Calculational Methods for Analysis of Postulated UFe...NUREG/CR-4360 Volume 2 ORNL/ENG/TM-31jV2...
Transcript of Calculational Methods for Analysis of Postulated UFe...NUREG/CR-4360 Volume 2 ORNL/ENG/TM-31jV2...
MARTIN MARIETT'A
OPERATED BYMARTIN MARlmA ENERGY SYSTEMS, INC.FOR THE UNITED STATESDEPARTMENT OF ENERGY
NUREG/CR-4360Volume 2
ORNL/ENG/TM-31/V2
Calculational Methods for Analysisof Postulated UFe Releases
W. R. Williams
Prepared for theU.S. Nuclear Regulatory Commission
Office of Nuclear Regulatory ResearchDivision of Risk Analysis
Transportation and Materials Risk Branchunder Interagency Agreement DOE 40-550-75
NOTICE
This report was prepared as an account of work sponsored by anagency of the United States Government. Neither the UnitedStates Government nor any agency thereof, or any of theiremployees, makes any warranty, expressed or implied, orassumes any legal liability or responsibility for any third party'suse, or the results of such use, of any information, apparatusproduct or process disclosed in this report, or represents that itsuse by such third party would not infringe privately ownedrights.
Available from
Superintendent of DocumentsU.S. Government Printing Office
Post Office Box 37082Washington. D.C. 20013-7982
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NRC FORM 335 1. REPORT NUMeER (Ass;gnedby DOC)
11181>U.S. NUCLEAR REGULATORY COMMISSION NUREG/CR-4360, Vol. 2
BIBLIOGRAPHIC DATA SHEET ORNL/ENG/TM-3l/V24. TITLE AND SUBTITLE (Add Volume No., If tJPprCJP"em) 2. (LellVe bl""k)
Calculational Methods for Analysis of PostulatedUF6 Releases 3. RECIPIENT'S ACCESSION NO.
7. AUTHOR(SI 5. DATE REPORT COMPLETED
MONTH I YEARW. R. Williams August 1984
9. PERFORMING ORGAN!ZATION NAME AND MAILING ADDRESS (Include ZiP Code) DATE REPORT ISSUED
Oak Ridge National Laboratory MONTH I YEAR
September 1985Post Office Box XOak Ridge, TN 37831 6 (Leave bllmk)
8. (Leave blank)
12. SPONSORING ORGANIZATION NAME AND MAILING ADDRESS (Include ZiP Code)10. PROJECT/TASK/WORK UNIT NO.
Division of Risk Analysis and OperationsOffice of Nuclear Regulatory Research 11 FIN NO.
U.S. Nuclear Regulatory CommissionWashington, DC 20555 B0495
13 TYPE OF REPORT IPE RIOD COVE RE D (lnc/uslve dates)
Topical
15. SUPPLEMENTARY NOTES 14. (Leave olank)
16. ABSTRACT (200 words or less)
Calculational methods and computer programs for the analysis of source terms forpostulated releases of UF6 are presented. Required thermophysical properties of UF6,HF, and H20 are described in detail. UF6 reacts with moisture in the ambientenvironment to form HF and H2O. The coexistence of HF and H20 significantly alterstheir pure component properties, and HF vapor polymerizes. A release rate model ofUF6 is presented that considers the transient conditions inside containment and theflashing, multiphase flow of UF6 along the release pathway. Transient compartmentmodels for simulating UF6 releases inside rooms ventilated by forced- and induced-draft systems are also described. The basic compartment model mass and energybalances are supported by simple heat transfer, ventilation system, and depositionmodels. A model that can simulate either a closed compartment or a steady-stateventilation system is also discussed. Listings of all main programs (including twoplotting routines) and subroutines are included. Example problems illustrate theanalysis of postulated releases using the described programs.
17. KEY WORDS AND DOCUMENT ANALYSIS 17a DESCRIPTORS
uranium hexafluoride (UF6) cylinder computer codesaccidents cold trap compartment modelsscenarios pigtail release rate modelsreleases fuel cycle physical and thermodynamic propertiesanalysis modeling
"
17l, IDENTIFIERS.OPEN·ENDED TERMS
18 AVAILABILITY STATEMENT 19 SECURITY CLASS ITh,s reporrJ 21 N~O/~Sunlimited unclassified
20. SE CU RI TY CLASS ITh,s page)22 =RI~.,p-, 9 _S·-unclassified
NRCFORM335 111811
NUREG/CR-4360Volume 2
ORNL/ENG/TM-31jV2Dist.Cat.RZ
Martin Marietta Energy Systems) Inc., EngineeringProcess Engineermg
Calculational Methods for Analysis ofPostulated UF6 Releases
W. R. Williams
Manuscript Completed:August 1984
Date of Issue: September 1985
Prepared for theU.S. Nuclear Regulatory Commission
Office of Nuclear Regulatory ResearchDivision of Risk Analysis
Transportation and Materials Risk Branch(T. Clark, Project Manager)
