . . . . 1.0
pounds
(lb)
kilograms
(kg)
cubic feet
(scf)
cu
meters
(nm3)
gallons
(gal) liters (l)Lbs H2
1 pound 1 0.4536 192 5.047 1.6928 6.408 5,000.0
1 kilogram 2.205 1 423.3 11.126 3.733 14.128
1 scf gas 0.005209 0.002623 1 0.02628 0.00882 0.03339
1 nm gas 0.19815 0.08988 38.04 1 0.3355 1.2699
1 gallon liquid 0.5906 0.2679 113.41 2.981 1 3.785ter qu . . . . .
Scf (standard cubic foot) gas measured at 1 atmosphere and 70F.
Nm
3
(normal cubic meter) gas measured at 1 atmosphere and 0C.Liquid measured at 1 atmosphere and boiling temperature.
All values rounded to nearest 4/5 significant numbers.
Hydrogen gas values expressed in the stable condition 75% ortho, 25% para.
Hydrogen liquid values expressed in the stable para condition.
Gas Liquid
Weight Gas Liquid
HELIUM CONVERSION DATA
HYDROGEN CONVERSION DATA
Helium
Quantity
HydrogenQuantity
Weight
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Scf H2
960,000
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KRYPTON CONVERSION DATA
pounds kilogramscubic feet
(Scf)
cu
meters
(nm3)
gallons liters
1 pound 1.0 0.4536 4.604 0.12098 0.04967 0.188
1 kilogram 2.205 1.0 10.147 0.2667 0.10939 0.4141
1 Scf gas 0.2172 0.09582 1.0 0.02628 0.010773 0.04078
1 nm3
gas 8.266 3.749 38.04 1.0 0.4101 1.5525
1 gallon liquid 20.13 9.131 92.69 2.436 1.0 3.7851 liter liquid 5.318 2.412 24.51 0.6441 0.2642 1.0
XENON CONVERSION DATA
pounds kilogramscubic feet
(Scf)
cu
meters
(nm3)
gallons liters
1 pound 1.0 0.4536 2.93 0.07692 0.03921 0.1484
1 kilogram 2.205 1.0 6.451 0.16958 0.08642 0.3271
1 Scf gas 0.3416 0.15495 1.0 0.02628 0.013392 0.05069
1 nm3
gas 13 5.897 38.04 1.0 0.5096 1.9291
1 gallon liquid 25.51 11.572 74.67 1.9623 1.0 3.7851 liter liquid 6.738 3.056 19.726 0.5185 0.2642 1.0
A Scf (standard cubic foot) of gas is measured at 1 atmosphere and 70 F.
A Nm3 (normal cubic meter) of gas is measured at 1 atmosphere and 0 C.
Liquid volume is measured at 1 atmosphere and its boiling temperature.
All values are rounded to the nearest 4/5 significant numbers.
Krypton
Quantity
Xenon Quantity
Weight Gas Volume Liquid volume
Weight Gas Volume Liquid Volume
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VELOCITY CONVERSION FACTORS
Multiply By To Obtain
0.01136 Miles/hour
0.01829 Kilometers/hour0.508 Centimeters/second
0.01667 Feet/second
0.6818 Miles per hour
1.097 Kilometers per hour
30.48 Centimeters per second
0.3048 Meters per second
0.5921 Knots
3.281 Feet per second
2.237 Miles per second
3.6 Kilometers per hour
1.467 Feet per second
0.447 Meters per second
1.609 Kilometers per hour0.8684 Knots
MISCELLANEOUS CONVERSION FACTORS
Multiply By To Obtain
Atmospheres 33.94 Feet of H2O (x 12 = Inches of H2O)
Atmospheres 29.92 Inches of mercury
Atmospheres 14.696 Pounds per square inch
Barrels (oil) 5.6146 Cubic feetBarrels (oil) 42 Gallons
Barrels/hour 0.7 Gallons per minute
Cubic feet 0.1781 Barrels
Cubic feet 7.4805 Gallons (U.S.)
Feet 0.3048 Meters
Feet of water at 60F 0.4331 Pounds per square inch
Feet per second 0.68182 Miles per hour
Gallons (U.S.) 0.02381 Barrels
Gallons (U.S.) 0.1337 Cubic feet
Gallons (U.S.) 231 Cubic inches
Gallons per minute 1.429 Barrels per hour Part/million 8.337 Pounds per million gallons
Lbf/square inch 2.309 Feet of water at 60F (x 12 = inches of H2O)
Lbf/square inch 2.036 Inches of mercury at 32 F
Lbm/million gallons 0.11982 Parts (Mass) per million
Water (U.S. gallon) 8.3378 Pounds per gallon of water @ 60oF
Water (cubic foot) 62.371 Pounds per cubic feet of water @ 60oF
Feet/Minute
Feet/Second
Meters per Second
Miles/Hour
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lbf/sq in Int'l atm kg/cm2 mm Hg at 32 F in. Hg at 32 F
1 pound/cu in 1.0 1728 231 27.68 27,6801 pound/cu ft -- 1.0 0.1337 0.016 16.019
1 pound/gal 0.00433 7.481 1.0 0.1198 119.83
1 gram/cu cm 0.03613 62.43 8.345 1.0 1,0001 gram/liter -- 0.06243 0.008345 0.001 1.0
PRESSURE CONVERSION FACTORS
lbf/sq in Int'l atm kg/cm2
mm Hg at 32 F in. Hg at 32 F
1 pound/sq in 1.0 0.06804 0.0703 51.713 2.0359
1 int atmosphere 14.696 1.0 1.0333 760 29.921
1 kilogram/sq cm 14.223 0.9678 1.0 735.56 28.958
1 mm Hg (Torr) 0.0193 0.00132 0.00136 1.0 0.0394
1 inch mercury 0.4912 0.0334 0.0345 25.4 1.0
1 foot water 0.4335 0.0295 0.0305 22.418 0.88261 bar 14.5 0.987 1.0198 750.06 29.529
Pressure
Multiply units in left column by proper factor below:
Multiply units in left column by proper facto
DENSITY CONVERSION FACTORS
Pressure
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ft. water at 39.2 F bar
2.307 0.06896
33.9 1.01325
32.81 0.9806
0.0446 0.00133
1.133 0.03386
1.0 0.0298933.455 1.0
below:
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ENERGY CONVERSION FACTORS
ft-lb Btu g-cal Joule kw-hr hp-hr
1 foot -pound 1.0 0.001285 0.3239 1.3558 -- --
1 Btu 778.2 1.0 252 1053.1 -- --
1 gram-calorie 3.088 0.003968 1.0 4.1868 -- --
1 int Joule 0.7376 0.000948 0.2388 1.0 -- --
1 int kilowatt-hour 2,655,000 3412.8 859,845 -- 1.0 1.341orsepower- our , , , -- . .
SPECIFIC ENERGY CONVERSION FACTORS
1 absolute 1.0 0.99984 0.23901 0.23885 0.42993
1 int Joule/gram 1.000165 1.0 0.23904 0.23892 0.43
1 calorie/gram 4.184 4.1833 1.0 0.99935 1.7988
1 int calorie/gram 4.1867 4.186 1.00065 1.0 1.8tu . . . . .
POWER CONVERSION FACTORS
p watt w tu m n tu r t- sec t- m n1 horsepower 1.0 745.7 0.7457 42.41 2,545 550 33,000
1 watt -- 1.0 0.001 0.057 3.412 0.7376 44.25
1 kilowatt 1.341 1,000 1.0 56.87 3412.1 737.6 44,254
1 Btu per minute -- -- -- 1.0 60 12.97 778.2metr c p . . . . , . . .
Multiply units in left column by proper factor below:
Multiply units in left column by proper factor below:
Power (rate of
energy use)
Energy
absolute
Joule/g
int
Joule/g cal/g int cal/g Btu/lb
Specific Energy
Multiply units in left column by proper factor below:
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g-ca sec metr c p178 1.014
0.2388 0.00136
238.8 1,360
4.199 0.0239. .
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AREA CONVERSION FACTORS
sq in sq ft acre sq mile sq cm sq m hectare
1 sq inch 1.0 0.0069 -- -- 6.452 -- --
1 sq foot 144 1.0 -- -- 929 0.0929 --
1 acre -- 43.56 1.0 0.001563 -- 4047 0.4047
1 sq mile -- 27,878,400 640 1.0 -- 2,590,000 259
1 sq centimeter 0.155 0.001076 -- -- 1.0 0.0001 --
1 sq meter 1550 10.76 0.000247 -- 1 0.000 1.0 --ectare -- -- . -- -- .
VOLUME CONVERSION FACTORS
cu in cu ft cu yd cu cm cu meter liter US gallon
1 cu inch 1.0 -- -- 16.387 -- 0.0164 0.00433
1 cu foot 1,728 1.0 0.037 28.317 0.0283 28.32 7.481
1cu yard 46.656 27 1.0 -- 0.7646 764.6 202
1 cu centimeter 0.061 -- -- 1.0 -- 0.001 --
1 cu meter 61.024 35.31 1.308 1,000,000 1.0 1,000 264.2
1 liter 61.024 0.0353 -- 1,000 0.001 1.0 0.2642
1 US gallon 231 0.1337 -- 3,785.4 -- 3.785 1.0mper a ga on . . -- , . -- . .
Multiply units in left column by proper factor below:
Volume
AreaMultiply units in left column by proper factor below:
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Imp
gallon
--
6.229
168.2
--
220
0.22
0.8327.
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LENGTH CONVERSION FACTORS
inch ft yd mile mm cm m km
1 inch 1.0 0.0833 0.0278 -- 25.4 2.54 0.0254 --
1 foot 12 1.0 0.3333 -- 304.8 30.48 0.3048 --
1 yard 36 3 1.0 -- 914.4 91.44 0.9144 --
1 mile -- 5,280 1760 1.0 -- -- 1,069.3 1.609
1 millimeter 0.0394 0.0033 -- -- 1.0 0.1 0.001 --
1 centimeter 0.3937 0.03281 0.0109 -- 10 1.0 0.01 --
1 meter 39.37 3.281 1.094 -- 1,000 100 1.0 0.001ometer -- , . -- -- , .
WEIGHT CONVERSION FACTORS
grain oz lb ton gram kgmetric
ton
1 grain 1.0 -- -- -- 0.0648 -- --
1 ounce 437.5 1.0 0.0625 -- 28.35 0.02835 --
1 pound 7,000 16 1.0 0.0005 453.6 0.4536 --
1 ton -- 32,000 2,000 1.0 -- 907.2 0.9072
1 gram 15.43 0.0353 -- -- 1.0 0.001 --
1 kilogran -- 35.274 2.205 -- 1,000 1.0 0.0011 metric ton -- 35,274 2,205 1.102 -- 1,000 1.0
Multiply units in left column by proper factor below:
1 micron = 0.001 millimeter
Length
Multiply units in left column by proper factor below:
Weight
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scf/mo
(millions)ton/day
scf/mo
(millions)ton/day
scf/mo
(millions)ton/day
1 1.38 1 1.21 1 0.087
2 2.76 2 2.42 2 0.174
3 4.14 3 3.62 3 0.26
4 5.52 4 4.83 4 0.35
5 6.9 5 6.04 5 0.43
6 8.28 6 7.25 6 0.52
7 9.66 7 8.45 7 0.61
8 11.04 8 9.66 8 0.69
9 12.42 9 10.87 9 0.7810 13.8 10 12.08 10 0.87
20 27.59 20 24.15 20 1.74
30 41.39 30 36.23 30 2.6
40 55.19 40 48.3 40 3.4750 69.98 50 60.38 50 4.34
ton/day scf/mo (millions) ton/day scf/mo (millions) ton/day scf/mo (millions)
10 7.25 10 8.28 10 115.2
12.5 9.06 12.5 10.35 12.5 114
25 18.12 25 20.7 25 288
50 36.24 50 41.41 50 575
75 54.36 75 62.11 75 864
100 72.5 100 82.82 100 1.152
TONNAGE CONVERSION FACTORS*
1 lb gaseous oxygen =
12.08 scf@ 14.7 psia and 70 F
1 ton gaseous oxygen =
13.80 scf@ 14.7 psia and 70 F
383,950 scf@ 14.7 psia and 70 F
*Based on a 30-day month.
