19.1.pdf

Manual of Petroleum Measurement Standards Standards Chapter 19—Evaporative Loss Measurement Section 1—Evaporative Loss from Fixed-Roof Tanks THIRD EDITION, MARCH 2002 ADDENDUM, ADDENDUM, AUGUST AUGUST 2008

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Copyright American Petroleum Institute Provided by IHS under license with API No reproduction or networking permitted without license from I HS

Licensee=Inspectorate Licensee=Inspectorate America Corp/5966443001 Corp/5966443001 Not for Resale, 06/05/2009 08:02:04 MDT

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Measurement of Petroleum Measurement Standards Chapter 19—Evaporative Loss Measurement Section 1—Evaporative Loss from Fixed-Roof Tanks Measurement Coordination Department THIRD EDITION, MARCH 2007 ADDENDUM, ADDENDUM, AUGUST AUGUST 2008

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SPECIAL NOTES

API publications necessarily address problems of a general nature. With respect to particular circumstances, local, state, and federal laws and regulations should be reviewed. API is not undertaking to meet the duties of employers, manufacturers, or suppliers to warn and properly train and equip their employees, and others exposed, concerning health and safety risks and precautions, nor undertaking their obligations under local, state, or federal laws. Information concerning safety and health risks and proper precautions with respect to particular materials and conditions should be obtained from the employer, the manufacturer or supplier of that material, or the material safety data sheet. Nothing contained in any API publication publication is to be construed construed as granting any right, by implication or otherwise, for the manufacture, sale, or use of any method, apparatus, or product covered by letters patent. Neither should anything contained in the publication be construed as insuring anyone against liability for infringement of letters patent. Generally, API standards are reviewed and revised, reaffirmed, or withdrawn at least every five years. Sometimes a one-time extension of up to two years will be added to this review cycle. This publication will no longer be in effect five years after its publication date as an operative API standard or, where an extension has been granted, upon republication. Status of the publication can be ascertained from the API Measurement Coordination Department [telephone (202) 682-8000]. A catalog of API publications and materials is published annually and updated quarterly by API, 1220 L Street, N.W., Washington, D.C. 20005. This document was produced under API standardization procedures that ensure appropriate notification and participation in the developmental process and is designated as an API standard. Questions concerning the interpretation of the content of this standard or comments and questions concerning the procedures under which this standard was developed should be directed in writing to the standardization manager, American Petroleum Institute, 1220 L Street, N.W., Washington, D.C. 20005. Requests for permission to reproduce or translate all or any part of the material published herein should also be addressed to the general manager. API standards are published to facilitate the broad availability of proven, sound engineering and operating practices. These standards are not intended to obviate the need for applying sound engineering judgment regarding when and where these standards should be utilized. The formulation and publication of API standards is not intended in any way to inhibit anyone from using any other practices. Any manufacturer marking equipment or materials in conformance with the marking requirements of an API standard is solely responsible for complying with all the applicable requirements of that standard. API does not represent, warrant, or guarantee that such products do in fact conform to the applicable API standard.

All rights reserved. reserved. No No part of of this work work may be be reprod reproduced, uced, store stored d in a retrieva retrievall system, system, or transmitted by any means, electronic, mechanical, photocopying, recording, or otherwise, without prior written permission from the publisher. Contact the Publisher, API Publishing Publishing Services, Services, 1220 1220 L Stree Street, t, N.W., N.W., Washingto Washington, n, D.C. 20005. 20005. Copyright © 2002/2008 American Petroleum Institute

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FOREWORD This standard was formerly API Publication 2518. API publications may be used by anyone desiring to do so. Every effort has been made by the Institute to assure the accuracy and reliability of the data contained in them; however, the Institute makes no representation, warranty, or guarantee in connection with this publication and hereby expressly disclaims any liability or responsibility for loss or damage resulting from its use or for the violation of any federal, state, or municipal regulation with which this publication may conßict. Suggested revisions are invited and should be submitted to the standardization manager, American Petroleum Institute, 1220 L Street, N.W., Washington, D.C. 20005.

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iii Copyright American Petroleum Institute Provided by IHS under license with API No reproduction or networking permitted without license from I HS


CONTENTS Page

19.1.1 19.1.1 GENERAL GENERAL . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1 19.1.1.1 Scope . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1 19.1.1.2 Referenced Referenced Publicat Publications ions . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2 19.1.2 PROCEDURES FOR CALCULATING CALCULATING LOSSES. . . . . . . . . . . . . . . . . . . . . . . . . . 3 19.1.2.1 Loss Equation Equations. s. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 3 19.1.2.2 Discussion Discussion of Variables ariables . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 10 19.1.2.3 Summary Summary of Calculat Calculation ion Procedure Procedure . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 39 19.1.2.4 Sample Problem. Problem. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 41 19.1.3 DESCRIPTION DESCRIPTION OF FIXED-ROOF FIXED-ROOF TANKS . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 42 19.1.3.1 General. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 42 19.1.3.2 Fixed-Roof Fixed-Roof Tanks . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 42 19.1.3.3 Roof Fittings Fittings . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 42 19.1.3.4 Insulation Insulation . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 44 19.1.3.5 Outside Outside Surface Surface of the the Tank Tank . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 44 19.1.4 DETAILS OF OF LOSS ANALYSIS. ANALYSIS. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 44 19.1.4.1 Introduction Introduction . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 44 19.1.4.2 19.1.4.2 Loss Mechan Mechanism ismss . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 45 19.1.4.3 Database Database for Loss Loss Analysis Analysis . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 47 19.1.4.4 Developme Development nt of Standing Standing Storage Storage Loss Equatio Equation n . . . . . . . . . . . . . . . . . . . . 48 19.1.4.5 Developme Development nt of Working Loss Equation Equation . . . . . . . . . . . . . . . . . . . . . . . . . . . 50

APPENDIX APPENDIX A

DOCUMENT DOCUMENTATIO ATION N RECORDS. RECORDS. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 53

APPENDIX APPENDIX B

METRIC METRIC UNITS UNITS . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 55

Figures 1

Fixe Fixedd-Roo Rooff Tan Tank k Geom Geomet etry ry . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 12

2

Dome Roof Outage ( H H RO). . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 13

3

Vapor apor Pressu Pressure re Func Functio tion n CoefÞc CoefÞcien ientt (A) of ReÞne ReÞned d Petrol Petroleum eum Stoc Stocks ks with with a Reid Vapor Vapor Pressure of 1 to 20 psi, Extrapolated to 0.1 psi . . . . . . . . . . . . . . . . 32

4

Vapor apor Pressu Pressure re Func Functio tion n CoefÞc CoefÞcien ientt (B) of ReÞne ReÞned d Petrol Petroleum eum Stoc Stocks ks with with a Reid Vapor Vapor Pressure of 1 to 20 psi, Extrapolated to 0.1 psi . . . . . . . . . . . . . . . . 32

5

True Vapor Pr Pressure (PV ) of ReÞned Petroleum Stocks with a Reid Vapor Pressure Pressure of of 1 to 20 psi . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 33

6

Vapor apor Press Pressure ure Functi Function on Coef CoefÞci Þcient ent (A) of Crud Crudee Oil Oil Stock Stockss with with a Reid Vapor Vapor Pressure of 2 to 15 psi, Extrapolated to 0.1 psi . . . . . . . . . . . . . . . . . . 35

7

Vapor apor Press Pressure ure Functi Function on Coef CoefÞci Þcient ent (B) of Crud Crudee Oil Oil Stock Stockss with with a Reid Vapor Vapor Pressure of 2 to 15 psi, Extrapolated to 0.1 psi . . . . . . . . . . . . . . . . . . 35

8

True Vapor Pr Pressure (PV ) of Crude Oil Stocks with a Reid Vapor Pressure Pressure of 2 to 15 15 psi . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 36

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Page

9

Vente ented d Vapor apor Satu Satura rati tion on Fact Factor or (K S ) . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 38

10

Worki orking ng Loss Loss Turno urnove verr Fac Facto torr (K N ). . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 39

11

Typical ypical FixedFixed-Roof Roof Tank. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 43

Tables 1

Nome Nomenc ncla latu ture re . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4

2

Summar Summary y of of Proc Procedur edures es for Calcula Calculatin ting g Stan Standin ding g Stor Storage age Loss ( LS ) . . . . . . . . . . . 6

3

Summ Summar ary y of Pro Proce cedur dures es for for Cal Calcu cula lati ting ng Wor Worki king ng Loss Loss ( LW ) . . . . . . . . . . . . . . . . . 8

4

Meteorological Da Data (T Selected U.S. U.S. Locations Locations . . . . . . . . . . . . 14 MAX , T MIN , I ) for Selected

5

Solar Absorptance (α) for Selected Tank Tank Surfaces. . . . . . . . . . . . . . . . . . . . . . . . . 19

6

Properties ( M V , W VC , PV , A, B) of Selected Petroleum Liquids. Liquids . . . . . . . . . . . . . . . 20

7

Proper Propertie tiess of Select Selected ed Petr Petroch ochemi emical calss . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 21

8

ASTM Dis Distillation Sl Slope (S ) for Selected ReÞned Petroleum Stocks. Stocks . . . . . . . . . . 34

9

Typical ypical Concent Concentrat ration ionss of Select Selected ed Chem Chemica icals ls in in Commo Common n Petro Petroleu leum m Produc Products. ts. 40

10

N ) for 123 Test Tanks Annu Annual al Stoc Stock k Turno urnove verr Rat Ratee ( N Tanks . . . . . . . . . . . . . . . . . . . . . . . 47

A-1 Contents Contents of Documen Documentation tation Records Records . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 53

vi Copyright American Petroleum Institute Provided by IHS under license with API No reproduction or networking permitted without license from I HS


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Chapter 19—Evaporative Loss Measurement Section 1—Evaporative Loss from Fixed-Roof Tanks 19.1.1 General 19.1.1.1

liquid stocks, stock vapor pressures, tank sizes, meteorological conditions, and operating conditions. The equations are applicable to properly maintained equipment under normal working conditions. The equations were developed for nonboiling stocks, although volatile liquid stocks with a true vapor pressure over 1.5 pounds per square inch absolute are not now typically stored in the U.S. in Þxed-roof tanks. To calculate emissions from tanks that contain material at or above their boiling point or the point at which material starts to ßash, the API model E&P Tank can be used. Without detailed Þeld information, the estimation techniques become more approximate when used to calculate losses for time periods shorter than one year. The equations are not intended to be used in the following applications:

SCOPE

This publication contains an improved method for estimating the total evaporative losses or the equivalent atmospheric hydrocarbon emissions from Þxed-roof tanks that contain multicomponent hydrocarbon mixture stocks (such as petroleum liquid stocks like crude oils) or single-component hydrocarbon stocks (such as petrochemical stocks like ethanol). The standing storage loss equation was improved in the second edition of API Publication 2518 [also identiÞed as API Manual of Petroleum Measurement Standards, Chapter 19.1 (API MPMS 19.1)] over that which appeared in the Þrst edition of API Bulletin 2518. The working loss equation in the second edition of API Publication 2518 remained the same as that in the First Edition. This third edition utilizes the same equations as those in the second edition, but presents simpliÞed calculation procedures as well as additional information. The following improvements have been incorporated into this edition:

a. To estimate estimate losses from unstable unstable or boiling boiling stocks or from petroleum liquids or petrochemicals for which the vapor pressure is not known or cannot readily be predicted. b. To estimate estimate losses from from Þxed-roof Þxed-roof tanks which which have an internal ßoating roof.

a. SimpliÞed SimpliÞed forms of the the emissions emissions estimating estimating equations equations for for the common scenario of a low volatility liquid (i.e., true vapor pressure not greater than 0.1 psia) stored in a Þxed roof tank with vents that are either open or have very low set points [i.e., not greater than 0.03 pounds (0.5 oz) per square inch].

c. To estimate estimate losses from from Þxed-roof Þxed-roof tanks which which have either either roof or shell insulation. A complete guide for estimating evaporative stock loss or the equivalent total atmospheric emissions from volatile stocks stored in Þxed-roof tanks is included in 19.1.2. Detailed equations are given in 19.1.2.1, for vertical aboveground tanks storing liquid stocks of low volatility at nearly atmospheric conditions. In addition, the following special cases are addressed in 19.1.2.1.4:

b. Methods Methods to estimate estimate emissions emissions from horizontal horizontal tanks. tanks. c. Methods Methods to account account for the vent vent setting setting when estimating estimating emissions from tanks with vent settings greater than 0.03 pounds (0.5 oz) per square inch (the previous edition accounted for the vent setting when estimating standing storage loss, but did not account for the vent setting when estimating working loss).

a. Horizo Horizonta ntall tanks. tanks. b. Higher volatili volatility ty stocks (true vapor vapor pressure greater greater than 0.1 psia).

d. Methods Methods to speciate estimated estimated emissions emissions of individual individual chemicals from the estimate of total hydrocarbon emissions for a multicomponent hydrocarbon mixture.

c. Higher vent vent settings settings [breather [breather vent vent settings, settings, P BP and P BV , beyond the typical range of ±0.03 pounds (0.5 oz) per square inch].

This publication was developed by the API Committee on Evaporation Loss Estimation. The equations presented are based on test-tank and Þeld-tank data. The equations are intended to provide loss estimates for general equipment types, since it is not within the scope of this publication to address speciÞc proprietary equipment designs. Types of Þxed-roof tanks and roof Þttings currently available are described for information only. This publication is not intended to be used as a guide for equipment design, selection, or operation. The equations are intended to be used to estimate average annual losses from uninsulated Þxed-roof tanks for various ` ` , , ` , , , ` ` , ` ` ` ` , , ` ` , ` `


A description of how to determine speciÞc values for the variables included in the equations is given in 19.1.2.2. References are made to tables and Þgures that include information about the most common (typical) values to use when speciÞc information is not available. The loss-estimation procedures are summarized in 19.1.2 (Tables 2 and 3). When the procedures in 19.1.2 are applied to a Þxed-roof tank storing a multicomponent hydrocarbon stock, the result is an estimate of the total hydrocarbon emissions from the tank. Guidance for speciating total hydrocarbon emissions into the emissions of the 1 Licensee=Inspectorate Licensee=Inspectorate America Corp/5966443001 Corp/5966443001 Not for Resale, 06/05/2009 08:02:04 MDT

2

CHAPTER 19—EVAPORATIVE LOSS MEASUREMENT

individual components is provided in 19.1.2.3.1. A sample problem estimating total emissions is presented in 19.1.2.4. Typical Þxed-roof tank construction is described in 19.1.3. The bases and development of the loss-estimation procedures presented in 19.1.2 are described in 19.1.4. The estimation procedures were developed to provide estimates of typical losses from Þxed-roof tanks that are properly maintained and in normal working condition. Losses from poorly maintained tanks may be greater. Because the loss equations are based on equipment conditions that represent a large population of tanks, a loss estimate for a group of Þxed-roof tanks will be more accurate than a loss estimate for an individual tank. It is difÞcult to determine precise values of the loss-related parameters for any individual tank. Equipment should not be selected for use based solely on evaporative-loss considerations. Many other factors not addressed in this publication, such as tank operation, maintenance, and safety, are important in designing and selecting tank equipment for a given application.

19.1.1 19. 1.1.2 .2 RE REFE FEREN RENCED CED PUB PUBLIC LICATI ATIONS ONS [l] API, Welded Steel Tanks for Oil Storage, Standard 650, Eighth Edition, Washington, D.C., November 1988. [2] U.S. Department of Commerce, National Oceanic and Atmospheric Administration, ÒComparative Climatic Data Through 1984,Ó National Climatic Data Center, Asheville, North Carolina, 1986. [3] Cinquemani, V., J.R. Owenby, Jr., and R.G. Baldwin, ÒInput for Solar Systems,Ó Prepared by the U. S. Department of Commerce, National Oceanic and Atmospheric Administration, Environmental and Information Service, National Climatic Center, Asheville, North Carolina, Prepared for the U.S. Department of Energy, Division of Solar Technology, under Interagency Agreement No. E (49-26)-1041, November 1978 (Revised August 1979). Evaporation Loss from Internal Internal Floating-Roof Floating-Roof [4] API, Evaporation Tanks, Publication 2519, Third Edition, Washington, D.C., June 1983.

[5] U.S. Environmental Protection Agency, ÒCompilation of Air Pollutant Emission Factors,Ó USEPA Report No, AP-42, Third Edition, Section 4.3, ÒStorage of Organic Liquids,Ó September 1985. Handbook of Chemistry Chemistry and [6] The Chemical Rubber Co., Handbook Physics, 5lst Edition, R.C. Weast, Editor, Cleveland, Ohio, pp. Dl46ÐDl65, 1970.

[7] API, Technical Data BookÑPetroleum ReÞning, Publication 999, Ninth Revision, Washington, D.C., 1988. [8] PerryÕs Chemical EngineersÕ Handbook , Sixth Edition, R.H. Perry, D.W. Green, and J.O. Maloney, Editors, McGraw-Hill Book Co., Inc., New York, York, New York, York, 1984.

[9] API, Use of Pressure-Vacuum Vent Valves for Atmospheric Pressure Tanks to Reduce Evaporation Loss, Bulletin 2521, First Edition, Washington, D.C., September 1966. [10] API, Venting Atmospheric and Low-Pressure Storage Tanks (Nonrefrigerated and Refrigerated), Standard 2000, Third Edition, Washington, D.C., January 1982. Evaporation Loss from Fixed-Roof Fixed-Roof Tanks Tanks, Bulletin [11] API, Evaporation 2518, First Edition, Washington, D.C., June 1962.

[12] Engineering-Science, Inc., ÒHydrocarbon Emissions From Fixed-Roof Petroleum Tanks,Ó Prepared for the Western Oil and Gas Association, July 1977. [13] Engineering-Science, Inc., ÒSynthetic Organic Chemical Manufacturing Industry, Emission Test Report, Breathing Loss Emissions From Fixed-Roof Petrochemical Storage Tanks,Ó Prepared for the U.S. Environmental Protection Agency, EPA Report No. EMB-78-OCM-5, February 1979. [14] Environmental Monitoring & Services, Inc. (subsidiary of Combustion Engineering Co.), ÒBreathing Loss Emissions From Fixed-Roof Tanks,Ó Tanks,Ó Final Report, Prepared for the API, Committee on Evaporation Loss Measurement, June 1985. [15] Beckman, DufÞe and Associates, ÒEvaporation Loss of Petroleum From Storage Tanks,Ó Final Report, Prepared for the API, Committee on Evaporation Loss Measurement, August 1, 1982. [16] Knodel, B.D. and Laverman, R.J., ÒData Base Generation, Analysis, and Revision of API Bulletin 2518, Task 1: Validate Computer Model,Ó Final Report for Task 1, Prepared by CBI Industries, Inc., Prepared for the API, Committee on Evaporation Loss Measurement, Task Group 2518, September 11, 1986. [17] Rinehart, J.K. and Laverman, R.J., ÒData Base Generation, Analysis, and Revision of API Bulletin 2518, Task 3: Correlate Data Base,Ó Final Report for Task 3, Prepared by CBI Industries, Inc., Prepared for the API, Committee on Evaporation Loss Measurement, Task Group 2518, August 26, 1988. [18] API, ÒEvaporation Loss in the Petroleum IndustryCauses and Control,Ó Publication 2513, First Edition, Washington, D.C., February 1959. [19] Rinehart, J.K. and Laverman, R.J., ÒData Base Generation, Analysis and Revision of API Bulletin 2518, Task 2: Generate Computer Data Base,Ó Final Report for Task 2, Prepared by CBI Industries, Inc., Prepared for the API, Committee on Evaporation Loss Measurement, Task Group 2518, February 16, 1987. [20] API, ÒSymposium on Evaporation Loss of Petroleum From Storage Tanks,Ó Papers Presented During the 32nd Annual Meeting of the American Petroleum Institute, Held in Chicago, Illinois, November 10, 1952, (Also Published in API Proceedings, Vol. 32, Part I, 1952, pp. 212Ð281).

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SECTION 1—EVAPORATIVE LOSS

19.1.2 19.1.2.1 19.1.2.1.1

Procedures For Calculating Losses

d. The daily daily ambient ambient temperature temperature range. e. The daily daily total solar solar insolation insolation on a horizontal horizontal surface. surface.

08

f. The atmosphe atmospheric ric pressur pressure. e.

General

g. The molecular molecular weight weight of the stock stock vapor. vapor.

Procedures for estimating the total annual evaporative stock loss, or the equivalent atmospheric hydrocarbon vapor emissions, from volatile stocks stored in fixed-roof tanks, are outlined in 19.1.2. The total loss, LT , is the sum of the standing storage loss, LS , and the working loss, LW : LT (pounds per year) = LS (pounds per year)

(1)

A complete list of nomenclature, including conversion relationships, is given in Table 1. In addition, descriptions of the variables used in the calculation procedure summaries of Tables 2 and 3 are repeated in those tables. A description of how to determine specific values for the variables is given in 19.1.2.2. The following conditions are assumed in the calculation procedures procedures presented presented in 19.1.2.1.2 19.1.2.1.2 and 19.1.2.1.3: 19.1.2.1.3: a. The tank is a vertical vertical cylinder (for (for horizontal horizontal cylindrical cylindrical tanks, see 19.1.2.1.4.1). b. The liquid stock stock has a true vapor vapor pressure pressure not greater greater than 0.1 psia (for higher volatility stocks, see 19.1.2.1.4.2). c. The vents vents are either open open or are set set at approximately approximately ±0.03 ±0.03 pounds (0.5 oz) per square square inch (for higher vent settings, see 19.1.2.1.4.3).

19.1.2.1.2

3

c. The daily average ambient temperature. temperature.

LOSS EQUATIONS

+ LW (p (pounds per year)

FROM FIXED-ROOF T ANKS

h. The stock stock liquid liquid surface surface temperature. temperature. The standing storage loss, L s , pertains to loss of stock vapors which occurs as a result of tank vapor space breathing. The standing storage loss can be estimated from Equation 2:

π 2 ⎝4 ⎠

L S = 365 K E H VO ⎛ -- D ⎞ K S W V

(2)

where K E , H VO, K S , and W V are calculated from Equations 3, 4, 5, and 6, respectively, and the tank diameter, D, is specified by the user user.. Vapor Space Expansion Factor, K E K E = 0.04

(3a)

A more accurate estimate of K E may be obtained using Equation 3b when the solar absorptance factor ( α) is known for the tank outside surface color and the average daily maximum and minimum ambient temperatures (T MAX and T MIN ) and the daily total solar insolation ( I ) are known for the tank location (in order to calculate the daily vapor temperature range, ΔT V , from Equation 25b). K E = 0.0018 ΔT V

(3b)

Standing Storage Loss, LS

The following minimum information is needed to calculate the standing storage loss, LS :

Vapor Space Outage, H VO H VO = H S – H L + H RO

(4)

a. The tank diameter diameter.. b. The tank shell height. height.

Vented Vapor Saturation Factor, K S

c. The tank tank roof type (cone (cone roof roof or dome dome roof). d. The tank tank outside outside surface color. color. e. The The tank tank locati location on.. f. The The stoc stock k type type.. g. The stock liquid bulk temperature. temperature.

1

K S = --------------------------------------------1 + 0.053 P VA H VO

(5)

Stock Vapor Density, W V

h. The stock vapor vapor pressure pressure (or the stock stock Reid vapor vapor pressure). pressure).

M V P VA W V = ----------------- R T L A

(6)

i. The The stock stock liqu liquid id leve level. l. Improved estimates of the standing storage loss can be obtained through a knowledge of some or all of the following additional information: a. The tank cone roof roof slope or dome roof roof radius. b. The breather breather vent vent pressure pressure and vacuum vacuum settings. settings.

` ` , , ` , , ,


The constant, 365, in Equation 2 is the number of daily events in a year, and has units of (year) –l. The constant, 0.04, in Equation 3a is dimensionless. The constant, 0.0018, in Equation 3b has units of (degrees Rankine) –1. The constant, 0.053, in Equation 5 has units of [(pounds per square inch absolute) feet] –1.