Washington, DC 20555under Interagency Agreement
DOE 40-550-75FIN B0495
Oak Ridge National LaboratoryP.O. Box X
Oak Ridge, Tennessee 37831operated by
MARTIN MARIETTA ENERGY SYSTEMS, INC.for the
U.S. DEPARTMENT OF ENERGYunder Contract No. DE-AC05-840R2l400
, ,II
CONTENTS
Volume 1
Acknowledgement. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. Vll
Executive Summary . IX
Abstract . XI
1. INTRODUCTION AND SUMMARY .
2. PHYSICAL AND THERMODYNAMIC PROPERTIES MODELS 3
2.1 Uranium Hexafluoride 3
2.Ll Vapor Pressure. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4
2.1.2 Equation of State and Vapor Compressibility
Factor. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 6
2.1.3 Density............................................................... 6
2.1.4 Viscosity.............................................................. 7
2.1.5 Thermal Conductivity . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 9
2.1.6 Heat Capacity . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 11
2.1.7 Enthalpy.............................................................. 13
2.1.8 Entropy............................................................... 14
2.1.9 Other Properties. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 16
2.Ll0 UF6 Reaction with H 20 . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 16
2.1.11 Flashing............................................................... 17
2.Ll2 Subroutines. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 19
2.2 HF-H20 System. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 20
2.2.1 Self-Association of HF Vapor. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 20
2.2.2 Partial Vapor Pressure of HF . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 23
2.2.3 Partial Vapor Pressure of H 20. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 25
2.2.4 Enthalpy of HF-H20 Vapor Mixtures. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 29
2.2.5 Enthalpy of HF-H20 Liquid Mixutes. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 31
2.2.6 HF-H20 Vapor-Liquid Equilibrium. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 31
2.2.7 Subroutines. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 34
2.3 Other Components .
2.4 Mixture Enthalpies .
. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 35
. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 35
3. RELEASE RATE MODELS .. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 37
37
. . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 37
3.1 Containment (Cylinder) Subroutines .
3.1.1 Internal Mass and Energy Balance .
III
3.1.2 Liquid-Vapor Interface Level and Phase
Composition of UF6 Leaving Containment 41
3.2 Flow Rate Subroutines 45
3.2.1 Flow Through a Ruptured Piping System . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 46
3.2.2 Flow Rates Through a Breach in Containment. . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 52
3.3 Main Program for Evaluating Release Rates from a
Cylinder . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 53
3.4 Cylinder Model Plotting Program . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 57
4. COMPARTMENT MODELS. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. . . . . . .. 59
4.1 Main Program Structure. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 62
4.1.1 Initial Statements 62
4.1.2 Input Data Requirements. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 67
4.1.3 Steady-State Conditions. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 69
4.1.4 Transient Analysis. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 71
4.1.5 Other Considerations. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 74
4.2 Ventilation System Subroutines. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 74
4.2.1 Steady-State Analysis. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 74
4.2.2 Transient Analysis. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 76
4.2.3 Stream Mixing. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 77
4.3 Source-Term Subroutine. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 78
4.4 Condensate Deposition Subroutine 79
4.5 Compartment Mass and Energy Balance Subroutines . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 79
4.5.1 Initial Conditions. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 81
4.5.2 Transient Behavior 83
4.6 Compartment Model Main Programs . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 86
4.6.1 Forced-Draft Compartment. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 86
4.6.2 Induced-Draft Compartment . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 89
4.6.3 Closed Compartment/Ventilation System. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 92
4.7 Compartment Model Plotting Program. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 93
5. EXAMPLE PROBLEMS . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 95
5.1 Release from a Cylinder. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 95
5.1.1 Release through a Breach in Containment. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 95
5.1.2 Release through a Ruptured Piping System 106
5.2 Release Inside a Compartment 112
5.3 Release into a Ventilation System 119
REFERENCES 123
iv
Volume 2
Appendix A. LISTINGS OF MAIN PROGRAMS ... . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1
A.1 FODRFT - A Forced-Draft Compartment Model. . . . . . . . . . . . . . . . . . . . . . . . .. . . . . . . . 4A.2 INDRFT - An Induced-Draft Compartment Model , . . . . . .. 19A.3 BATCH - A Closed Compartment/Ventilation System
Model 36A.4 CYLIND - A Cylinder Release Model . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 45A.5 COMPLT - A Plotting Program for FODRFT and
INDRFT Results. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. . . . . . .. 55A.6 CYLPLT - A Plotting Program for CYLIND Results . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 59
Appendix B. LISTINGS OF SUBROUTINES . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 67
B.1 BREACH.................................................................. 68B.2 COMPRT.................................................................. 75B.3 CPUF6.................................................................... 81B.4 DENTHL 82B.5 DENUF6.................................................................. 85B.6 DPFLOW.................................................................. 86B.7 EQTUF6 89B.8 FLASH.................................................................... 91B.9 HCOEFF.................................................................. 97B.10 HFPOLY . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. . . . . . .. 98B.ll HHFH20 100B.12 HUF6 " 103B.13 HUMID 104B.14 INTMEB 105B.15 LEVEL 109B.16 MIXFLW 114B.17 PHASE.. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 117B.18 PHFH20 122B.19 PIPSYS 125B.20 REMOVE 134B.21 RESIST 135B.22 ROOM 137B.23 SETRAY 138B.24 SSBLOW 141B.25 STERM 142B.26 SUF6. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 146B.27 THCUF6 147B.28 TRBLOW 148B.29 VISUF6 149B.30 VPRUF6 150B.31 ZUF6 152
v
Appendix C. EXAMPLE PROBLEM OUTPUT 153
Example 1 154
Case 1 " 154Case 2 156
Case 3 159Case 4 162
Example 2 163Case 1 " 163
Case 3 165Example 3 . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 166
Case 1 166Case 2 167
Case 3 168Example 4. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 169
Case 1 169Case 2 176
Case 3 183Case 4 190
Example 5 197
VI
Appendix ALISTINGS OF MAIN PROGRAMS
This appendix contains listings of the main programs described in Chaps. 3 and 4. These programs include the transient compartment model programs FODRFT (Appendix A.I) and INDRFT(Appendix A.2), the closed compartment/ventilation system model BATCH (Appendix A.3), a program for simulating releases from a cylinder through a breach in containment or a piping system,BYLIND (Appendix A.4), and the plotting programs COMPLT (Appendix A.S) and CYLPLT(Appendix A.6). COMPLT plots output from FODRFT and INDRFT, while CYLPLT plots output from CYLIND.