Oxygen Nitrogen Hydrogen
1 lb gaseous hydrogen =
192.0 scf@ 14.7 psia and 70 F
1 ton gaseous hydrogen =
24,160 scf@ 14.7 psia and 70 F
1 lb gaseous nitrogen =
1 ton gaseous nitrogen =
27,605 scf@ 14.7 psia and 70 F
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TONNAGE CONVERSION CHART
To obtain values for plants of larger size, multiply each value by the same factor.
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This table is taken fro
is badly presented dat
The table is now label
Dew
Point (oF)
PPM H2O
(Volume)
Percent
Volume
H2O
Dew
Point (oF)
PPM H2O
(Volume)
Percent
Volume
H2O
, . - , .
82 37,432 3.7432 -5 970 0.097
81 36,138 3.6138 -6 920 0.092
80 34,844 3.4844 -7 870 0.087
79 33,842 3.3842 -8 820 0.082 -130 -9078 32,840 3.284 -9 780 0.078 -120 -84
77 31,838 3.1838 -10 740 0.074 -110 -7976 30,836 3.0836 -11 700 0.07 -105 -76
75 29,833 2.9833 -12 660 0.066 -104 -76
74 28,831 2.8831 -13 630 0.063 -103 -75
73 27,829 2.7829 -14 590 0.059 -102 -74
72 26,827 2.6827 -15 560 0.056 -101 -74
71 25,825 2.5825 -16 530 0.053 -100 -7370 25,057 2.5057 -17 500 0.05 -99 -73
69 24,290 2.429 -18 475 0.0475 -98 -72
68 23,522 2.3522 -19 448 0.0448 -97 -72
67 22,755 2.2755 -20 422 0.0422 -96 -71
66 21,987 2.1987 -21 400 0.04 -95 -71
65 21,220 2.122 -22 378 0.0378 -94 -70
64 20,452 2.0452 -23 359 0.0359 -93 -69
63 19,685 1.9685 -24 330 0.033 -92 -69
62 18,917 1.8917 -25 317 0.0317 -91 -68
61 18,336 1.8336 -26 300 0.03 -90 -6860 17,754 1.7754 -27 283 0.0283 -89 -67
59 17,174 1.7174 -28 265 0.0265 -88 -6758 16,593 1.6593 -29 250 0.025 -87 -66
57 16,011 1.6011 -30 235 0.0235 -86 -66
56 15,430 1.543 -31 222 0.0222 -85 -65
55 14,849 1.4849 -32 210 0.021 -84 -64
54 14,268 1.4268 -33 196 0.0196 -83 -64
53 13,687 1.3687 -34 105 0.0105 -82 -63
52 13,329 1.3329 -35 174 0.0174 -81 -63
51 12,971 1.2971 -36 164 0.0164 -80 -6250 12,613 1.2613 -37 153 0.0153 -79 -62
49 12,255 1.2255 -38 144 0.0144 -78 -61
48 11,898 1.1898 -39 136 0.0136 -77 -61
47 11,540 1.154 -40 128 0.0128 -76 -60
46 11,182 1.1182 -41 119 0.0119 -75 -5945 10,824 1.0824 -42 113 0.0113 -74 -5944 10,466 1.0466 -43 105 0.0105 -73 -58
43 10,068 1.0068 -44 98 0.0098
42 9,670 0.967 -45 92 0.0092
41 9,272 0.9272 -46 87 0.0087 Air Products published
40 8,874 0.8874 -47 82 0.0082
39 8,475 0.8475 -48 76 0.0076
DEWPOINT TO PPM CONVERSION TABLE
Con
Dew Point VS. Pa
Dew Point
F C
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38 8,077 0.8077 -49 72 0.0072
37 7,679 0.7679 -50 67 0.0067 Moisture content in pu
36 7,281 0.7281 -51 62 0.0062 use the following table:35 6,883 0.6883 -52 59 0.0059 *At 1 atmosphere pr34 6,633 0.6633 -53 55 0.0055
33 6,383 0.6383 -54 51 0.005132 6,133 0.6133 -55 48 0.0048
31 5,883 0.5883 -56 44.6 0.00446
30 5,633 0.5633 -57 41.8 0.00418
29 5,383 0.5383 -58 39.0 0.0039
28 5,133 0.5133 -59 36.5 0.00365
27 4,883 0.4883 -60 34.0 0.0034
26 4,633 0.4633 -61 31.7 0.00317
25 4,453 0.4453 -62 29.4 0.00294
24 4,274 0.4274 -63 27.5 0.00275
23 4,094 0.4094 -64 25.6 0.0025622 3,915 0.3915 -65 23.6 0.00236
21 3,735 0.3735 -66 22.1 0.00221
20 3,556 0.3556 -67 20.6 0.00206
19 3,376 0.3376 -68 19.2 0.00192
18 3,197 0.3197 -69 17.9 0.00179
17 3,017 0.3017 -70 16.6 0.00166
16 2,897 0.2897 -71 15.4 0.00154
15 2,776 0.2776 -72 14.3 0.00143
14 2,656 0.2656 -73 13.3 0.00133
13 2,535 0.2535 -74 12.3 0.00123
12 2,415 0.2415 -75 11.4 0.00114
11 2,294 0.2294 -76 10.5 0.00105
10 2,174 0.2174 -77 9.8 0.00098
9 2,053 0.2053 -78 9.1 0.00091
8 1,933 0.1933 -79 8.4 0.00084
7 1,854 0.1854 -80 7.8 0.00078
6 1,775 0.1775 -81 7.2 0.00072
5 1,695 0.1695 -82 6.6 0.00066
4 1,616 0.1616 -83 6.2 0.00062
3 1,537 0.1537 -84 5.7 0.00057
2 1,458 0.1458 -85 5.3 0.00053
1 1,378 0.1378 -86 4.78 0.000478
0 1,299 0.1299 -87 4.50 0.00045
-1 1,220 0.122 -88 4.15 0.000415
-2 1,153 0.1153 -89 3.84 0.000384
-3 1,087 0.1087 -90 3.53 0.000353
73
72
76
75
74
79
78
77
82
81
80
85
84
83
88
87
86
91
90
89
94
93
92
97
96
95
100
99
98
103
102
101
110
105
104
Dew Point*,oF
130
120
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39
42
41
40
45
44
43
48
47
46
51
50
49
54
53
52
57
56
55
60
59
58
64
63
62
67
66
65
70
*10,000 PPM = 1.0% 69
68
71
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an Air Liquide Website and shows that the PPM in Gas Data Book
because it failed to identify the PPM as Volumetric Basis - not Mass.
d accurately in this worksheet. (Art M. 05/06/03)
Moisture
This is yet another sad example of sloppy and un-specific
engineering that seems to populate even the most
0.10 serious and large technological business companies
0.25 world-wide.
0.63
1.00 ALL published or communicated engineering data should
1.06 be clearly and accurately labeled as to specific units
1.18 as well as significatnt figures.
1.29
1.40
1.531.66
1.81
1.96
2.15
2.35
2.54
2.76
3.00
3.28
3.53
3.84
4.154.50
4.78
5.3
5.7
6.2
6.6
7.2
7.8
8.4
9.1
9.8
10.5
11.4
12.3
13.3
the following Dew Point conversion data in their Website:
ersion Table
ts Per Million Moisture (Vol.)
ppm
(vol/vol)
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e gases. To convert parts per million by volume of water vapor to dew point,
ssure.
13.3
14.3
10.5
11.4
12.3
8.4
9.19.8
6.6
7.2
7.8
5.3
5.7
6.2
4.154.50
4.78
3.28
3.53
3.84
2.54
2.76
3.00
1.96
2.15
2.35
1.53
1.66
1.81
1.18
1.29
1.40
0.63
1.00
1.08
ppm, Vol/Vol
0.100.25
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136
113
119
128
92
98
105
76
82
87
62
67
71
51
55
59
41.8
44.6
48
34.0
36.5
39.0
25.6
27.5
29.4
20.6
22.1
23.6
16.6
17.9
19.2
15.4
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Calibrated ForSpecific
GravityAir D.A. Argon
Endo or
AmmoniaHelium Hydrogen
Natural
GasNitrogen Oxygen Propane
ir 1 1 1.841 0.851 1.302 2.692 3.793 1.24 1.021 0.951 0.811
ry Air (D.A.) 0.295 0.543 1 0.462 0.707 1.462 2.06 0.674 0.554 0.517 0.44
rgon 1.38 1.175 2.163 1 1.529 3.162 4.456 1.457 1.199 1.118 0.952
ndo or Ammonia 0.59 0.768 1.414 0.654 1 2.068 2.914 0.953 0.784 0.731 0.623elium 0.138 0.371 0.684 0.316 0.484 1 1.409 0.461 0.379 0.353 0.301
ydrogen 0.0695 0.264 0.485 0.224 0.343 0.71 1 0.387 0.269 0.251 0.214
atural Gas 0.65 0.806 1.484 0.686 1.05 2.17 3.058 1 0.823 0.767 0.654
itrogen 0.96 0.98 1.804 0.834 1.276 2.638 3.717 1.215 1 0.932 0.794
Oxygen 1.105 1.051 1.935 0.895 1.369 2.83 3.987 1.304 1.073 1 0.852
ropane 1.522 1.234 2.271 1.05 1.606 3.321 4.68 1.53 1.259 1.174 1
0 0.5 1 2 3 4 5 10 15 20 30 40
0.5 1.01 1 0.98 0.95 0.93 0.9 0.88 0.78 0.71 0.66 0.58 0.5
1 1.03 1.02 1 0.97 0.94 0.92 0.89 0.8 0.73 0.67 0.59 0.5
2 1.06 1.05 1.03 1 0.97 0.94 0.92 0.82 0.75 0.69 0.61 0.5
3 1.1 1.08 1.06 1.03 1 0.97 0.95 0.85 0.77 0.71 0.63 0.5
4 1.13 1.11 1.09 1.06 1.03 1 0.97 0.87 0.79 0.73 0.65 0.5
5 1.16 1.14 1.12 1.09 1.05 1.03 1 0.89 0.81 0.75 0.66 0.
10 1.3 1.27 1.25 1.22 1.18 1.15 1.12 1 0.91 0.84 0.74 0.6
15 1.42 1.4 1.38 1.33 1.29 1.26 1.23 1.1 1 0.92 0.82 0.7
20 1.53 1.51 1.49 1.44 1.4 1.36 1.33 1.18 1.08 1 0.88 0.
30 1.75 1.71 1.69 1.64 1.59 1.55 1.51 1.34 1.22 1.13 1 0.