4


Table 1—Nomenclature Reference Information Symbol

08

A B D D E H E H L H LX H R H RO H S S H VO I K B K E K P K S S K N L LS LT LW M V N P A P BP P BV Δ P B P VA P VI P VN P VX Δ P V Q

08

R R R RS RVP S S R T 5 T 15 T A T AA T AN T AX ΔT A T B T LA T LN T LX T MAX T MIN T V V ΔT V V LX

Description

Units

Constant in the vapor pressure equation Constant in the vapor pressure equation Tank diameter Effective tank diameter, horizontal tanks Effective tank height, horizontal tanks Stock liquid height (or innage) Stock maximum liquid height Tank roof height Roof outage (or shell height equivalent to the volume contained under the roof) Tank shell height Vapor space outage (or height) Daily total solar insolation on a horizontal surface Vent setting correction factor Vapor space expansion factor Working loss product factor Vented vapor saturation factor Working loss turnover factor End-to-end length, horizontal tanks Standing storage loss Total loss Working loss Stock vapor molecular weight Stock turnover rate Atmospheric pressure Breather vent pressure setting (always a positive value) Breather vent vacuum setting (always a negative value) Breather vent pressure setting range Stock vapor pressure at the daily average liquid surface temperature pressure pressure of the vapor space space at initial initial (normal (normal operating) operating) condition conditionss for pressurized pressurized service service Stock vapor pressure at the daily minimum liquid surface temperature Stock vapor pressure at the daily maximum liquid surface temperature Stock daily vapor pressure range Stock annual net throughput (associated with increasing the stock liquid level in the tank) Ideal gas constant (10.731) Tank dome roof radius Tank shell radius Stock Reid vapor pressure Stock ASTM-D86 distillation slope at 10 volume percent evaporated Tank cone roof slope Temperature at which 5 volume percent is evaporated Temperature at which 15 volume percent is evaporated Ambient temperature Daily average ambient temperature Daily minimum ambient temperature Daily maximum ambient temperature Daily ambient temperature range Liquid bulk temperature Daily average liquid surface temperature Daily minimum liquid surface temperature Daily maximum liquid surface temperature Daily maximum ambient temperature Daily minimum ambient temperature Vapor temperature Daily vapor temperature range Tank maximum liquid volume (or tank liquid capacity)


Dimensionless °R ft ft ft ft ft ft ft ft ft Btu/ft2 da day Dimensionless Dimensionless Dimensionless Dimensionless Dimensionless ft lb/yr or bbl/yr lb/yr or bbl/yr lb/yr or bbl/yr lb/lb-mole Turnovers/yr psia psig psig psi psia psig psia psia psi bbl/yr psia ft 3/lb-mole °R ft ft psi °F/vol % ft/ft °F °F °R °R °R °R °R °R °R °R °R oF oF °R °R ft3


Equations 31, 34 32, 35 — 10 11 — — 17 16 — 4 9, 15 3, 14 43 5 8 — 2, 12, 44 1 7, 13, 46 — 42 — — 40 29, 37

30, 38 28, 36 39

Tables

Figures

6, 7 6, 7 — — — —

3, 6 4, 7 1

1 — 1 2 1 —

— — — — 4 — — —

— 2

— — 9 10 — — —

3 6, 7 — — — — 6, 7

5, 8

6, 7 6, 7

5, 8 5, 8

— — —

—

—

33 — — — 20 19 18 21 23 24 27 26 — — 25 —

— — — — 8 — — — —

lb 1 — — 1a — — —

— —

— — — —

— — 4 4 — —

— —

— —

` , , ` , ` , , ` , , ` ` ` ` , , , ` ` ` , ` ` , , ` ` ` ` , ` ` , , , ` , , ` ` -

SECTION 1—EVAPORATIVE LOSS FROM FIXED-ROOF T ANKS

5

Table 1—Nomenclature (Continued) Reference Information Symbol V V W L W V W VC

Description

Units

Tank vapor space volume Stock liquid density Stock vapor density Stock condensed vapor density at 60°F

Equations

Tables

ft3

Figures

45

lb/gal lb/ft3 lb/gal

6 41

— 7 — 6, 7

— — — —

Dimensionless Dimensionless Dimensionless Dimensionless

22 — — —

5 5 5 —

— — — —

— —

— —

— —

— — — — — — — — — — — — — — — — — — — — — — — — — — — —

— — — — — — — — — — — — — — — — — — — — — — — — — — — —

— — — — — — — — — — — 08 — — — — — — — — — — — — — 08 — — — —

— — — — —

— — — — —

— — — — —

— — —

— — —

— — —

Greek Symbol Notation α α R α s π

Tank surface solar absorptance Tank roof surface solar absorptance Tank shell surface solar absorptance Constant (3.14159) Function Notation

Exp( ) Exponential value of the quantity in parentheses ln ( ln ( ) Natural logarithm logarithm value of the quantity quantity in parenthes parentheses es Subscript Notation A A A A N A X B BP BV E L L A L N L X MA X MIN N P R RO S T V VA VC VI VN VO V X W

Ambient, or atmospheric Ambient average Ambient minimum, degrees Rankine Ambient maximum, degrees Rankine Breather, or liquid bulk Breather pressure Breather vacuum Expansion Liquid Liquid average Liquid minimum Liquid maximum Ambient maximum, degrees Fahrenheit Ambient minimum, degrees Fahrenheit Turnover Product Roof Roof outage Standing, or shell, or saturation Total Vapor Vapor average Vapor condensed Initial or normal operating condition of the vapor space Vapor minimum Vapor outage Vapor maximum Working Unit Notation

Btu lb lb-mole °R °F

Br B ritish thermal unit Pound mass Pound mole Degree Rankine Degree Fahrenheit

Conversion Relationships °R = °F + 459.67 psia = psig + 14.696 14.696 barrels = pounds/(42 pounds/(42 WVC)

--``,,`,,,``,````,,``,```,,,``-`-`,,`,,`,`,,`---



08

6


Table able 2—Summary of Procedures for Calculating Standing Storage Loss ( LS ) Standing Storage Loss Equation LS (lb/yr)

Variable K E

∆T V

Description

= 365 K E H VO (π/4) D 2 K S W V

Equation

Vapor space expansion factor

Dimensionless

= 0.04

3a

= 0.0018 ∆T V

3b

Daily vapor temperature range = 0.72 ( T MAX Ð T MIN ) + 0.028 α I

Units

(2) Source

Calculate from Equation 3a or 3b for stocks with a true vapor pressure not greater than 0.1 psia, stored in tanks with the breather vent setting range not greater than ±0.5 oz/in 2 Calculate from Equation 14 for stocks with a higher stock vapor pressure or for tanks with a higher vent setting range

¡R

Calculate from Equation 25b

25b

T MAX

Daily maximum ambient temperature

oF

User speciÞed or Table 4

T MIN

Daily minimum ambient temperature

oF


α

Tank surface solar absorptance

I

Daily total solar insolation on a horizontal surface

H VO

Vapor space outage = H S Ð H L + H RO

Dimensionless

User speciÞed or Table 5 Calculate from Equation 22 for different color roof and shell

Btu/ft 2 day


ft

Calculate from Equation 4

4

H S

Tank shell height

ft

User speciÞed (Figure 1)

H L

Stock liquid height (or innage)

ft


Roof outage

ft

Calculate from Equation 16a for a cone roof Calculate from Equation 16b for a dome roof

ft

User speciÞed (Figure 1), or Equation 17a for a cone roof Equation 17b for dome roof

` ` , , ` , , , ` ` , ` ` ` ` , , ` ` , ` ` ` , , , ` ` ` ` , , ` , , ` , ` , , ` -

H RO

H R

S R

= (1/3) H R

16a

= H R [(1/2) + (1/6)( H R /RS )2]

16b

Tank roof height

= S R RS

17a

= R R Ð ( R R R 2 Ð RS 2)0.5

17b

Tank cone roof slope


ft/ft



SECTION 1—EVAPORATIVE LOSS FROM FIXED-ROOF TANKS

7

Table able 2—Summary of Procedures for Calculating Standing Storage Loss ( L LS ) (Continued) Standing Storage Loss Equation LS (lb/yr)

Variable

Description

= 365 K E H VO (π/4) D 2 K S W V

Equation

Units

(2) Source

RS

Tank shell radius

ft


R R

Tank dome roof radius

ft


D

Tank diameter

ft

User speciÞed

K S

Vented vapor saturation factor

Dimensionless 5

1 K S = --------------------------------------------1 + 0.053 PVA H VO PVA


Stock vapor pressure at the daily average liquid surface temperature

= exp[ A Ð ( B/T B/T LA)]

psia

Calculate from Equation 29 or Figure 5 for reÞned petroleum stocks Figure 8 for crude oil stocks

29

A

Constant in the 2-constant vapor pressure equation

Dimensio Dimensionles nlesss

Table 6 for for selected selected petrol petroleum eum liqui liquid d stocks stocks Table 7 for selected petrochemical stocks Equation 31 or Figure 3 for reÞned petroleum stocks Equation 34 or Figure 6 for crude oil stocks

B


¡R

Tabl able 6 for for sele seleccted ted petro etrole leu um liqu iquid sto stocks cks Table 7 for selected petrochemical stocks Equation 32 or Figure 4 for reÞned petroleum stocks Equation 35 or Figure 7 for crude oil stocks

T LA

Daily average liquid surface temperature

¡R


¡R

User speciÞed or Table 4 and Equations 18 Ð 20

= T AA + 0.56(6 α Ð 1) + 0.0079

αI

T AA

Daily average ambient temperature

W V

Stock vapor density

M V PVA = ----------------- R T LA R

Ideal gas constant (10.731)

24b

lb/ft3


6

3

psia ft lb-mole ¡R

-----------------------

M V

Stock vapor molecular weight

lb/lb-mole

User speciÞed or Table 6 for selected petroleum liquid stocks Table 7 for selected petrochemical stocks 64 for gasoline 50 for U.S. mid-continent crude oil stocks

--``,,`,,,``,````,,``,```,,,``-`-`,,`,,`,`,,`---



8


Table 3—Summary of Procedures for Calculating Working Loss (LW ) Working Loss Equations = N H L X (π (π/4) D /4) D2 K N K P K B W V L W (lb/yr) = N Variable N

Description Stock turnover rate Q = 5.614 -----------------------------------2 ( π ⁄ 4 ) D H L X

08

Q

Stock annual net throughput

D

Units turnover/yr

Source User specified or Calculate from Equation 42

(42)

bbl/yr

User specified

Tank diameter

ft

User specified

H LX

Stock maximum liquid height

ft

User specified

K N

Working loss turnover factor =1 (for N<36) ( 180 + N ) ------------------------6 N

(for N >36)

Dimensionless

Calculate from Equation 8a or 8b

(8a) (8b)

K P

Working loss product factor

Dimensionless

0.75 for crude oil stocks 1.0 for refined petroleum stocks 1.0 for single-component petrochemical stocks

K B

Vent setting correction factor

Dimensionless

Calculate from Equation 9 for breather vent setting 2 pressure range, Δ P B , B , not greater than ±0.5 oz/in Calculate from Equation 15 for higher vent settings

= 1.0 W V

Stock vapor density = ( M M V P VA) / ( R R T LA)

M V

Stock vapor molecular weight

P VA

Stock vapor pressure at the daily average liquid surface temperature = exp [ A – A – ( B/T B/T LA)]

` ` , , ` , , , ` ` , ` ` ` ` , , ` ` , ` ` ` , , , ` ` ` ` , , ` , , ` ,

Equation

(7)

A


B


R

ideal gas constant (10.731)

T LA

Daily average liquid surface temperature = T 0.56(6α – 1) + 0.0079α 0.0079α I AA + 0.56(6α

T AA

Daily average ambient temperature

α

Tank surface solar absorptance

I

Daily total solar insolation on a horizontal surface


9 lb/ft3


6 lb/lb-mole

psia

User specified or Table 6 for selected petroleum liquid stocks Table 7 for selected petrochemical stocks 64 for gasoline 50 for U.S. midcontinent crude oil stocks Calculate Calculate from from Equation Equation 29 or Figure 5 for refined petroleum stocks Figure 8 for crude oil stocks

(29) Dimens Dimensionl ionless ess

°R

Table able 6 for for selec selected ted petrole petroleum um liqui liquid d stocks stocks Table 7 for selected petrochemical stocks Equation 31 or Figure 3 for refined petroleum stocks Equation 34 or Figure 6 for crude oil stocks Table ble 6 for for se selected pe petrol roleum liqui quid st stock ocks Table 7 for selected petrochemical stocks Equation 32 or Figure 4 for refined petroleum stocks Equation 35 or Figure 7 for crude oil stocks

psia ft3/lb-mole oR °R


oR

User specified or Table 4 and Equations 18 through 20

24b

Dimensionless

Btu/ft2 day day

User specified or Table 5 Calculate from Equation 22 for different color roof and shell User User spe specifi cifieed or or Tab Tablle 4



9

The procedures used to calculate the standing storage loss are summarized in Table 2.

The procedures used to calculate the working loss are summarized in Table 3.

19.1. 19.1.2.1 2.1.3 .3 Working orking Loss, Loss, LW

19.1 19.1.2 .2.1 .1.4 .4 Spec Specia iall Case Cases s

The working loss, LW , can be calculated from the following information:

19.1.2 19. 1.2.1. .1.4.1 4.1 Horiz Horizont ontal al Tank Tanks s

a. The stock stock vapor vapor molecul molecular ar weight. weight. b. The stock vapor vapor pressure pressure (or the stock stock Reid vapor vapor pressure). c. The tank diamete diameterr and stock maximu maximum m liquid height height or the the stock annual net throughput (associated with increasing the stock liquid level). d. The stock turnover turnover rate. e. The The stoc stock k type type.. Improved estimates of the working loss can be obtained through a knowledge of some or all of the following additional information:

If a user needs to estimate emissions from a horizontal Þxed-roof tank, the length and diameter of the horizontal tank may be transformed to the diameter and height of an equivalent vertical tank. First, assume that the horizontal tank is a cylinder (i.e., that the cross section at its middle extends all the way to each of its ends). Then, by assuming the horizontal tank to be one-half full, the surface of the liquid in the tank describes a rectangle, having a length equal to the length of the tank and a width equal to the cross-sectional diameter of the tank. This liquid-surface rectangle of the horizontal tank may be converted to a circle of equal area to describe an equivalent vertical tank. The diameter, D E , of the equivalent vertical tank is calculated from Equation 10.

a. The breather breather vent pressur pressuree settings. settings. D E =

b. The stock stock liquid liquid surface surface temperatur temperature. e. The working loss, LW , pertains to loss of stock vapors which occurs as a result of tank emptying and Þlling operations. The working loss can be estimated from Equation 7:

π

L W = N H LX  -- D 4

 K N K P 

2

K B W V

(7)

If the annual net throughput, Q, is known, the terms N , 2 H LX , and (π/4) D can be replaced by the following equivalence:

π

N H LX  -- D 4

 = 

2

5.614 Q

where the constant, 5.614, has units of cubic feet per barrel. The working loss turnover factor, K N , is calculated from Equation 8a when the stock turnover rate, N , does not exceed 36 tank turnovers per year, and from Equation 8b when the tank turnovers exceed 36 per year. K N = 1

(for N ≤36)

K )/(6 N ) N = (180 + N )/(6

(for N ≥36)

where L = length of the the horizontal horizontal tank (for tanks tanks with with rounded ends, use the overall length), and D = diameter diameter of a vertical vertical cross-se cross-section ction of of the horihorizontal tank.

The height, H E , of the equivalent vertical tank is determined by calculating the height of the vertical tank that will result in an enclosed volume approximately equal to that of the horizontal tank. By assuming the volume of the horizontal tank to be equal to the cross-sectional area of the tank times the length of the tank, the height, H eq uivalent vertical E , of an equivalent tank may be calculated from Equation 11. H E = (π /4) D

(11)

The standing storage loss of the horizontal tank may be H calculated by substituting D E for D and ( H E /2) for H VO in Equation 2, as shown in Equation 12.

(8b)

(9)

H E π 2 L S = 365 K E  -------  -- D E  K S W V  2   4 

(12)

Alternatively, the standing storage loss of the horizontal tank may be calculated without Þrst determining D E and H E , if the head space volume of the horizontal tank is known. Equation 12 would be modiÞed by substituting the head space volume, expressed in cubic feet, for the term,

--``,,`,,,``,````,,``,```,,,``-`-`,,`,,`,`,,`---


(10)

(8a)

The vent setting correction factor, K B, is equal to 1 for a breather vent setting range, ∆P B, not greater than the typical range of ±0.03 pounds (0.5 oz) per square inch. K B = 1

L D ----------π ⁄ 4


10


2 H [( H E /2) (π/4 D E )], and the standing storage loss could then be calculated. For underground horizontal tanks, assume that no standing storage losses occur ( LS = 0) because the insulating nature of the earth limits the diurnal temperature change. The working loss of the horizontal tank may be estimated by substituting D E in place of D, and H E in place of H LX , in Equation 7. This modiÞed form of Equation 7 is shown in Equation 13.

π

L W = N H E  -- D E  K N K P K B W V  4  2

When: P BP + P A K N -------------------PVI + P A

19.1.2.1 19.1.2.1.4.2 .4.2 Higher Higher Volatilit olatility y Stock Stocks s When the liquid stock has a true vapor pressure greater than 0.1 psia, a more accurate estimate of the vapor space expansion factor, K E , should be calculated from Equation 14.

(14)

> 1.0

Then:

(13)

Alternatively, the working loss of the horizontal tank may be calculated without Þrst determining D E and H E , if the annual net throughput, Q, of the horizontal tank is known. Given the annual net throughput, the working loss may be calculated from Equation 7 by replacing the N , H LX , and (π/4) 2 D terms with the equivalent term, 5.614 Q.

∆ T V ∆ P V Ð ∆ P B K E = ---------- + -------------------------- ≥ 0 T LA P A Ð PVA

sion is less than or equal to 1), use the value of 1 for K B from Equation 9.

K B =

P VI + P A -------------------- Ð PVA K N ----------------------------------P BP + P A Ð PVA

(15)

where K working loss loss turnove turnoverr (saturati (saturation) on) factor factor N = working (dimensionless),

breather vent vent pressure pressure setting, setting, in pounds per P BP = breather square inch gauge, P A = atmospheric atmospheric pressure, pressure, in in pounds pounds per per square square inch absolute, PVI = pressure pressure of the the vapor vapor space space at initia initiall (normal (normal operating) conditions, in pounds per square inch gauge, K setting correction correction factor factor (dimension (dimensionless) less),, B = vent setting PVA = stock vapor pressure pressure at the the daily daily average average liquid liquid surface temperature, in pounds per square inch absolute.

where the stock daily vapor pressure range, ∆PV , may be calculated from Equation 39a or 39b. The standing storage loss of the tank storing the higher volatility stock would then be calculated from Equation 2 using the value of K E determined from Equation 14. When the calculation of Equation 14 yields a negative value for K E , use zero as the value of K E . This will result in an estimated standing storage loss of zero, on the basis that the vent pressure setting range, ∆P B, is sufÞciently high to prevent breathing losses from occurring during the average conditions assumed. The working loss of the tank storing the higher volatility stock would be calculated from Equation 7 without any modiÞcation.

The standing storage loss of the tank with the higher vent settings is calculated from Equation 2 using the value of K E determined from Equation 14. When the calculation of Equation 14 yields a negative value for K E , use zero as the value of K E as explained in 19.1.2.1.4.2. The working loss of the tank with the higher vent settings is calculated from Equation 7 using the value of K B determined from Equation 15, if the given condition is met, to account for any reduction in emissions due to condensation of vapors prior to the opening of the vent.

19.1.2 19. 1.2.1. .1.4.3 4.3 Higher Higher Vent Sett Setting ings s

19.1. 19.1.2.2 2.2 DIS DISCUS CUSSIO SION N OF VARI VARIABL ABLES ES

When the breather vent settings are signiÞcantly higher than the typical range of plus and minus one-half ounce per square inch, a more accurate estimate of the vapor space expansion factor, K E , may be calculated from Equation 14. Higher vent settings may also warrant the use of a value less than 1 for the vent setting correction factor, K B, as determined from Equation 15. When the following condition is met, then a vent setting correction factor, K B, may be determined using Equation 15. When this condition is not met (i.e., the value of the expres-

19.1 19.1.2 .2.2 .2.1 .1 Gene Genera rall

` ` , , ` , , , ` ` , ` ` ` ` , , ` ` , ` ` ` , , , ` ` ` ` , , ` , , ` , ` , , ` -


Information is summarized in 19.1.2.2.2 and 19.1.2.2.3 on how to determine speciÞc values for the variables in the loss equations given in 19.1.2.1. Tables, graphs, and the range of values of the variables for which the loss equations are applicable are cited for reference. To obtain the most accurate estimate, detailed information pertinent to the speciÞc tank or tanks under consideration should be used. The typical values included in 19.1.2.2 and



the cited tables and Þgures should be used only when actual detailed information is not available. More detailed discussion of the deÞnition, development and effects of the variables is given in 19.1.4.

where H outage (or additional additional shell shell height height equivale equivalent nt RO = roof outage to the volume contained under the roof), in feet, H tank roof roof heigh height, t, in feet, feet, R = tank S roof slope, slope, in feet per foot, foot, R = tank cone roof

19.1.2.2 19.1.2.2.2 .2 Standin Standing g Storag Storage e Loss Loss Variables ariables The standing storage loss, LS , is related in Equation 2 to the following variables: a. Tank vapor vapor space volume, volume, V V (expressed in terms of H VO and D). b. Stock vapor vapor density density,, W V .

RS = tank tank shell shell radi radius, us, in in feet. feet.

If the tank cone roof slope, S R, is not known, a typical value of 0.0625 feet per foot may be assumed.

19.1 19.1.2 .2.2 .2.2 .2.1 .1.2 .2 Dome Dome Roo Rooff For a dome roof, the roof outage (or additional shell height equivalent to the volume contained under the roof), H RO, may be determined from Figure 2 or calculated from Equation 16b:

c. Vapor space space expansion expansion factor factor,, K E . d. Vented vapor vapor saturation saturation factor, factor, K S . These variables can be calculated using Equations 3 through 6. Data sources and proper usage for each of the variables in Equations 3 through 6 are described in 19.1.2.2.2.1 through 19.1.2.2.2.13.

19.1. 19.1.2.2 2.2.2. .2.1 1

The vapor space outage, H VO, is the height of a cylinder of tank diameter, D, whose volume is equivalent to the vapor space volume of a Þxed-roof tank, including the volume under the cone or dome roof. Figure 1 illustrates the geometry of a Þxed-roof tank with either a cone roof or dome roof. The vapor space outage may be determined from Equation 4: (4)

where H VO = vapor vapor space space outag outage, e, in feet, feet,

tank shell shell height height,, in feet, feet, H S = tank H liquid height, height, in feet, feet, L = stock liquid H outage (or additional additional shell height height equivale equivalent nt RO = roof outage

to the volume contained under the roof), in feet.

H RS )2] RO = H R [1/2 + 1/6 ( H R/ R

(16b)

H R R2 Ð RS 2)0.5 R = R R Ð ( R

(17b)

where

Vapor apor Space Space Outage Outage,, H VO

H VO = H S Ð H L + H RO

where outage (or addition additional al shell height height equiv equivalent alent H RO = roof outage to the volume contained under the roof), in feet, tank roof roof height height,, in feet feet,, H R = tank RS = tank tank shell shell radi radius, us, in in feet, feet,

tank dome roof roof radiu radius, s, in feet. feet. R R = tank Figure 2 shows for a dome roof that the ratio H RO:H R varies from 0.500 to 0.666. This may be compared to the same ratio for a cone roof which, from Equation 16a, is a constant value of 0.333. Section 3.10.6 of API Standard 650 [1] indicates that the tank dome roof radius, R R, varies between a minimum of 0.8 D and a maximum of 1.2 D. If the tank dome roof radius is not known, a typical value of 1.0 D may be assumed. In this case, Equations 16b and 17b simplify to Equations 16c and 17c:

19.1 19.1.2 .2.2 .2.2 .2.1 .1.1 .1 Cone Cone Roo Rooff For a cone roof, the roof outage (or additional shell height equivalent to the volume contained under the roof), H RO, can be calculated from Equation 16a: H RO

1 = -- H R 3

11

(16a)

H RO = 0.137 RS

(16c)

H R = 0.268 RS

(17c)

19.1.2 19. 1.2.2. .2.2.2 2.2 Me Mete teor orolo ologic gical al Data Data,, T MAX , T MIN , I The meteorological data needed to estimate the standing storage loss, LS , consists of: a. Daily maximum maximum ambient ambient temperature temperature,, T MAX ;

where

b. Daily minimu minimum m ambient ambient temperatur temperature, e, T MIN ; H R = S R RS


(17a)

c. Daily total total solar solar insolation insolation on a horizontal horizontal surfac surface, e, I .


` , , ` , ` , , ` , , ` ` ` ` , , , ` ` ` , ` ` , , ` ` ` ` , ` ` , , , ` , , ` ` -

12


Cone roof slope, S R

R

H

S

H

L

H

R S

D

Cone Roof

R

H

R R

` ` , , ` , , , ` ` , ` ` ` ` , , ` ` , ` ` ` , , , ` ` ` ` , , ` , , ` , ` , , ` -

S

H

L

H

R S

D

Dome Roof

Figure 1—Fixed-Roof 1—Fixed-Roof Tank Geometry Geometry




13

Equations 20 and 21, respectively: T AX + T AN T AA = -----------------------2

(20)

∆T A = T AX Ð T AN

(21)

where T average ambient ambient tempera temperature, ture, in in degrees degrees AA = daily average Rankine, T maximum ambien ambientt tempera temperature, ture, in AX = daily maximum degrees Rankine, T minimum ambien ambientt tempera temperature, ture, in AN = daily minimum degrees Rankine,

∆T A

19.1.2.2 19.1.2.2.2.3 .2.3 Tank Paint Paint Solar Solar Absorp Absorptanc tance, e, α

Figure Figure 2—Do 2—Dome me Roof Roof Outage Outage (H RO ) The term insolation refers to incident-solar-radiation. ` ` , , ` , , , ` ` , ` ` ` ` , , ` ` , ` ` ` , , , ` ` ` ` , , ` , , ` , ` , , ` -

When possible, meteorological data for the tank site should be used. If this data is not available, meteorological data from the nearest local weather station may be used. Data for selected U.S. locations are listed in Table 4. Data for other U.S. locations may be found in weather station records [2,3]. The daily maximum and minimum ambient temperatures are reported in degrees Fahrenheit, but must be converted to degrees Rankine from Equations 18 and 19, respectively: T AX = T MAX + 459.67

(18)

T AN = T MIN + 459.67

(19)

where T maximum ambient ambient tempera temperature, ture, in AX = daily maximum

The tank outside surface solar absorptance, α, is a function of the tank surface color, surface shade or type, and surface condition. Table 5 lists the solar absorptance for selected tank surfaces. Section E of the Documentation File contains additional solar absorptance values for a variety of paint colors. If speciÞc information is not available on the tank surface color and surface condition, a white shell and roof, with the paint in good condition, can be assumed to represent the most common or typical tank surface in use. If the tank roof and shell are painted a different color, Equation 22 may be used to determine the tank surface solar absorptance, α.

α

T maximum ambient ambient tempera temperature, ture, in MAX = daily maximum

degrees Fahrenheit, T minimum ambient ambient temper temperature, ature, in AN = daily minimum

degrees Rankine, T minimum ambient ambient temper temperature, ature, in MIN = daily minimum

degrees Fahrenheit. The daily average ambient temperature, T AA, and the daily ambient temperature range, ∆T A, may be calculated from

a R + a S = ---------------2

(22)

where

α α R

= tank surfac surfacee solar absorptance absorptance (dimen (dimensionle sionless), ss),

αS

= tank shell shell surface surface solar absorpt absorptance ance (dimens (dimensionionless).

degrees Rankine,


= daily ambient ambient temperat temperature ure range, range, in in degrees degrees Rankine.