Table A.I lists the subroutines required for the execution of each main program, excluding theplotting programs. COMPLT and CYLPLT require the availability of DISSPLA version 9.0* onthe user's system. These subroutines are listed in Appendix B. Table A.2 identifies the input/outputdevice numbers used in each main program.
-For information on DISSPLA, contact Integrated Software Systems Corporation, 10505 Sorrento Valley Road, SanDiego, CA, 92121.
1
3
Table A.2. I/O device numbers
Output files
Program Input FilesTo othersprograms
For printing/plotting
FODRFT 40,22° 48b,49 41,42,43,44,45,46,47c
INDRFT 40,22° 48b ,40 41,42,43,44,45,46,47c
BATCH 5 6CYLIND 20 22,30,31 30COMPLT 48b ,49 dCYLPLT 30,31 d
°Input device number 22 is an optional input file toFODRFT and INDRFT.
bThe file written to device 48 by FODRFT or INDRFTfor use by COMPLT is unformatted.
CFODRFT and INDRFT output files provide conditionsin the compartment (41), inlet flow conditions (42), sourceterm conditions (43), outlet flow conditions (44), depositionrate information (45), condensate accumulation on the floor(46), and release summary (47).
dCompressed data files are generated via an initial call tothe subroutine COMPRS.
4
A.I FODRFT - A Forced-Draft Compartment Model
COMMON BLOCK VARIABLES
THE FOLLOWING VARIABLES ARE USED.
INLET STREAM NODE NUMBER
COMPONENT MOLECULAR WEIGHTS, LB/LB MOLE
NODE TEMPERATURE, DEG FNODE PRESSURE, PSIANODE HEAT TRANSFER SURFACE TEMPERATURE, DEG F
NODE VOLUME, FT**3RESISTANCE COEFFICIENT, --, OR RESISTANCE TERM,RESISTANCE TERM, PSI-SEC**2/LB-FT**3DEPOSITION AREA, FT**2DEPOSITION VELOCITY, FT/SEC
NODE ENTHALPY, BTU, OR ENTHALPY RATE, BTU/(DELT)HEAT TRANSFER RATE, BTU/SEC OR BTU/(DELT)COOLING RATE, BTU/HR (INPUT) OR BTU/SEC( INTERNAL)HEAT TRANSFER COEFFICIENT, BTU/SEC-FT**2-DEG FHEAT TRANSFER AREA, FT**2
( 9)
COMPARTMENTINLET AIR BLOWERSOURCE TERMFORCED DRAFT EXHAUSTCONDENSATE FALLOUTCOMPARTMENT FLOORAMBIENT
(30,4)
(30)(30)(30)
(30)(30)(30)
(30)(30)
(30,9) NODE MASS, LB, OR MASS FLOW RATE, LB/(DELT)RELATIVE HUMIDITY, % (AS INPUT) OR FRACTION( INTERNAL)
HTCOEF (30)HTAREA (30)
/MOU·JT/
IIN
WMOL
HQRATEQCOOL
MASSRH
VOLKRCOEF
DPAREA (30)DEPVEL
TCPCTSURF
1234567
/ENTHAL/
/COMPTP/
/VOLUME/
/ISTRMS/
/LBMASS/
C THIS PROGRAM MODELS A RELEASE OF UF6 OR HF INTO A COMPARTMENTC HAVING A FORCED DRAFT VENTILATION SYSTEM. NODE NUMBERS ANDC STREAM DEFINITIONS FOR THIS MODEL ARE AS FOLLOWS.CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCC
5
OTHER DIMENSIONED VARIABLES
UNDIMENSIONED VARIABLES
IOL~ (30,4) OUTLET STREAM NODE NUMBER
ICONTRL/
EQUI(jALENCED VARIABLES
VOLUMETRIC FLOW RATE, FT**3/MINFLOW AREA FOR PRESSURE-DROP-CONTROLLEDNODE, FT**2
MAXIMUM NUMBER OF NODES ALLOWED BY CODING OFSUBROUTINESMAXIMUM NUMBER OF INLET STREAMS AND OUTLETSTREAMS