40 1.93 1.9 1.87 1.81 1.76 1.71 1.67 1.49 1.36 1.25 1.11 1
50 2.1 2.06 2.03 1.97 1.91 1.86 1.81 1.62 1.47 1.36 1.2 1.0
Actual PSIG
METERED GAS CONVERSION FACTORS
Calibration Pressure
xample: If the flowmeter is calibrated for air and argon is being metered, multiply the reading with 0.851 to get the actual argon flow. If the
ctual pressure is different from the calibration pressure, use the correction factor from the calibration pressure chart.
AS CONVERSION FACTORS
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onversion factor = (P actual + 14.7/P cal + 14.7)0.5
P actual = actual pressure, psig
P cal = calibrated pressure, psig
xample: If the flowmeter is calibrated for 50 psig and the actual pressure is 10 psig, multiply the reading with 0.62 to get the actual flow. If in addition, the
alibrated for a different gas than the gas being measured, multiply this number with the correction factor from the metered gas conversion factor.
Where:
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50
0.48
0.49
0.51
0.52
0.54
0.55
0.62
0.68
0.73
0.83
0.92
1
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er is
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Gross Net O2 + N2 = Air CO2 H2O N2
Carbon solid C 12.011 14,093 14,093 2.664 8.863 11.527 3.664 -- 8.863
Hydrogen H2 2.016 61,100 51,623 7.9 26.407 34.344 -- 8.937 26.407
Carbon monoxide CO 28.010 4,347 4,347 0.6 1.9 2.471 1.571 -- 1.9
Methane CH4 16.043 23,879 21,520 4 13.257 17.265 2.744 2.246 13.275Ethane C2H6 30.070 22,320 20,432 3.7 12.394 16.119 2.927 1.798 12.394
Propane C3H8 44.097 21,661 19,994 3.6 12.074 15.703 2.994 1.634 12.074
Ethylene C2H4 28.054 21,644 20,295 3.4 11.385 14.807 3.138 1.285 11.385
Propylene C3H6 42.081 21,041 19,691 3.4 11.385 14.807 3.138 1.285 11.385
Acetylene C2H2 26.038 21,500 20,776 3.1 10.224 13.297 3.381 0.692 10.224
Gross Net O2 + N2 = Air CO2 H2O N2
Hydrogen H2 2.016 325 275 0.5 1.882 2.382 -- 1 1.882
Carbon monoxide CO 28.010 322 322 0.5 1.882 2.382 1 -- 1.882
Methane CH4 16.043 1,013 913 2 7.528 9.528 1 2 7.528
Ethane C2H6 30.070 1,792 1,641 3.5 13.175 16.675 2 3 13.175
Propane C3H8 44.097 2,590 2,385 5 18.821 23.821 3 4 18.821
Ethylene C2H4 28.054 1,614 1,513 3 11.293 14.293 2 2 11.293
Propylene C3H6 42.081 12,336 2,186 4.5 16.939 21.439 3 3 16.939
Acetylene 2 2 26.038 1,499 1,448 2.5 9.411 11.911 2 1 9.411
Mol
WeightSymbol Btu per cu ft @ 60F Required for Combustion
Heat of Combustion Cubic Feet per Cubic Feet of Combustible Gas
Products of CombustionName of Gas
COMBUSTION CONSTANTS OF HYDROCARBON GASES (VOLUME BASIS)
Name of Gas
COMBUSTION CONSTANTS OF HYDROCARBON GASES (WEIGHT BASIS)
Mol
WeightSymbol
Heat of Combustion
Btu per Lb
Pound per Pound of Combustible Gas
Required for Combustion Products of Combustion
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No. 2 Fuel Oil 0.1 86.8 13 -- 7.18 19,214 138,000 14.46 1,381 291No. 4 Fuel Oil 0.3 87.6 12 0.1 7.6 18,821 143,000 14.22 1,437 302
No. 6 Fuel Oil 0.5 88.2 11 0.3 8.15 18,400 150,000 13.96 1,513 319
Air
required
9.56
scf/ft3
Air
required
136 scf/lb
10.22----8Bituminous Coal 1.78
COMBUSTION REQUIREMENTS OF TYPICAL FUELS
Name of Fuel% S % C % H % Ash
Analysis Required for Combustion
Btu/galnet Btu/lblbs/gas lbs Air/lbscf
Air/galscf O2/gal
Heat of Combustion
5
O2required 2
scf/ft3
75.3
Natural Gas CH4 90%; C2H6 5%1,000
Btu/ft3
Specific
Grav. 0.6
13,500
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Kw In Out Volts Amps BCLb/Hr
CO2
Scfh N2,
O2, A
15 0.75" 0.75" 220/440 40/20 6 375 4,00030 0.75" 0.75" 220/440 80/40 8
1/8 750 7,500
45 0.75" 0.75" 220/440 120/60 101/4 1,125 11,500
60 0.75" 0.75" 220/440 160/80 13 1,500 15,000
75 0.75" 1" 220/440 200/100 151/4 1,875 19,000
90 0.75" 1" 440 120 171/2 2,250 22,500
105 0.75" 1" 440 140 193/4 2,625 26,500
120 0.75" 1" 440 160 22 3,000 30,000
135 1" 1" 440 180 241/8 3,375 33,750
150 1" 11/2" 440 200 26
3/8 3,750 37,500
165 1" 11/2" 440 220 28
1/2 4,125 41,500
180 1" 11/2" 440 240 30
3/4 4,500 45,000
195 1"1
1
/2"440 260 33 4,875 49,000
250 Max
15 Min
250 Max15 Min
*Gap or space between the extrusions is 5" for improved resistance to ice bridging.
STEAM VAPORIZER SPECIFICATIONS
AMBIENT VAPORIZER SPECIFICATIONS
ELECTRIC VAPORIZER SPECIFICATIONS (for vaporizing stored Liquefied Gases)
Flow scfh Fluid
3" 300 lb
ANSI Flange 1,400
2" Female
Pipe
Steam
Pressure
Steam
Inlet psig
50,000 N2/O2 500
1" Mueller
Flange
2" Mueller
Flange 700
2" Female
Pipe
MAWP
psigN2 Inlet N2 Outlet Required
100,000 N2/O2 500
1.5" Mueller
Flange
Rating -- 8 Hr
Rating --
Continuous
A2SSEG-10X1 23 x 10 x 165
23 x 23 x 165
23 x 36 x 165
Model Dimension, inches
2,000 scfh
2,400 scfh
23 x 49 x 165
23 x 62 x 165
36 x 49 x 165
A4SSEG-10X1
A6SSEG-10X1
A8SSEG-10X1
A10SSEG-10X1
A12SSEG-10X1
4,800 scfh
A16SSEG-10X1 49 x 49 x 165
A30SSEG-10X1
400 scfh1,428 scfh
2,856 scfh 800 scfh
1,200 scfh
1,600 scfh
A36SSEG-10X1
49 x 75 x 165
62 x 75 x 16575 x 75 x 165 25,704 scfh
3,200 scfh
49 x 62 x 165A20SSEG-10X1
A24SSEG-10X1
4,000 scfh
6,000 scfh7,200 scfh
4,284 scfh
5,712 scfh
7,140 scfh
8,568 scfh
11,424 scfh
14,280 scfh
17,136 scfh
21,420 scfh
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Wt lbs
100150
180
210
240
275
310
345
375
405
440
575
605
Fluid Fluid
Inlet Outlet
Condensate
Out
2" Male Pipe 320 F 70 F
2" Male Pipe 320 F 70 F
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Art Montemayor LCO2 Vaporization March 15, 2004
Rev: 0Hi Montemayor, 15-Mar-04
Thank you very much for your reply. Your willingness to help is greatly appreciated.
The problem we deal with is CO2 supply for carbonated beverage bottling facility with several bottling
lines, and varying working regime.
The normal CO2 consumption is 3,000 Kg/Hr, but we have to take into account peak loads of
4,800 Kg/Hr and lowest load of 1,200 Kg/Hr.
Liquid CO2 source is @ -20 C (19.25 Bar a). [-4oF & 264.4 psig]
Gaseous CO2 min. temp. supply requirement is @ 0 C.
Water source is 100 CU.M (26,406 gallons) treated water storage tank. This is an external, not insulated
tank, thus its temp. is effected by the ambient temp. The a.m. tank is foodstuff grad, so using of antifreeze
is not permitted. (What is "a.m. tank"??)
Preference of water heating is for energy saving considerations, and the experience of steam heating for
this application is very troublous (and nearest steam source available is 200 MTR away).
Average water supply temp. is 14 C, lowest winter temp. is 10 C, max. temp. is 28 C.
Water supply circulation pump: 70 CU.M/Hr(308 gpm).
As I've mentioned before, my concern is of water freezing and ice accumulation on external tube surface.
Another question is whether flow rate reduction is permitted when CO2 consumption is at its lower level?
(In case CO2 consumption is stopped, water circulation remains, and CO2 space is drained off).
I hope now you can have the full information needed in order to handle this problem.
Excel Workbook you suggest for Industrial Gas data and information is most interesting to me for both
this job and other jobs we have.
My address is: [email protected]
Once again, thank you very, very much for your assistance!
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Art Montemayor LCO2 Vaporization March 15, 2004
Rev: 0
Vaporizer Control Operation:
1. LCO2 automatic valve opens when storage tank pressure is less than pre-set value (19.25 barA)
2. Water heat sink source is constantly circulating a minimum of 285 gpm of water at
50 oC. This water exits the vaporizer at 41 oF and is circulated to a heating source prior to being
circulated at the required 50oF MINIMUM.
3. The vaporized LCO2 is vented directly back to the storage tank vapor space and the gaseous
consumption is derived from the common pipe joining the vaporizer and the storage tank.
If the gaseous CO2 demand decreases, the storage tank pressure starts to increase and the pressure
controller on the LCO2 block valve activates the actuator on the block valve, shutting LCO2 flow
to the vaporizer. Storage tank pressue ceases to increase.
4. Upon subsequent gaseous CO2 demand increase, storage tank pressure starts to decrease and
the pressure controller opens the LCO2 block valve to the vaporizer, initiating vaporization and an
increase in gaseous CO2 availability for the consumption.
5. The vaporizer coil must be physically and mechanically situated at a lower level than the lowest
LCO2 tank level in order to have gravity flow to the coil. The coil must be allowed to freely vaporize
LCO2 and return the product vapor directly back to the tank vapor space. The LCO2 block valvemust have bubble-tight capability to positively shut-off LCO2 supply when required. The heating
water source must be available at the design rate 100% of the time that vaporization is required.