= tank roof roof surface surface solar solar absorpt absorptance ance (dimens (dimensionionless),

19.1.2.2 19.1.2.2.2.4 .2.4 Liquid Liquid Bulk Bulk Temperat emperature, ure,T B The liquid bulk temperature, T B, is the average temperature of the liquid stock in the storage tank. This information is usually available from tank gaging records or other tank operating records. The liquid bulk temperature is used to estimate the daily average liquid surface temperature, T LA (see 19.1.2.2.2.5).


14


Table 4—Meteorologic 4—Meteorological al Data Data (T MAX , T MIN , I ) for Selected U.S. Locations Property

Monthly Averages

Location

Symbol

Units

Jan.

Feb.

Mar.

Apr.

May

Jun.

Jul.

Aug.

Sep.

Oct.

Nov.

Annual Dec. Average

Birmingham Airport, AL

T MAX

¡F

52.1

57.3

65.2

15.2

81.6

87.9

90.3

89.7

84.6

74.8

63.7

55.9

T MIN

¡F

33.0

35.2

42.1

50.4

58.3

65.9

69.8

69.1

63.6

50.4

40.5

35.2

51.1

I

Btu/ft2 day

707

967

1296

1674

1857

1919

1810

1724

1455

1211

858

661

1345

T MAX

¡F

57.0

60.9

68.1

77.0

83.6

89.8

91.5

91.2

86.9

77.5

67.0

59.8

75.9

T MIN

¡F

36.4

38.8

45.5

53.3

61.1

68.4

71.8

71.1

66.4

53.1

43.0

37.9

53.9

I

Btu/ft2 day

752

1013

1341

1729

1897

1972

1841

1746

1468

1262

915

719

1388

T MAX

¡F

27.0

31.2

34.4

42.1

49.8

56.3

60.5

60.3

54.8

44.0

34.9

27.7

43.6

T MIN

¡F

14.4

17.4

19.3

28.1

34.6

41.2

45.1

45.2

39.7

30.6

22.8

15.8

29.5

I

Btu/ft2 day

122

334

759

1248

1583

1751

1598

1189

791

437

175

64

838

T MAX

¡F

65.2

69.7

74.5

83.1

92.4

102.3

105.0

102.3

98.2

87.7

14.3

66.4

85.1

T MIN

¡F

39.4

42.5

46.7

53.0

61.5

70.6

79.5

77.5

70.9

59.1

46.9

40.2

57.3

I

Btu/ft2 day

1021

1374

1814

2355

2677

2739

2487

2293

2015

1577

1151

932

1869

T MAX

¡F

64.1

67.4

71.8

80.1

88.8

98.5

98.5

95.9

93.5

84.1

72.2

65.0

81.7

T MIN

¡F

38.1

40.0

43.8

49.7

57.5

61.4

73.8

72.0

61.3

56.7

45.2

39.0

54.2

I

Btu/ft2 day

1099

1432

1864

2363

2671

2730

2341

2183

1979

1602

1208

996

1872

T MAX

¡F

48.4

53.8

62.5

73.7

81.0

88.5

93.6

92.9

85.7

75.9

61.9

52.1

72.5

T MIN

¡F

26.6

30.9

38.5

49.1

58.2

66.3

70.5

68.9

62.1

49.0

37.7

30.2

49.0

I

Btu/ft2 day

744

999

1312

1616

1912

2089

2065

1877

1502

1201

851

682

1404

T MAX

¡F

49.8

54.5

63.2

73.8

81.7

89.5

92.7

92.3

85.6

75.8

62.4

53.2

72.9

T MIN

¡F

29.9

33.4

41.2

50.9

59.2

67.5

71.4

69.6

63.0

50.4

40.0

33.2

50.8

I

Btu/ft2 day

731

1003

1313

1611

1929

2107

2032

1861

1518

1228

847

674

1404

T MAX

¡F

57.4

63.7

68.6

75.1

83.9

92.2

98.8

94.4

90.8

81.0

67.4

57.6

77.7

T MIN

¡F

38.9

42.6

45.5

50.1

57.2

64.3

70.1

68.5

63.8

54.9

44.9

38.7

53.3

I

Btu/ft2 day

766

1102

1595

2095

2509

2749

2684

2421

1992

1458

942

677

1749

T MAX

¡F

66.0

67.3

68.0

70.9

73.4

77.4

83.0

83.8

82.5

78.4

72.7

67.4

74.2

T MIN

¡F

44.3

45.9

47.7

50.8

55.2

58.9

62.6

64.0

61.6

56.6

49.6

44.7

53.5

I

Btu/ft2 day

928

1215

1610

1938

2065

2140

2300

2100

1701

1326

1004

847

1598

T MAX

¡F

64.6

65.5

65.1

66.7

69.1

72.0

75.3

76.5

76.4

74.0

70.3

66.1

70.1

T MIN

¡F

41.3

48.6

49.1

52.2

55.7

59.1

62.6

64.0

62.5

58.5

52.1

47.8

55.0

I

Btu/ft2 day

926

1214

1619

1951

2060

2119

2308

2080

1681

1317

1004

849

1594

T MAX

¡F

52.6

59.4

64.1

71.0

19.1

87.4

93.3

91.7

87.6

11.7

63.2

53.2

73.4

T MIN

¡F

37.9

41.2

42.4

45.3

50.1

55.1

57.9

51.6

55.8

50.0

42.8

37.9

47.8

I

Btu/ft2 day

597

939

1458

2004

2435

2684

2688

2368

1907

1315

782

538

1643

T MAX

¡F

55.5

59.0

60.6

63.0

66.3

69.6

71.0

71.8

73.4

70.0

62.7

56.3

64.9

T MIN

¡F

41.5

44.1

44.9

46.6

49.3

52.0

53.3

54.2

54.3

51.2

46.3

42.2

48.3

I

Btu/ft2 day

708

1009

1455

1920

2226

2317

2392

2117

1742

1226

821

642

1553

Montgomery, AL

Homer, AK

Phoenix, AZ

Tucson, AZ

Fort Smith, AR

Little Rock, AR

BakersÞeld, CA

Long Beach, CA

Los Angeles Airport, CA ` ` , , ` , , , ` ` , ` ` ` ` , , ` ` , ` ` ` , , , ` ` ` ` , , ` , , ` , ` , , ` -

Sacramento, CA

San Francisco Airport, CA



73.2


15

Table 4—Meteorological 4—Meteorologi cal Data (T MAX , T MIN , I ) for Selected U.S. Locations (Continued) Property Location Santa Maria, CA

Denver, CO

Grand Junction, CO

Wilmington, DE

Atlanta, GA

Savannah, GA

Honolulu, HI

Chicago, IL

Springfield, IL

Symbol

Units

Jan.

Feb.

Mar.

Apr.

May

Jun.

Jul.

Aug.

Sep.

Oct.

Nov.

Annual Dec. Average

T MAX

°F

62.8

64.2

63.9

65.6

67.3

69.9

72.1

72.8

74.2

73.3

68.9

64.6

68.3

T MIN

°F

38.8

40.3

40.9

42.7

46.2

49.6

52.4

53.2

51.8

47.6

42.1

38.3

45.3

I

Btu/ft2 day

854

1141

1582

1921

2141

2349

2341

2106

1730

1353

974

804

1608

T MAX

°F

43.1

46.9

51.2

61.0

70.7

81.6

88.0

85.8

77.5

66.8

52.4

46.1

64.3

T MIN

°F

15.9

20.2

24.7

33.7

43.6

52.4

58.7

57.0

47.7

36.9

25.1

18.9

36.2

I

Btu/ft2 day

840

1127

1530

1879

2135

2351

2273

2044

1727

1301

884

732

1568

T MAX

°F

35.7

44.5

54.1

65.2

76.2

87.9

94.0

90.3

81.9

68.7

51.0

38.7

65.7

T MIN

°F

15.2

22.4

29.7

38.2

48.0

56.6

63.8

61.5

52.2

41.1

28.2

17.9

39.6

I

Btu/ft2 day

791

1119

1554

1986

2380

2599

2465

2182

1834

1345

918

731

1659

T MAX

°F

39.2

41.8

50.9

63.0

72.7

81.2

85.6

84.1

77.8

66.7

54.8

43.6

63.5

T MIN

°F

23.2

24.6

32.6

41.8

51.7

61.2

66.3

65.4

58.0

45.9

36.4

27.3

44.5

I

Btu/ft2 day

571

827

1149

1480

1710

1883

1823

1615

1318

984

645

489

1208

T MAX

°F

51.2

55.3

63.2

73.2

79.8

85.6

87.9

87.6

82.3

72.9

62.6

54.1

71.3

T MIN

°F

32.6

34.5

41.7

50.4

58.7

65.9

69.2

68.7

63.6

51.4

41.3

34.8

51.1

I

Btu/ft2 day

718

969

1304

1686

1854

1914

1812

1709

1422

1200

883

674

1345

T MAX

°F

60.3

63.1

69.9

77.8

84.2

88.6

90.8

90.1

85.6

77.8

69.5

62.5

76.7

T MIN

°F

37.9

40.0

46.8

54.1

62.3

68.5

71.5

71.4

67.6

55.9

45.5

39.4

55.1

I

Btu/ft2 day

795

1044

1399

1761

1852

1844

1784

1621

1364

1217

941

754

1365

T MAX

°F

79.9

80.4

81.4

82.7

84.8

86.2

87.1

88.3

88.2

86.7

83.9

81.4

84.2

T MIN

°F

65.3

65.3

67.3

68.7

70.2

71.9

73.1

73.6

72.9

72.2

69.2

66.5

69.7

I

Btu/ft2 day

1180

1396

1622

1796

1949

2004

2002

1967

1810

1540

1266

1133

1639

T MAX

°F

29.2

33.9

44.3

58.8

70.0

79.4

83.3

82.1

75.5

64.1

48.2

35.0

58.7

T MIN

°F

13.6

18.1

27.6

38.8

48.1

57.7

62.7

61.7

53.9

42.9

31.4

20.3

39.7

I

Btu/ft2 day

507

760

1107

1459

1789

2007

1944

1719

1354

969

566

402

1215

°F

32.8

38.0

48.9

64.0

74.6

84.1

87.1

84.7

79.3

67.5

51.2

38.4

62.6

T MAX

°F

16.3

20.9

30.3

42.6

52.5

62.0

65.9

63.7

55.8

44.4

32.9

23.0

42.5

Btu/ft2 day

585

861

1143

1515

1866

2097

2058

1806

1454

1068

677

490

1302

T MAX

°F

34.2

38.5

49.3

63.1

73.4

82.3

85.2

83.7

77.9

66.1

50.8

39.2

62.0

T MIN

°F

17.8

21.1

30.7

41.7

51.5

60.9

64.9

62.7

55.3

43.4

32.8

23.7

42.2

I

Btu/ft2 day

496

747

1037

1398

1638

1868

1806

1644

1324

977

579

417

1165

°F

39.8

46.1

55.8

68.1

77.1

87.4

92.9

91.5

82.0

71.2

55.1

44.6

67.6

T MIN I

Indianapolis, IN

Wichita, KS

T MAX

°F

19.4

24.1

32.4

44.5

54.6

64.7

69.8

67.9

59.2

46.9

33.5

24.2

45.1

Btu/ft2 day

704

1058

1406

1783

2036

2264

2239

2032

1616

1250

871

690

1502

T MAX

°F

40.8

45.0

54.9

67.5

76.2

84.0

87.6

86.7

80.6

69.2

55.5

45.4

66.1

T MIN

°F

24.1

26.8

35.2

45.6

54.6

63.3

67.5

66.1

59.1

46.2

36.6

28.9

46.2

I

Btu/ft2 day

546

789

1102

1467

1720

1904

1838

1680

1361

1042

653

488

1216

T MAX

°F

61.1

64.5

71.6

79.2

85.2

90.6

91.4

90.8

87.4

80.1

70.1

63.8

78.0

T MIN

°F

40.5

42.7

49.4

57.5

64.3

70.0

72.8

72.0

68.3

56.3

47.2

42.3

57.0

I

Btu/ft2 day

785

1054

1379

1681

1871

1926

1746

1677

1464

1301

920

737

1379

T MIN I

Louisville, KY

Baton Rouge, LA

Monthly Averages

--``,,`,,,``,````,,``,```,,,``-`-`,,`,,`,`,,`---



08

16


Table 4—Meteorological 4—Meteorologic al Data (T MAX , T MIN , I ) for Selected U.S. Locations (Continued) Property Location Lake Charles, LA 08

New Orleans, Orleans, LA

08

Detroit, MI

Grand Rapids, MI

Minneapolis-St. Paul, MN

Symbol

Units

Jan.

Feb.

Mar.

Apr.

May

Jun.

Jul.

Aug.

Sep.

Oct.

Nov.

Annual Dec. Average

T MAX

°F

60.8

64.0

70.5

77.8

84.1

89.4

91.0

90.8

87.5

80.8

70.5

64.0

77.6

T MIN

°F

42.2

44.5

50.8

58.9

65.6

71.4

73.5

72.8

68.9

57.7

48.9

43.8

58.3

I

Btu/ft2 day

728

1010

1313

1570

1849

1970

1788

1657

1485

1381

917

706

1365

T MAX

°F

61.8

64.6

71.2

78.6

84.5

89.5

90.7

90.2

86.8

79.4

70.1

64.4

77.7

T MIN

°F

43.0

44.8

51.6

58.8

65.3

70.9

73.5

73.1

70.1

59.0

49.9

44.8

58.7

I

Btu/ft2 day

83.5

1112

1415

1780

1968

2004

1814

1717

1514

1335

973

779

1437

T MAX

°F

30.6

33.5

43.4

57.7

69.4

79.0

83.1

81.5

74.4

62.5

47.6

35.4

58.2

T MIN

°F

16.1

18.0

26.5

36.9

46.7

56.3

60.7

59.4

52.2

41.2

31.4

21.6

38.9

I

Btu/ft2 day

417

680

1000

1399

1716

1866

1835

1576

1253

876

478

344

1120

T MAX

°F

29.0

31.7

41.6

56.9

69.4

78.9

83.0

81.1

73.4

61.4

46.0

33.8

57.2

T MIN

°F

14.9

15.6

24.5

35.6

45.5

55.3

59.8

58.1

50.8

40.4

30.9

20.7

37.7

I

Btu/ft2 day

370

648

1014

1412

1755

1957

1914

1676

1262

858

446

311

1135

°F

19.9

26.4

37.5

56.0

69.4

78.5

83.4

80.9

71.0

59.7

41.1

26.7

54.2

T MAX T MIN I

Jackson, MS

T MAX

08

Las Vegas, NV

Newark, NJ

Roswell, NM

Buffalo, NY 08

New York, York, NY NY (LaGuardia Airport)

2.4

8.5

20.8

36.0

47.6

57.7

62.7

60.3

50.2

39.4

25.3

11.7

35.2

464

764

1104

1442

1737

1928

1970

1687

1255

860

480

353

1170

°F

56.5

60.9

68.4

77.3

84.1

90.5

92.5

92.1

87.6

78.6

67.5

60.0

76.3

°F

34.9

37.2

44.2

52.9

60.8

67.9

71.3

70.2

65.1

51.4

42.3

37.1

52.9

754

1026

1369

1708

1941

2024

1909

1781

1509

1271

902

709

1409

T MAX

°F

29.9

37.9

44.0

55.9

66.4

76.3

86.6

84.3

72.3

61.0

44.4

36.0

57.9

T MIN

°F

11.8

18.8

23.6

33.2

43.3

51.6

58.0

56.2

46.5

37.5

25.5

18.2

35.4

I

Btu/ft2 day

486

763

1190

1526

1913

2174

2384

2022

1470

987

561

421

1325

T MAX

°F

56.0

62.4

68.3

77.2

87.4

98.6

10 104.5

10 101.9

94.7

81.5

66.0

57.1

79.6

T MIN

°F

33.0

37.7

42.3

49.8

59.0

68.6

75.9

73.9

65.6

53.5

41.2

33.6

52.8

I

Btu/ft2 day

978

1340

1824

2319

2646

2778

2588

2355

2037

1540

1086

881

1864

T MAX

°F

38.2

40.3

49.1

61.3

71.6

80.6

85.6

84.0

76.9

66.0

54.0

42.3

62.5

T MIN

°F

24.2

25.3

33.3

42.9

53.0

62.4

67.9

67.0

59.4

48.3

39.0

28.6

45.9

I

Btu/ft2 day

552

793

1109

1449

1687

1795

1760

1565

1273

951

596

454

1165

T MAX

°F

55.4

60.4

67.7

76.9

85.0

93.1

93.7

91.3

84.9

75.8

63.1

56.7

75.3

T MIN

°F

27.4

31.4

37.9

46.8

55.6

64.8

69.0

67.0

59.6

47.5

35.0

28.2

47.5

I

Btu/ft2 day

1047

1373

1807

2218

2459

2610

2441

2242

1913

1527

1131

952

1810

T MAX

°F

30.0

31.4

40.4

54.4

65.9

75.6

80.2

78.2

71.7

60.2

47.0

65.0

55.8

T MIN

°F

17.0

17.5

25.6

36.3

46.3

56.4

61.2

59.3

52.7

47.2

33.6

22.5

39.3

I

Btu/ft2 day

349

546

889

1315

1597

1804

1776

1513

1152

784

403

283

1034

T MAX

°F

37.4

39.2

47.3

59.6

69.7

78.7

83.9

82.3

75.2

64.2

52.9

41.5

61.0

T MIN

°F

26.1

27.3

34.6

44.2

53.7

63.2

68.9

68.2

61.2

50.5

41.2

30.8

47.5

I

Btu/ft2 day

548

795

1118

1457

1690

1802

1784

1583

1280

951

593

457

1171

I

08

°F Btu/ft2 day

Btu/ft2 day

T MIN

Billings, MT

Monthly Averages

--``,,`,,,``,````,,``,```,,,``-`-`,,`,,`,`,,`---




17

Table 4—Meteorological 4—Meteorologi cal Data (T MAX , T MIN , I ) for Selected U.S. Locations (Continued) Property Location Cleveland, OH

Symbol

Units

Jan.

Feb.

Mar.

Apr.

May

Jun.

Jul.

Aug.

Sep.

Oct.

Nov.

Annual Dec. Average

T MAX

°F

32.5

34.8

44.8

57.9

68.5

78.0

81.7

80.3

74.2

62.7

49.3

37.5

58.5

T MIN

°F

18.5

19.9

28.4

38.3

47.9

57.2

61.4

60.5

54.0

43.6

34.3

24.6

40.7

Btu/ft2 day

388

601

922

1350

1681

1843

1828

1583

1240

867

466

318

1091

T MAX

°F

34.7

38.1

49.3

62.3

72.6

81.3

84.4

83.0

76.9

65.0

50.1

39.4

61.5

T MIN

°F

19.4

21.5

30.6

40.5

50.2

59.0

63.2

61.7

54.6

42.8

33.5

24.7

41.8

I

Btu/ft2 day

459

677

980

1353

1647

1813

1755

1641

1282

945

538

387

1123

T MAX

°F

30.7

34.0

44.6

59.1

70.5

79.9

a3.4

81.8

75.1

63.3

47.9

35.5

58.8

T MIN

°F

15.5

17.5

26.1

36.5

46.6

56.0

60.2

58.4

51.2

40.1

30.6

20.6

38.3

I

Btu/ft2 day

435

680

991

1384

1717

1878

1849

1616

1276

911

498

355

1133

T MAX

°F

46.6

52.2

61.0

71.7

79.0

87.6

93.5

92.8

84.7

74.3

59.9

50.7

71.2

T MIN

°F

25.2

29.4

37.1

48.6

57.7

66.3

70.6

69.4

61.9

50.2

38.6

29.1

48.6

I

Btu/ft2 day

801

1055

1400

1725

1918

2144

2128

1950

1554

1233

901

725

1461

T MAX

°F

45.6

51.9

60.8

72.4

79.7

87.9

93.9

93.0

85.0

74.9

60.2

50.3

71.3

T MIN

°F

24.8

29.5

31.7

49.5

58.5

67.5

72.4

70.3

62.5

50.3

37.1

29.3

49.2

I

Btu/ft2 day

732

978

1306

1603

1822

2021

2031

1865

1473

1164

827

659

1373

T MAX

°F

46.8

50.6

51.9

55.5

60.2

63.9

67.9

68.6

67.8

61.4

53.5

48.8

58.1

T MIN

°F

35.4

37.1

36.9

39.7

44.1

49.2

52.2

52.6

49.2

44.3

39.7

37.3

43.1

I

Btu/ft2 day

315

545

866

1253

1608

1656

1746

1499

1183

713

387

261

1000

T MAX

°F

44.3

50.4

54.5

60.2

66.9

72.7

79.5

78.6

74.2

63.9

52.3

46.4

62.0

T MIN

°F

33.5

36.0

37.4

40.6

46.4

52.2

55.8

55.8

51.1

44.6

38.6

35.4

44.0

I

Btu/ft2 day

310

554

895

1308

1663

1773

2031

1674

1217

124

388

260

1067

T MAX

°F

38.6

41.1

50.5

63.2

73.0

81.7

86.1

84.6

77.8

66.5

54.5

43.0

63.4

T MIN

°F

23.8

25.0

33.1

42.6

52.5

61.5

66.8

66.0

58.6

46.5

37.1

28.0

45.1

I

Btu/ft2 day

555

795

1108

1434

1660

1811

1758

1575

1281

959

619

470

1169

T MAX

°F

34.1

36.8

47.6

60.7

70.8

79.1

82.7

81.1

74.8

62.9

49.8

38.4

59.9

T MIN

°F

19.2

20.7

29.4

39.4

48.5

57.1

61.3

60.1

53.3

42.1

33.3

24.3

40.7

I

Btu/ft2 day

424

625

943

1317

1602

1762

1689

1510

1209

895

505

347

1069

T MAX

°F

36.4

37.7

45.5

57.5

67.6

76.6

81.7

S0.3

73.1

63.2

51.9

40.5

59.3

T MIN

°F

20.0

20.9

29.2

38.3

47.6

57.0

63.3

61.9

53.8

43.1

34.8

24.1

41.2

I

Btu/ft2 day

506

739

1032

1374

1655

1776

1695

1499

1209

907

538

419

1112

°F

5602

59.5

67.1

77.0

83.8

89.2

91.9

91.0

85.5

76.5

67.1

58.8

75.3

I

Columbus, OH

Toledo, OH

Oklahoma, City, OK

Tulsa, OK

Astoria, OR

Portland, OR

Philadelphia, PA

Pittsburgh, PA

Providence, RI

Columbia, SC

T MAX

°F

33.2

34.6

41.9

50.5

59.1

66.1

70.1

69.4

63.9

50.3

40.6

34.7

51.2

Btu/ft2 day

762

1021

1355

1747

1895

1947

1842

1703

1439

1211

921

722

1380

T MAX

°F

22.9

29.3

40.1

58.1

70.5

80.3

86.2

83.9

73.5

62.1

43.7

29.3

56.7

T MIN

°F

1.9

8.9

20.6

34.6

45.7

56.3

61.8

59.7

48.5

36.7

22.3

10.1

33.9

I

Btu/ft2 day

533

802

1152

1543

1894

2100

2150

1842

1410

1005

608

441

1290

T MIN I

Sioux Falls, SD

Monthly Averages

--``,,`,,,``,````,,``,```,,,``-`-`,,`,,`,`,,`---



08

18


Table 4—Meteorologica 4—Meteorologicall Data Data (T MAX , T MIN , I ) for Selected U.S. Locations (Continued) Property Location Memphis, TN

Amarillo, TX

Corpus Christi, TX

Dallas, TX

Houston, TX

Midland-Odessa, TX

Salt Lake City, UT

Richmond, VA

Seattle, WA (Sea-Tac airport)

Charleston, WV

Huntington, WV

Cheyenne, WY

Monthly Averages

Symbol

Units

Jan.

Feb.

Mar.

Apr.

May

Jun.

Jul.

Aug.

Sep.

Oct.

Nov.