START OF REVERSE FLOW (NOT USED)END OF REVERSE FLOW (NOT USED)
WE IGHT FRACTI ON OF HF MONOMER TO TOTAL HF VAPORWEIGHT FRACTI~~ OF HF TRIMER TO TOTAL HF VAPORWEIGHT FRACTION OF HF HEXAMER TO TOTAL HF VAPORMOLECULAR WEIGHT OF HF MONOMER, LB/LB MOLE
C~1PONENT MASS FLOW RATE, LB/SECINCREMENTAL SOURCE MASS, LBINCREMENTAL RELEASE TIME, SECTEMPERATURE OF INCREMENTAL SOURCE, DEG FPRESSURE OF INCREMENTAL SOURCE, PSIACOMPONENT IDENTIFIERTITLE ARRAYPLOT NUMBER ARRAY
VARIABLE TO SPECIFY TYPE OF RELEASE, SEE CARD 5TOTAL MASS OF RELEASE, LBVARIABLE TO SPECIFY ISENTROPIC OR ISENTHALPICRELEASE, SEE CARD 5
NATURAL LOG OF MINIMUM NUMBER ACCEPTED BY THECOMPUTERCUMULATIVE SIMULATION TIME, SECTIME INTERVAL USED FOR TRANSIENT SIMULATION, SECMAXIMUM SIMULATION TIME, SECFLAG TO CONTROL PRINTING OF OUTPUTTOTAL RELEASE TIME, SEC
ACFM (30)FLAREA (30)
( 9)(5)( 5)(5)( 5)( 9)
(10)(6,4)
INOUT
VOL
INODES
AMINLN
ITYPESOURCEISEN
C1C3C6WMBHF
RATEMSOURCTSOURCTEMPPRESNAMETITLEDWGNUM
TSTART (30)TSTOP (30)
TIMEDELTMAXTIMIFLAGTRELS
/POLYMRI
IMISCEL/
IRVFLOW/
CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCC
CCCCCCCCCCCCCCCCCCCCCC
6
FLAG IN ESTABLISHING INITIAL STEADY STATECONDITIONS ABOUT NODE 2
NUMBER OF INCREMENTAL RELEASES IN TOTAL RELEASE(MAXIMUM OF 5)MOLECULAR WEIGHT, LB/LB MOLEMOLECULAR WEIGHT OF URANIUM, LB/LB MOLETOTAL MASS OF SOURCE MATERIAL RELEASED, LBVAPOR PRESSURE OF SOURCE, PSIAPRINT INTERVAL, SECRATIO OF MOLES OF WATER VAPOR TO TOTAL MOLES OFMOIST AIRPRODUCT OF HEAT TRANSFER COEFICIENT AND AREA,BTU/SEC-DEG FCOUNTER TO CONTROL PRINTING OF OUTPUTCURRENT INCREMENT OF TOTAL RELEASESOURCE TERM INPUT INTERVAL, SECMASS FLOW RATE OF UF6 SOLIDS ONTO THE FLOOR,LB/(DELT)OUTPUT DEVICEENTHALPY PATE, BTU/SECCOMPARTMENT CONCENTRATION OF URANIUM, LB/FT**3CtJo1PARTMENT CONCENTRATI ON OF HF, LB/FT**3CUMULATIVE MASS OF UF6 RELEASED TO THEATMOSPHERE, LBCUMULATIVE MASS OF U02F2 RELEASED TO THEATMOSPHERE, LBCUMULATIVE MASS OF URANIUM RELEASED TO THEATMOSPHERE, LBCUMULATIVE MASS OF HF RELEASED TO THEATMOSPHERE, LBCUMULATIVE MASS OF HF THAT CAN BE FORMED FROMUF6 RELEASED TO THE ATMOSPHERE, LBCUMULATIVE MASS OF HF RELEASED TO OR FORMED INTHE ATMOSPHERE, LB
HFUF6
CHECK
HFTOT
HFREL
UTOT
UOFREL
UA
MWMWURANMRELSPTESTPRINTRATIO
IRELST
ICOUNTIRELSDELTATSOLIDS
IDEVHRATEDENUDENHFUF6REL
LOGICAL VARIABLES
CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCC THE FOLLOWING SUBROUTINES ARE CALLED BY FODRFT.CCCCCCCCCCCCCCC
COMPRTDENTHLDPFLOWHCOEFFHUMIDPHFH20REMOVERESISTROOMSETRAYSSBLOWSTERMVPRUF6
7
DENUF6EQTUF6FLASHHFPOLYHHFH20HUF6PHASESUF6ZUF6
C
C THE FOLLOWING SUBROUTINES ARE ALSO REQUIRED.CCC
CCCCCCCC***********************************************************************CC INITIAL STATEMENTSC ==================C