Water source @ 50 oFWater overflow
@ 41 oF
Liquid CO2 Storage Tank
PC
To BottlingMachineconsumption
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Art Montemayor LCO2 Vaporization March 15, 2004
Rev: 0
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Art Montemayor LCO2 Vaporization March 15, 2004
Rev: 0
308 gpm
4,800 kg/hr = 10,560 lb/hr
121.57 Btu/lb @ -4.3 oF & 284.7 psia, saturated liquid
1,283,737 Btu/hr
Design water inlet temperature = 10oC = 50
oF
5oC = 41
oF
W = Water rate, lb/hr
Cp = 1.00 Btu/lb -oF
DT = 9oF
W = 142,637 lb/hr = 285 gpm
Water Storage tank capacity = 26,406 gallons
93 minutesVaporizer time available =
Heating water rate available =
Vaporizer Heat Load =
LCO2 Latent Heat of Vaporization =
LCO2 Design vaporization rate =
Design water outlet temp. =
TCp
QW
TCpWQ
D
D
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Art Montemayor LCO2 Vaporization March 15, 2004
Rev: 0
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Art Montemayor LCO2 Vaporization March 15, 2004
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Art Montemayor NIST Thermodynamic Values for Saturated C
-109.40 14.696 97.560 0.010250 -64.111 -0.13031 0.17575
-100.00 22.310 96.900 0.010320 -61.211 -0.12201 0.26316
-68.98 76.696 73.463 0.013612 35.291 35.484 0.12701 0.23713 0.46671 3123.9 0.87775
-67.91 78.696 73.329 0.013637 35.79 35.989 0.12829 0.23627 0.46701 3112.2 0.89960
-66.85 80.696 73.196 0.013662 36.279 36.484 0.12953 0.23545 0.46730 3100.6 0.92145
-65.81 82.696 73.065 0.013686 36.76 36.970 0.13076 0.23468 0.46757 3089.2 0.94329
-64.80 84.696 72.936 0.013711 37.232 37.447 0.13195 0.23394 0.46783 3078.0 0.96513
-63.80 86.696 72.809 0.013735 37.696 37.917 0.13313 0.23325 0.46808 3066.9 0.98697
-62.82 88.696 72.683 0.013758 38.152 38.379 0.13428 0.23259 0.46832 3056.1 1.0088
-61.85 90.696 72.560 0.013782 38.601 38.833 0.13541 0.23196 0.46855 3045.4 1.0306
-60.90 92.696 72.437 0.013805 39.042 39.280 0.13652 0.23136 0.46877 3034.8 1.0525
-59.97 94.696 72.317 0.013828 39.477 39.719 0.13760 0.23079 0.46899 3024.4 1.0743
-59.05 96.696 72.197 0.013851 39.904 40.153 0.13867 0.23025 0.46920 3014.1 1.0961
-58.14 98.696 72.080 0.013874 40.326 40.579 0.13972 0.22974 0.46940 3004.0 1.1180
-57.25 100.7 71.963 0.013896 40.741 41.000 0.14076 0.22924 0.46961 2993.9 1.1398
-56.37 102.7 71.848 0.013918 41.149 41.414 0.14177 0.22878 0.46981 2984.0 1.1616
-55.50 104.7 71.735 0.013940 41.552 41.823 0.14277 0.22833 0.47001 2974.2 1.1835
-54.65 106.7 71.622 0.013962 41.95 42.226 0.14375 0.22790 0.47021 2964.5 1.2053
-53.81 108.7 71.511 0.013984 42.342 42.623 0.14472 0.22750 0.47042 2954.9 1.2272
-52.98 110.7 71.402 0.014005 42.728 43.016 0.14567 0.22711 0.47062 2945.4 1.2490
-52.16 112.7 71.293 0.014027 43.11 43.403 0.14661 0.22674 0.47082 2936.1 1.2709
-51.35 114.7 71.185 0.014048 43.487 43.785 0.14753 0.22638 0.47102 2926.8 1.2928
-50.55 116.7 71.079 0.014069 43.858 44.163 0.14844 0.22605 0.47123 2917.5 1.3147
-49.76 118.7 70.974 0.014090 44.225 44.535 0.14934 0.22572 0.47144 2908.4 1.3366
-48.98 120.7 70.870 0.014110 44.588 44.904 0.15022 0.22541 0.47165 2899.4 1.3585
-48.21 122.7 70.767 0.014131 44.946 45.268 0.15110 0.22512 0.47187 2890.4 1.3804
-47.46 124.7 70.665 0.014151 45.3 45.627 0.15196 0.22484 0.47209 2881.6 1.4023
-46.71 126.7 70.564 0.014172 45.65 45.983 0.15280 0.22457 0.47232 2872.7 1.4242
-45.96 128.7 70.464 0.014192 45.996 46.335 0.15364 0.22431 0.47254 2864.0 1.4461
-45.23 130.7 70.364 0.014212 46.338 46.682 0.15447 0.22406 0.47278 2855.4 1.4681
-44.51 132.7 70.266 0.014232 46.676 47.026 0.15528 0.22382 0.47302 2846.8 1.4900
-43.79 134.7 70.169 0.014251 47.011 47.367 0.15609 0.22360 0.47326 2838.3 1.5120
-43.08 136.7 70.072 0.014271 47.342 47.703 0.15689 0.22338 0.47351 2829.8 1.5340
-42.38 138.7 69.977 0.014290 47.669 48.036 0.15767 0.22318 0.47376 2821.4 1.5560
-41.69 140.7 69.882 0.014310 47.993 48.366 0.15845 0.22298 0.47402 2813.1 1.5780
-41.00 142.7 69.788 0.014329 48.314 48.693 0.15922 0.22279 0.47428 2804.8 1.6000
-40.32 144.7 69.695 0.014348 48.631 49.016 0.15997 0.22261 0.47455 2796.6 1.6221
-39.65 146.7 69.602 0.014367 48.946 49.336 0.16072 0.22244 0.47483 2788.5 1.6441
-38.98 148.7 69.511 0.014386 49.257 49.653 0.16146 0.22227 0.47511 2780.4 1.6662
-38.32 150.7 69.420 0.014405 49.565 49.968 0.16220 0.22211 0.47539 2772.3 1.6883-37.67 152.7 69.329 0.014424 49.871 50.279 0.16292 0.22196 0.47569 2764.4 1.7104
-37.02 154.7 69.240 0.014443 50.173 50.587 0.16364 0.22182 0.47599 2756.4 1.7325
-36.38 156.7 69.151 0.014461 50.473 50.893 0.16435 0.22168 0.47629 2748.5 1.7546
-35.75 158.7 69.063 0.014480 50.77 51.196 0.16505 0.22155 0.47660 2740.7 1.7767
-35.12 160.7 68.975 0.014498 51.065 51.496 0.16575 0.22142 0.47692 2732.9 1.7989
-34.50 162.7 68.888 0.014516 51.356 51.794 0.16643 0.22130 0.47724 2725.2 1.8211
-33.88 164.7 68.802 0.014534 51.646 52.089 0.16711 0.22118 0.47757 2717.5 1.8433
-33.27 166.7 68.717 0.014553 51.933 52.382 0.16779 0.22107 0.47790 2709.9 1.8655
-32.67 168.7 68.631 0.014571 52.217 52.672 0.16846 0.22097 0.47824 2702.3 1.8877
-32.07 170.7 68.547 0.014589 52.499 52.960 0.16912 0.22087 0.47859 2694.8 1.9100
-31.47 172.7 68.463 0.014606 52.779 53.246 0.16977 0.22077 0.47894 2687.3 1.9322
-30.88 174.7 68.380 0.014624 53.056 53.530 0.17042 0.22068 0.47930 2679.8 1.9545
-30.29 176.7 68.297 0.014642 53.332 53.811 0.17106 0.22060 0.47966 2672.4 1.9768
-29.71 178.7 68.215 0.014660 53.605 54.090 0.17170 0.22051 0.48003 2665.0 1.9991
Temperature
(F)
Pressure
(psia)
Density(l)
(lbm/ft3)
Volume(l)
(ft3/lbm)
Cp(l)
(BTU/lbm*R)
Sound Spd.(l)
(ft/s)
Density(v)
(lbm/ft3)
Internal Energy(l)
(BTU/lbm)
Enthalpy(l)
(BTU/lbm)
Entropy(l)
(BTU/lbm*R)
Cv(l)
(BTU/lbm*R)
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Art Montemayor NIST Thermodynamic Values for Saturated C-29.14 180.7 68.133 0.014677 53.876 54.367 0.17233 0.22044 0.48040 2657.7 2.0215
-28.57 182.7 68.052 0.014695 54.145 54.642 0.17295 0.22036 0.48079 2650.4 2.0439
-28.00 184.7 67.971 0.014712 54.412 54.915 0.17357 0.22029 0.48117 2643.2 2.0662
-27.44 186.7 67.891 0.014730 54.677 55.186 0.17419 0.22022 0.48157 2636.0 2.0886
-26.88 188.7 67.811 0.014747 54.939 55.455 0.17480 0.22016 0.48196 2628.8 2.1111
-26.33 190.7 67.732 0.014764 55.201 55.722 0.17540 0.22010 0.48237 2621.7 2.1335
-25.78 192.7 67.653 0.014781 55.46 55.988 0.17600 0.22004 0.48278 2614.6 2.1560
-25.23 194.7 67.575 0.014798 55.717 56.251 0.17659 0.21999 0.48319 2607.5 2.1785
-24.69 196.7 67.497 0.014816 55.973 56.513 0.17718 0.21994 0.48361 2600.5 2.2010
-24.16 198.7 67.419 0.014833 56.227 56.773 0.17777 0.21989 0.48404 2593.5 2.2235
-23.63 200.7 67.342 0.014850 56.479 57.031 0.17835 0.21985 0.48447 2586.5 2.2461
-23.10 202.7 67.266 0.014866 56.729 57.287 0.17892 0.21981 0.48491 2579.6 2.2687
-22.57 204.7 67.189 0.014883 56.978 57.542 0.17949 0.21977 0.48535 2572.7 2.2913
-22.05 206.7 67.113 0.014900 57.225 57.795 0.18006 0.21973 0.48580 2565.9 2.3139
-21.53 208.7 67.038 0.014917 57.47 58.047 0.18062 0.21969 0.48626 2559.0 2.3365
-21.02 210.7 66.963 0.014934 57.714 58.297 0.18118 0.21966 0.48671 2552.3 2.3592
-20.51 212.7 66.888 0.014950 57.957 58.546 0.18173 0.21963 0.48718 2545.5 2.3819
-20.00 214.7 66.814 0.014967 58.197 58.793 0.18228 0.21961 0.48765 2538.8 2.4046
-19.50 216.7 66.740 0.014984 58.437 59.038 0.18282 0.21958 0.48812 2532.1 2.4274
-19.00 218.7 66.666 0.015000 58.675 59.283 0.18337 0.21956 0.48860 2525.4 2.4502
-18.50 220.7 66.593 0.015017 58.911 59.525 0.18390 0.21954 0.48909 2518.8 2.4730
-18.01 222.7 66.520 0.015033 59.146 59.766 0.18444 0.21952 0.48958 2512.2 2.4958
-17.52 224.7 66.448 0.015049 59.38 60.006 0.18497 0.21950 0.49008 2505.6 2.5186
-17.03 226.7 66.376 0.015066 59.612 60.245 0.18549 0.21948 0.49058 2499.1 2.5415
-16.55 228.7 66.304 0.015082 59.843 60.482 0.18602 0.21947 0.49108 2492.5 2.5644
-16.07 230.7 66.232 0.015098 60.073 60.718 0.18653 0.21946 0.49159 2486.1 2.5873