Annual Dec. Average

T MAX

¡F

48.3

53.0

61.4

72.9

81.0

88.4

91.5

90.3

84.3

74.5

61.4

52.3

71.6

T MIN

¡F

30.9

34.1

41.9

52.2

60.9

68.9

72.6

70.8

64.1

51.3

41.1

34.3

51.9

I

Btu/ft2 day

683

945

1278

1639

1885

2045

1972

1824

1471

1205

817

629

1366

T MAX

¡F

49.1

53.1

60.8

71.0

79.1

88.2

91.4

89.6

82.4

72.7

58.7

51.8

70.1

T MIN

¡F

21.7

26.1

32.0

42.0

51.9

61.5

66.2

64.5

56.9

45.5

32.1

24.8

43.8

I

Btu/ft2 day

960

1244

1631

2019

2212

2393

2281

2103

1761

1404

1033

872

1659

T MAX

¡F

66.5

69.9

76.1

82.1

86.7

91.2

94.2

94.1

90.1

83.9

75.1

69.3

81.6

T MIN

¡F

46.1

48.7

55.7

63.9

69.5

74.1

75.6

75.8

72.8

64.1

54.9

48.8

62.5

I

Btu/ft2 day

898

1147

1430

1642

1866

2094

2186

1991

1687

1416

1043

845

1521

T MAX

¡F

54.0

59.1

67.2

76.8

84.4

93.2

97.8

97.3

89.7

79.5

66.2

58.1

76.9

T MIN

¡F

33.9

37.8

44.9

55.0

62.9

70.8

74.7

73.7

67.5

56.3

44.9

37.4

55.0

I

Btu/ft2 day

822

1071

1422

1627

1889

2135

2122

1950

1587

1276

936

780

1468

T MAX

¡F

61.9

65.7

72.1

79.0

85.1

90.9

93.6

93.1

88.7

81.9

71.6

65.2

79.1

T MIN

¡F

40.8

43.2

49.8

58.3

64.7

70.2

72.5

72.1

68.1

57.5

48.6

42.7

57.4

I

Btu/ft2 day

772

1034

1297

1522

1775

1898

1828

1686

1471

1276

924

730

1351

T MAX

¡F

57.6

62.1

69.8

78.8

86.0

93.0

94.2

93.1

86.4

77.7

65.5

59.7

77.0

T MIN

¡F

29.7

33.3

40.2

49.4

58.2

66.6

69.2

68.0

61.9

51.1

39.0

32.2

49.9

I

Btu/ft2 day

1081

1383

1839

2192

2430

2562

2389

2210

1844

1522

1176

1000

1802

T MAX

¡F

37.4

43.7

51.5

61.1

72.4

83.3

93.2

90.0

80.0

66.7

50.2

38.9

64.0

T MIN

¡F

19.7

24.4

29.9

37.2

45.2

53.3

61.8

59.7

50.0

39.3

29.2

21.6

39.3

I

Btu/ft2 day

639

989

1454

1894

2362

2561

2590

2254

1843

1293

788

570

1603

T MAX

¡F

46.7

49.6

58.5

70.6

77.9

84.8

88.4

87.1

81.0

70.5

60.5

50.2

68.8

T MIN

¡F

26.5

28.1

35.8

45.1

54.2

62.2

67.2

66.4

59.3

46.7

37.3

29.6

46.5

I

Btu/ft2 day

632

877

1210

1566

1762

1872

1774

1601

1348

1033

733

567

1248

T MAX

¡F

43.9

48.8

51.1

56.8

64.0

69.2

15.2

13.9

68.1

59.5

50.3

45.6

58.9

T MIN

¡F

34.3

36.8

37.2

40.5

46.0

51.1

54.3

54.3

51.2

45.3

39.3

36.3

43.9

I

Btu/ft2 day

262

495

849

1294

1714

1802

2248

1616

1148

656

337

211

1053

T MAX

¡F

41.8

45.4

55.4

67.3

76.0

82.5

85.2

84.2

78.7

67.7

55.6

45.9

65.5

T MIN

¡F

23.9

25.8

34.1

43.3

51.8

59.4

63.8

63.1

56.4

44.0

35.0

27.8

44.0

I

Btu/ft2 day

498

707

1010

1356

1639

1776

1683

1514

1272

972

613

440

1123

T MAX

¡F

41.1

45.0

55.2

67.2

75.7

82.6

85.6

84.4

78.7

67.7

55.2

45.2

65.3

T MIN

¡F

24.5

26.6

35.0

44.4

52.8

60.7

65.1

64.0

57.2

44.9

35.9

28.5

45.0

I

Btu/ft2 day

526

757

1067

1448

1710

1844

1769

1580

1306

1004

638

467

1176

T MAX

¡F

37.3

40.7

43.6

54.0

64.6

75.4

83.1

S0.8

72.1

61.0

46.5

40.4

58.3

T MIN

¡F

14.8

17.9

20.6

29.6

39.7

48.5

54.6

52.8

43.7

34.0

23.1

18.2

33.1

I

Btu/ft2 day

766

1068

1433

1771

1995

2258

2230

1966

1667

1242

823

671

1491



` , , ` , ` , , ` , , ` ` ` ` , , , ` ` ` , ` ` , , ` ` ` ` , ` ` , , , ` , , ` ` -


Table 5—Solar Absorptance (α) for Selected Tank Surfacesa Solar Absorptance (α) (dimensionless) Surface Condition Surface Color

Shade or Type

Poor

Aluminum

Specular

0.39

0.49

Aluminum

Diffuse

0.60

0.68

Beige/Cream

0.35

0.49

Brown

0.58

0.67

Gray

Light

0.54

0.63

Gray

Medium

0.68

0.74

Green

Dark

0.89

0.91

Red

Primer

0.89

0.91

Rust

Red iron oxide

0.38

0.50

0.43

0.55

0.17

0.34

0.10

0.15

0.97

0.97

Tan White

—

Aluminum b 08

Good

Mill finish, unpainted

Black

Notes: aIf specific information is not available, a white shell and roof, with the paint in good condition, can be assumed to represent the most common or typical tank surface in use. bThis refers to aluminum as the base metal, rather than aluminumcolored paint.

If the liquid bulk temperature is not available, it may be estimated from Equation 23: T B = T AA +

6α – 1

(23)

where T B T AA

α

= liquid liquid bulk temper temperatur ature, e, in degrees degrees Rankin Rankine, e, = daily daily average average ambient ambient temperat temperature, ure, in degrees degrees Rankine, = tank surface solar absorptance absorptance (dimensionless). (dimensionless).

The constants, 6 and 1, in Equation 23 have units of degrees Rankine.

19.1.2.2.2.5

Daily Average Liquid Surface Temperature, T LA

The daily average liquid surface temperature, T LA, is used to calculate the stock vapor pressure at the daily average liquid surface temperature, P VA.


19

If actual daily average liquid surface temperature data for the tank is not available, this temperature can be estimated from Equation 24a: T LA =

0.44T AA + 0.56T B + 0.0079α I

(24a)

where T LA

= daily daily average average liquid liquid surface surface temper temperatur ature, e, in degrees Rankine.

T AA

= daily daily average average ambient ambient tempera temperature ture,, in degrees degrees Rankine.

T B

= liquid liquid bulk temper temperatur ature, e, in degrees degrees Rankin Rankine. e.

α

= tank surface solar absorptance absorptance (dimensionless). (dimensionless).

I

= daily total solar solar insolation insolation on a horizontal horizontal surface, surface, in British thermal units per square foot day.

The constants, 0.44 and 0.56, in Equation 24a are dimensionless. The constant, 0.0079, in Equation 24a has units of degrees Rankine square-foot day per British thermal unit. Combining Equations 23 and 24a, the daily average liquid surface temperature may alternatively be expressed as shown in Equation 24b: T LA = T AA + 0.56 (6α –

1) + 0.0079α I

(24b)

The calculations of Equations 23 and 24 are based on a heat transfer model that assumes the liquid and vapor phases within the tank to be in equilibrium with each other and with atmospheric conditions, but does not account for heat transfer effects due to changes in mass (i.e., due to stock liquid of a different temperature entering the tank). This assumption is reasonably valid only when the tank stands idle for an extended period of time. When a tank is frequently filled and emptied, the actual daily average liquid surface temperature, T LA, may deviate significantly from this assumption. In such cases, the use of actual temperature data may significantly improve the accuracy of the loss estimate.

19.1.2.2.2.6

Daily Vapor Temperature Range,

The daily vapor temperature range, from Equation 25a: ΔT V =

ΔT V , may

0.72 ΔT A + 0.028α I

ΔT V

be estimated

(25a)

where ΔT V = ΔT A

daily vapor vapor temperature range, in degrees degrees Rankine. Rankine.

= daily ambient temperature range, in degrees Rankine.


` , , ` , ` , , ` , , ` ` ` ` , , , ` ` ` , ` ` , , ` ` ` ` , ` ` , , , ` , , ` ` -

20


= (T AX – T AN ) = (T MAX + 459.6) – (T MIN + 459.6) =

08

I =

α

where

(T MAX – T MIN )

T LX

daily total solar solar insolation insolation on a horizontal horizontal surface, surface, in British thermal units per square foot day.

= daily daily maximum maximum liquid liquid surface surface tempera temperature ture,, in degrees Rankine,

T LA

= daily daily average average liquid liquid surface surface tempera temperature ture,, in degrees Rankine,

T LN

= daily daily minimum minimum liquid liquid surface surface temperat temperature, ure, in degrees Rankine,

ΔT V

= daily daily vapor vapor temperatu temperature re range, range, in degrees degrees Rankine.

= tank surface surface solar absorptanc absorptancee (dimensionless). (dimensionless).

Given that (T AX – T AN ) is equal to (T MAX – T MIN ), the daily vapor temperature range can be calculated directly from the meteorological data of Table 4, using Equation 25b. ΔT V =

0.72 (T MAX – T MIN ) + 0.028α I

19.1.2.2.2.8

(25b)

The stock vapor molecular weight, M V , can be determined by analysis analysis of vapor vapor samples or by calculation calculation from the com com position of the liquid. liquid.

The constant, 0.72, in Equation 25b is dimensionless. The constant, 0.028, in Equation 25b has units of degrees Rankine square-foot day per British thermal unit.

19.1.2.2.2.7 19.1.2.2.2.7

19.1.2.2.2.8.1 19.1.2.2.2.8. 1

The daily maximum and minimum liquid surface temperatures, T LX and T LN , respectively, are used for calculating the stock vapor pressures P VX and P VN .

19.1.2.2.2.8.1.1 19.1.2.2.2.8. 1.1

T LN = T LA –

0.25

19.1.2.2.2.8.1.2 19.1.2.2.2.8. 1.2

(26)

Crude Oil Stocks

In the absence of specific information, a typical value of 50 pounds per pound-mole pound-mole can be assumed for U.S. midcontimidcontinent crude oils (including both reactive and nonreactive frac-

(27)

ΔT V

Refined Petroleum Stocks

In the absence of specific information, a typical value of 64 pounds per pound-mole pound-mole can be assumed assumed for gasoline. gasoline.

If data on these liquid surface temperatures are not available, they may be estimated from Equations 26 and 27: 0.25 ΔT V

Petroleum Liquid Stocks

The vapor molecular weight of selected petroleum liquids (multicomponent stocks) is given in Table 6.

Daily Maximum and Minimum Liquid Surface Temperatures, T LX , T LN

T LX = T LA +

Vapor Molecular Weight, M V

Table 6—Properties (M V , W VC , P V , A, B) of Selected Petroleum Liquids Vapor Condensed Molecular Vapor Density Weight (60°F)

Vapor Pressurea (at 60°F)

Vapor Pressure Equation Constants b

Temperature Range For Constants A and B

M V

W VC

(lb/lb-mole)

(lb/gal)

PV (psia)

A (Dimensionless)

B (°R)

Minimum (°F)

Maximum (°F)

Refined petroleum stocks

—

—

—

c

c

—

—

Crude oil stocks

—

—

—

c

c

—

—

Jet naphtha (JP-4)

80

5.4

1.27

11.368

5,784.3

40

100

Jet kerosene

130

6.1

0.00823

12.390

8,933.0

40

100

Distillate fuel oil no. 2

130

6.1

0.00648

12.101

8,907.0

40

100

Residual oil no. 6

190

6.4

0.0000430

10.104

10,475.5

40

100

Petroleum Liquid

` ` , , ` , , , ` ` , ` ` ` ` , , ` ` , ` ` ` , , , ` ` ` ` , , ` , , ` , ` , , ` -

Notes: aVapor pressure calculated at 60°F using constants A and B. bThe vapor pressure equation is P = exp [A – (B/T )], where P is the vapor pressure in psia, T is the liquid surface temperature in °R, and V L V L exp is the exponential function. cThe vapor pressure equation constants A and B are listed in Equations 31 and 32 for refined petroleum stocks, and Equations 34 and 35 for crude oil stocks. These constants are from Reference [4]. Sources: The vapor pressure equation constants A and B were developed from a correlation of the vapor pressures given in Reference [5] (except as indicated in Note b). The other properties are also from References [5].



08

N P C r o o o p r v y e i r d p e i r d g o h d b t u A c y m t I i H e o n S i r c o u a r n n n d e e P t r e w l i t r o c o r l k e n e i n s u g e m p w I e i n s r t h t m i i A t u t t e P t e d I w i t h o u t l i c e n s e f r o m I H S

` , , ` , ` , , ` , , ` ` ` ` , , , ` ` ` , ` ` , , ` ` ` ` , ` ` , , , ` , , ` ` -

Table 7—Properties 7—Properties of Selected Petroche Petrochemicals micalsa Constants for AntoineÕs Equationb

Chemical Name

CAS No.

Molecular Weight

Liquid Density at 60¡F (lb/gal)

Top Line: Bottom Line:

Vapor Pressure (psia) at: 40¡F

50¡F

60¡F

70¡F

80¡F

90¡F

100¡F

¡C ¡R

¡C Ñ

A Dimensionless

B (degrees)

C (degrees)

Acetaldehyde

00075-07-0

44.00

6.576

12.184

8.005

1,600.0

291.81

Acetic acid

00064-19-7

60.05

8.788

0.169

7.387

1,533.3

222.31

Acetic anhydride

00108-24-7

102.09

9.013

0.053

7.149

1,444.7

199.82

Temperature Range Min. (¡F)

Max. (¡F)

S Acetone c d

00067-64-1

Acetonitrile c

N L i o c t e f n o r s R e e e = s I n a s l p e , e 0 c 6 t o / 0 a r 5 t / 2 e 0 A 0 m 9 0 e r i 8 c : a 0 2 C : o 0 4 p r M / 5 D 9 T 6 6 4 4 3 0 0 1

58.08

00075-05-8

41.05

6.628

6.558

1.682

0.638

2.185

0.831

2.862

1.083

3.713

1.412

4.699

1.876

5.917

2.456

7.251

3.133

Acrylamide

00079-06-1

71.09

9.364

Acrylic acid

00079-10-7

72.10

8.864

0.015

0.024

0.037

0.055

0.082

0.119

0.169

Acrylonitrile c d

00107-13-1

53.06

6.758

0.812

0.967

1.373

1.779

2.378

3.133

4.022

Allyl alcohol c d e

00107-18-6

Allyl chloride c d e

58.08

00107-05-1

76.53

7.125

7.864

0.00009

0.135

2.998

0.193

3.772

0.261

4.797

0.387

6.015

0.522

7.447

0.716

9.110

1.006

11.025

1,210.6

14.254

6,920.2

7.119

1,314.4

229.66 Ð74.9

11.293

3,939.9

273.16

8.539

2,305.8

266.55

222.47

7.038

1,232.5

14.132

7,191.8

11.187

4,068.5

17.107

9,579.2

5.297

418.4 6,689.5

7.320

1,731.5

206.05

6.905

1,211.0

220.79

8.529

Benzene c

00071-43-2

78.11

7.365

Butane (Ðn) e f

58.12

5.007

25.960

6.809

935.9

238.73

Butene (2-methyl-1)

70.13

5.420

10.246

6.486

1,039.7

236.65

00071-36-3

74.12

6.760

0.057

7.477

1,362.4

178.77

00075-65-0

74.12

6.595

17.223

9,430.3

0.870

1.160

1.508

1.972

2.610

3.287

173.3

O S S F R O M

F I X E D

Ð4.0

205.9

Ð94.0

112.3

Ð4.7

432.5

128.17

93.10

1 — E

L

Ð59.8

14.456

E C T I O N

V A P O R A T I V E

392.7

00062-53-3

0.638

418.1

230.00

Aniline

Butyl alcohol (Ðn) c

0.006

7.117

R

O O F

T

A N K S

{butanol (Ð1)} Butyl alcohol (Ðtert)


0.290

0.425

0.638

0.909

1.238

1.702

Table 7—Properties 7—Properties of Selected Petroch Petrochemicals emicalsa (C (C on tinu ed )

2 1

2 2

` , , ` , ` , , ` , , ` ` ` ` , , , ` ` ` , ` ` , , ` ` ` ` , ` ` , , , ` , , ` ` -

Constants for AntoineÕs Equationb

Chemical Name

CAS No.

Molecular Weight


70¡F

80¡F

90¡F

100¡F

A Dimensionless

0.715

1.006

1.320

1.740

2.185

2.684

3.481

6.837

1,173.8

218.13

6.933

1,348.5

233.79

6.942

1,169.1

241.59

Butyl ether (diÐt)

06163-66-2

130.23

6.400

Carbon disulÞde c d

00075-15-0

76.13

10.588

3.036

3.867

4.834

6.014

7.387

9.185

11.215

Carbon tetrachloride c d

00056-23-5

153.84

13.366

0.793

1.064

1.412

1.798

2.301

2.997

3.771

00109-63-9

92.57

C (degrees)

60¡F

7.430

Chlorobutane (Ð1)

B (degrees)

50¡F

92.57

112.60

¡C Ñ

40¡F

Vapor Pressure (psia) at:

00109-69-3

00108-90-7

¡C ¡R


Butyl chloride (Ðn) c e

Chlorobenzene

N L i o c t e f n o r s R e e e = s I n a s l p e , e 0 c 6 t o / 0 a r 5 t / 2 e 0 A 0 m 9 0 e r i 8 c : a 0 2 C : o 0 4 p r M / 5 D 9 T 6

0.174

0.647

9.239

0.133

7.380

1.261

13.329

6,146.2

6.934

1,242.4

13.522

6,908.7

6.978

1,431.1

6.837

Chlorobutane (Ð2)

00078-86-4

92.57

7.270

2.007

Chloroform c d

00067-66-3

119.39

12.488

1.528

1.934

2.475

3.191

4.061

5.163

6.342

Chloroprene c

00126-99-8

88.54

8.046

1.760

2.320

2.901

3.655

4.563

5.685

6.981

Chlorotoluene (Ðo)

00095-49-8

126.59

9.020

Cresol (Ðm)

00108-39-4

108.10

8.629

1,173.8


Max. (¡F)

Ð100.8

492.8

Ð58.0

528.8

230.00

217.55

1,149.1

224.68

6.493

929.4

196.03

13.865

6,792.5

6.161

783.5

179.70

0.039

7.368

1,735.8

230.00

0.0014

7.508

1,856.4

199.07

H A P T E R

1 9 — E

218.13

6.799

C

V A P O R A T I V E

L

Ð72.4

489.2

O S S

M

E A S U R E M E N T


Table 7—Properties 7—Properties of Selected Petroch Petrochemicals emicalsa (C (C on tinu ed ) Constants for AntoineÕs Equationb

Chemical Name


80¡F

90¡F

100¡F

A Dimensionless

0.715

1.006

1.320

1.740

2.185

2.684

3.481

6.837

1,173.8

218.13

6.933

1,348.5

233.79

6.942

1,169.1

241.59

130.23

6.400

Carbon disulÞde c d

00075-15-0

76.13

10.588

3.036

3.867

4.834

6.014

7.387

9.185

11.215

Carbon tetrachloride c d

00056-23-5

153.84

13.366

0.793

1.064

1.412

1.798

2.301

2.997

3.771

92.57

0.647

9.239

0.133

7.380

1.261

00078-86-4

92.57

7.270

Chloroform c d

00067-66-3

119.39

12.488

1.528

1.934

2.475

3.191

4.061

5.163

6.342

Chloroprene c

00126-99-8

88.54

8.046

1.760

2.320

2.901

3.655

4.563

5.685

6.981

Chlorotoluene (Ðo)

00095-49-8

126.59

9.020

Cresol (Ðm)

00108-39-4

108.10

Cresol (Ðo) d

00095-48-7

108.14

6,146.2

6.934

1,242.4

13.522

6,908.7

6.978

1,431.1

6.493

929.4

196.03

13.865

6,792.5

6.161

783.5

179.70

0.039

7.368

1,735.8

230.00

8.629

0.0014

7.508

1,856.4

199.07

8.738

0.002

165.16

8.629

Cyclohexane c

00110-82-7

84.16

6.522

Cyclohexanol d

00108-93-0

100.20

8.029

0.0006

0.677

0.928

1.218

1.605

2.069

2.610

3.249

0.002

7.910

0.054

6.911

1,435.5 11,308.6

7.035

1,511.1

161.85

6.841

1,201.5

222.65

109.13

6.255

912.9 7,091.7

7.849

2,137.2

Ð100.8

492.8

Ð58.0

528.8

C H A P T E R

1 9 — E V A P O R A T I V E

L

Ð72.4

16.296

13.697

Max. (¡F)

218.13

224.68

108.10

Min. (¡F)

217.55

1,149.1

00106-44-5

2.007

1,173.8

Temperature Range

230.00

6.799

Cresol (Ðp)

98.20

13.329

6.837

Chlorobutane (Ð2)

00108-94-1

C (degrees)

70¡F

06163-66-2

00109-63-9

B (degrees)

60¡F

Butyl ether (diÐt)

112.60

¡C Ñ

50¡F

7.430

00108-90-7

¡C ¡R

40¡F

92.57

Cyclohexanone

f r o m I H S

Molecular Weight


00109-69-3

Chlorobutane (Ð1)

N P C r o o o p r v y e i r d p e i r d g o h d b t u A c y m t I i H e o n S i r c o u a r n n n d e e P t r e w l i t r o c o r l k e n e i n s u g e m p w I e i n s r t h t m i i A t u t t e P t e d I w i t h o u t l i c e n s e

CAS No.



Butyl chloride (Ðn) c e

Chlorobenzene


2 2

` , , ` , ` , , ` , , ` ` ` ` , , , ` ` ` , ` ` , , ` ` ` ` , ` ` , , , ` , , ` ` -

489.2

O S S

M

E A S U R E M E N T

100.8

375.4

Ð49.5

495.5

273.16

Table 7—Properties 7—Properties of Selected Petroche Petrochemicals micalsa (C (C on tinu ed ) Constants for AntoineÕs Equationb

Chemical Name

CAS No.

Molecular Weight


Cyclohexene

00110-83-8

82.15

6.750

Cyclopentane c d e

00287-92-3

70.13

6.248



50¡F

60¡F

70¡F

80¡F

90¡F

100¡F

1.098

2.514

3.287

4.177

5.240

6.517

8.063

9.668

¡C ¡R

¡C Ñ

A Dimensionless

B (degrees)

C (degrees)

6.886

1,230.0

224.10

231.36

6.887

1,124.2

14.338

6,711.5

Cyclopentanone

00120-92-3

84.12

7.900

0.132

2.902

162.9

63.22

Cyclopentene

00142-29-0

68.12

6.430

3.263

6.921

1,121.8

223.45

Decane (Ðn) d

00124-18-5

142.29

6.092

0.021

0.026

0.033

0.042

0.053

0.066

15.046

9,882.0

201.89

16.100

0.089

7.304

1,644.4

232.00

Dibromopropane (1,3)

00109-64-8

201.89

16.510

0.027

7.550

1,890.6

240.00

Dichloroethane (1,1) c e

00075-34-3

98.97

9.861

1.682

2.243

2.901

3.771

4.738

5.840

7.193

6.977

1,174.0

229.06

Dichloroethane (1,2) c d

00107-06-2

98.97

10.500

0.561

0.773

1.025

1.431

1.740

2.243

2.804

7.025

1,272.3

222.90

13.804

7,200.2

00540-59-0

96.95

10.763

1.450

2.011

2.668

3.461

4.409

5.646

Max. (¡F)

Ð90.4

120.7

S E C T I O N

62.8

00078-75-1

(cisÐ1,2) c e

Min. (¡F)

0.083


Dichloroethylene

Temperature Range

6.807

7.022

1,205.4

V A P O R A T I V E

L

O S S F R O M

F Ð48.1

230.6

343.4

1 — E

545.0

I X E D

R

O O F

T A



Chemical Name

f r o m I H S


CAS No.

Molecular Weight


Cyclohexene

00110-83-8

82.15

6.750

Cyclopentane c d e

00287-92-3

70.13

6.248



50¡F

60¡F

70¡F

80¡F

90¡F

100¡F

1.098

2.514

3.287

4.177

5.240

6.517

8.063

9.668

¡C ¡R

¡C Ñ

A Dimensionless

B (degrees)

C (degrees)

6.886

1,230.0

224.10

231.36

6.887

1,124.2

14.338

6,711.5

Cyclopentanone

00120-92-3

84.12

7.900

0.132

2.902

162.9

63.22

Cyclopentene

00142-29-0

68.12

6.430

3.263

6.921

1,121.8

223.45

Decane (Ðn) d

00124-18-5

142.29

6.092

0.021

0.026

0.033

0.042

0.053

0.066

15.046

9,882.0

201.89

16.100

0.089

7.304

1,644.4

232.00


00109-64-8

201.89

16.510

0.027

7.550

1,890.6

240.00

Dichloroethane (1,1) c e

00075-34-3

98.97

9.861

1.682

2.243

2.901

3.771

4.738

5.840

7.193

6.977

1,174.0

229.06

Dichloroethane (1,2) c d

00107-06-2

98.97

10.500

0.561

0.773

1.025

1.431

1.740

2.243

2.804

7.025

1,272.3

222.90

13.804

7,200.2

96.95

10.763

1.450

2.011

2.668

3.461

4.409

5.646

Max. (¡F)

Ð90.4

120.7

S E C T I O N

62.8

00078-75-1

00540-59-0

Min. (¡F)

0.083


Dichloroethylene

Temperature Range

6.807

7.022

1,205.4

343.4

V A P O R A T I V E

L

O S S F R O M

F Ð48.1

545.0

I X E D

R

O O F

230.6

(cisÐ1,2) c e Dichloroethylene

1 — E

T

00156-60-5

96.95

10.524

161.03

10.470

118.18

2.552

3.384

4.351

5.530

6.807

8.315

10.016

6.965

1,141.9

231.90

0.003

7.344

1,882.5

215.00

6.920

0.394

6.758

1,191.6

203.12

104.15

6.990

0.810

6.908

1,229.5

217.01

A N K S

(transÐ1,2) c Dichlorotoluene (3,4)

Diethoxyethane (1,1)

00105-57-7

Diethoxymethane

Diethyl (n,n) aniline

00091-66-7

149.23

7.763

0.002

7.466

1,993.6

218.50

Diethyl ketone

00096-22-0

86.13

6.780

0.402

6.858

1,216.3

204.00

2 3 --``,,`,,,``,````,,``,```,,,``-`-`,,`,,`,`,,`---



Chemical Name ` ` , , ` , , , ` ` , ` ` ` ` , , ` ` , ` ` ` , , , ` ` ` ` , , ` , , ` , ` , , ` -

CAS No.

