Compressed Industrial Gases Hof Master

7/30/2019 Compressed Industrial Gases Hof Master

1/97

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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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


3/97

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


4/97

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


5/97


6/97

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


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.


OZONE CONVERSION DATA

Weight Gas Liquid

Weight Gas LiquidOzone

Quantity

CarbonMonoxide

Quantity

CARBON MONOXIDE CONVERSION DATA


7/97

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


8/97

Scf H2

960,000


9/97

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


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


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.


Krypton

Quantity

Xenon Quantity

Weight Gas Volume Liquid volume

Weight Gas Volume Liquid Volume


10/97

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


11/97

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


12/97

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:


13/97

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 . . . . , . . .



Power (rate of

energy use)

Energy

absolute

Joule/g

int

Joule/g cal/g int cal/g Btu/lb

Specific Energy



14/97

g-ca sec metr c p178 1.014

0.2388 0.00136

238.8 1,360

4.199 0.0239. .


15/97

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 . . -- , . -- . .


Volume

AreaMultiply units in left column by proper factor below:


16/97

Imp

gallon

--

6.229

168.2

--

220

0.22

0.8327.


17/97

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


1 micron = 0.001 millimeter

Length


Weight


18/97

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


19/97

TONNAGE CONVERSION CHART

To obtain values for plants of larger size, multiply each value by the same factor.


20/97


21/97

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


22/97

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


23/97

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


24/97

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)


25/97

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


26/97

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


27/97

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


28/97

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:


29/97

50

0.48

0.49

0.51

0.52

0.54

0.55

0.62

0.68

0.73

0.83

0.92

1


30/97

er is


31/97

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


32/97

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


33/97

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


34/97

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


35/97

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!

Page 35 of 97FileName: 142168304.xls.ms_office

WorkSheet: LCO2 Vaporization


36/97


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




37/97


Rev: 0




38/97


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




39/97


Rev: 0




40/97


Rev: 0




41/97

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)

Page 41 of 97


42/97

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

Page 42 of 97


43/97

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

Page 43 of 97


44/97

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


45/97

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


46/97

ABSOLUTE TEMPERATURE CHART


47/97

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


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



WorkSheet: CO2 Cylinder Specs


48/97

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


49/97

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)


WorkSheet: LCO2 Storage Vessels


50/97

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


WorkSheet: LCO2 Storage Vessels


51/97

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


52/97

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


53/97

Art Montemayor High Pressure Compressed Gas Cylinders March 12, 2003

Rev: 0


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


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)



HIGH PRESSURE ALUMINUM CYLINDER SPECIFICATIONS

Model DOT Spec


WorkSheet: HP Cylinders


54/97

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


55/97

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


56/97

Where: V = Total nitrogen volume required (scf)

Vo = Water volume of equipment (cf)

n = Number of nitrogen volumes required

V = nVo


57/97

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


58/97

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)


59/97

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.


60/97


61/97

.


62/97

*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


63/97

drawn

or


64/97

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.


65/97

3.

4.

50 Hertz only.

This turbine burns heavy fuel oil only.


66/97

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


67/97


68/97

VAPOR RELEASE LIQUID HYDROGEN CHART


69/97

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


70/97

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


71/97

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


72/97

(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.


73/97

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


74/97

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


75/97

Total

Line of

Sight

Distance

50 ft

1 ft

75ft/35ft

10 ft

25 ft

50 ft

15 ft


76/97

25 ft

75 ft

25 ft

50 ft

25 ft

50 ft

50 ft

25 ft

50 ft

50 ft

10 ft

5 ft


77/97

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.


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

Documents

Compressed Industrial Gases Hof Master