-15.59 232.7 66.161 0.015115 60.301 60.953 0.18705 0.21945 0.49211 2479.6 2.6103-15.12 234.7 66.090 0.015131 60.528 61.186 0.18756 0.21944 0.49263 2473.2 2.6332
-14.65 236.7 66.019 0.015147 60.754 61.418 0.18807 0.21943 0.49316 2466.7 2.6562
-14.18 238.7 65.949 0.015163 60.978 61.649 0.18858 0.21943 0.49369 2460.4 2.6793
-13.71 240.7 65.879 0.015179 61.202 61.879 0.18908 0.21943 0.49422 2454.0 2.7023
-13.25 242.7 65.809 0.015196 61.424 62.107 0.18958 0.21942 0.49476 2447.7 2.7254
-12.79 244.7 65.739 0.015212 61.645 62.335 0.19007 0.21942 0.49531 2441.4 2.7485
-12.34 246.7 65.670 0.015228 61.865 62.561 0.19057 0.21942 0.49586 2435.1 2.7717
-11.88 248.7 65.601 0.015244 62.084 62.786 0.19106 0.21943 0.49641 2428.8 2.7948
-11.43 250.7 65.532 0.015260 62.301 63.010 0.19154 0.21943 0.49697 2422.6 2.8180
-10.98 252.7 65.464 0.015276 62.518 63.233 0.19203 0.21943 0.49754 2416.4 2.8413
-10.53 254.7 65.396 0.015292 62.733 63.455 0.19251 0.21944 0.49810 2410.2 2.8645
-10.09 256.7 65.328 0.015307 62.947 63.676 0.19299 0.21945 0.49868 2404.1 2.8878
-9.65 258.7 65.260 0.015323 63.161 63.895 0.19346 0.21946 0.49926 2397.9 2.9111
-9.21 260.7 65.193 0.015339 63.373 64.114 0.19394 0.21946 0.49984 2391.8 2.9345
-8.77 262.7 65.125 0.015355 63.584 64.332 0.19441 0.21948 0.50043 2385.7 2.9578-8.34 264.7 65.058 0.015371 63.794 64.548 0.19487 0.21949 0.50102 2379.7 2.9812
-7.91 266.7 64.992 0.015387 64.004 64.764 0.19534 0.21950 0.50162 2373.6 3.0047
-7.48 268.7 64.925 0.015402 64.212 64.979 0.19580 0.21951 0.50222 2367.6 3.0281
-7.05 270.7 64.859 0.015418 64.419 65.193 0.19626 0.21953 0.50282 2361.6 3.0516
-6.63 272.7 64.793 0.015434 64.626 65.406 0.19672 0.21954 0.50343 2355.6 3.0751
-6.20 274.7 64.727 0.015450 64.831 65.617 0.19717 0.21956 0.50405 2349.7 3.0987
-5.78 276.7 64.661 0.015465 65.036 65.829 0.19762 0.21958 0.50467 2343.8 3.1223
-5.37 278.7 64.596 0.015481 65.239 66.039 0.19807 0.21960 0.50529 2337.8 3.1459
-4.95 280.7 64.530 0.015497 65.442 66.248 0.19852 0.21962 0.50592 2332.0 3.1695
-4.54 282.7 64.465 0.015512 65.644 66.456 0.19897 0.21964 0.50655 2326.1 3.1932
-4.13 284.7 64.400 0.015528 65.845 66.664 0.19941 0.21966 0.50719 2320.2 3.2169
-3.72 286.7 64.336 0.015543 66.045 66.871 0.19985 0.21968 0.50783 2314.4 3.2407
-3.31 288.7 64.271 0.015559 66.244 67.076 0.20029 0.21970 0.50848 2308.6 3.2645
-2.91 290.7 64.207 0.015575 66.442 67.281 0.20073 0.21973 0.50913 2302.8 3.2883
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Art Montemayor NIST Thermodynamic Values for Saturated C-2.50 292.7 64.143 0.015590 66.64 67.486 0.20116 0.21975 0.50979 2297.0 3.3121
-2.10 294.7 64.079 0.015606 66.837 67.689 0.20159 0.21978 0.51045 2291.3 3.3360
-1.70 296.7 64.015 0.015621 67.033 67.892 0.20202 0.21980 0.51111 2285.5 3.3599
-1.31 298.7 63.952 0.015637 67.228 68.094 0.20245 0.21983 0.51178 2279.8 3.3838
-0.91 300.7 63.888 0.015652 67.423 68.295 0.20287 0.21986 0.51245 2274.1 3.4078
-0.52 302.7 63.825 0.015668 67.616 68.495 0.20330 0.21989 0.51313 2268.5 3.4318
-0.13 304.7 63.762 0.015683 67.809 68.695 0.20372 0.21992 0.51381 2262.8 3.4559
0.26 306.7 63.699 0.015699 68.001 68.894 0.20414 0.21995 0.51450 2257.2 3.4799
0.65 308.7 63.636 0.015714 68.193 69.092 0.20456 0.21998 0.51519 2251.5 3.5040
1.04 310.7 63.574 0.015730 68.384 69.289 0.20497 0.22001 0.51588 2245.9 3.5282
1.42 312.7 63.511 0.015745 68.574 69.486 0.20539 0.22004 0.51658 2240.3 3.5524
1.80 314.7 63.449 0.015761 68.763 69.682 0.20580 0.22007 0.51728 2234.8 3.5766
2.18 316.7 63.387 0.015776 68.951 69.877 0.20621 0.22010 0.51799 2229.2 3.6008
2.56 318.7 63.325 0.015792 69.139 70.072 0.20662 0.22014 0.51870 2223.7 3.6251
2.94 320.7 63.263 0.015807 69.327 70.266 0.20702 0.22017 0.51942 2218.2 3.6495
3.31 322.7 63.201 0.015823 69.513 70.459 0.20743 0.22021 0.52014 2212.7 3.6738
3.68 324.7 63.139 0.015838 69.699 70.652 0.20783 0.22024 0.52087 2207.2 3.6982
4.06 326.7 63.078 0.015853 69.884 70.844 0.20823 0.22028 0.52160 2201.7 3.7226
4.43 328.7 63.017 0.015869 70.069 71.035 0.20863 0.22031 0.52233 2196.3 3.7471
4.79 330.7 62.956 0.015884 70.253 71.226 0.20903 0.22035 0.52307 2190.8 3.7716
5.16 332.7 62.894 0.015900 70.436 71.416 0.20943 0.22039 0.52381 2185.4 3.7962
5.53 334.7 62.834 0.015915 70.619 71.606 0.20982 0.22042 0.52456 2180.0 3.8207
5.89 336.7 62.773 0.015930 70.801 71.795 0.21021 0.22046 0.52531 2174.6 3.8454
6.25 338.7 62.712 0.015946 70.982 71.983 0.21061 0.22050 0.52606 2169.2 3.8700
6.61 340.7 62.652 0.015961 71.163 72.171 0.21099 0.22054 0.52682 2163.9 3.8947
6.97 342.7 62.591 0.015977 71.343 72.358 0.21138 0.22058 0.52759 2158.5 3.9194
7.33 344.7 62.531 0.015992 71.523 72.545 0.21177 0.22062 0.52836 2153.2 3.9442
7.68 346.7 62.471 0.016008 71.702 72.731 0.21216 0.22066 0.52913 2147.9 3.9690
8.04 348.7 62.411 0.016023 71.881 72.916 0.21254 0.22070 0.52991 2142.6 3.9939
8.39 350.7 62.351 0.016038 72.059 73.101 0.21292 0.22074 0.53069 2137.3 4.0188
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pounds kilograms cubic feet cu meters cubic feet cu meters gallons
lbs kg scf nm3
scf nm3
gal1 pound 1.0 0.4536 36.1423 0.94982 12.04744 0.3166 0.151315
1 kilogram 2.205 1.0 79.6788 2.09396 26.55961 0.698 0.3336
1 scf gas
dissociated 0.0277 0.01255 1.0 0.02628 0.3333 0.00876 0.004187
1 nm3
gas
dissociated 1.0528 0.4776 38.04 1.0 12.68 0.3333 0.1593
1 scf gas
undissociated 0.083 0.0377 3 0.07884 1.0 0.02628 0.01256
1 nm3
gas
undissociated 3.1585 1.4327 114.16 3 38.04 1.0 0.47927
1 gal liquid 6.609 2.9977 238.855 6.277106 79.61828 2.09 1.0
1 liter liquid 1.746 0.792 63.1056 1.658416 21.03521 0.55 0.2642
pounds kilograms cubic feet cu meters cubic feet cu meters gallons
lbs kg scf nm3 scf nm
3 gal
1 pound 1.0 0.4536 45.3318 1.19132 22.6659 0.5957 0.1467
1 kilogram 2.205 1.0 99.9378 2.62636 49.9689 1.3132 0.3234
1 scf gas
dissociated 0.0221 0.01 1.0 0.02628 0.5 0.0131 0.0032
1 nm3 gas
dissociated 0.8394 0.3808 38.04 1.0 19.03 0.5 0.1231
1 scf gas
undissociated 0.0441 0.02 2 38.04 1.0 0.02628 0.0065
1 nm3 gas
undissociated 1.679 0.7615 76.1 2 38.04 1.0 0.24626
1 gal liquid 6.817 3.0923 309.042 8.12162 154.521 4.06 1.01 liter liquid 1.8011 0.817 81.6491 2.14574 40.8246 1.07 0.2642
METHANOL AND DISSOCIATED METHANOL CONVERSION DATA
AMMONIA AND DISSOCIATED AMMONIA CONVERSION DATA
Quantity
Liq
Weight Gas (Dissociated) Gas (Undissociated) Liq
Weight Gas (Dissociated) Gas (Undissociated)
Quantity
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liters
l0.5727
1.2626
0.0158
0.603
0.048
1.809
3.785
1.0
liters
l
0.5552
1.224
0.0122
0.466
0.024
0.9321
3.7851.0
uid
uid
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ABSOLUTE TEMPERATURE CHART
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Art Montemayor March 12, 2002
inches cm lbs kg psi bars cu in liters
Medical B 3AA 2015 3.31 x 13.125 8.4 x 33.3 4.18 1.89 2,015 138.9 88 1.44
D 3AA 2015 4.18 x 16.75 10.6 x 42.5 7.5 3.39 2,015 138.9 180 2.95
E 3AA 2015 4.18 x 25.75 10.6 x 65.4 10.5 4.76 2,015 138.9 295 4.84M 3AA 2015 7 x 43 178 x 109.2 61.3 27.8 2,015 138.9 1,345 22.04
inches cm lbs kg psi bars cu in liters
10 oz 3E 1800 1.94 x 11.88 4.928 x 30.175 2.3 1.04 1,800 124.1 25.5 0.418
21/2 lbs 3AA 1800 3.56 x 14.62 9.042 x 37.135 5.25 2.38 1,800 124.1 108 1.77
5 lbs 3AA 1800 5.73 x 14.00 13.385 x 35.6 10.1 4.58 1,800 124.1 221 3.62
10 lbs 3AA 1800 7.0 x 18.0 17.78 x 45.72 23 10.43 1,800 124.1 495 8.11
15 lbs 3AA 1800 7.0 x 22.88 17.78 x 58.115 30 13.61 1,800 124.1 644 10.55
20 lbs 3AA 1800 7.75 x 23.25 19.685 x 59.0 31.2 14.95 1,800 124.1 840 13.7750 lbs 3AA 1800 8.625 x 45.38 21.908 x 115.2 84.9 38.5 1,800 124.1 2,160 35.4
All CO2, stored and distributed using these type of high pressure steel cylinders, exists as a saturated liquid at the
storage pressure that corresponds to the contents' temperature. For CO2 at an ambient temperature of80oF, the
corresponding cylinder pressure is 955 psig. These cylinders are filled with LCO2 at high pressure.