IMPLICIT REAL*8 (A-H,J-Z)C
LOGICAL CHECKC
DIMENSION FLAREA(30), ACFM(30), RATE(9), MSOURC(5), TSOURC(5),* TEMP(5), PRES(5)
DIMENSION NAME(9), TITLE(10), DWGNUM(6,4)C
C
C
C
COMMON ILBMASSI MASS(30,9), RHCOMMON ICOMPTPI TC(30), PC(30), TSURF(30)COMMON IMOLWT/ WMOL(9)COMMON IVOLUMEI VOL(30), KRCOEF(30), DPAREA(30), DEPVELCOMMON IENTHALI H(30), QRATE(30), QCOOL(30), HTCOEF(30),
* HTAREA(30)COMMON IISTRMSI IIN(30,4), IOUT(30,4)COMMON ICONTRLI AMINLN, TIME, DELT, MAXTIM, IFLAG, TRELSCOMMON IPOLYMRI Cl, C3, C6, WMBHFCOMMON IMISCELI ITYPE, SOURCE, ISENCOMMON IRVFLOWI TSTART(30), TSTOP(30)
EQUIVALENCE (VOL(l),ACFH(l),FLAREA(l»
DATA NAME 18HAIR V, 8HH20 L, 8HH20 V, 8HHF L,* 8HHF V, 8HUF6 S, 8HUF6 L, 8HUF6 V, 8HU02F2 S I
CALL SETRAY(INODES, INOUT)CC NODE ASSIGNMENTC ===============C
IIN(l,l) = 2IIN(1,2) = 3IIN(2,1) = 7IIN(4,1) = 1IIN(5,1) = 1IIN(6,1) = 5
C
8
IOUT(l,l) = 4IOUT(1,2) =5IOUT(4,1) = 7IOUT(S,l) =6
CC READ STATEMENTSC ===============CC ALL INPUT DATA EXCEPT THAT ON CARDS 1 AND 9 ARE READ IN FREE FORMAT.C ON CARDS 1 AND 9, COUNT CHARACTERS STARTING IN COLUMN 1.CCC ICI CARD 1. READ TITLE (MAXIMUM OF 80 CHARACTERS).C
READ (40,4000) TITLECCC ICI CARD 2. READ AMBIENT TEMPERATURE (F), PRESSURE (PSIA), AND RELATIVEC HUMIDITY (%).C
READ (40,*) TC(7), PC(7), RHC
IF (RH.GT.l.DO) RH = RH/l.D2CCC ICI CARD 3. READ COMPARTMENT TEMPERATURE (F), PRESSURE (PSIA), VOLUMEC (FT**3), AND FLOOR (DEPOSITION) AREA (FT**2).C
READ (40,*) TC(l), PC(l), VOL(l), DPAREA(l)CCC ICI CARD 4. READ INLET AIR BLOWER FLOW RATE (ACFM).C
READ (40,*) ACFM(2)CCC ICI CARD 5.CCCCCCCC
READ HEAT TRANSFER SURFACE AREA IN COMPARTMENT (FT**2),HEAT TRANSFER SURFACE TEMPERATURE (F), AND COOLING RATE(BTU/HR). A NEGATIVE COOLING RATE IMPLIES A HEATING RATE.WHILE THE VALUE OF THE SURFACE AREA IS NOT PARTICULARLYIMPORTANT BECAUSE THE PRODUCT OF THE SURFACE AREA AND THEHEAT TRANSFER COEFFICIENT TO BE CALCULATED WILL BECONSTANT, A SURFACE TEMPERATURE GREATER THAN THECOMPARTMENT TEMPERATURE MUST BE SPECIFIED.
READ (40,*) HTAREA(l), TSURF(l), QCOOL(l)C
QCOOL(l) = QCOOL(1)/3.6D3C
CC /C/ CARD 6.CCCCCCCCCCCCCCCCCCCC
9
READ SOURCE TYPE, NUMBER OF RELEASES, BASIS FOR FLASH, ANDMOLECULAR WEIGHT. SOURCE TYPE IS GIVEN BY THE FOLLOWING:
4 LIQUID HF5 VAPOR HF7 LIQUID UF6 (VAPOR SOURCE TERM GENERATED)
-7 LIQUID UF6 (VAPOR/SOLID SOURCE TERM GENERATED)8 VAPOR UF6
22 INPUT PROVIDED IN FOR22.DAT
IF SOURCE TYPE 22 IS SPECIFIED, SET NUMBER OF RELEASES TOZERO. NO MORE THAN FIVE RELEASES MAY BE SPECIFIED, WHICHARE TO R~~ CONSECUTIVELY. THE BASIS FOR THE FLASH IS GIVENBY THE FOLLOWING:
o ISENTROPIC1 ISENTHALPI C
THE DEFAULT MOLECULAR WEIGHT FOR UF6 IS 352.025; ENTER AVALUE LESS THAN 100 IF THAT VALUE IS ACCEPTABLE.