Molecular Weight


Diethyl sulÞde

00352-93-2

90.18

6.970

Diethylamine c d e

00109-89-7

73.14

5.906



50¡F

60¡F

70¡F

80¡F

90¡F

100¡F

0.699 1.644

1.992

2.862

3.867

4.892

6.130

7.541

¡C ¡R

¡C Ñ

A Dimensionless

B (degrees)

C (degrees)

6.928

1,257.8

218.66 144.1

5.802

583.3

13.788

6,617.7

Diethylbenzene (1,2)

134.22

7.330

0.009

6.988

1,576.9

200.51


134.22

7.170

0.010

7.004

1,575.3

200.96


Max. (¡F)

Ð27.4

410.0

C Diethylbenzene (1,4)


2 4

134.22

7.180

0.010

6.998

1,588.3

201.97

6.850

1,139.3

218.70

Di-isopropyl ether c e

00108-20-3

102.17

6.075

Dimethoxyethane (1,2)

00110-71-4

90.12

7.220

2.146

6.719

1,050.5

209.20

Dimethyl formamide

00068-12-2

73.09

7.578

0.040

6.928

1,400.9

196.43

1.199

1.586

2.127

2.746

3.481

4.254

5.298

H A P T E R


L

Dimethyl hydrazine (1,1)

00057-14-7

60.10

7.882

1.895

7.408

1,305.9

225.53

O S S

M

Dimethyl phthalate Dimethylbutane (2,3)

00131-11-3

194.20

9.965

0.00000002

4.522

700.3

51.42

86.18

5.510

3.058

6.810

1,127.2

228.90

E A S U R E M E N T



Chemical Name ` ` , , ` , , , ` ` , ` ` ` ` , , ` ` , ` ` ` , , , ` ` ` ` , , ` , , ` , ` , , ` -

CAS No. 00352-93-2

90.18

6.970

Diethylamine c d e

00109-89-7

73.14

5.906



50¡F

60¡F

70¡F

80¡F

90¡F

0.699 1.644

1.992

2.862

3.867

4.892

6.130

7.541

¡C Ñ

A Dimensionless

B (degrees)

C (degrees)

6.928

1,257.8

218.66 144.1

5.802

583.3

13.788

6,617.7

134.22

7.330

0.009

6.988

1,576.9

200.51


134.22

7.170

0.010

7.004

1,575.3

200.96


Max. (¡F)

Ð27.4

410.0

C 134.22

7.180

0.010

6.998

1,588.3

201.97

6.850

1,139.3

218.70

Di-isopropyl ether c e

00108-20-3

102.17

6.075

Dimethoxyethane (1,2)

00110-71-4

90.12

7.220

2.146

6.719

1,050.5

209.20

Dimethyl formamide

00068-12-2

73.09

7.578

0.040

6.928

1,400.9

196.43

1.199

1.586

2.127

2.746

3.481

4.254

5.298

H A P T E R


L

Dimethyl hydrazine (1,1)

00057-14-7

60.10

7.882

1.895

7.408

1,305.9

O S S

225.53

M

Dimethyl phthalate

194.20

9.965

0.00000002

4.522

700.3

51.42

Dimethylbutane (2,3)

86.18

5.510

3.058

6.810

1,127.2

228.90

00131-11-3

Dimethylcyclopentane

87.50

6.290

0.932

6.817

1,219.5

221.95

Dimethylpentane (2,2)

100.20

5.610

1.316

6.815

1,190.0

223.30


100.20

5.790

0.841

6.854

1,238.0

221.82


100.20

5.600

1.459

6.826

1,192.0

225.32


100.20

5.780

1.029

6.827

1,228.7

225.32

88.10

8.659

7.431

1,554.7

240.34

E A S U R E M E N T

(1,1)

N P C r o o o p r v y e i r d p e i r d g o h d b t u A c y m t I i H e o n S i r c o u a r n n n d e e P t r e w ` ` , , , ` ` ` , ` ` , , ` ` ` ` , ` ` , , , ` , , ` ` t l i r o c o r l k e n e i n s u g e m p w I e i n s r t h t m i i A t u t t e P t e d I w i t h o u t l i c e n s e

00123-91-1

0.232

0.329

0.425

0.619

0.831

1.141

1.508

Table 7—Properties 7—Properties of Selected Petroche Petrochemicals micalsa (C (C on tinu ed ) Constants for AntoineÕs Equationb Top Line: Bottom Line:

¡C ¡R

¡C Ñ

B (degrees)

C (degrees)

CAS No.

Molecular Weight


Dipropyl ether c e

00111-43-3

102.17

6.260

Epichlorohydrin

00106-89-8

92.50

9.848

0.194

8.229

2,086.8

273.16

Ethanolamine (mono-)

00141-43-5

61.09

8.344

0.002

7.456

1,577.7

173.37

Ethyl acetate c d

00141-78-6

88.10

7.551

0.580

0.831

1.102

1.489

1.934

2.514

3.191

7.101

1,245.0

217.88

14.478

7,517.5

Ethyl acrylate c

00140-88-5

100.11

7.750

0.213

0.290

0.425

0.599

0.831

1.122

1.470

7.965

1,897.0

273.16

Ethyl alcohol c d

00064-17-5

46.07

6.610

0.193

0.406

0.619

0.870

1.218

1.682

2.320

8.321

1,718.2

237.52

00075-00-3

64.52

7.678

Chemical Name


50¡F

60¡F

70¡F

80¡F

90¡F

100¡F

A Dimensionless

0.425

0.619

0.831

1.102

1.431

1.876

2.320

6.948

1,256.5

219.00

{ethanol} Ethyl chloride N L i o c t e f n o r s R e e e = s I n a s l p e , e 0 c 6 t o / 0 a r 5 t / 2 e 0 A 0 m 9 0 e r i 8 c : a 0 2 C : o 0 4 p r M / 5 D 9 T 6

100¡F

¡C ¡R


Dioxane (1,4) c

f r o m I H S

Molecular Weight


Diethyl sulÞde



2 4

16.591

16.380

8,760.7

6.986

1,030.0


Max. (¡F)

S Ð46.1

455.0

E C T I O N

1 — E

Ð24.3

467.6

238.61

V A P O R A T I V E

L

Ethyl ether c

00060-29-7

74.12

5.988

00075-04-7

45.08

5.690

4.215

5.666

7.019

8.702

10.442

13.342

6.920

1,064.1

228.80

7.054

987.3

220.00

O S S F R O M

{diethyl ether} Ethylamine Ethylbenzene d Ethylcyclopentane

00100-41-4

106.17 98.19

7.227 6.380

14.103 0.109 0.475

6.975

1,424.3

14.036

8,423.3

6.887

1,298.6

F I X E D

R

213.21 14.4 220.68

619.7

O O F

T A

N P C r o o o p r v y e i r d p e i r d g o h d b t u A c y m t I i H e o n S i r c o u a r n n n d e e P t r e w ` ` , , , ` ` ` , ` ` , , ` ` ` ` , ` ` , , , ` , , ` ` t l i r o c o r l k e n e i n s u g e m p w I e i n s r t h t m i i A t u t t e P t e d I w i t h o u t l i c e n s e f r o m I H S

Table 7—Properties 7—Properties of Selected Petroche Petrochemicals micalsa (C (C on tinu ed ) Constants for AntoineÕs Equationb Top Line: Bottom Line:

¡C Ñ

B (degrees)

C (degrees)

CAS No.

Molecular Weight

Dipropyl ether c e

00111-43-3

102.17

6.260

Epichlorohydrin

00106-89-8

92.50

9.848

0.194

8.229

2,086.8

273.16

Ethanolamine (mono-)

00141-43-5

61.09

8.344

0.002

7.456

1,577.7

173.37

Ethyl acetate c d

00141-78-6

88.10

7.551

0.580

0.831

1.102

1.489

1.934

2.514

3.191

7.101

1,245.0

217.88

14.478

7,517.5

Ethyl acrylate c

00140-88-5

100.11

7.750

0.213

0.290

0.425

0.599

0.831

1.122

1.470

7.965

1,897.0

273.16

Ethyl alcohol c d

00064-17-5

46.07

6.610

0.193

0.406

0.619

0.870

1.218

1.682

2.320

8.321

1,718.2

237.52

00075-00-3

64.52

7.678

Chemical Name


50¡F

60¡F

70¡F

80¡F

90¡F

100¡F

A Dimensionless

0.425

0.619

0.831

1.102

1.431

1.876

2.320

6.948

1,256.5

219.00

{ethanol} Ethyl chloride N L i o c t e f n o r s R e e e = s I n a s l p e , e 0 c 6 t o / 0 a r 5 t / 2 e 0 A 0 m 9 0 e r i 8 c : a 0 2 C : o 0 4 p r M / 5 D 9 T 6 6 4 4 3 0 0 1

¡C ¡R


16.591

16.380

8,760.7

6.986

1,030.0


Max. (¡F)

S Ð46.1

455.0

E C T I O N

1 — E

Ð24.3

467.6

238.61

V A P O R A T I V E

L

Ethyl ether c

00060-29-7

74.12

5.988

00075-04-7

45.08

5.690

4.215

5.666

7.019

8.702

10.442

13.342

6.920

1,064.1

228.80

7.054

987.3

220.00

O S S F R O M

{diethyl ether} Ethylamine Ethylbenzene d

00100-41-4

Ethylcyclopentane Ethyleneoxide

00075-21-8

Ethylpentane (Ð3)

106.17

14.103

7.227

0.109

6.975

1,424.3

14.036

8,423.3

6.380

0.475

6.887

1,298.6

220.68

44.00

7.227

17.842

7.128

1,054.5

237.76

100.20

5.820

0.700

6.876

1,251.8

219.89

00462-06-6

96.10

8.520

0.937

7.187

1,381.8

235.60

Formic acid

00064-18-6

46.00

10.182

0.521

7.581

1,699.2

260.70

Freon 11 c

00075-69-4

137.38

12.480

6.884

1,043.0

236.88

00110-00-9

68.08

7.821

6.975

1,060.9

227.74

10.900

13.401

16.311

19.692

23.600

R

14.4

Fluorobenzene

8.804

I X E D

213.21

98.19

7.032

F

619.7

O O F

T

A N K S

{trichloroßuoromethane} Furan

7.961

2 5



2 6

` , , ` , ` , , ` , , ` ` ` ` , , , ` ` ` , ` ` , , ` ` ` ` , ` ` , , , ` , , ` ` -


Chemical Name

CAS No.

Molecular Weight


Furfural

00096-01-1

96.09

9.648

Heptane (Ðn) c d e

00142-82-5

100.20

5.727



50¡F

60¡F

70¡F

80¡F

90¡F

100¡F

0.014 0.290

0.406

0.541

0.735

0.967

1.238

1.586

¡C ¡R

¡C Ñ

A Dimensionless

B (degrees)

C (degrees)

6.575

1,198.7

162.80 216.54

6.897

1,264.9

13.984

7,615.8

Heptene (Ð1)

98.19

5.810

0.677

6.902

1,258.3

219.30

Hexadiene (1,5)

82.15

5.730

2.890

6.574

1,013.5

214.80


Max. (¡F)

Ð29.2

477.5

C Hexane (Ðn) c d

00110-54-3

86.17

5.527

1.102

1.450

1.876

2.436

3.055

3.906

4.892

0.007

6.876

1,171.2

13.824

6,907.2

224.41

7.860

1,761.3

196.66

Ð65.0

1 9 — E

Hexanol (Ð1)

00111-27-3

102.18

6.760

Hydrogen cyanide c

00074-90-8

27.03

5.772

6.284

7.831

9.514

11.853

15.392

18.563

22.237

7.528

1,329.5

260.40

00078-83-1

74.12

6.712

0.058

0.097

0.135

0.193

0.271

0.387

0.541

7.474

1,314.2

186.55

V A P O R A T I V E

220.74

O S S

{hydrocyanic acid} N L i o c t e f n o r s R e e e = s I n a s l p e , e 0 c 6 t o / 0 a r 5 t / 2 e 0 A 0 m 9 0 e r i 8 c : a 0 2 C : o 0 4 p r M / 5 D 9 T 6

408.9

H A P T E R

Isobutyl alcohol c

L

Isooctane c e

26635-64-3

114.22

5.794

0.213

0.387

0.580

0.812

1.093

1.392

1.740

6.812

1,257.84

Isopentane c e

00078-78-4

72.15

5.199

5.878

7.889

10.005

12.530

15.334

18.370

21.657

6.833

1,040.7

235.45

Isoprene c e

00078-79-5

68.11

5.707

4.757

6.130

7.677

9.668

11.699

14.503

17.113

7.012

1,126.2

238.88

M

E A S U R E M E N T



2 6

` , , ` , ` , , ` , , ` ` ` ` , , , ` ` ` , ` ` , , ` ` ` ` , ` ` , , , ` , , ` ` -


Chemical Name

CAS No.

Molecular Weight


Furfural

00096-01-1

96.09

9.648

Heptane (Ðn) c d e

00142-82-5

100.20

5.727



50¡F

60¡F

70¡F

80¡F

90¡F

100¡F

0.014 0.290

0.406

0.541

0.735

0.967

1.238

1.586

¡C ¡R

¡C Ñ

A Dimensionless

B (degrees)

C (degrees)

6.575

1,198.7

162.80 216.54

6.897

1,264.9

13.984

7,615.8

Heptene (Ð1)

98.19

5.810

0.677

6.902

1,258.3

219.30

Hexadiene (1,5)

82.15

5.730

2.890

6.574

1,013.5

214.80


Max. (¡F)

Ð29.2

477.5

C Hexane (Ðn) c d

00110-54-3

86.17

5.527

1.102

1.450

1.876

2.436

3.055

3.906

4.892

0.007

6.876

1,171.2

13.824

6,907.2

224.41

7.860

1,761.3

196.66

Ð65.0

408.9

1 9 — E

Hexanol (Ð1)

00111-27-3

102.18

6.760

Hydrogen cyanide c

00074-90-8

27.03

5.772

6.284

7.831

9.514

11.853

15.392

18.563

22.237

7.528

1,329.5

260.40

00078-83-1

74.12

6.712

0.058

0.097

0.135

0.193

0.271

0.387

0.541

7.474

1,314.2

186.55

V A P O R A T I V E

220.74

O S S

{hydrocyanic acid} N L i o c t e f n o r s R e e e = s I n a s l p e , e 0 c 6 t o / 0 a r 5 t / 2 e 0 A 0 m 9 0 e r i 8 c : a 0 2 C : o 0 4 p r M / 5 D 9 T 6 6 4 4 3 0 0 1

H A P T E R

Isobutyl alcohol c

L

Isooctane c e

26635-64-3

114.22

5.794

0.213

0.387

0.580

0.812

1.093

1.392

1.740

6.812

1,257.84

Isopentane c e

00078-78-4

72.15

5.199

5.878

7.889

10.005

12.530

15.334

18.370

21.657

6.833

1,040.7

235.45

Isoprene c e

00078-79-5

68.11

5.707

4.757

6.130

7.677

9.668

11.699

14.503

17.113

7.012

1,126.2

238.88

Isopropyl alcohol c d

00067-63-0

60.09

6.573

0.213

0.329

0.483

0.677

0.928

1.296

1.779

219.61

{isopropanol} Isopropyl benzene d

00098-82-8

120.20

7.211

0.051

00527-84-4

134.22

7.300

0.014

Methacrylonitrile c e

00126-98-7

67.09

6.738

0.483

0.657

0.870

1.160

1.470

1.934

2.456

Methyl acetate c d

00079-20-9

74.08

7.831

1.489

2.011

2.746

3.693

4.699

5.762

6.961

{cumene} Isopropylbenzene

8.118

1,580.9

16.769

9,113.6

6.963

1,460.8

M

E A S U R E M E N T

Ð15.0

449.6

37.2

306.3

207.78

15.009

9,359.7

6.940

1,548.1

203.15

6.980

1,275.0

220.70 219.73

(1-methyl-2)

Methyl acrylate c d



00096-33-3

86.09

7.996

0.599

0.773

1.025

1.354

1.798

2.398

7.065

1,157.6

14.334

7,002.9

Ð71.0

437.0

14.997

7,786.4

Ð46.7

176.4

3.055


Chemical Name Methyl alcohol c d

CAS No. 00067-56-1

Molecular Weight 32.04



40¡F

50¡F

60¡F

70¡F

80¡F

90¡F

100¡F

6.630

0.735

1.006

1.412

1.953

2.610

3.461

4.525


{methanol} Methyl ethyl ketone c d

00078-93-3

72.10

6.747

Methyl isobutyl ketone

00108-10-1

100.20

6.677

Methyl methacrylate c d

00080-62-6

100.11

7.909

0.116

0.213

0.348

0.541

0.773

1.064

1.373

Methyl propyl ether c

00557-17-5

74.12

6.166

3.674

4.738

6.091

7.058

9.417

11.602

13.729

Methyl styrene (alpha)

00098-83-9

118.00

7.586

Methylcyclohexane c

00108-87-2

98.18

6.441

0.715

0.928

1.199

1.489

2.069

2.668

3.345

0.212

0.024 0.309

0.425

0.541

0.735

0.986

1.315

1.721

A Dimensionless

¡C ¡R

¡C Ñ

B (degrees)

C (degrees)

7.897

1,474.1

15.948

8,131.3

6.974

1,209.6


Max. (¡F)

Ð47.2

435.2

Ð54.9

175.3

229.13 216.00

14.381

7,380.2

6.672

1,168.4

191.90

8.409

2,050.5

274.40

14.800

8,127.7

6.119

708.7

179.90

6.923

1,486.9

202.40

6.823

1,270.8

221.42

S Ð22.9

213.8

E C T I O N

1 — E

V A P O R A T I V E

L

Methylcyclopentane c

00096-37-7

Methyldichlorosilane Methylene chloride c d Methylhexane (Ð2)

00075-09-2

84.16

6.274

129.06

8.910

84.94 100.21

11.122 5.660

0.909

1.160

1.644

2.224

2.862

3.616

4.544

5.718 3.094

4.254

5.434 0.799

6.787

8.702

10.329

13.342

6.863

1,186.1

226.04

7.028

1,167.8

240.70

7.409

1,325.9

14.897

6,857.5

6.873

1,236.0

O S S F R O M

F I X E D

R

252.60 Ð94.0 219.55

105.3

O O F

T A




Chemical Name Methyl alcohol c d

CAS No.

Molecular Weight

00067-56-1

32.04



40¡F

50¡F

60¡F

70¡F

80¡F

90¡F

100¡F

6.630

0.735

1.006

1.412

1.953

2.610

3.461

4.525


{methanol} Methyl ethyl ketone c d

00078-93-3

72.10

6.747

Methyl isobutyl ketone

00108-10-1

100.20

6.677

Methyl methacrylate c d

00080-62-6

100.11

7.909

0.116

0.213

0.348

0.541

0.773

1.064

1.373

Methyl propyl ether c

00557-17-5

74.12

6.166

3.674

4.738

6.091

7.058

9.417

11.602

13.729

Methyl styrene (alpha)

00098-83-9

118.00

7.586

Methylcyclohexane c

00108-87-2

98.18

6.441

0.715

0.928

1.199

1.489

2.069

2.668

3.345

0.212

0.024 0.309

0.425

0.541

0.735

0.986

1.315

1.721

A Dimensionless

¡C ¡R

¡C Ñ

B (degrees)

C (degrees)

7.897

1,474.1

15.948

8,131.3

6.974

1,209.6


Max. (¡F)

Ð47.2

435.2

Ð54.9

175.3

229.13 216.00

14.381

7,380.2

6.672

1,168.4

191.90

8.409

2,050.5

274.40

14.800

8,127.7

6.119

708.7

179.90

6.923

1,486.9

202.40

6.823

1,270.8

221.42

S Ð22.9

213.8

E C T I O N

1 — E

V A P O R A T I V E

L

Methylcyclopentane c

00096-37-7

Methyldichlorosilane Methylene chloride c d

00075-09-2

84.16

6.274

129.06

8.910

84.94

11.122

0.909

1.160

1.644

2.224

2.862

3.616

4.544

5.718 3.094

4.254

5.434

6.787

8.702

10.329

13.342

6.863

1,186.1

226.04

7.028

1,167.8

240.70

7.409

1,325.9

14.897

6,857.5

100.21

5.660

0.799

6.873

1,236.0

219.55

Methylhexane (Ð3)

100.21

5.720

0.744

6.868

1,240.2

219.22

Methylpentane (Ð2)

86.18

5.440

2.731

6.839

1,135.4

226.57

01634-04-4

88.15

6.200

6.867

1,116.1

224.74

00110-91-8

87.12

8.337

0.109

7.718

1,745.8

235.00

128.17

9.555

0.0007

7.011

1,733.7

201.86

123.10

10.057

0.002

7.115

1,746.6

201.80

1.920

2.500

3.220

4.110

5.180

6.470

8.000

F I X E D

R

252.60

Methylhexane (Ð2)

Methyl-tert-butyl ether g

O S S F R O M

Ð94.0

105.3

O O F

T

A N K S

{MTBE} Morpholine Naphthalene e h Nitrobenzene

00098-95-3

2 7 --``,,`,,,``,````,,``,```,,,``-`-`,,`,,`,`,,`---



2 8

` , , ` , ` , , ` , , ` ` ` ` , , , ` ` ` , ` ` , , ` ` ` ` , ` ` , , , ` , , ` ` -


Chemical Name

CAS No.

Molecular Weight



40¡F

50¡F

60¡F

70¡F

80¡F

90¡F

100¡F

A Dimensionless 7.282


Nitromethane c e

00075-52-5

61.04

9.538

0.213

0.251

0.348

0.503

0.715

1.006

1.334

Nonane (Ðn)

00111-84-2

128.26

5.992

0.040

0.051

0.065

0.083

0.106

0.135

0.171

Octane (Ðn) d e

00111-65-9

114.23

5.867

0.087

0.112

0.145

0.188

0.244

0.315

0.408

Octanol (Ð1)

00111-87-5

130.23

6.890

0.0008

¡C ¡R

¡C Ñ

B (degrees)

C (degrees)

1,446.9

15.241

9,469.8

6.920

1,352.0

14.231

8,350.6

12.070

4,506.8


Max. (¡F)

36.3

301.1

6.8

538.5

227.60

209.15 319.90

C 202.30

13.947

0.035

6.740

1,378.0

197.00

H A P T E R

Pentadiene (1,2)

68.12

5.770

4.827

6.918

1,105.0

228.85

1 9 — E

Pentadiene (1,4)

68.12

5.490

10.019

6.835

1,018.0

231.46

Pentadiene (2,3)

68.12

5.790

4.160

6.962

1,126.8

227.84

V A P O R A T I V E

233.01

O S S

Pentachloroethane


00076-01-7

L

Pentane (Ðn) c d e Pentene (Ð1) Pentyne (Ð1)

00109-66-0 00109-67-1

72.15

5.253

4.293

5.454

6.828

8.433

10.445

12.959

15.474

6.853

1,064.8

13.300

5,972.6

Ð105.9

70.14

5.330

8.688

6.844

1,044.0

233.50

68.12

5.760

5.663

6.967

1,092.5

227.18

376.3

M

E A S U R E M E N T



2 8

` , , ` , ` , , ` , , ` ` ` ` , , , ` ` ` , ` ` , , ` ` ` ` , ` ` , , , ` , , ` ` -


Chemical Name

f r o m I H S

CAS No.

Molecular Weight



40¡F

50¡F

60¡F

70¡F

80¡F

90¡F

100¡F

A Dimensionless 7.282


Nitromethane c e

00075-52-5

61.04

9.538

0.213

0.251

0.348

0.503

0.715

1.006

1.334

Nonane (Ðn)

00111-84-2

128.26

5.992

0.040

0.051

0.065

0.083

0.106

0.135

0.171

Octane (Ðn) d e

00111-65-9

114.23

5.867

0.087

0.112

0.145

0.188

0.244

0.315

0.408

Octanol (Ð1)

00111-87-5

130.23

6.890

0.0008

¡C ¡R

¡C Ñ

B (degrees)

C (degrees)

1,446.9

15.241

9,469.8

6.920

1,352.0

14.231

8,350.6

12.070

4,506.8


Max. (¡F)

36.3

301.1

6.8

538.5

227.60

209.15 319.90

C 202.30

13.947

0.035

6.740

1,378.0

197.00

H A P T E R

Pentadiene (1,2)

68.12

5.770

4.827

6.918

1,105.0

228.85

1 9 — E

Pentadiene (1,4)

68.12

5.490

10.019

6.835

1,018.0

231.46

Pentadiene (2,3)

68.12

5.790

4.160

6.962

1,126.8

227.84

V A P O R A T I V E

233.01

O S S

Pentachloroethane


00076-01-7

L

Pentane (Ðn) c d e Pentene (Ð1)

00109-66-0 00109-67-1

72.15

5.253

4.293

5.454

6.828

8.433

10.445

12.959

15.474

6.853

1,064.8

13.300

5,972.6

Ð105.9

70.14

5.330

8.688

6.844

1,044.0

233.50

Pentyne (Ð1)

68.12

5.760

5.663

6.967

1,092.5

227.18

Phenol d h

94.11

8.937

0.006 15.658

10,769

Phosgene

00075-44-5

98.92

11.500

19.788

6.843

941.3

230.00

Picoline (Ð2)

00108-99-6

93.12

7.928

0.122

7.032

1,415.7

211.63

Propanethiol (Ð1)

76.16

7.010

1.942

6.928

1,183.3

224.62

Propanethiol (Ð2)

76.16

6.830

3.595

6.877

1,113.9

226.16

60.10

6.700

0.212

7.848

1,499.2

204.64

Propyl alcohol (Ðn)

00071-23-8

376.3

M

E A S U R E M E N T

{propanol (Ð1)}




¡C ¡R

¡C Ñ

A Dimensionless

B (degrees)

C (degrees)

6.955

1,294.4

206.70

6.927

1,044.1

210.84

CAS No.