These cylinders, with the exception of those used as fire extinguishers, have valves that release saturated CO 2 gas
from the top, vapor portion of the cylinder while the cylinder is held upright. If the cylinder is inverted, the valves will
dispel saturated LCO2 to the atmosphere, which flashes into a mixed-product stream of cold CO 2 gas and dry ice "snow".
The product mixture resulting from this "flash" of LCO2 is initially at a temperature of-109oF and can cause severe
burns to human skin.
This effect, attained by adiabatically expanding the LCO2, is used to good advantage in CO2 Fire Extinguishers. The
fire extinguisher is manufactured in the same manner and under the same mechanical design parameters as the
conventional storage and distribution CO2 cylinder. The only exception is that the CO2 Fire Extinguisher has a valve
that incorporates a copper or brass syphon tube that preferentially dispels (and expands) LCO2 and not CO2 gas.
That is why a CO2 Fire Extinguisher should be held upright when applying it to a fire.
All CO2 cylinders contain saturated Liquid CO2 when at a temperature below its Critical Temperature (87.908oF).
When the cylinders are at a temperature above the Critical, the CO 2 exists in the Supercritical Phase - where the fluid
is neither a gas or a liquid.
When the cylinders contain a liquefied gas, the cylinder must have a vapor space allowed over the saturated liquid in
order to allow for liquid expansion upon high ambient temperatures, without generating excessive hydraulic pressures.The observable filling densities of the various cylinder sizes are calculated below:
cu in
10 oz 3E 1800 25.5 0.70 89.13% 110.28%
21/2 lbs 3AA 1800 108 2.97 84.18% 104.15%
Model DOT Spec
0.57
2.40
Water
Capacity
Liq. CO2
Capacity @
70oF, lb
Fill
Density
@ 70oF
Liq. CO2 Capacity
@ 85oF, lb
Fill
Density
@ 85oF
Note: All medical gas capacities assume oxygen with 10% overfill.
CARBON DIOXIDE GAS CYLINDER SPECIFICATIONS
Water Capacity
(volume)Model DOT Spec
Dimensions Nominal Weight Service Pressure
MEDICAL GAS CYLINDER SPECIFICATIONS
Water Capacity
(volume)Model DOT Spec
Dimensions Nominal Weight Service Pressure
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Gas CGA#
Acetylene (commercial) 300 .825-14NGO-RH-EXT (flat nipple) 3,000
Acetylene 510 .885-14NGO-LH-INT(bullet nipple) 500
Acetylene (B) 520 .895-18NGO-RH-EXT 500Acetylene (MC) 200 .625-20NGO-RH-EXT (conical nipple) 500
Air (industrial) 590 .965-14NGO-LH-INT 3,000
Air (breathing) 346 .825-14NGO-RH-EXT (large round nipple) 3,000
Air (to 5,500 psig) 347 .825-14NGO-RH-EXT (long round nipple) 5,500
Ammonia 240 3/8-18NGT-RH-INT 500
Argon 580 .965-14NGO-RH-INT 3,000
Argon (to 5500 psig) 680 1.045-14NGO-RH-INT 5,500
Butane 510 .885-14NGO-LH-INT (bullet nipple) 500
Carbon Dioxide 320 .825-14NGO-RH-EXT (flat nipple) 3,000
Carbon Monoxide 350 .825-14NGO-LH-EXT (round nipple) 3,000
Corrosive 660 1.030-14NGO-RH-EXT (face washer) 3,000
Ethane 350 .825-14NGO-LH-EXT (round nipple) 3,000
Fuel Gas 350 .825-14NGO-LH-EXT (round nipple) 3,000
Fuel Gases (to 5,500 psi) 695 1.045-14NGO-LH-INT 5,500
Helium 580 .965-14NGO-RH-INT 3,000
Helium (to 5,500 psig) 680 1.045-14NGO-RH-INT 5,500
Hydrogen 350 .825-14NGO-LH-EXT (round nipple) 3,000
Hydrogen (to 5,500 psig) 695 1.045-14NGO-LH-INT 5,500
Medical Mixtures 500 .885-14NGO-RH-INT (bullet nipple) 3,000
Methane 350 .825-14NGO-LH-EXT (round nipple) 3,000
Methane (to 5,500 psig) 695 1.045-14NGO-LH-INT 5,500
Nitrogen 580 .965-14NGO-RH-INT 3,000
Nitrogen (to 5,500 psig) 680 1.045-14NGO-RH-INT 5,500
Nitrous Oxide 326 .825-14NGO-RH-EXT (small round nipple) 3,000
Oxygen 540 .903-14NGO-RH-EXT 3,000
Oxygen (to 4,000 psig) 577 .960-14NGO-RH-EXT 4,000
Oxygen (to 5,500 psig) 701 1.103-14NGO-RH-EXT 5,500
Ozone 755 1.125-14UNS-2A-LH-EXT (short nipple) 3,000
Propane 510 .885-14NGO-LH-INT (bullet nipple) 500
Propane + Butane 555 .903-14NGO-LH-EXT 3,000
Sulfur Hexafluoride 590 .965-14NGO-LH-INT 3,000
CGA VALVE SPECIFICATIONSOutlet Connections PSIG
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Art Montemayor Liquid CO2 Storage Tanks March 12, 2003
Rev: 0
Capacity (tons)Empty Weight*
(lbs)Dim. A Dim. B Dim. C
13 11,500 19' 18' 6"
14 12,500 24' 19' 10" - 6"
24 18,600 30' 29' 6"
31 23,500 37' 36' 6"
34 30,000 44' 39'-11" 8"
45 34,500 50' 50' 8"50 40,000 60' 55'-11" 12"
Capacity (tons) Empty Weight*(lbs)
Height Dia. PadDimensions
14 15,500 19' - 9" 7' - 4" 9' x 9'
30 30,000 35' - 9" 7' - 4" 10' x 10'50 40,000 39' - 5" 8' - 8" 13' x 13'
Liquid Carbon Dioxide (LCO2) is conventionally stored and distributed to consumers under saturated
conditions. Normal Design conditions are 250 psig and -8.34oF.
However, the usual and customary conditons under which LCO2 is initially charged to storage vessels is
200 psig and -20oF --- which are the process conditions under which LCO 2 is liquefied in a production plant.
The reason for producing -20oF saturated LCO2 is that an Ammonia mechanical refrigeration cycle is
normally employed to liquefy the CO2 and the Ammonia evaporator temperature that best suits this application
TYPICAL CO2 VESSEL (HORIZONTAL)
* Estimate onlySee Tech Specs 1068
* All concrete pad thickness = 24"
* Estimate onlySee Tech Specs 1067 and 1016
* All concrete pads are 11' wide x "A" long
TYPICAL CO2 VESSEL (VERTICAL)
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Art Montemayor Liquid CO2 Storage Tanks March 12, 2003
Rev: 0is approximately -25oF and this results in a -20
oF LCO2 product.
LCO2 main storage and consumer tanks are kept refrigerated (usually at 250 psig & -8.34oF) by integrated
mechanical refrigeration units that employ either Ammonia or Freon refrigerants. The refrigeration system cycles
on-and-off, as required to keep the LCO2 pressure within the design criteria of the tank.
Art Montemayor
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30 21' 9 - 5/8" 43,322 45,623 45,330 43,038 43,67034 21' 9 - 5/8" 48,066 50,619 50,294 47,751 48,453
38 21' 9 - 5/8" 53,516 56,359 55,996 31,655 53,947
49 21' 9 - 5/8" 69,604 73,302 72,830 69,147 70,164
55 34' 9 - 5/8" 127,881 134,675 133,808 127,043 128,910
10 34' -4" 22" 127,881 134,761 133,894 127,124 128,993
7 40' 22" 108,510 114,275 112,539 -- 109,3839 40' 22" 139,372 146,776 145,832 -- 140,494
1500 MVE
(SS) 66 180 7,400 22,081 17,797 25,332 1,541
3000 MVE
(SS) 96 194 16,600 45,181 36,841 51,490 3,000
6000 MVE
(NP) 96 330 28,800 85,962 69,282 98,580 6,000
9000 VCS
(NP) 114 372 46,700 132,443 107,423 151,370 9,00011,000 MVE
(NP) 114 433 57,681 162,478 131,876 185,611 11,000
Note 1:
Note 2:
Note 4:
Note 5:
Tare Wt
lbs
Note 3: For 3,000 11,000 gallon vessel standard vaporization is 5,000 scfh.
For 1,500-gallon vessel standard vaporization is 2,000 scfh.
Taylor Wharton numbers are slightly different.
This table is not for construction use.
TUBE TRAILER VOLUME CAPACITIES
GENERIC CRYOGENIC VESSEL INFORMATION
For oxygen vessel pads an apron of 12' x 12' must be added.
Tube
Length
Filled Wt
O2 (lbs)
Filled Wt
N2 (lbs)
Filled Wt
Ar (lbs)
Net Cap
gallons
For total volume in scf mulitiply gallons times 93.11 for N2, 115.1 for O2, and 112.5
Tube
O.D.
Helium
scf
Height
inches
Oxygen
scf
Nitrogen
scf
Argon
scf
Hydrogen
scf
Capacities shown are trailers filled at 2,640 psig and 70 F.
Size gallonsDia
inches
Number of
Tubes on
Trailer
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63,61451,438
57,270
74,486
136,852
--
116,122149,149
250/400/600 14' x 14' x 15" #4 @ 12" #6 @ 12"
250/400/600 18' x 14' x 15" #4 @ 12" #7 @ 10"
250/400/600 6' x 16' x 18" #4 @ 12" #7 @ 8"
250/400/600 36' x 20' x 18" #4 @ 12" #8 @ 8"
250/400/600 36' x 20' x 21" #4 @ 10" #8 @ 11"
Pad Size
Breathing Air
scf
for Ar.