READ (40,*) ITYPE, IRELST, ISEN, MWC
IF (MW.LT.l00.DO) GO TO 10C
WMOL(9) = WMOL(9) - WMOL(6) +MWWMOL(6) =MWWMOL(7) =MWWMOL(8) =t1..J
C10 CONTINUE
CMWURAN = WMOL (6) - 113.99DO
CIF (ITYPE.EQ.22) GO TO 30
CCC /C/ CARD 7.CCCCCCCC
-- DO NOT USE "CARD 7" CARDS IF ITYPE = 22. --
READ FOR EACH INCREMENTAL RELEASE THE DURATIcr~ (SEC), MASS(LB), TEMPERATURE (DEG F), AND PRESSURE (PSIA). SPECIFY ASMANY SETS OF DATA AS THE NUMBER OF RELEASES (IRELST). IFTHE PRESSURE GIVEN IS LESS THAN OR EQUAL TO ZERO OR GREATERTHAt~ THE VAPOR PRESSURE, THE PRESSURE IS SET EQUAL TO THEVAPOR PRESSURE FOR THAT INCREMENT.
C
C
READ (40,*) (TSOURC(I), MSOURC(I), TEMP(I), PRES(I), I=l,IRELST)
TRELS = 0.00
MRELS = O.DO
10
CDO 20 I20=1,IRELST
CTRELS = TRELS + TSOURC(I20)
CMRELS = MRELS + MSOURC(I20)
C
C
C
C
IF (ITYPE.EQ.5) CALL PHFH20(TEMP(I20), 1.DO, O.DO, PTEST,* O.DO, O.DO)
IF (ITYPE.EQ.8) CALL VPRUF6(TEMP(I20), PTEST)
IF (PRES(I20).GT.PTEST .OR. PRES(I20).LE.0.DO)* PRES(I20) = PTEST
20 CONTINUE
30 CONTINUECCC /C/ CARD 8.CC
READ TIME INTERVAL FOR CALCULATIONS (SEC), DURATION OFSIMULATION (SEC), AND PRINT INTERVAL (SEC).
READ (40,*) DELT, MAXTIM, PRINTC
IFLAG = IDINT(PRINT/DELT+0.01DO)CCC /CI CARD 9.CCCCCCCCCCC
-- THESE CARDS ARE OPTIONAL. --
READ DRAWING NUMBERS FOR PLOTS (LIMITED TO 20 CHARACTERS-THE LAST CHARACTER MUST BE A DOLLAR SIGN ($».
1ST CARD 9 = CL~ULATIVE URANIUM RELEASED2ND CAR~ 9 = CUMULATIVE HF RELEASED3RD CARD 9 = URANIUM CONCENTRATION IN COMPARTMENT4TH CARD 9 = HF CONCENTRATION IN COMPARTMENT5TH CARD 9 = TEMPERATURE IN COMPARTMENT6TH CARD 9 = PRESSURE IN COMPARTMENT
DO 40 140=1,6C
C
C
C
READ (40,4010,END=50) (DW&~UM(I40,I), 1=1,4)WRITE (49,4010) (DWGNUM(I40,I), 1=1,4)
40 CONTINUE
50 CONTINUE
WRITE (49,4020)CC***********************************************************************C
11
C STEADY STATE CONDITIONSC =======================CC SET STEADY-STATE CONDITIONS FOR THE COMPARTMENT, EXHAUST, AND INLETC AIR NODES.C
CALL HUMID(7, RH, RATIO)C
VOL( 7) = 1. D9C
C
C
C
C
C
C
C
C
C
CALL ROOM(7, RATIO)
CALL ROOM(1, RATIO)
CALL SSBLOW(2, RATIO)
MASS(4,1) =MASS(2,1)MASS(4,3) =MASS(2,3)
TC(4) =TC(l)PC(4) = PC(1)
KRCOEF(4) = O.DO
CALL RESIST(4)
CALL DENTHL(TC(4), PC(4), 4, H(4»
CALL HCOEFF(1)
UA =HTCOEF(1) * HTAREA(1)C
C***********************************************************************CC TITLE BLOCKSC ============CC WRITE TITLE AND PROGRAM IDENTIFIER.C
DO 60 160=1,7C
IDEV = 40 + 160C
CWRITE (IDEV,4030) TITLE
60 Cl:M"INUECC WRITE NODE NAMES AND IMPORTANT CONSTANTS FOR EACH FILE.C
WRITE (41,4100) VOL(1), UA, TSURF(1), QCOOL(1)C
CWRITE (42,4200) ACFM(4), TC(7), PC(7)
IF (ITYPE.EQ.4) WRITE (43,4304)
C
C
c
c
c
C
c
c
c
C
c
12
IF (ITYPE.EQ.5) WRITE (43,4305)IF (IABS(ITYPE).EQ.7) WRITE (43,4307)IF (ITYPE.EQ.B) WRITE (43,430B)