Molecular Weight

Propyl nitrate (Ðn)

00627-13-4

105.09

8.780

Propylamine (Ðn) c e

00107-10-8

59.11

6.030

Propylene glycol

00057-55-6

76.11

8.646

0.0009

8.208

2,085.9

203.54

Propylene oxide

00075-66-9

58.10

7.169

6.674

8.277

1,656.9

273.16

Pyridine

00110-86-1

79.10

8.162

0.233

7.041

1,373.8

214.98

Resorcinol

00108-46-3

110.11

10.616

0.00007

6.924

1,884.5

186.06

Styrene d

00100-42-5

104.15

7.560

224.09

Chemical Name

f r o m I H S



Tetrachloroethane


50¡F

60¡F

70¡F

80¡F

90¡F

100¡F

0.262 2.456

3.191

4.157

0.072

5.250

6.536

8.044

9.572

7.140

1,574.5

14.295

8,725.2

00630-20-6

167.85

13.336

0.132

6.898

1,365.9

209.74

00079-34-5

167.85

13.236

0.043

6.631

1,228.1

179.90

(1,1,2,2) Tetrachloroethylene ` ` , , ` , , , `

00127-18-4

165.83

13.545

0.207

6.980

1,386.9

Min. (¡F)

217.53

Max. (¡F)

S E C T I O N

1 — E

19.4

(1,1,1,2) Tetrachloroethane

Temperature Range

293.4

V A P O R A T I V E

L

O S S F R O M

F I X E D

R

O O F

Tetrahydrofuran

00109-99-9

72.12

7.421

2.038

6.995

1,202.3

226.25

T A




¡C ¡R

¡C Ñ

A Dimensionless

B (degrees)

C (degrees)

6.955

1,294.4

206.70

6.927

1,044.1

210.84

CAS No.

Molecular Weight

Propyl nitrate (Ðn)

00627-13-4

105.09

8.780

Propylamine (Ðn) c e

00107-10-8

59.11

6.030

Propylene glycol

00057-55-6

76.11

8.646

0.0009

8.208

2,085.9

203.54

Propylene oxide

00075-66-9

58.10

7.169

6.674

8.277

1,656.9

273.16

Pyridine

00110-86-1

79.10

8.162

0.233

7.041

1,373.8

214.98

Resorcinol

00108-46-3

110.11

10.616

0.00007

6.924

1,884.5

186.06

Styrene d

00100-42-5

104.15

7.560

224.09

Chemical Name

f r o m I H S



Tetrachloroethane


50¡F

60¡F

70¡F

80¡F

90¡F

100¡F

0.262 2.456

3.191

4.157

5.250

6.536

8.044

9.572

0.072

7.140

1,574.5

14.295

8,725.2


S E C T I O N

1 — E

19.4

00630-20-6

167.85

13.336

0.132

6.898

1,365.9

209.74

00079-34-5

167.85

13.236

0.043

6.631

1,228.1

179.90

Max. (¡F)

293.4

(1,1,1,2) Tetrachloroethane Tetrachloroethylene

00127-18-4

165.83

13.545

0.207

6.980

1,386.9

L

O S S F R O M

F I X E D

(1,1,2,2) ` ` , , ` , , , ` ` , ` ` ` ` , , ` ` , ` ` ` , , , ` ` ` ` , , ` , , ` , ` , , ` -

V A P O R A T I V E

R

217.53

O O F

Tetrahydrofuran

00109-99-9

72.12

7.421

Toluene c d

00108-88-3

92.13

7.261

Trichloroethane (1,1,1) c d

00071-55-6

133.42

11.216

Trichloroethane (1,1,2)

00079-00-5

133.40

11.163

Trichloroethylene c d

00079-01-6

131.40

12.272

2.038 0.174 0.909

0.213 1.218

0.309 1.586

0.425 2.030

0.580 2.610

0.773 3.307

1.006 4.199

0.245 0.503

0.677

0.889

1.180

1.508

2.030

2.610

6.995

1,202.3

226.25 219.48

6.954

1,344.8

13.829

7,770.6

8.643

2,136.6 7,256.4

6.951

1,314.4

209.20 192.70

6.518

1,018.6 7,529.8

Trichloropropane (1,2,3)

00096-18-4

147.43

11.575

139.194

6.903

788.2

243.23

Trißuoroethane

00076-13-1

187.38

13.178

4.376

6.880

1,099.9

227.50

(trichloro 1,1,2)

A N K S

Ð16.1

606.2

Ð61.6

165.4

Ð46.8

188.1

302.80

14.373

14.374

T

2 9


tions). Since a large variability in vapor molecular weights has been observed in foreign crude oils, no average value has been developed for these stocks.

19.1.2.2 19.1.2.2.2.8 .2.8.2 .2 Petro Petroche chemica micall Stocks Stocks For single-component petrochemical stocks, the molecular weight of the vapor is equal to the molecular weight of the liquid, which is given in Table Table 7 for selected petrochemicals.

19.1.2.2.2. 19.1.2.2.2.9 9 Daily Daily Maximum Maximum,, Avera Average, ge, and and Minimu Minimum m Vapor Pressures, P VX , P VA, P VN The stock vapor pressure must be determined at three different temperatures: a. The daily maximum maximum liquid liquid surface surface tempera temperature, ture, T LX . b. The daily average average liquid liquid surface surface temperature temperature,, T LA. c. The daily minimu minimum m liquid surface surface tempera temperature, ture, T LN

31

B = consta constant nt in the the vapo vaporr press pressure ure equati equation, on, in degrees Rankine, exp exp = expo expone nent ntia iall fun funct ctio ion. n.

19.1.2.2 19.1.2.2.2.9 .2.9.1 .1 Petro Petroleum leum Liquid Liquid Stocks Stocks For selected petroleum liquid stocks, the stock vapor pressure may be calculated from Equations 28, 29, and 30, where the constants A and B are listed in Table 6.

19.1.2.2 19.1.2.2.2.9 .2.9.1.1 .1.1 Refined Refined Petro Petroleum leum Stocks Stocks For reÞned petroleum stocks, the stock vapor pressure may be determined from Figure 5 or calculated from Equations 28, 29, and 30. For reÞned petroleum stocks, the constants A and B are functions of both the Reid vapor pressure, RVP, and the ASTM Distillation Slope, S . The constants A and B can be determined from Figures 3 and 4 or calculated from Equations 31 and 32, respectively:

` , , ` , ` , , ` , , ` ` ` ` , , , ` ` ` , ` ` , , `


tions). Since a large variability in vapor molecular weights has been observed in foreign crude oils, no average value has been developed for these stocks.

19.1.2.2 19.1.2.2.2.8 .2.8.2 .2 Petro Petroche chemica micall Stocks Stocks

B = consta constant nt in the the vapo vaporr press pressure ure equati equation, on, in degrees Rankine, exp exp = expo expone nent ntia iall fun funct ctio ion. n.

19.1.2.2 19.1.2.2.2.9 .2.9.1 .1 Petro Petroleum leum Liquid Liquid Stocks Stocks

For single-component petrochemical stocks, the molecular weight of the vapor is equal to the molecular weight of the liquid, which is given in Table Table 7 for selected petrochemicals.

19.1.2.2.2. 19.1.2.2.2.9 9 Daily Daily Maximum Maximum,, Avera Average, ge, and and Minimu Minimum m Vapor Pressures, P VX , P VA, P VN The stock vapor pressure must be determined at three different temperatures: a. The daily maximum maximum liquid liquid surface surface tempera temperature, ture, T LX . b. The daily average average liquid liquid surface surface temperature temperature,, T LA. c. The daily minimu minimum m liquid surface surface tempera temperature, ture, T LN . These three liquid surface temperatures are discussed in 19.1.2.2.2.5 and 19.1.2.2.2.7. The corresponding three stock vapor pressures, PVX , PVA, and PVN , can be calculated from Equations 28, 29, and 30, respectively: PVX = exp [A Ð (B/T LX )]

(28)

PVA = exp [A Ð (B/T LA)]

(29)

PVN = exp [A Ð (B/T LN )]

(30)

For selected petroleum liquid stocks, the stock vapor pressure may be calculated from Equations 28, 29, and 30, where the constants A and B are listed in Table 6.

19.1.2.2 19.1.2.2.2.9 .2.9.1.1 .1.1 Refined Refined Petro Petroleum leum Stocks Stocks For reÞned petroleum stocks, the stock vapor pressure may be determined from Figure 5 or calculated from Equations 28, 29, and 30. For reÞned petroleum stocks, the constants A and B are functions of both the Reid vapor pressure, RVP, and the ASTM Distillation Slope, S . The constants A and B can be determined from Figures 3 and 4 or calculated from Equations 31 and 32, respectively: A = 15.64 Ð 1.854 S 0.5 Ð (0.8742 Ð 0.3280 S 0.5) ln ( RVP) (31) (31) B = 8742 Ð 1042 S 0.5 Ð(1049 Ð 179.4 S 0.5) ln ( RVP)

PVX = stock vapor pressure pressure at the the daily daily maximum maximum liqliquid surface temperature, in pounds per square inch absolute, PVA = stock vapor pressure pressure at the the daily daily average average liquid liquid surface temperature, in pounds per square inch absolute, PVN = stock vapor pressure pressure at the the daily daily minimum minimum liqliquid surface temperature, in pounds per square inch absolute, T maximum liquid liquid surfac surfacee temperat temperature, ure, in in LX = daily maximum degrees Rankine, T average liquid liquid surfac surfacee temperatur temperature, e, in LA = daily average degrees Rankine, T minimum liquid liquid surface surface temperatu temperature, re, in LN = daily minimum degrees Rankine,

A = consta constant nt in in the the vapor vapor pressu pressure re equat equation ion (dimen (dimen-sionless),

(32)

where RVP = stock Reid vapor vapor pressur pressure, e, in pounds per square square inch, S = stoc Petroleum leum stock k ASTM ASTM-D -D86 86Ñ Ñ Distillation of Petro Products distillation slope at 10 volume percent evaporated, in degrees Fahrenheit per volume percent,

where


31

ln = natu natura rall loga logari rith thm m func functi tion. on. The slope, S , is the slope of the ASTM-D86 distillation data at 10 volume percent evaporated and can be calculated from the distillation data using Equation 33: where T 15 Ð T 5 S = ------------------10

(33)

S = stock ASTM-D86 ASTM-D86 distillat distillation ion slope slope at 10 10 volvolume percent evaporated, in degrees Fahrenheit per volume percent, T 5 = temperature temperature at at which which 5 volume volume percent percent is is evapevaporated, in degrees Fahrenheit,

temperature at which which 15 volume volume percent percent is is T 15 = temperature evaporated, in degrees Fahrenheit. The constant, 10, in Equation 33 has units of volume percent.


` , , ` , ` , , ` , , ` ` ` ` , , , ` ` ` , ` ` , , ` ` ` ` , ` ` , , , ` , , ` ` -

32


Figure 3—Vapor 3—Vapor Pressure Pressure Function Function Coefficient Coefficient (A ) of Refined Petroleum Stocks with a Reid Vapor Pressure of 1 to 20 psi, Extrapolated to 0.1 psi

` , , ` , ` , , ` , , ` ` ` ` , , , ` ` ` , ` ` , , ` ` ` ` , ` ` , , , ` , , ` ` -

Figure 4—Vapor 4—Vapor Pressure Pressure Function Function Coefficient Coefficient (B ) of Refined Petroleum Stocks with a Reid Vapor Pressure of 1 to 20 psi, Extrapolated to 0.1 psi




33

` , , ` , ` , , ` , , ` ` ` ` , , , ` ` ` , ` ` , , ` ` ` ` , ` ` , , , ` , , ` ` -

Figure 5—True 5—True Vapor Vapor Pressure Pressure (P V ) of Refined Petroleum Stocks with a Reid Vapor Pressure of 1 to 20 psi



34


Table 8—ASTM Distillation Distillation Slope Slope (S ) for Selected Refined Petroleum Stocks

Reid Vapor Pressure RVP, (psi)

ASTM-D86 Distillation Slope at 10 Volume Percent Evaporated (¡F/v /vol ol.. %) S , (¡F

Aviation gasoline

Ñ

2.0

Naphtha

2Ð8

2.5

Motor gasoline

Ñ

3.0

Light naphtha

9Ð14

3.5

ReÞned Petroleum Stock

equation rather than the 2-constant form used in Equations 28, 29, and 30.

Ð1

PVX = 0.0193 0.019337 37 log

Ð1

PVA = 0.0193 0.019337 37 log

In the absence of ASTM-D86 distillation data on reÞned petroleum stocks, approximate values of the distillation slope, S , from Table 8 may be used.

19.1.2 19. 1.2.2. .2.2.9 2.9.1. .1.2 2

Crude Crude Oil Stock Stocks s

RVP) A = 12.82 Ð 0.9672 ln( RVP

(34)

B = 7261 Ð 1216 ln( RVP)

(35)

where vapor pressur pressure, e, in pounds per square square RVP = stock Reid vapor inch, ln = natu natura rall loga logari rith thm m func functi tion on..

19.1.2.2 19.1.2.2.2.9 .2.9.2 .2 Petr Petroch ochemic emical al Stocks Stocks For selected petrochemical stocks, the stock vapor pressure may be calculated from Equation 28, 29, and 30, where the constants A and B are from the 2-constant form of AntoineÕs equation. The 2-constant values of A and B are listed on the bottom line of the entry for AntoineÕs equation constants in Table 7, for those chemicals for which values are provided. Use of the values of A and B from the 3-constant form of AntoineÕs equation would yield meaningless results. The loss equations are applicable to nonboiling stocks, although volatile stocks with a true vapor pressure over 1.5 pounds per square inch absolute are not now typically stored in the U.S. in Þxed-roof tanks. Alternatively, Alternatively, a more accurate estimation of the vapor pressure of petrochemical stocks may be calculated from Equations 36, 37, and 38, which use a 3-constant form of AntoineÕs


B A Ð -------------------------------------------------- LA  -5----T 27 3.15 15  + C  -9------ Ð 273. 

B A Ð -------------------------------------------------- LN  -5----T 27 3.15 15  + C  -9------- Ð 273. 

(36)

(37)

(38)

where

For crude oil stocks, the stock vapor pressure may be determined from Figure 8 or calculated from Equations 28, 29, and 30. For crude oil stocks, the constants A and B are functions of only the Reid vapor pressure, RVP, and can be determined from Figures 6 and 7 or calculated from Equations 34 and 35, respectively:

` ` , , ` , , , ` ` , ` ` ` ` , , ` ` , ` ` ` , , , ` ` ` ` , , ` , , ` , ` , , ` -

Ð1

PVN = 0.01933 0.019337 7 log

B A Ð -------------------------------------------------- LX  -5----T 27 3.15 15  + C  -9------ Ð 273. 

PVX = stock vapor pressure pressure at the the daily daily maximum maximum liqliquid surface temperature, in pounds per square inch absolute, PVA = stock vapor pressure pressure at the the daily daily average average liquid liquid surface temperature, in pounds per square inch absolute, PVN = stock vapor pressure pressure at the the daily daily minimum minimum liqliquid surface temperature, in pounds per square inch absolute, T maximum liquid liquid surfac surfacee temperat temperature, ure, in in LX = daily maximum degrees Rankine, T average liquid liquid surface surface temperature temperature,, in LA = daily average degrees Rankine, T minimum liquid liquid surfac surfacee temperatu temperature, re, in LN = daily minimum degrees Rankine,

A = consta constant nt in in the the vapor vapor pressu pressure re equat equation ion (dimen (dimen-sionless), B = consta constant nt in the the vapor vapor pressu pressure re equatio equation, n, in in degrees Celsius, C = consta constant nt in the the vapor vapor pressu pressure re equatio equation, n, in in degrees Celsius. The constant, 0.019337, is a conversion factor with units of pounds per square inch absolute per millimeter of mercury. The terms (5 T LX / 9 Ð 273.15), (5T LA / 9 Ð 273.15), and (5T LN /9 Ð 273.15) convert the liquid surface temperatures, T LX , T LA, and T LN , from degrees Rankine to degrees Celsius. The constants A, B, and C are listed in Table 7 for selected petrochemicals. The 3-constant values of A, B, and C are listed on



35

` , , ` , ` , , ` , , ` ` ` ` , , , ` ` ` , ` ` , , ` ` ` ` , ` ` , , , ` , , ` ` -

Figure 6—Vapor 6—Vapor Pressure Pressure Function Function Coefficient Coefficient (A ) of Crude Oil Oi l Stocks with a Reid Vapor Pressure of 2 to 15 psi, Extrapolated to 0.1 psi

Figure 7—Vapor 7—Vapor Pressure Pressure Function Function Coefficient Coefficient (B ) of Crude Oil Oi l Stocks with a Reid Vapor Pressure of 2 to 15 psi, Extrapolated to 0.1 psi



36


Figure 8—True 8—True Vapor Vapor Pressure Pressure (P V ) of Crude Oil Stocks with a Reid Vapor Pressure of 2 to 15 psi

--``,,`,,,``,````,,``,```,,,``-`-`,,`,,`,`,,`---



SECTION 1—EVAPORATIVE LOSS

the top line of the entry for Antoine’s equation constants in Table 7, for those chemicals for which values are provided.

19.1.2.2.2.10

Daily Vapor Pressure Range, ΔPV

The stock daily vapor pressure range, lated from Equation 39a:

Δ P V ,

FROM FIXED-ROOF T ANKS

19.1.2.2.2.11

37

Breather Vent Pressure Setting Range, ΔP B

The breather vent pressure setting range, Δ P B, is used in Equation 14 and may be calculated from Equation 40:

can be calcuΔ P B = P BP – P BV

Δ P V = P VX – P VN

(39a)

(40)

where ΔPB

where

= breather vent pressure pressure setting range, in pounds pounds per square square inch,

Δ P V

= stock daily vapor vapor pressure pressure range, in pounds pounds per per square inch,

PBP = breather vent pressure pressure setting setting (always a positive positive value), in pounds per square inch gauge,

P VX

= stock stock vapor vapor pressu pressure re at the daily daily maximum maximum liqliquid surface temperature, in pounds per square inch absolute,

PBV = breather breather vent vent vacuum vacuum setting setting (always (always a neganegative value), in pounds per square inch gauge.

P VN

= stock stock vapor vapor pressur pressuree at the daily daily minimum minimum liqliquid surface temperature, in pounds per square inch absolute.

In order to calculate the stock daily vapor pressure range, Equation 39a, it is first necessary to determine the stock vapor pressure at the daily maximum liquid surface temperature, T LX , and at the daily minimum liquid surface temperature, T LN . These temperatures are discussed in 19.1.2.2.2.7. An approximate method of estimating the stock daily vapor pressure range is from Equation 39b: Δ P V , from

Δ P V =

08

0.50 B P VA Δ T V ---------------------------------------2 T L A

(39b)

where Δ P V

19.1.2.2.2.12

= stock vapor pressure pressure at the daily daily average average liquid surface temperature, in pounds per square inch absolute,

T LA

= daily daily average average liquid liquid surface surface temper temperatur ature, e, in degrees Rankine,

ΔT V

= daily daily vapor vapor temperatu temperature re range, range, in degrees degrees Rankine.

Although Equation 39b is less accurate than Equation 39a, it is easier to use since it requires the stock vapor pressure at only the daily average liquid surface temperature, T LA.

Vented Vapor Saturation Factor, KS

The vented vapor saturation factor, K S , accounts for the degree of stock vapor saturation in the vented vapor. The vented vapor saturation factor may be estimated from Equation 5 or determined from Figure 9.

= stock daily vapor vapor pressure pressure range, in pounds pounds per per square inch,

B = cons consta tant nt in the the vapo vaporr press pressure ure equ equati ation on,, in degrees Rankine, P VA

The breather vent pressure setting, P , and breather vent BP vacuum setting, P , should be available from the tank owner BV or operator. If specific information on the breather vent pressure setting and vacuum setting is not available, assume +0.03 pounds per square inch gauge for P BP and –0.03 pounds per square inch gauge for P . BV If the fixed-roof tank is of bolted or riveted construction in which the roof or shell plates are not gas tight, assume that Δ P B is 0 pounds per square inch, even if a breather vent is used.

K S

1 = -------------------------------------------1 + 0.053 P VA H VO

(5)

where K S

= vented vapor saturation factor, factor, (dimension (dimensionless), less),

P VA

= stock stock vapor vapor pressure pressure at the daily daily average average liquid liquid surface temperature, in pounds per square inch absolute,

H VO

= vapor vapor spac spacee outag outage, e, in feet. feet.

The constant, 0.053, in Equation 5 has units of [(pounds per square square inch absolute) absolute) feet] –1.

19.1.2.2.2.13

Condensed Vapor Density, W VC

19.1.2.2.2.13.1 19.1.2.2.2.13. 1

Petroleum Liquid Stocks

For selected petroleum liquid stocks, the stock condensed vapor density at 60°F is given in Table 6. --``,,`,,,``,````,,``,```,,,``-`-`,,`,,`,`,,`---



38


Figure 9—Vented 9—Vented Vapor Vapor Saturation Saturation Factor Factor ( K S )

b. Stock vapor vapor density density,, W V .

For reÞned petroleum stocks and crude oil stocks, the stock condensed vapor density, W VC , is lower than the stock liquid density, W L. If this information is not known, it can be estimated from Equation 41, which was developed primarily for gasoline stocks: W VC = 0.08 M V

c. Produc Productt fact factor or,, K P d. Turnove Turnoverr (saturation) (saturation) factor factor,, K N . e. Vent setting setting correction correction factor factor,, K B. The variables pertaining to stock vapor density, W V , were discussed in 19.1.2.2.2. The additional working loss variables of stock annual net throughput, Q; working loss turnover factor, K N ; working loss product factor, K P; and vent setting correction factor, K B; are discussed in 19.1.2.2.3.1 through 19.1.2.2.3.4.

(41)

where W VC = stock condens condensed ed vapor vapor density density,, in pounds pounds per gallon, M V = stock vapor vapor molecular molecular weight, in pounds pounds per per pound-mole.

19.1. 19.1.2.2 2.2.3. .3.1 1

The constant, 0.08, in Equation 41 has units of poundmoles per gallon.

The annual net throughput, Q, as used in this publication, is the total volume of stock that is pumped into the tank in a year that results in an increase in the level of the stock liquid in the tank. If Þlling and withdrawal occur equally and simultaneously so that the liquid level does not change, the net throughput is zero. The annual net throughput is presented in Equation 7 as a function of the volume of the tank and the number of turnovers. The volume of the tank is expressed in terms of the tank diameter, D, and the stock maximum liquid height, H LX .

19.1.2.2 19.1.2.2.2.1 .2.13.2 3.2 Petro Petroche chemica micall Stocks Stocks For single-component petrochemical stocks, the stock condensed vapor density is equal to the stock liquid density, W L. For selected petrochemical stocks, the stock liquid density at 60¡F is given g iven in Table 7.

19.1.2 19. 1.2.2. .2.3 3

Annual Annual Net Throug Throughpu hput, t, Q

Workin orking g Loss Loss Vari Variab ables les

19.1.2.2 19.1.2.2.3.2 .3.2 Turnove urnoverr Factor Factor,, K N

The working loss, LW , is related in Equation 7 to the following variables:

For tanks where the annual net throughput, Q, is large, resulting in frequent tank turnovers (greater than 36 turnovers per year), the vented air-stock vapor mixture is not saturated

a. Volume of displaced displaced vapors, vapors, Q (expressed in terms of N , H LX , and D). --``,,`,,,``,````,,``,```,,,``-`-`,,`,,`,`,,`---




39

D = tank tank diame diameter ter,, in feet, feet, H stock maximu maximum m liquid liquid height height,, in feet. feet. LX = stock

In Equation 42, the constant, 5.614, has units of cubic feet per barrel.

19.1.2 19. 1.2.2. .2.3.3 3.3 Produ Product ct Fact Factor or,, K P The working loss product factor, K P, accounts for the effect of different types of liquid stocks on evaporative loss during tank working. The use of this product factor applies only to working losses and should not be used for estimating standing storage losses. Product factors have been developed for multicomponent hydrocarbon liquid mixtures, including crude oil stocks and reÞned petroleum stocks (such as gasolines and naphthas), as well as for single-component petrochemical stocks. K P = 0.75 for crude oil stocks.

(43a)

K P = 1. 1.00 for reÞned petroleum stocks.

(43b)

K P = 1.00 for single-component petro-barrels chemical stocks.

(43c)

Figure 10—Working 10—Working Loss Turnover urnover Factor Factor ( K N ) with stock vapor. The working loss turnover factor, K N , is used to account for this non-saturation condition in the vented vapor. The turnover factor can be determined from Figure 10 or calculated from Equations 8a and 8b: 180 + N K N = ------------------6 N K N = 1

(for N > > 36)

(for N ≤ 36 36

(8a)

(8b)

where K working loss turnover turnover factor factor (dimensionl (dimensionless), ess), N = working N = stock turnover turnover rate, rate, in turnovers turnovers per year year.

In Equation 8b, the constant, 180, has units of turnovers per year, and the constant, 6, is dimensionless. The stock turnover rate, N , may be calculated from Equation 42: 5.614 Q N = ---------------------------

 π--  D2 H LX  4

(42)

where

19.1.2.2 19.1.2.2.3.4 .3.4 Vent Setti Setting ng Correct Correction ion Facto Factorr, K B Previous editions of 19.1 (i.e., the Þrst and second editions of API Publication 2518) did not include a vent setting correction factor, K B, in the calculation of working losses. The method for estimating working loss in those editions assumed that the tank behaves as if freely vented during the tank Þlling process. This assumption is reasonable for very low breather vent settings (such as the typical level of one-half ounce per square inch). As the breather vent settings increase, however, the freely-vented assumption becomes increasingly conservative (i.e., results in an overestimate of working loss). The calculation of the vent setting correction factor is performed in two steps. The Þrst step is a check to determine whether the compression of the vapor space during Þlling, prior to opening of the vent, is sufÞcient to bring the concentration of vapors in the head space above the saturation point. If the vapor concentration is shown to reach the saturation point, it is assumed that condensation takes place. The amount of vapor reduction due to condensation is then calculated in accordance with the ideal gas laws, as formulated in Equation 15.

N = stock turnover turnover rate, rate, in turnovers turnovers per year, year,

19.1.2 19. 1.2.3 .3 SUMMA SUMMARY RY OF OF CAL CALCUL CULAT ATION ION PROCEDURE

Q = stock annual net throughp throughput ut (associa (associated ted with with increasing the stock liquid level in the tank), in barrels per year,

Tables 2 and 3 summarize the equations and information necessary to estimate the total evaporative loss, LT , from a Þxed-roof tank, including the standing storage loss, LS , and --``,,`,,,``,````,,``,```,,,``-`-`,,`,,`,`,,`---



40


the working loss, LW . The information in these tables is the same as that presented in 19.1.2.1 and 19.1.2.2, but without all of the important descriptive qualiÞers presented in those sections. Therefore, questions about the information in Tables 2 and 3 should be answered by referring to 19.1.2.1 and 19.1.2.2 for more detailed information.