Bottom
RebarTop RebarMAWP psi
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Art Montemayor High Pressure Compressed Gas Cylinders March 12, 2003
Rev: 0
inches cm lbs kg psi bars cu in liters
20 Scf 3AA 2015 5.27 x 14 13.4 x 35.6 10.1 4.58 2,015 138.9 221 3.6
40 Scf 3AA 2015 7 x 18 17.8 x 45.7 23 10.43 2,015 138.9 495 8.1
55 Scf 3AA 2015 7 x 22.88 17.8 x 58.1 30 13.61 2,015 138.9 644 10.6
80 Scf 3AA 2015 7 x 32.38 17.8 x 82.2 42 19.05 2,015 138.9 985 16.1
110 Scf 3AA 2015 7 x 43 17.8 x 109.2 55 24.94 2,015 138.9 1,345 22
125 Scf 3AA 2265 7 x 43 17.8 x 109.2 55 24.94 2,265 156.2 1,345 22
150 Scf 3AA 2015 7 x 46.25 17.8 x 117.5 59 26.76 2,015 138.9 1,660 27.2
220 Scf 3AA 2015 8.99 x 51 22.8 x 129.5 114 51.7 2,015 138.9 2,640 43.3
250 Scf 3AA 2265 9.04 x 51 23 x 129.5 115 52.2 2,265 156.2 2,640 43.3
300 Scf 3AA 2400 9.27 x 55 23.5 x 139.7 135 61.2 2,400 165.5 2,980 48.4
400 Scf 3AA 2400 10.51 x 56 26.7 x 142.2 190 86.2 2,400 165.5 3,960 64.9
3600 psi 3AA 3600 9.31 x 51 23.6 x 129.5 180 81.6 3,600 248.2 2,640 43.3
6000 psi 3AA 6000 9.28 x 51 23.5 x 129.5 267 121.1 6,000 413.7 2,285 37.4
inches cm lbs kg psi bars cu in liters
AL-150 3AL2015 8 x 48 20 x 122 50 23 65 30 1.04 30
AL-88 3AL2216 7 x 33 18 x 84 32 15 35 16 0.56 16
AL-33 3AL2216 7 x 16 18 x 41 16 7.3 13 5.9 0.21 5.9
Water Capacity
(volume)
HIGH PRESSURE STEEL CYLINDER SPECIFICATIONS
Water Capacity
(volume)DOT Spec
Model(Cap., Scf)
Dimensions Nominal Weight Service Pressure
Dimensions Nominal Weight Service Pressure
HIGH PRESSURE ALUMINUM CYLINDER SPECIFICATIONS
Model DOT Spec
Page 53 of 97FileName: 142168304.xls.ms_office
WorkSheet: HP Cylinders
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DENSITIES AT VARIOUS SATURATION PRESSURES
Liquid
Densitylbs/ft
3
Gas
Densityscf/gal
Liquid
Densitylbs/ft
3
Gas
Densityscf/gal
Liquid
Densitylbs/ft
3
Gas Density
scf/gal
0 71.17 115.10 50.44 93.11 87.51 112.50
5 70.42 113.72 49.62 91.55 85.77 110.89
10 69.80 112.73 49.00 90.40 84.77 109.60
25 67.86 109.59 47.50 87.63 82.46 106.61
50 65.55 105.86 45.69 84.18 79.90 103.31
75 63.76 102.97 44.19 81.53 77.90 100.71
100 62.43 100.82 42.88 79.12 76.15 98.45
150 59.80 96.57 40.70 75.08 73.16 94.59
200 57.62 93.05 38.76 71.51 70.28 90.87250 55.60 89.79 36.83 67.95 67.79 87.65
Oxygen Nitrogen ArgonSaturation
Pressure
psig
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Nitrogen purging is easily adapted to any process installation. Different methods are used depending on
the type and shape of the equipment to be purged and on the location of the purging inlets and outlets
.
This method is used for equipment with simple cross sections - such as piplines. The volume of nitrogen
required corresponds to the physical volume of the pipe. In many piplines, a rubber scraping piston, or "pig,"
is introduced and propelled through the pipe by the nitrogen pressure to clean the line.
The nitrogen volume required to purge equipment with a simple cross section is determined using the
Where: V = Total nitrogen volume required (scf) = 340
Vo = Water volume of pipeline (cf) = 1,000.0
P = Nitrogen absolute pressure in the pipeline during purging (psia) = 5.0(Fill in the data in the YELLOW cells and get the answer in BOLD RED.)
This method is used when conditions do not permit a sweeping action of nitrogen through the vessel. The
vessel is repeatedly pressurized and mixed with nitrogen gas and then the mixture is exhausted. The total
volume of nitrogen depends on the number of pressurizing purges required to reduce the contaminant to an
acceptable level and can be determined by using this formula:
Where: V = Total nitrogen volume required (scf)
Vo = Water volume of vessel or tank (cf)P = Absolute pressure after pressurization with nitrogen (psia)
Pa = Absolute pressure after exhaust (psia)
n = Number of purges = C log Co/(log Pa log P)
Co = Initial content of gas to be removed
C = Final content of gas to be removed
This method is used for equipment cross sections such as distillation columns, kilns, reactors, etc.
Nitrogen partially mixes with the gas to be purged out, and then the mixture exits through an outlet located
as far as possible from the inlet. The nitrogen required to reduce a contaminate to a desired level can befound using the graph below and the total volume of nitrogen needed can be computed from the following
formula:
2. Pressurization Purging
V = 1.2nVoP/Pa
3. Dilution Purging
1. Displacement Purging
HOW TO PURGE WITH NITROGEN
following formula:
V = VoP/14.7
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Where: V = Total nitrogen volume required (scf)
Vo = Water volume of equipment (cf)
n = Number of nitrogen volumes required
V = nVo
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1 Displacement
2 Dilution Pf = Pi = 14.7
3 Dilution Pi = 14.7; Pf = 29.4
4 Pressure Purge Pi = 19.7; Pf = 24.7
5 Pressure Purge Pi = 19.7; Pf = 34.7
Where: Pf = pressure final
Pi = pressure initial
Purging Technique:
PURGING EFFICIENCY (C/Co) AS A FUNCTION OF NITROGEN VOLUME
(TANK VOLUMES) FOR VARIOUS PURGING TECHNIQUES
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Lean Rich
Acetaldehyde 70 36 365 4.1 55 12
Acetone 133 0 1,000 2.6 12.8 11.6
Acetylene 119 -- 571 2.5 81 --
Alkyl chloride 113 -25 737 3.3 11.1 12.6
Ammonia 28 -- 1,204 16 25 15
Benzene 176 12 1,044 1.4* 7.1 11.2
1-3 Butadiene 24 -- 804 2 11.5 10.4
Butane 32 -- 761 1.9 8.5 12.1
1-Butene 20 -- 723 1.6 9.3 11.4
2-Butene 34 -- 615 1.8 9.7 11.7
n- Butyl formate 225 64 612 1.7 8 12.4
Carbon disulfide 115 22 212 1.3 44 5.4
Carbon monoxide 310 -- 1,128 12.5 74 5.6Cyclopropane 27.4 -- 928 2.4 10.4 11.7
11 Dischloroethylene 99 5 856 5.6 11.4 10
Dimethyl 22 butane 121 54 797 1.2 7 12.1
Ethane 127 -- 959 3 12.5 11
Ethanol 173 55 793 4.3 19 10.6
Ethyl bromide 101 -- 952 6.7 11.3 14
Ethyl chloride 54 58 966 3.8 15.4 13
Ethylene 152 -- 842 3.1 32 10
Ethylene oxide 56.4 < 0 804 3 100 --
Ethyl ether 94 -49 356 1.9 48 --
Ethyl formate 130 -4 851 2.7 13.5 10.4
Gasoline (octane 60) -45 536 1 7.6 11.6 --Gasoline (octane 92) 734 1.5 8 11.6 -- --
Gasoline (octane 100) -36 853 1 7.4 11.6 --
Heptane 209 25 433 1.2 6 11.6
Hexane 156.2 7 453 1.2 7.5 11.9
Hydrogen 422 -- 1,085 4 75 5
Isobutane 11 -- 864 1.8 8.4 12
Isopropyl Ether 154.4 -18 830 1.4 21 10
Methane -263 -- 999 5.3 14 12.1
Methanol 151 52 867 7.3 35 9.7
Methyl acetate 135 14 935 3.1 16 10.9
Methylamine 19.4 -- 806 4.9 20.7 10.7
Methyl butene 87.4 < 20 -- -- -- 11.4
Methyl chloride -11 -- 1,170 10.7 17.4 15
Methyl formate 89.6 -2 853 5.9 20 10.1
Pentane 97 < -40 588 1.5 7.8 12.1
Propane -44 -- 871 2.2 10 11.4
Propylene -54.4 -- 770 2.4 10.3 11.5ny c or e --
Flammability Limit
in Air Volume % (4)
Max.
Oxygen
Content
Vol. % (5)
FLAMMABILITY CHARACTERISTICS OF COMMON GASES AND LIQUIDS
Product
Boiling
Point F
(1)
Flash
Point F
(2)
Auto-
Ignition F
(3)
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1. Boiling point temperature at standard atmospheric pressure.
2. Flash point minimum temperature at which the vapors of a combustible liquid will be ignited by
a flame in certain experimental conditions.
3. Auto-ignition temperature: minimum temperature at which a product will spontaneously oxidize in air
4. Flammability limit: volume percentage of combustible gas in air such that below the lean limit or
above the rich limit, the mixture is non-flammable.
5. Maximum oxygen content: oxygen percentage in a combustible gas mixture below which the mixturis non-flammable at 212 F.
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.
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*Flash gas as a percentage of liquid after depressurization to atmospheric pressure.
Flash gas as a percentage of saturated pressurized liquid.
Example: Estimate how much vapor is released when 1000 gallons of liquid nitrogen at 80 psig is with
from a vessel into a transport trailer at atmospheric pressure.
Solution: From the chart above, using the lower line with the storage tank pressure of 80 psig, the va
released is 18% of the liquid discharged.
FLASH FROM SATURATED PRESSURIZED LIQUIDS
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drawn
or
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240#
Satt
ABB GT 35 16,900 10,670 180.3 22,800 7,880 179.7 60.5
ABB GT 10 24,630 9,970 245.6 35,500 6,755 239.8 108.0
ABB GT 8C 52,800 9,920 523.8 77,700 6,640 515.9 234.6
ABB GT11N 83,800 10,370 869 125,400 6,825 855.9 397.2
ABB GT 13D 97,700 10,564 1032.1 147,100 6,920 1,017.9 466.6
ABB GT 11N2 109,300 9,977 1090.5 163.8 6,550 1,072.9 490.0
General Electric LM1600PA 13,425 9,560 128.3 18,700 6,870 128.5 53.1
General Electric LM2500 22,800 9,273 211.4 30,900 6,850 211.7 92.2
General Electric PG5371PA 26,300 11,990 315.3 38,700 8,146 315.3 143.4
General Electric LM2500+ 27,040 9,330 252.3 38,480 6,637 255.4 100.7
General Electric LM5000 34,450 9,180 316.3 44,600 7,094 316.4 259.9General Electric LM6000 36,970 8,795 325.2 53,000 6,620 350.9 132.9
General Electric PG6541B 38,340 10,880 417.1 59,200 7,020 415.6 193.2
General Electric PG6101FA 70,150 9,980 700.1 108,400 6,440 698.1 330.7
General Electric PG7111EA 83,500 10,480 875.1 128,700 6,800 875.2 399.8
General Electric PG7161EC 116,000 9,890 1147.2 177,800 6,460 1,148.6 517.2
General Electric PG9171E 123,400 10,100 1246.3 188,400 6,610 1,245.3 707.8
Pratt & Whitney FT 8 25,420 8,950 227.5 32,280 7,010 226.3 85.0
Pratt & Whitney FT 8 Twin 51,100 8,905 455 65,310 6,930 452.6 190.0
Siemens V64.3A 70,000 9,270 648.9 101,000 6,230 629.2 296.8
Siemens V84.2 106,180 10,120 1074.5 151,000 6,625 1,000.4 512.3
Siemens V84.3A 170,000 8,980 1526.6 254,000 6,890 1,750.1 602.9
Solar Mars 100S 10,695 10,505 112.4 28,700 7,750 222.4 48.9Westinghouse 251B12 47,680 10,670 508.7 69,800 7,230 504.7 233.0
Westinghouse Trent 48,690 8,570 417.3 61,788 6,778 418.8 145.0
Westinghouse 501D5A 119,200 9,910 1181.3 168,070 7,024 1,180.5 530.0
Westinghouse 501F 162,410 9,660 1568.9 236,200 6,425 1,517.6 750.0
1.
2.
3.
4.
5.
1.
2.
Combined CycleBase Ste
KPPH
GAS TURBINE CAPACITY TABLE
kwOutput
Heat Ratebtu/kw
Simple Cycle
Model
Notes:
MMbtuInput
kwOutput
Heat Ratebtu/kw
ManufacturerMmbtuInput
substantially alter the kw output.