IF (ITYPE.NE.22) WRITE (43,4310)
IF (ITYPE.EQ.4) WRITE (43,4320) (TSOURC(I), MSOURC(I),* TEMP(I), 1=1,5)
IF (ITYPE.EQ.5) WRITE (43,4330) (TSOURC(I), MSOURC(I),* TEMP(I), PRES(I), 1=1,5)
IF (IABS(ITYPE).EQ.7) WRITE (43,4340) (TSOURC(I), MSOURC(I),* TEMP(I), 1=1,3)
IF (IABS(ITYPE).EQ.7 .At~D. ISEN.EQ.O) WRITE (43,4341) TSOURC(4),* MSOURC(4), TEMP(4)
IF (IABS(ITYPE).EQ.7 .AND. ISEN.EQ.1) WRITE (43,4342) TSOURC(4),* MSOURC(4), TEMP(4)
IF (IABS(ITYPE).EQ.7) WRITE (43,4343) WMOL(6), TSOURC(5),* MSOURC(5), TEMP(5)
IF (ITYPE.EQ.B) WRITE (43,4350) (TSOURC(I), MSOURC(I),* TEMP(I), PRES(I), 1=1,3)
IF (ITYPE.EQ.B .AND. ISEN.EQ.O) WRITE (43,4351) TSOURC(4),* MSOURC(4), TEMP(4), PRES(4)
IF (ITYPE.EQ.B .AND. ISEN.EQ.1) WRITE (43,4352) TSOURC(4),* MSOURC(4), TEMP(4), PRES(4)
IF (ITYPE.EQ.B) WRITE (43,4353) WMOL(6), TSOURC(5), MSOURC(5),* TEMP(5), PRES(5)
CIF (ITYPE.NE.22) WRITE (43,4360) TRELS, MRELS
CIF (,I TYPE . EQ. 7) WRITE (43,4370)
CIF (ITYPE.EQ.22) WRITE (43,4380)
CWRITE (44,4400) KRCOEF(4)
CWRITE (45,4500) DEPVEL, DPAREA(1)
CWRITE (46,4600)
CWRITE (47,4700)
CC WRITE COLUMN HEADINGS.C
WRITE (41,4110) NAMEC
----------------------------------------
13
DO 70 170=2,4C
IDEV = 40 + 170C
WRITE (IDEV,4210) NAMEC
70 CONTINUEC
WRITE (45,4510) NAMEC
WRITE (46,4610) NAMEC
WRITE (47,4710)CC***********************************************************************CC TRANSIENT ANALYSISC ==================CC BEGIN TRANSIENT ANALYSIS.C
TIME = 0.00C
ICOUNT = IFLAGC
IRELS = 1C
TRELS = 0.00CCC ICI OPTIONAL SOURCE TERM INPUT: CARD 1. ENTER TIME INTERVAL FOR SOURCEC TERM INPUT (SEC).C
IF (ITYPE.EQ.22) READ (22,*) DELTATC
80 CONTINUECC EVALUATE SOURCE TERMCC
IF (TIME.LT.TRELS) GO TO 120C
IF (ITYPE.NE.22) GO TO 100CCC ICI OPTIONALCCCCCC
SOURCE TERM INPUT: CARD 2. ENTER INITIAL TIME FOR RELEASEINTERVAL (SEC)j MASS FLOW RATE (LB/SEC) FOR EACH OF THE NINECOMPONENTS IN THE FOLLOWING ORDER: AIR, H20(L), H20(V),HF(L), HF(V), UF6(S), UF6(L), UF6(V), U02F2j SOURCE TERMTEMPERATURE FOR INTERVAL (DEG F)j AND SOURCE TERM PRESSUREFOR THE INTERVAL (PSIA).
14
READ (22,*,END=120) TRELS, (RATE(I),I=1,9),TC(IIN(1,2)),* PC(IIN(1,2))
C
C
C
DO 90 190=1,9
MASS(IIN(1,2),I90) = RATE(I90)*DELT
90 CONTINUEC
CCALL DENTHL(TC(IIN(1,2)),PC(IIN(1,2)),IIN(1,2),H(IIN(1,2)))
TRELS = TRELS + DELTATC
GO TO 120C
100 CONTINUEC
IF (IRELS.GT.IRELST) GO TO 120C
TRELS = TSOURC(IRELS)C
SOURCE = MSOURC(IRELS)C
CTC(3) = TEMP(IRELS)
PC(3) = PRES(IRELS)C
CCALL STERM(3, 1, SOLIDS)
TRELS = O.DOC
CDO 110 I110=1,IRELS
TRELS = TRELS + TSOURC(1110)C
110 CONT INUEC
IRELS = IRELS + 1C
120 CONTI NUEC
IF (TIME.GE.TRELS) IIN(1,2) ~ iNODES
===================
·CALL TRBLOW(2)· -- NOT CALLED SINCE INLET BLOWER PRODUCESCONSTANT FLOW RATES THROUGHOUT TRANSIENTANALYSIS.