Section 5, may be followed. The calculation steps are summarized in the footnote to Chapter 19.4, First Edition, Table 4. More detailed guidance for this procedure is found in Chapter 19.4, First Edition, Section 7.2. This procedure requires the following information:

19.1.2.3 19.1.2.3.1 .1 Speciati Speciation on of of Evap Evaporat orative ive Losses Losses When the procedures in 19.1.2 are applied to a Þxed-roof tank storing a multicomponent hydrocarbon stock, the result is an estimate of the total hydrocarbon emissions from the tank. The process of breaking down the total emissions of a mixture into its speciÞc components is commonly referred to as speciation . Guidance for speciating total hydrocarbon emissions into the emissions of the individual components is provided in APIÕs Manual of Petroleum Measurement Stan Recommended Practice Practice for Speciation Speciation of dards, Chapter 19.4, Recommended Evaporative Evaporative Losses Losses. When speciated emissions are desired for only a portion of the components in a mixture, such as those deemed to be toxic, the calculation example of Chapter 19.4, First Edition,

¥

total hydrocarbon emissions as estimated in accordance with 19.1.2,

¥

vapor molecular weight of of the stock,

¥

true vapor pressure of the stock at the average liquid surface temperature,

¥

liquid molecular weight of of the stock,

¥

molecular weight of each component to be speciated (for single components, liquid-phase and vapor-phase molecular weights are the same),

¥

true vapor pressure pressure of each component to be speciated, at the average liquid surface temperature, and

¥

liquid weight fraction of each component to be speciated (i.e., the weight fraction of the component in the liquid mixture).

Table 9—Typical 9—Typical Concentrations of Selected Chemicals in Common Petroleum Products

Liquid Molecular Weight 1

Gasoline

JP-4 (Jet Naphtha)

Jet A (Jet Kerosene)

Diesel (Distillate Fuel Oil No.2)

92

120

162

188

Component

Typical Liquid Concentration, Weight Percent

n-Hexane

1.0

1.5

0.005

0.0001

Benzene

1.8

0.6

0.004

0.0008

Iso-octane2

4.0

0.0

0.0

0.0

Toluene

7.0

2.0

0.133

0.032

Ethylbenzene

1.4

0.5

0.127

0.013

Xylenes3

7.0

2.5

0.31

0.29

Cumene4

0.5

0.2

0.0

0.0

Note 5

0.0

0.0

0.0

1,2,4- Trimethylbenzene

2.5

0.0

0.0

1.0

Cyclohexane

0.2

1.2

0.0

0.0

MTBE

Notes: 1. Liquid molecular weights from fr om ÒMemorandum from Patrick B. Murphy, Radian/RTP Radian/RTP to James F. Durham, EPA/CPB EPA/CPB Concerning Petroleum ReÞnery Liquid HAP and Properties Data, August 10, 1993,Ó as adopted in versions 3.1 and 4.0 of EPAÕs TANKS software. 2. Iso-octane is also known as 2,2,4 trimethylpentane. 3. The Chemical Database in EPAÕs TANKS software includes m,o-Xylenes. For convenience, use m- to represent all xylenes. 4. Cumene is also known as isopropylbenzene. 5. MTBE concentrations vary signiÞcantly. EPA, EPA, in the Background Information Document for the Gasoline Distribution Industry (Stage I) MACT Rule, suggests the following liquid concentrations:

MTBE %

Norm Normal al Gaso Gasolline ine Refo Reforrmula ulated ted w/M w/MTB TBE E Oxyg Oxygeenate nated d w/MT w/MTBE BE -------------------------------------------------------------------------------------------------------------------------------------------------------------------------0.0 8 .8 12.0

Copyright American Petroleum Institute Provided by IHS under license with API No reproduction or networking permitted without license from I HS ` ` , , ` , ,



If data are not available for a speciÞc stock, the values given in Table 9 may be assumed for the common petroleum products shown.

41

{since PVA < 0.1 psia; P B = ±0.03 pounds (0.5 oz) per square inch} (3b)

∆T V = 0.72 (T MAX Ð T MIN ) + 0.028α I

(25b)

19.1 19.1.2 .2.4 .4 SA SAMP MPLE LE PR PROB OBLE LEM M 19.1 19.1.2 .2.4 .4.1 .1 Prob Proble lem m Estimate the total annual evaporative loss, in pounds per year, given the following information:

T MAX = 67.6¡F

(given)

T MIN = 45.1¡F

(given)

α = 0.17

(Table 5)

A Þxed-roof tank has the following characteristics: I = = 1502 Btu/ft 2day

a. A diamet diameter er of 100 feet feet..

(given)

∆T V = 23.3 oF

b. A shell shell height height of 40 40 feet. feet. c. A cone roof roof with with roof slope not given. given.

K E = 0.042

d. A typical or or average average liquid liquid level level of 20 feet. e. A maximum maximum liquid liquid level level of of 38 feet. feet.

H VO = H S Ð H L + H RO

f. The tank is painted painted white, white, and the the paint is in good good condition. g. The breather vent pressure pressure setting setting is 0.03 pounds pounds per square inch gauge and the breather vent vacuum setting is Ð0.03 pou nds per square s quare inch gauge. The product stored in the tank has the following characteristics: a. A stock of diesel fuel fuel (distilla (distillate te fuel oil no. 2). 2).

H S = 40 feet

(given)

H L = 20 feet

(given)

1 H RO = ( /3) H R

(16a)

H R = S R RS

(17a)

S R = 0.0625 feet/foot (default per 19.1.2.2.2.1.1) RS = 50 feet

b. The Reid vapor vapor pressure pressure is is not known. known.

(4)

(given)

H R = 3.1 feet

c. The stock vapor vapor and liquid liquid compositi composition on are not given. given. d. An annual net throughput throughput of 3.0 million million barrels barrels per year. year. The ambient conditions are not known at the tank location, but the nearest city is Wichita, KS, for which the following values are given:

H RO = 1.0 feet H VO = 21.0 feet D = 100 feet

(given)

a. A daily maximum maximum ambient ambient temperature temperature of 67.6¡F 67.6¡F (Table (Table 4). b. A daily minimum minimum ambient ambient temperature temperature of 45.1¡F (Table (Table 4). c. A daily total total solar insolatio insolation n on a horizontal horizontal surface surface of 1502 British thermal units per square foot day (Table 4). d. An atmospheric atmospheric pressure pressure of 14.0 pounds pounds per square square inch absolute (EPAÕs TANKS software).

1 K S = ---------------------------------------------1 + 0.053 PVA H VO PVA = exp [A Ð (B/T LA)]

(5) (29)

A = 12.101 (dimensionless)

(Table 6)

19.1 19.1.2 .2.4 .4.2 .2 Solu Soluti tion on

B = 8,907.0¡R

(Table 6)

19.1. 19.1.2.4 2.4.2. .2.1 1

T LA = T AA + 0.56 (6 x Ð1) + 0.0079 x I

Stand Standing ing Stora Storage ge Loss, Loss, LS

Calculate the standing storage loss, LS , by following the steps in Table 2: LS = 365 K E H VO

 π-- D2 K S W V  4 

K E = 0.0018 ∆T V ` ` , , ` , , , ` ` , ` ` ` ` , , ` `


(2)

T AA = (T AX + T AN ) / 2

(24b) (20)

T AX = T MAX + 459.67

(18)

T AN = T MIN + 459.67

(19)

T AA = 516.0¡R


42


19.1. 19.1.2.4 2.4.2. .2.3 3

T LA = 518.0¡R

Calculate the total loss, LT , from Equation 1:

PVA = 0.006 psia K S = 0.99

LT (pounds per year) = LS (pounds per year) + LW (p (pounds per year)

M V PVA W V = ----------------- R T LA

R = 10.731 psia ft 3 / lb mole ¡R

(Table 6) (Table 2)

19.1.2 19. 1.2.4. .4.2.2 2.2 Workin orking g Los Loss, s, LW Calculate the working loss, LW , by following the steps in Table 3:

π 2 K K K W  N P B V

L W = N H LX  -- D 4

(7)

(42)

Q = 3,000,000 bbl/yr

(given)

D = 100 feet

(given)

H LX = 38 feet

(given)

N = = 56.4 K N = (180 + N ) / (6 N )

(8b)

K N = 0.70 K P = 1 K B = 1 inch}

(Table 3) {since P B = ±0.03 pounds (0.5 oz) per square (9)

W V = 0.00014 lb/ft3 {from the Standing Storage Loss calculation} calculation}

LW = 1,651 lb/yr

19.1. 19 .1.3 3

Descri Des cripti ption on of Fixed Fixed-Ro -Roof of Tanks anks

This section describes evaporative evaporative loss-related construction features of Þxed-roof tanks. Figure 11 shows a typical Þxedroof tank. Fixed-roof tanks are vessels that have a vertical cylindrical shell and a Þxed roof. In addition to the shell and roof, the basic components and construction features include:

LS = 351 lb/yr

 π--  D2 H LX  4

LT = 2,002 pounds per year

19.1.3 .1.3.1 .1 GENE GENER RAL

W V = 0.00014 lb/ft3

5.614 Q N = ----------------------------

(1)

= 351 + 1,651

(6)

M V = 130 lb/lb mole ` ` , , ` , , , ` ` , ` ` ` ` , , ` ` , ` ` ` , , , ` ` ` ` , , ` , , ` , ` , , ` -

Total otal Loss, Loss, LT

a. Roof Þttings Þttings that penetrat penetratee the Þxed roof roof and serve serve operaoperational functions. b. Shell and roof roof insulation insulation on tanks tanks that store store stocks stocks in a heated condition. c. Shell and and roof surface surface type type and conditio condition. n. General types of these components, which are available in a range of commercial designs, are described in this section. Included in these descriptions are comments on the potential for evaporative loss, as well as some design and operational characteristics. Other factors, such as tank maintenance and safety, are important in designing and selecting tank equipment, but are outside the scope of this publication.

19.1. 19.1.3.2 3.2 FIXEDFIXED-ROO ROOF F TANK ANKS S The Þxed-roof tank is the minimum accepted standard for the storage of volatile liquids. Large, modern Þxed-roof tanks are of all-welded construction and are designed to be liquid and vapor tight. Some older Þxed-roof tanks may be of riveted or bolted construction. In this publication, it is assumed that the tank roof and shell are vapor tight. These are available in a range of sizes from 20 to 300 feet in diameter and up to 65 feet in shell height. The Þxed roof may be column-supported or self-supported, and may be cone-shaped, domeshaped, or ßat. Some Þxed-roof tanks incorporate an internal ßoating roof, but these types of storage tanks are not covered by this publication.

19.1 19.1.3 .3.3 .3 ROOF ROOF FITT FITTIN INGS GS Several roof Þttings penetrate the tank roof to allow for operational functions and are potential sources of evaporative loss. Other accessories that are used that do not penetrate the roof or shell are not potential sources of evaporative loss.




Roof Þttings can be a source of evaporative loss when they are not sealed. The most common types of roof Þttings Þttings used on Þxed-roof tanks are described in 19.1.3.3.1 through 19.1.3.3.4. The evaporative loss contribution of properly sealed roof Þttings is negligible in comparion to the standing loss and the working loss, and thus no roof Þttings loss estimation procedure is included in this publication.

19.1.3.3 19.1.3.3.1 .1 Pressur Pressure-V e-Vacuu acuum m Vents Vents Pressure-vacuum (PV) vents are mounted on the tank roof to provide sufÞcient venting capacity to protect the tank from the damaging effects of overpressure or overvacuum. When a pressure is formed within the tank vapor space that exceeds the pressure set point, the PV vent opens to release vapors from the tank until the pressure is reduced below its set point. When a vacuum is formed within the the tank vapor space that exceeds the vacuum set point, the PV vent opens to admit air into the tank until the vacuum is reduced below its set point. API Bulletin 2521 [9] describes the use of PV vents on Þxed-roof tanks and presents factors that should be considered in their selection and maintenance. API Standard 2000 [10] describes the sizing requirements for PV vents on Þxedroof tanks and covers both normal and emergency venting conditions.

43

PV vents on atmospheric pressure Þxed-roof tanks are usually set at 0.75 inches of water column, or approximately 0.5 ounce per square inch. The required normal pressure venting capacity or vacuum venting capacity should accommodate breathing and product movement up to the maximum safe working pressure or vacuum of the tank. Open vents of the mushroom or return-bend type are not normally used on Þxed-roof tanks storing volatile liquids since they permit higher losses. PV vents should receive regular inspection and maintenance, the frequency depending upon local conditions. PV vents are sometimes equipped with ßame arrestors. When a ßame arrestor is used, additional consideration must be given in sizing the PV vent to allow for the ßow restriction caused by the ßame arrestor. The use of a ßame arrestor also increases maintenance requirements, since the ßame arrestor must receive frequent inspections and cleaning to ensure blockage-free operation.

19.1.3 19. 1.3.3. .3.2 2

Gauge Gauge-H -Hat atch ch/Sa /Samp mple le Wells Wells

Gauge-hatch/sample wells provide access for manually gauging the stock level in the tank and for taking thief samples of the tank contents. Gauge-hatch/sample wells consist of a pipe penetration on the tank roof that is equipped with a self-closing cover. cover. A gasketed cover may be used to further reduce evaporative losses.

` , , ` , ` , , ` , , ` ` ` ` , , , ` ` ` , ` ` , , ` ` ` ` , ` ` , , , ` , , ` ` -

Figure 11—Typical 11—Typical Fixed-Roof Fixed-Roof Tank Tank



44


Gauge-hatch/sample wells are usually located by the gaugerÕs platform, which is mounted at the top of the tank shell. Some vapor loss may occur during manual gauging and stock sampling operations, during which time the gaugehatch/sample well cover is open. This loss can be minimized by reducing the period of time that the cover is left open.

19.1 19.1.3 .3.3 .3.3 .3 Floa Floatt Gau Gauge ges s Float gauges are used to indicate the level of stock within the tank. Float gauges consist of a ßoat that rests on the liquid surface and its connected to a liquid level indicator mounted on the exterior of the tank shell by a cable or tape that passes through a guide system. The cable or tape passes through the tank roof and is normally contained in a sealed conduit to eliminate evaporative loss.

the use of insulation, and thus overpredicts the estimated loss for insulated Þxed-roof tanks.

19.1. 19.1.3.5 3.5 OUTSID OUTSIDE E SURFACE SURFACE OF THE THE TANK Painting the tank shell and roof is important in both reducing evaporative loss and preserving the tank. The use of a highly reßective surface, such as white paint, will result in a lower tank metal temperatures and lower heat input to the tank vapor space, thereby reducing the breathing loss. It is important to establish a tank paint inspection and maintenance program to preserve the paint reßectance and eliminate tank exterior corrosion. Unpainted aluminum dome roofs also provide a highly reßective surface, while avoiding the maintenance concerns inherent to paint.

19.1 19 .1.4 .4 De Deta tail ils s of Los Loss s Anal Analys ysis is 19.1 19.1.4 .4.1 .1 INTR INTROD ODUC UCTI TION ON

19.1 19.1.3 .3.3 .3.4 .4 Roof Roof Man Manho hole les s Roof manholes are used to provide access to the interior of the tank for the purpose of construction or maintenance. Roof manholes normally consist of a circular opening in the tank roof with a peripheral vertical neck attached to the roof and a removable cover. The opening is sized to provide for the passage of personnel and materials through the tank roof. The cover can rest directly on the neck, or a gasket can be used between the cover and the neck to reduce evaporative loss. Bolting the cover to the neck further reduces evaporative loss.

19.1 19.1.3 .3.4 .4 INSU INSULA LATI TION ON Insulation can be used on the tank shell and roof to reduce heat input or heat loss. Some stocks must be stored in a heated condition to permit proper handling. Tanks for warm service may require insulated shells and roofs, depending upon the local climatic conditions, stock properties, and required storage temperature. Various types of insulation systems have been used including: a. Prefabrica Prefabricated ted rigid rigid panel panel insulatio insulation. n. b. Prefabrica Prefabricated ted Þbrous Þbrous blanket blanket insulation. insulation. c. Sprayed-on Sprayed-on polyuret polyurethane hane foam foam insulatio insulation. n. Insulation systems should be equipped with a suitable exterior vapor barrier to reduce the ingress of moisture, which can result in a loss of insulation effect as well as corrosion of the tank shell. Insulation on the tank shell or roof can reduce the standing storage loss by reducing the ambient heat input or loss to the tank vapor space. The standing storage loss estimation procedure described in this publication does not include factors for


The Þrst edition [11] of API Bulletin 2518 was issued in June 1962. That publication was the result of a compilation and study of extensive test data on evaporative loss from Þxed-roof tanks storing gasoline and crude oil. A breathing loss correlation was developed from the test data that included stocks with a true vapor pressure between 1.5 and 8.8 pounds per square inch absolute. Currently, volatile liquids with a true vapor pressure exceeding 1.5 pounds per square inch absolute are not stored in Þxed-roof tanks in the U.S. The use of the breathing loss correlation presented in the Þrst edition of API Bulletin 2518 [11] for stocks with a true vapor less than 1.5 pounds per square inch absolute has been found to a result in an over-prediction of the breathing loss. For this reason, recent studies have addressed the breathing loss by developing a database which could be used to provide a breathing loss estimation procedure that is suitable for use over the entire range of true vapor pressures for stocks that are stored in Þxed-roof tanks. During the period from 1977 through 1984, three speciÞc testing programs involved measurement of the breathing loss from Þxed-roof tanks. In 1977, 44 tests were performed on 21 Þeld tanks for the Western Oil and Gas Association (WOGA) [12] that stored crude oils, distillates and fuel oils. In 1978, 15 tests were performed on six Þeld tanks for the U.S. Environmental Protection Agency (EPA) (EPA) [13] that stored isopropanol, ethanol, glacial acetic acid, formaldehyde, ethylbenzene, and cyclohexane. In 1984 and 1985, ten tests were performed on one test tank for API [14] that stored Fuel Oil No. 2. The test methods utilized to perform these 69 tests were similar for each of the three test programs. This test method involved collecting and measuring the volume of air-vapor mixture that was emitted from the Þxed-roof tank during its daily breathing cycle. In addition, the data included stock property data, tank construction data, meteorological data,


` , , ` , ` , , ` , , ` ` ` ` , , , ` ` ` , ` ` , , ` ` ` ` , ` ` , , , ` , , ` ` -


and tank operating data. Each test was of one-day duration, covering a single breathing cycle. Although the API tests [14] were performed on a single 20foot diameter test tank, the amount of information collected were extensive. The vertical temperature distribution inside the tank, extending from below the liquid level upward through the vapor space to the tank roof, was continuously monitored during each test by a series of temperature sensors uniformly positioned on a vertical staff inside the test tank. These temperature measurements included the liquid bulk temperature, liquid surface temperature, vapor space temperature, and metal temperatures on the tank roof and shell. This temperature data provided valuable insight into the convective mixing which occurs in the tank vapor space during the daily heating cycle. To study the thermal response of a Þxed-roof tank, a computer program model was developed [15] that simulated the daily heating cycle. A series of differential equations were solved by step-wise integration over the course of the daily heating cycle to evaluate the thermal response of each of the tank elements including the tank shell, roof, liquid surface, liquid bulk, and vapor space. The computer program was used to develop a computer database that included the predicted breathing loss and tank thermal response for a total of 561 sets of conditions that covered a wide range of tank construction, stock properties, and meteorological conditions. When the thermal response and breathing loss predicted by the API computer model were compared against the data collected in the API tests [14], excellent agreement was found [16]. Using the API computer database, several proposed loss equations were evaluated [17]. Based upon a comparison with the API computer database, a standing storage loss equation was selected. This loss equation is not a correlation of test data, as was the breathing loss equation in the Þrst edition of API Bulletin 2518 [11], but rather is an equation resulting from a theoretical model of the breathing loss process. Section G of the Documentation File for API Manual of Petroleum Measurement Standards, Chapter 19.1, contains a sensitivity analysis of the standing storage loss equation. This sensitivity analysis examined the effect on breathing loss of each important variable as it was independently varied over a range of conditions that included a base-case condition. Section H of the Documentation File for API Manual of Petroleum Measurement Standards, Chapter 19.1, contains a comparison of the standing storage loss equation with the WOGA [12], EPA [13], and API [14] test data. This comparison includes a comparison of the calculated vapor space temperature range, calculated vented gas volume outßow, and calculated daily standing storage loss with that measured in the tests. The API tests provided an extensive and accurate set of test data for comparison with the API standing storage loss equation. The average percent difference between the calculated and measured standing storage loss was 14.3 percent for

the API test data. The EPA and WOGA test data also conÞrmed the suitability of the standing storage loss equation.

19.1 19.1.4 .4.2 .2 LOSS LOSS MEC MECHA HANI NISM SMS S 19.1 19.1.4 .4.2 .2.1 .1 Gene Genera rall Every liquid stock has a Þnite vapor pressure, dependent upon the surface temperature and composition of the liquid, that produces a tendency for the liquid to evaporate. Through evaporation, all liquids tend to establish an equilibrium concentration of vapors above the liquid surface, Under completely static conditions, an equilibrium vapor concentration would be established, after which no further evaporation would occur. However, Þxed-roof tanks are exposed to dynamic conditions that disturb this equilibrium, leading to additional evaporation. These dynamic conditions are responsible for continued evaporation, resulting in stock loss and atmospheric emissions. Evaporation is the natural process in which a liquid is converted to a vapor. Evaporation loss occurs when the evaporated vapor escapes to the atmosphere.

19.1.4 19. 1.4.2. .2.2 2

Evap Evapor orat ative ive Loss Loss

The total evaporative loss from a Þxed-roof tank is the sum of the standing storage loss and the working loss. Evaporative loss from Þxed-roof tanks may be divided into two categories-standing storage loss and working loss.

19.1.4 19. 1.4.2. .2.2.1 2.1 Stan Standin ding g Stora Storage ge Loss Loss Standing storage loss is the evaporative loss of stock vapor resulting from the thermal expansion and contraction of the tank air-vapor mixture resulting from the daily heating cycle. This loss is also referred to as the breathing loss and occurs without any change in liquid level in the tank.

19.1 19.1.4 .4.2 .2.2 .2.2 .2 Worki orking ng Loss Loss Working loss is the evaporative loss of stock vapor resulting from a change in liquid level in the tank, and includes both Þlling loss and emptying loss.

19.1 19.1.4 .4.2 .2.2 .2.2 .2.1 .1 Fill Fillin ing g Loss Loss Filling loss occurs during an increase in liquid level in the tank, when the air-vapor mixture in the tank vapor space is compressed and causes the pressure in the tank to exceed the PV vent pressure setting, expelling vapors from the tank.

19.1.4 19. 1.4.2. .2.2.2 2.2.2 .2 Empty Emptying ing Loss Loss Loss of stock vapors from the tank does not occur during emptying, because the direction of ßow through the vents is from outside to inside. The fresh air that is drawn into the tank induces additional evaporation of stock vapors. These

--``,,`,,,``,````,,``,```,,,``-`-`,,`,,`,`,,`---


45


46


vapors are accounted for in the saturation levels assumed in the working loss turnover factor, K N , and the standing storage loss saturation factor, K S . There is not, however, a separate contribution to stock vapor loss that takes place during emptying of the tank.

19.1.4.2 19.1.4.2.3 .3 Standin Standing g Stor Storage age Loss Loss Mecha Mechanism nisms s Several mechanisms are involved in evaporative loss during standing storage. The primary driving force for standing storage loss from a Þxed-roof tank is the daily heating cycle, which causes the tank vapor space temperature to increase during daytime hours and decrease during nighttime hours. This heating causes the air-vapor mixture in the tank vapor space to expand and increase in pressure up to the PV vent pressure setting, at which time vapor is vented from the tank vapor space, resulting in evaporative loss. Following the maximum vapor space temperature, which normally occurs in the early afternoon hours, cooling causes the air-vapor mixture in the tank vapor space to shrink and decrease in pressure. When the pressure falls below the PV vent vacuum setting, air is drawn into the tank vapor space which then becomes only partially saturated with stock vapor. During daytime hours, the tank is exposed to ambient heating by both solar insolation and convective heat exchange with the ambient air. The tank roof is exposed to direct and diffuse solar insolation, as well as to convective heat exchange with the ambient air. The sunny-side of the tank shell is exposed to direct, diffuse, and ground-reßected solar insolation, as well as convective heat exchange with the ambient air. The shady-side of the tank shell is exposed to diffuse and ground-reßected solar insolation, as well as convective heat exchange with the ambient air. During the nighttime hours, the tank roof and shell exchange heat by convective heat transfer with the ambient air, there being no solar insolation. This daily heating cycle causes the tank roof and shell to vary in temperature and exchange heat with the air-vapor mixture in the tank vapor space. During the daily heating cycle, the air-vapor mixture in the tank vapor space exchanges heat with the tank roof interior surface, tank shell interior surface and the stock liquid surface. This heat transfer causes convective motion of the airvapor mixture in the tank vapor space. Also during the daytime when the tank vapor space is heated, some heat is transferred to the liquid surface causing it to increase in temperature, resulting in a higher stock vapor pressure at the liquid surface. Evaporation occurs at the liquid surface as the stock tries to establish equilibrium conditions with the air-vapor mixture in the tank vapor space. Stock vapor evaporated from the liquid surface mixes with the air-vapor mixture and is convected upward toward the vent area by the convection currents that are induced during the daily heating cycle. Also, diffusion of

stock vapor occurs from the liquid surface to the tank vapor space. As the liquid surface temperature increases during the daily heating cycle, additional stock evaporates in trying to establish saturated conditions above the liquid surface. At the top of the tank vapor space, stock vapor mixes with the air which was drawn into the tank vapor space through the PV vent during the prior daily heating cycle. The combined effects of convection and diffusion affect the degree of saturation that occurs at the top of the tank vapor space. The combined effect of the above loss mechanisms results in movement of stock vapor from the liquid surface to the area below the PV vent, and eventually through the PV vent as the pressure exceeds the PV vent pressure setting. The degree of saturation in the vented vapor depends upon the mass transfer rate of stock vapor from the liquid surface to the top of the tank vapor space by convection convection and diffusion. These mechanisms typically result in vapor stratiÞcation, with the vapor concentration being lowest at the top of the tank vapor space and approaching saturation at the liquid surface.