Base steam is at GTG base rate, open cycle, open cycle, with no supplemental firing for two points only for illu
Remarks:
This information is for preliminary estimating only. Accurate estimations require a detailed set of site condition
Simple cycle output is at ISO conditions with no HRSG and with DLN burner technology where available.
Combined cycle kw output is using most favorable steram generation conditions for equipment. ISO condition
Some machines can use water or steam injection for NO x control or power augmentation. Such injection may
Most any combination of pressure and temperature is available.
50 Hz configuration is available with no appreciable change in KW output.
This turbine can be steam or water injected for additional power output and/or NOx control.
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3.
4.
50 Hertz only.
This turbine burns heavy fuel oil only.
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Remarks
42.0 1, 2
98.0 1, 2
200.0 1, 2
335.9 2
390.0 3, 4
430.0
44.3
79.0 1, 2
119.6 1, 2
84.6 1
238.0 1, 2109.5 1
168.8 1, 2
293.9
343.8 1, 2
450.0 1, 2
621.7 2, 3
67.0 1
134.0 1
260.0 1
442.9
589.1 1, 2
40.8 2200.0 2
110.0 1
450.0 2
660.0 2
am,
600#600F
stration.
s.
and inlet and outlet
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VAPOR RELEASE LIQUID HYDROGEN CHART
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60F and
14.7 psia
60F and
100 psig1/4" 3/8" 1/2" 3/4" 1" 1-1/4" 1-1/2" 2"
1 0.128 0.018
2 0.256 0.285 0.064 0.02
3 0.384 0.605 0.133 0.042
4 0.153 1.04 0.226 0.071
5 0.641 1.58 0.343 0.106 0.027
6 0.769 2.23 0.408 0.148 0.037
8 1.025 3.89 0.848 0.255 0.062 0.019
10 1.282 5.96 1.26 0.356 0.094 0.029
15 1.922 13 2.73 0.334 0.201 0.062
20 2.563 22.8 4.76 1.43 0.345 0.102 0.026
25 3.204 7.34 2.21 0.526 0.156 0.039 0.019
30 3.845 10.5 3.15 0.748 0.219 0.055 0.026
35 4.486 14.2 4.24 1 0.293 0.073 0.035
40 5.126 18.4 5.49 1.3 0.379 0.095 0.044
45 5.767 23.1 6.9 1.62 0.474 0.116 0.55550 6.408 8.49 1.99 0.578 0.149 0.067 0.019
60 7.69 2-1/2" 12.2 2.85 0.819 0.2 0.094 0.027
70 8.971 16.5 3.83 1.1 0.27 0.126 0.036
80 10.25 0.019 21.4 4.96 1.43 0.35 0.162 0.04690 11.53 0.023 27 6.25 1.8 0.437 0.203 0.058
100 12.82 0.029 3" 7.69 2.21 0.534 0.247 0.07
125 16.02 0.044 11.9 3.39 0.825 0.38 0.107
150 19.22 0.062 0.021 17 4.87 1.17 0.537 0.151
175 22.43 0.083 0.028 23.1 6.6 1.58 0.727 0.205
200 25.63 0.107 0.036 30 8.54 2.05 0.937 0.264
225 28.84 0.134 0.045 10.8 2.59 1.19 0.331
250 32.04 0.164 0.055 13.3 3.18 1.45 0.404
275 35.24 0.191 0.666 16 3.83 1.75 0.484
300 38.45 0.232 0.078 19 4.65 2.07 0.573325 41.65 0.27 0.09 22.3 5.32 2.42 0.673
350 44.87 0.313 0.104 25.8 6.17 2.8 0.776
375 48.06 0.119 29.6 7.05 3.2 0.887
400 51.26 0.134 33.6 8.02 3.64 1
425 54.47 0.151 37.9 9.01 4.09 1.13
450 57.67 0.168 10.2 4.59 1.26
475 60.88 0.187 11.3 5.09 1.4
500 64.08 0.206 12.5 5.61 1.55
550 70.49 0.248 15.1 6.79 1.87
600 76.9 0.293 18 8.04 2.21
650 83.3 0.342 21.1 9.43 2.6
700 89.71 0.395 24.3 10.9 3750 96.12 0.451 27.9 12.6 3.44
800 102.5 0.513 31.8 14.2 3.9
850 108.9 0.576 35.9 16 4.4
900 115.3 0.642 40.2 18 4.91
950 121.8 0.715 20 5.47
1,000 128.2 0.788 22.1 6.06
1,100 141 0.948 26.7 7.29
1200 153.8 1.13 31.8 8.63
PRESSURE DROP IN PIPE (AIR)
Cfm of Compressed air
at:
Air pressure drop in pounds per square inch per 100 feet of Schedule 40 pipe for air
at 100 psig and 60F
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1,300 166.6 1.32 37.3 10.1
1,400 179.4 1.52 11.8
1,500 192.2 1.74 13.5
1,600 205.1 1.97 15.3
1,800 203.7 2.5 19.3
2,000 256.3 3.06 23.9
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MINIMUM SAFE DISTANCE FOR LIQUID HYDROGEN
39.633 ,500 350115,000 15,00175,000
1
(a)
-1
Sprinklered
building/stru
cture or
unsprinklere
d
building/stru
cture having
noncombusti
ble contents. 5(1,3)
5(1,3)
5(1,3)
-2
Unsprinklere
d
building/stru
cture with
combustible
contents.
Adjacent
wall(s) with
fire-
resistancerating less
than 3
hours(2)
25 50 75Adjacent
wall(s) with
fire-
resistance
rating of 3
hours or
greater(2)
5 5 5
(b)
-1
Sprinklered
building/stru
cture 50 50 50
-2
Unsprinklere
d
building/stru
cture 50 75 100
2
Type of Exposure
Building Structure
Wall(s) adjacent to
system constructed of
noncombustible or
system constructed of
combustible materials
Minimum Distance (ft) from Liquefied Hydrogen Systems to Exposures(4)
Total Liquefied Hydrogen Storage
(cap in gal)
Wall openings
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(a) Openable 75 75 75
(b)
Unopenab
le 25 50 50
3 75 75 75
4 50 75 100
5 5 5 5
6 50 75 75
7 75 75 75
8 50 75 100
9 50 50 50
10 75 75 75
11 25 50 75
12 5(3)
5(3)
5(3)
1
2
3
4
Flammable gas storage (other than
oxidizers (See NFPA 50B, 5-1.3)
Combustible solids
Open flames and welding
,
conditioning or ventilating
combustible liquids (above ground
and vent or fill openings if belowground) (See NFPA 50B, 5-1.3)
hydrogen containers
Exclusive of windows and doors.
of product shall be considered. The 5-ft distance in Nos. 1 and 12
facilitates maintenance and enhances ventilation.
protective structures have a minimum fire resistance rating of two
hours interrupt the line of sight between uninsulated portions of the
Places of public assembly
Public ways, railroads and property
Protective structures
of a system shall have a fire resistance rating of at least
1/2 hour.
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MINIMUM SAFE DISTANCE FOR LIQUID PETROLEUM GAS
Safe distance from:
0 to 500 gal w.c. 501 to 1000 gal w.c.
Central A/C compressor (any electrical service) 10 feet 15 feet
Perimeter of the building 10 feet 15 feet
Nearest line of adjoining property 10 feet * 15 feet
MINIMUM SAFE DISTANCE FOR LIQUID OXYGEN
Type of Exposure
Building structures
*a) 'Wood frame construction
*b) 'Other than wood frame construction
c) 'Confining areas
Wall openings
All classes of flammable and combustible liquid storage
a) 'Above-ground storage
0 to 1000 gallons
>1000 gallons
Distance may be
reduced to 15 ft forClass III b combustible
liquids
b) Below ground storage
Horizontal: Distance
between tanks
ASME Containers
* LP-gas container(s) of 500 gallon aggregate capacity or less in vapor service is exempt from adjoining
property line requirements.
Note: Proximity of power lines cannot reach vessel if broken.
Minimum Distance (ft) from Bulk Oxygen Systems to Exposures
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Distance between O2
and tank openings
Flammable gases above ground
a) Liquified hydrogen
b) Other liquified gases
0 to 1000 gallons
>1000 gallons
c)
Non-liquified or
dissolved gases
0 to 25,000 scf
>25,000 scf
Rapid burning solid materials (paper, excelsior,etc.)
Slow burning solid materials (coal, heavy timber)
Place of public assembly
Piping outlets and vent/fill connections from areas occupied by non-ambulatory patients
Public sidewalks or parked vehicles
Nearest property line
*These distances do not apply where protective structures having a minimum fire resistance of two hours
interrupt the line-of-sight between uninsulated portions of the bulk oxygen storage installation and the
exposure. In such cases, the minimum distance required should be that required for system maintenance.
For SI units: 1 ft = 0.305M; 1 gallon = 3.785 L
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Total
Line of
Sight
Distance
50 ft
1 ft
75ft/35ft
10 ft
25 ft
50 ft
15 ft
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25 ft
75 ft
25 ft
50 ft
25 ft
50 ft
50 ft
25 ft
50 ft
50 ft
10 ft
5 ft
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Btu(IT)/min Btu (IT)/hr kg cal/hr ton (US)
comm
ton (Brit)
commfrigorie/hr
1 ton (US ) comm 200 12,000 3,025.9 1 0.8965 3,025.9
1 ton (British) comm 223.08 13,385 3,375.2 1.1154 1 3,375.2
1 frigorie/hr 0.06609 3.9657 1 0.0003305 0.0002963 1
RefrigerantRefrigerant
Temp F
Pressure
psia
Latent Heat
Btu/Lb
Sensible
Heat Btu/Lb
Total Heat
Btu/Lb
Ice (H2O) (melting) 32 14.7 144 8 152Liquid CO2 (flashed to snow) 109 14.7 113.0* 29.8 149.8
Dry Ice (subliming) 109 14.7 246.3 29.8 276.1
PSIGRefrigerant
Temp F
Pressure
psia
Latent Heat
Btu/Lb
Sensible
Heat Btu/Lb
Total Heat
Btu/Lb
0 at 1 atm 320.4 14.7 85.4 90.8 176.2
15 at 30 psia 308.6 30 81.5 88.9 170.4
26 at 40 psia 303.2 40 79.8 87.9 167.7
36 at 50 psia 298.7 50 77.7 87.4 165.1
56 at 70 psia 291.3 70 74.7 86.4 161.5
REFRIGERATION CONVERSION FACTORS
CO2 snow is flashed from liquid CO2 at 314.7 psia storage pressure. Snow yield is 46% by weight.
Liquid carbon dioxide is stored at zero degrees and maintained at zero degrees by a mechanical
refrigerator. This permits storage of liquid carbon dioxide without loss.
Refrigeration
REFRIGERATION VALUES TO +40 F FOR EXPENDABLE REFRIGERANTS
during a continuous 24-hour period.
Water Ice (H2O) has a liquid residue while the other refrigerants are converted to the gas phase.
Multiply units in left column by proper factor below:
The Btu here is the International Steam Table Btu (IT). However, 1 frigorie = 1 kg cal (NOT IT)
One ton of refrigeration is the heat required to melt one ton (2,000 lbs) of ice at 32 F to water at 32 F
NITROGEN REFRIGERATION CONVERSION FACTORS
*This latent heat value