19.1. 19.1.4.2 4.2.4 .4 Working orking Loss Loss Mechan Mechanism isms s Working loss is the combined effect of both Þlling loss and emptying loss.

19.1. 19.1.4.2 4.2.4. .4.1 1

Fillin Filling g Loss Mech Mechani anism sms s

During tank Þlling, as the stock liquid level increases, the air-vapor mixture in the tank vapor space is compressed until its pressure reaches the PV vent pressure setting. At this condition, the PV vent opens and air-vapor mixture is expelled from the tank vapor space to maintain the vapor space pressure near the pressure relief setting. At this condition, a volume of liquid entering the tank displaces an essentially equal volume of air-vapor mixture from the tank vapor space. As the tank Þlling process proceeds, the degree of saturation in the vented vapor approaches saturation conditions. The degree of saturation in the vented vapor depends upon the time interval between the tank Þlling process and the prior tank emptying process, during which period of time the stock tried to establish equilibrium conditions in the tank vapor space. The method of estimating working loss in earlier editions of 19.1 assumed that the tank behaves as if freely vented during the tank Þlling process. In other words, the method assumed that the volume of air and vapor displaced from the tank is equal to the volume of liquid brought into the tank. This assumption is reasonable for very low breather vent settings (such as the typical level of one-half ounce per square inch). As the breather vent settings increase, however, the freely-vented assumption may become conservative (i.e., result in an overestimate of working loss). When the breather vent pressure setting is sufÞciently high, signiÞcant compres-

--``,,`,,,``,````,,``,```,,,``-`-`,,`,,`,`,,`---




sion of the vapor space may occur before the vent opens. Vapors will begin to condense if compression of the vapor space continues after it has achieved saturated conditions, thereby reducing the volume of vapors released to the atmosphere. The vent setting correction factor, K B, has been added to the calculation of working loss in order to account for the condensation that may occur with higher vent settings.

19.1. 19.1.4.2 4.2.4. .4.2 2

Table 10—Annual 10—Annual Stock Turnove Turnoverr Rate (N ) for 123 Test Tanks Tanks ( Turnovers per Year) N (T

Empt Emptyin ying g Loss Loss Mechani Mechanism sms s

During tank emptying, as the stock liquid level decreases, the pressure of the air-vapor mixture in the tank vapor space decreases. When the pressure reaches the PV vent vacuum setting, air enters the tank vapor space through the PV vent. During a rapid emptying process, the volume of stock removed from the tank is approximately equal to the volume of air entering the tank vapor space. The stock tries to establish equilibrium conditions with the entering air by evaporation from the liquid surface. Stock evaporated from the liquid surface moves upward by convection and diffusion and mixes with the air which has entered the tank vapor space. The rate at which the stock vapor tends to saturate the entering air during tank emptying may reduce to some extent the volume of entering air. As discussed in 19. 1.4.2.3, these mechanisms tend to result in stratiÞcation of vapors in the tank vapor space. There is no loss of stock vapors from the tank during the emptying process, and subsequent loss of stock vapors are accounted for in the standing storage and Þlling loss mechanisms.

19.1. 19.1.4.3 4.3 DATABA DATABASE SE FOR FOR LOSS LOSS ANAL ANALYSI YSIS S 19.1. 19.1.4.3 4.3.1 .1 Stand Standing ing Stora Storage ge Loss Loss Data Data The combined set of 69 tests included 10 from the API tests [14], 15 from the EPA EPA tests [13] and 44 from the WOGA tests [12]. The API tests [14] were performed on a single 20-foot diameter test tank that stored Fuel Oil No. 2. The stock true vapor pressure ranged from 0.0054 to 0.014 pounds per square inch absolute, with a vapor molecular weight of 110 pounds per pound-mole. The tank vapor space outage was 8.85 feet during the entire test series. Although the API test data was limited to a single tank with a constant liquid level, the extensive amount of tank temperature data and meteorological data permitted a rigorous comparison and validation of the API computer model. The 15 EPA tests [13] were performed on six tanks, each containing a separate single component petrochemical that included isopropanol, ethanol, glacial acetic acid, ethylbenzene, and cyclohexane. The tanks ranged in diameter from 54 to 120 feet, with the vapor space outage varying from 11.4 to

Number of Tests

<10

117

10

2

20

1

30

3

27.1 feet. A single temperature probe was used to measure the tank vapor space temperature during the daily heating cycle. Although the amount of tank vapor space temperature data in the EPA tests was not as extensive as it was in the API tests, it provided a valuable check on the vapor space temperature predicted, by the API computer model and the standing storage loss equations. Since the stocks used in each tank in the EPA tests were single components petrochemicals, it was possible to accurately calculate the degree of saturation in the vented vapor during the daily heating cycle. This data provided a valuable basis for developing the vented vapor saturation factor, K s. The stock vapor pressure at the daily average liquid surface temperature in the EPA tests varied from 0.23 to 1.95 pounds per square inch absolute. The 44 WOGA tests [12] were performed on 21 tanks that contained crude oils, distillates, and fuel oils. These tanks ranged in diameter from 50 to 175 feet, with vapor space outages that ranged from 1.8 to 40.1 feet. The stock true vapor pressure at the daily average liquid surface temperature varied from 0.11 to 4.5 1 pounds per square inch absolute. Out of the 44 WOGA tests, 12 were found suitable for use in developing the vented vapor saturation factor, K s, and eight had sufÞcient detailed information to provide a comprehensive comparison with the standing storage loss equations. In the WOGA tests, the tank vapor space temperature was not measured, so it was not possible to compare the measured and predicted vapor space temperature range.

19.1.4 19. 1.4.3. .3.2 2

Workin orking g Los Loss s Dat Data a

From a survey of petroleum companies and petroleum tank builders, working loss data on 123 tanks were compiled. The stock turnover rate, N , for the 123 tests is summarized in Table 10. Data were collected on numerous items in each test in order to evaluate their effect on the working loss. Variables selected for potential correlation included: measured working loss, stock true vapor pressure (as determined from the stock Reid vapor pressure and the stock liquid bulk temperature), and the turnover rate.

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47


48


19.1.4 19. 1.4.4 .4 DEVEL DEVELOPM OPMENT ENT OF STAN STANDIN DING G STORAGE LOSS EQUATION

tion derived from the ideal gas law and from the pressure, temperature, and volume conditions that exist in the vapor space of a Þxed-roof tank containing a volatile liquid stock during the daily heating cycle.

19.1 19.1.4 .4.4 .4.1 .1 Gene Genera rall The standing storage loss equation was developed from a physical model of the breathing loss process. This equation was derived from the ideal gas law and from the pressure, temperature, and volume conditions that exist in the vapor space of a Þxed-roof tank containing a volatile liquid stock during the daily heating cycle. This derivation closely follows that in Appendix I of API Bulletin 2513 [18]. Section A of the Documentation File contains the derivation of the standing storage loss equation. The standing storage loss equation requires an estimation of the vapor space temperature range, ∆T V . A comprehensive heat transfer model of the daily heating cycle provided an analytical equation was validated by the test data. Section C of the Documentation Þle contains the derivation of the vapor space temperature range equation. It was necessary to incorporate a vented vapor saturation factor, K S , to account for the nonsaturation conditions which are present in the vented air-vapor mixture. Again, a physical model was used to develop an analytical equation for the vented vapor saturation factor. Some of the parameters in the analytical equation, however, could not be directly calculated from the available test data, and thus the analytical expression was used only as a guide in developing a correlation equation for the vented vapor saturation factor. Section B of the Documentation File contains the development of the vented vapor saturation factor, K S . Previous editions of 19.1 (i.e., the Þrst and second editions of API Publication 2518) presented the standing storage loss as shown in Equation 44, which is converted to the form of Equation 2 by substituting the right hand side of Equation 44 for the tank vapor space volume, V V . ` ` , , ` , , , ` ` , ` ` ` ` , , ` ` , ` ` ` , , , ` ` ` ` , , ` , , ` , ` , , ` -

LS = 365 V V W V K E K S

(44)

where V V is calculated from Equation 45. Tank Vapor Vapor Space Volume, V V

π

V V = ( -- ) D 2 H VO 4

19.1.4.4 19.1.4.4.2 .2

(45)

Vapor Space Space Expansi Expansion on Fact Factor or

The vapor space expansion factor, K E , is deÞned as the ratio of the volume of air-vapor mixture expelled during a daily breathing cycle to the volume of the tank vapor space. A theoretical equation was developed for the vapor space expansion factor based upon a physical model of the breathing process. This derivation closely followed that originally described in Appendix I of API Bulletin 2513 [18]. The equa-


At sufÞciently high vent settings, the breather vent pressure setting range may become large enough to result in a negative calculated value of K E . This indicates that the vent settings are sufÞciently high so as to not open during the daily breathing cycle, and the standing storage loss should be taken as zero. The simpliÞed expressions of Equations 3a and 3b, for approximating the vapor space expansion factor for liquid stocks with true vapor pressure less than or equal to 0.1 psia, assume typical breather vent settings of plus and minus onehalf ounce per square inch (i.e., ±0.03 psig) and thus a breather vent pressure setting range, ∆P B, of 0.06 psig. At higher vent settings, this simpliÞcation becomes increasingly conservative (i.e., results in overestimating emissions). The absolute level of the standing storage loss for these low vapor pressure stocks, however, may be so small that further reÞnement of the estimate is not warranted. Section A of the Documentation File contains the development of the vapor space expansion factor, K E .

19.1.4.4 19.1.4.4.3 .3 Vente Vented d Vapo Vaporr Saturat Saturation ion Fact Factor or The vented vapor saturation factor, K S , is deÞned as the ratio of the daily average stock vapor concentration in the vented vapor to the daily average saturated stock vapor concentration. When K S = 1, the vented gas is completely saturated; when K S = 0, the vented gas contains no stock vapor. Using a theoretical model for the mass transfer process of stock vapor from the liquid surface to the PV vent during the daily breathing cycle, a theoretical equation was developed. This equation contains the pertinent parameters that affect the vented vapor saturation factor, K S . The equation indicates that K S tends toward 1 as the vapor space outage, H VO, tends toward 0. It also indicates that K S tends toward 0 as the stock vapor pressure at the daily average liquid surface temperature, PVA, tends toward atmospheric pressure, P A. The equation contains an overall mass transfer coefÞcient for the transfer of stock vapor from the liquid surface to the PV vent. InsufÞcient information was available to evaluate the overall mass transfer coefÞcient, and thus the theoretical equation provided only a guide to show the dependency of K S on PVA, H VO and other parameters. Although it may be possible to develop a more complete theoretical equation for the vented vapor saturation factor, K S , it was decided instead to develop a correlation based on actual test data. However, the simpliÞed theoretical equation was used as a guide in selecting the analytical form for the correlation equation and in selecting the parameters to include in the correlation.



The API test data [14], EPA test data [13], and WOGA test data [12] were used to develop the correlation for the vented vapor saturation factor, K S . The vented vapor saturation factor was calculated for all ten of the API tests [14]. The vented vapor saturation factor for the API test data was close to one, with an average value for the ten tests of 0.964. For the 15 EPA tests [13], 12 were found suitable for calculated a vented vapor saturation factor. Since the daily average liquid surface temperature, T LA, was not measured during EPA tests, Equation 22 in 19.1.2.2.2.5 was used to estimate the daily average liquid surface temperature. This temperature was used for determining the stock vapor pressure at the daily average liquid surface temperature, PVA. For the EPA tests, the vented vapor saturation factor varied from 0.18 to 0.93, depending upon the stock vapor pressure at the daily average liquid surface temperature, PVA, and vapor space outage, H VO. For the 44 WOGA tests [12], 21 were found suitable for calculating a vented vapor saturation factor. Again, since the daily average liquid surface temperature, T LA, was not measured during the WOGA tests, Equation 22 in 19.1.2.2.2.5 was used to estimate the daily average liquid surface temperature. For the WOGA tests, the vented vapor saturation factor varied from 0.21 to 0.96, depending upon the stock vapor pressure at the daily average liquid surface temperature, PVA, and the vapor space outage, H VO. A total of 34 data points were selected to develop the vented vapor saturation factor correlation from the combined set of API, EPA, and WOGA test data. The resulting correlation was in agreement with the theoretical analysis in that it showed the same dependency of K S on PVA and H VO. Section B of the Documentation File contains both the development of the theoretical equation and the correlation for the vented vapor saturation, K S .

19.1.4.4 19.1.4.4.4 .4

Vapor Space Space Temperat emperature ure Range Range

The daily vapor space temperature range, ∆T V , is deÞned as the difference between the daily maximum vapor space temperature, T VX , and the daily minimum vapor space temperature, T VN . A heat transfer model was developed that described the heat transfer processes which occurred during the daily heating cycle. The model was based upon the following assumptions: a. The gas space is fully fully mixed mixed (i.e., it is at a uniform uniform tempertemperature at any given time during the daily heating cycle).

49

sun. Each tank wall element may be characterized by a single temperature, which varies during the daily heating cycle. d. The effects effects of rain and snow snow precipitation precipitation are not included included in the model. e. The heat capacity capacity terms terms in the energy energy balance balance equations equations can be neglected in comparison to the other heat transfer terms. Using these assumptions, heat balance differential equations were developed for each of the tank wall elements and the gas space. These ordinary differential equations were essentially the same as those used in the API computer model [15], where they were there solved by step-wise numerical integration. Assumption e allowed the differential equations to be reduced to a set of four simultaneous algebraic equations, which could be solved for the temperature of the gas space. The wall elements were assumed to exchange heat on both their inside and outside surfaces. The inside of each element was assumed to exchange heat with the vapor space gas by natural convection heat transfer. The outside of each element was assumed to exchange heat with the ambient air by convection and receive solar insolation. Certain typical solar insolation parameters were used (see Section D of the documentation File for the development of the solar insolation parameters) to simplify the vapor space temperature range equation. A sensitivity analysis indicated the vapor space temperature range depended little upon the ratio of the outside to inside convection heat transfer coefÞcients, and an average value was selected for these heat transfer coefÞcients. The resulting equation was further simpliÞed to the case where the ratio of the tank vapor space outage, H VO, to tank diameter, D, is equal to 1.0. The simpliÞed heat transfer model was compared [17] with the 561 sets of data in the API computer database [19] and found to result in an average difference of about 4 percent. Section C of the Documentation File contains the development of the vapor space temperature range, ∆T V . Section H of the Documentation File contains a comparison of the measured and calculated vapor space temperature range for the API, EPA, and WOGA test data.

19.1.4 19. 1.4.4. .4.5 5

Surf Surfac ace e Solar Solar Absorp Absorpta tance nce

The solar absorptance, α, is deÞned as the fraction of the solar insolation absorbed by a surface.

b. The liquid remains remains at a constant constant temperature temperature during during the daily heating cycle.

The exterior surface of Þxed-roof tanks are normally coated with a paint to reduce corrosion and reßect solar insolation. A wide range of paint colors have been used, sometimes with a different color on the tank roof than on the tank shell.

c. The tank wall wall in the gas space space can be treated treated as three sepaseparate elements: (1) the roof; (2) the half of the tank shell facing away from the sun; and (3) the half of the tank shell facing the

The absorptance of tank surfaces depends upon the tank color, surface type, and surface condition. Newly painted surfaces, or surfaces in a good condition, will have a lower solar



` , , ` , ` , , ` , , ` ` ` ` , , , ` ` ` , ` ` , , ` ` ` ` , ` ` , , , ` , , ` ` -

50


absorptance than weathered painted surfaces or surfaces in poor condition. At the time that the Þrst edition [11] of API Bulletin 2518 was published, the importance of surface absorptance on breathing loss was recognized. A surface with a low absorptance, such as white paint, was known to affect the breathing loss in two signiÞcant ways: a. It reduces reduces the transfer transfer of heat heat to and from from the tank tank vapor space and therefore reduces the volume of breathing loss. b. It reduces reduces the transfer transfer of heat to the the liquid bulk bulk and theretherefore reduces the breathing loss by lowering the stock vapor pressure. During the development of the Þrst edition [11] of API Bulletin 2518, extensive work was directed at gathering solar absorptance data on paints. Discussions were held and correspondence was exchanged with paint chemists and the staff of one large paint manufacturer. As a result of this work, a set of point factors, listed in Table 2 in the Þrst edition [11] of API Bulletin 2518, was developed. These paint factors are not suitable for use in conjunction with the current standing storage loss equation, and had to be converted to values of solar absorptance. Figure IV-3 IV-3 in the Þrst edition [11] of API Bulletin 2518 provided a relationship between the paint factor and solar absorptance. This Þgure was used to convert the paint factors into the solar absorptance values that appear in Table Table 5. Section C of the Documentation File contains the development of Equation 22, which is used to determine the tank surface solar absorptance, α, when the tank roof and shell are painted different colors. Section E of the Documentation File contains the development of the solar absorptance, α, values that are listed in Table 5.

19.1.4.4 19.1.4.4.6 .6 Liquid Liquid Surf Surface ace Temperat emperature ure The standing storage breathing loss equations require determining the stock vapor pressure at the daily maximum liquid surface temperature, T LX ; the daily average liquid surface temperature, T ; and the daily minimum surface tem LA perature, T LN . A theoretical equation was developed for estimating these liquid surface temperatures that is based upon a heat transfer analysis of the liquid surface during the daily heating cycle. The resulting equations require input of the liquid bulk temperature, T B. The liquid bulk temperature, T B, is the daily average temperature of the liquid stock in the storage tank. This information is usually available from tank gaging records or other tank operating records. If the liquid bulk temperature is not available, it may be estimated from the daily average ambient temperature, T AA, and the tank paint solar absorptance, α, by ` ` , , ` , , , ` ` , ` ` ` ` , , ` ` , ` ` ` , , , ` ` ` ` , , ` , , ` , ` , , ` -


the relationship described in Figure IV-2 in the Þrst edition [11] of API Bulletin 2518. Equation 21 in 19.1.2.2.2.4 is a linear Þt of the data presented in Figure IV-2 from the Þrst edition of API Bulletin 2518 [11], with the assumption that the liquid bulk temperature in a white tank is the same as the average ambient temperature, T AA. Section F of the Documentation File contains the development of the liquid surface temperature equations.

19.1. 19.1.4.5 4.5 DEVEL DEVELOPM OPMENT ENT OF WORKING ORKING LOSS LOSS EQUATION 19.1 19.1.4 .4.5 .5.1 .1 Gene Genera rall The working loss equation which appears in this publication is essentially the same as that which appeared in the Þrst edition [11] of API Bulletin 2518. The equation which appeared in the Þrst edition of API Bulletin 2518 was converted from working loss units of barrels per year into Equation 7 in 19.1.2.1.3 which expresses working loss units in pounds per year. It should also be noted that the formula was originally given in Appendix II of API Bulletin 2513 [18]. Of the test data assembled on 123 working tanks, only six tanks exceeded ten turnovers per year. The remaining 117 tanks had less than 10 turnovers per year. Because so much of the test data available had a very low turnover rate, the data were analyzed using the equation given in Appendix II of API Bulletin 2513 [18], which incorporates the turnover factor, K N , as a multiplier. When K N = 1, the equation represents the loss resulting from the displacement of a volume of saturated air-vapor mixture by an equal volume of liquid pumped into the tank. Previous editions of 19.1 (i.e., the Þrst and second editions of API Publication 2518) presented the working loss as shown in Equation 46. This is achieved by substituting the tank maximum liquid volume, V LX , for the corresponding terms in Equation 7, and then substituting the stock annual net throughput, Q, for N and and V LX . Expressing the stock annual net throughput in barrels per year requires that it be multiplied by the conversion factor, 5.614 cubic feet per barrel. Substituting for the stock vapor density, W V , as shown in Equation 6, and selecting 63¡F (523¡R) as a typical value for the liquid surface temperature, T LA, allows W V to be expressed as (0.0001781 M V PVA). Combining this coefÞcient with the throughput conversion factor of 5.614 gives the coefÞcient of 0.0010 used in previous editions. The working loss calculation shown in Equation 46 does not contain a vent setting correction factor, K B, because previous editions of 19.1 conservatively ignored any condensation of vapors that may occur prior to the opening of the pressure relief vent. LW = 0.0010 M V PVA Q K N K P


(46)


where Q = stock annual net throughp throughput ut (associa (associated ted with with increasing the stock liquid level in the tank) barrels per year,

= ( N N V LX ) / 5.614 where the constant 5.614 has units of cubic feet per barrel, V maximum liquid liquid volume volume (cubic feet), LX = tank maximum 2 = H LX (π/4) D .

The constant, 0.0010, in Equation 46 has units of pound moles per (pounds per square inch absolute) barrel. Section I of the Documentation File contains a development of the working loss equation.

19.1. 19.1.4.5 4.5.2 .2 Turno urnove verr Fac Factor tor The turnover factor, K N , is deÞned as the fraction of saturation in the vented vapor during working loss. When K N = 1, the vented vapor is saturated with stock vapor; when K N = 0, the vented vapor contains no stock vapor. For stock turnover rates, N , up to 30 turnovers per year, the available test data substantiated a value of K N = 1. No test data was available for turnover rates greater than 30 turnovers per year. Based upon a suggested relationship between the working K N , and the stock turnover rate, N , which was published in the API Proceedings, V.32, V.32, Part I, 1952, 1952 , pp. 212Ð281 [20]. Equation 39 in 19.1.2.2.3.2 was developed for high turn` ` , , ` , , , ` ` , ` ` ` ` , , ` ` , ` ` ` , , , ` ` ` ` , , ` , , ` , ` , , ` -


51

over rates (exceeding 36 turnovers per year). This equation results in a value of K N = 0.74 at one turnover per week and K N = 0.25 at one turnover per day. Section J of the Documentation File contains the development of the turnover factor, K N .

19.1.4 19. 1.4.5. .5.3 3

Produ Product ct Fact Factor or

The working loss product factor, K P, accounts for the effect of different types of liquid stocks on evaporative loss during tank working. The use of this product factor applies only to working loss and should not be used when estimating standing storage loss. The product factor, K P, was included in the working loss equation to account for the effects of different types of liquid stocks on evaporative loss. These effects (such as weathering) are in addition to those accounted for by considering differences in stock true vapor pressure and vapor molecular weight. In the Þrst edition [11] of API Bulletin 2518, a product factor, K P, of 0.75 was selected for crude oil stocks. The available test data on crude oil working loss were found to be scattered and not sufÞciently accurate to permit a formal correlation. However, a review of the scattered data, as well as other considerations, supported a product factor of 0.75 for crude oil. Section K of the Documentation File presents additional information on the development of the product factor, K P.


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APPENDIX A—DOCUMENTATION RECORDS The documentation records are maintained at American Petroleum Institute, Measurement Coordination Department, 1220 L Street, Northwest, Washington, D.C. 20005. The records are available for inspection at the above address. Copies of some of the sections may be obtained from API on request for a copying fee.

Table A-1—Contents A-1—Contents of Documentatio Documentation n Records Section

Description Introduction Standing Storage Loss

A

Devel Developm opment ent of Vapor apor Space Space Expans Expansion ion Factor Factor,, K E

B

Devel Developm opment ent of of Vent Vented ed Vapor apor Satura Saturatio tion n Facto Factor, r, K S

C

Devel Developm opment ent of Vapor apor Space Space Tempera emperatur turee Range Range,,

D

Deve Develo lopm pmen entt of Sol Solar ar Iso Isola lati tion on Par Param amet eters ers

E

Deve Develo lopm pmen entt of Sur Surfa face ce Sol Solar ar Abso Absorp rpta tanc nce, e, α

F

Devel Developm opment ent of Liqu Liquid id Surfac Surfacee Temp Tempera eratur turee Equat Equation ionss

G

Sensit Sensitiv ivity ity Analys Analysis is of of Standi Standing ng Stor Storage age Loss Loss Equat Equation ion

H

Compar Compariso ison n of of Stan Standin ding g Stor Storage age Loss Loss Equa Equatio tion n with with Test Data

∆T V

Working Loss I

Deve Develo lopm pmen entt of Worki orking ng Loss Loss Equa Equati tion on

J

Deve Develo lopm pmen entt of of Tur Turno nov ver Fac Facto torr, K N

K

Deve Develo lopm pmen entt of Pro Produ duct ct Fac Facto torr, K P

L

Compar Compariso ison n of Working orking Loss Loss Equat Equation ion with with Test Test Data Data

53 --``,,`,,,``,````,,``,```,,,``-`-`,,`,,`,`,,`---



` ` , , ` , , , ` ` , ` ` ` ` , , ` ` , ` ` ` , , , ` ` ` ` , , ` , , ` , ` , , ` -



APPENDIX B—METRIC UNITS B.1 General To convert the inch pound units employed in the text to equivalent SI units of the International System of Units, the guidelines of the API MPMS, Chapter 15, shall be followed. The unit of length is either the kilometer, designated km, or the meter, designated m. The unit of mass is the kilogram, designated kg. The unit of volume is the cubic meter, designated m 3. The unit of time is the year, designated yr. The unit of temperature is the degree Celsius, designated ¡C, or the kelvin, designated K. The unit of heat energy is the joule, designated J.

B.2 Pressure The unit of pressure is the kilopascal, designated kPa.

55 --``,,`,,,``,````,,``,```,,,``-`-`,,`,,`,`,,`---



--``,,`,,,``,````,,``,```,,,``-`-`,,`,,`,`,,`---



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TR 2567, Evaporation Loss from Storage Tank Floating-roof Landings

TR 2568, Evaporative Loss from the Cleaning of Storage Tanks

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