CC EVALUATE FLOW RATESCCCCC
CCALL DPFLOW(4)
CIF (PC(1).LE.PC(7)) WRITE (44,4410) TIME
15
CC CALCULATE DEPOSITION RATE.C
CCALL REMOVE(1, 5)
IF (ICOUNT.LT.IFLAG) GO TO 150CC OUTPUT NODE DATAC ================CC WRITE COMPARTMENT DATA.C
WRITE (41,4120) TIME, (MASS(1,I),I=1,9), TC(1), PC(1)CC WRITE DATA FOR FLOWING STREAMS.C
DO 140 1140=2,5C
IF (TIME.GE.TRELS .AND. I140.EQ.3) GO TO 140C
DO 130 1130=1,9C
C
C
C
C
C
RATE(I130) = MASS(I140,I130)/DELT
130 CONTINUE
IDEV = 40 + 1140
HRATE = H(I140)/DELT
IF (I140.LE.4) WRITE (IDEV,4120) TIME, RATE, TC(I140),* PC(I140)
IF (I140.GT.4) WRITE (IDEV,4120) TIME, RATE
140 CONTINUECC WRITE MASSES OF CONDENSED MATERIALS ON FLOOR.C
WRITE (46,4120) TIME, (MASS(6,I),I=1,9)C
ICOUNT = 0CC WRITE SUMMARY DATA ON RELEASE.C
WRITE (47,4720) TIME, UF6REL, UOFREL, UTOT, HFREL, HFUF6, HFTOT,* DENU, DENHF
CC WRITE SUMMARY DATA FOR PLOTTING.C
IF (TIME.GT.TRELS) WRITE (48,*) TIME, UTOT, HFTOT, DENU, DENHF,* TC(1), PC(1)
C150 CONTINUE
C
16
IF (TIME.LE.60.DO .AND. TIME.LE.TRELS) WRITE (48,*) TIME, UTOT,* HFTOT, DENU, DENHF, TC(l), PC(l)
CIF (TIME.GT.60.DO .AND. TIME.LE.TRELS .AND.
* 10*(ICOUNT/10).EQ.ICOUNT)* WRITE (48,*) TIME, UTOT, HFTOT, DENU, DENHF, TC(l), PC(l)
CC EVALl~TE COMPARTMENT CONDITIONSC ===============================C
TIME =TIME + DELTC
IF (TIME.GT.MAXTIM) STOPC
ICOUNT = ICOUNT + 1CC PERFORM MASS AND ENENGY BALANCE FOR THE COMPARTMENT.C
CALL COMPRT(l, 2, INODES)CC CALCULATE COMPARTMENT CONCENTRATIONS OF URANIUM AND HF.C
DENU = «MASS(1,6) + HASS(l,7) + MASS(l,8»/WMOL(6)* + MASS(1,9)/WMOL(9»*MWURAN/VOL(1)
CDENHF = (MASS(l,4) + MASS(l,5»/VOL(1)
CC ACCUMULATE SOLID PARTICLES AND LIQUID DROPLETS ON THE FLOOR.C
DO 160 1160=1,9C
MASS(6,I160) = MASS(6,I160) + MASS(5,I160)C
160 CONTINUEC
IF (ITYPE.EQ.7 .AND. TIME.LE.TRELS) t1ASS(6,6) =HASS(6,6)* + SOLIDS
CC ACCUMULATE TOTAL MASS QUANTITIES OF URANIUM AND HF RELEASED TO THEC ATMOSPHERE.C
C
C
C
C
C
C
UF6REL = UF6REL + MASS(4,6) + MASS(4,7) + t1ASS(4,8)
UOFREL = UOFREL + MASS(4,9)
UTOT = (UF6RELIWMOL(6) + UOFRELIWMOL(9»*MWURAN
HFREL = HFREL + MASS(4,4) + MASS(4,5)
HFUF6 = 4.DO*UF6REL*WMOL(4)IWMOL(6)
HFTOT = HFREL + HFUF6
GO TO 80
_/- ,
17
CC***********************************************************************CC FORMAT STATEMENTSC =================C
4000 FORMAT (10A8)C
4010 FORMAT (4A5)C
4020 FORMAT (6(lH$,/))C
4030 FORMAT (/1 TITLE: / ,10A8,/,/0 DATA GENERATED BY FODRFT* /A FORCED DRAFT VENTILATION SYSTEM TRANSIENT' ,* ' COMPARTMENT MODEL./)
C4100 FORMAT (/0 COMPARTMENT CONDITIONS/ ,T60,/COMPARTMENT VOLUME
* F11.0,/ FT**2/,/,T60,/U*A PRODUCT =/,* 1PE11.3,/ BTU/SEC-DEG F' ,/,T60,/SURFACE TEMPERATURE =/,* OPF11.1,/ DEG F/,I,T60,/COOLING RATE =/ ,lPE11.3,* / BTU/SEC/)
C4110 FORMAT (/0 TIME',42X,/COMPONENT MASS (LB)/,39X,
* /TEMPERATURE PRESSURE/ ,1,/ (SEC)/ ,9(3X,A8),* / (DEG F) (PSIA)/,/,lH)
C4120 FORMAT (F10.1,lP9Ell.3,OP2F10.4)
C4200 FORMAT ('0 INLET AIR BLOWER/ ,T60,/FLOW RATE =/ ,Fll.1,
* / ACFM/ ,/,T60,/AMBIENT TEMPERATURE =/ ,F11.3,/ DEG F/ ,I,* T60,/AMBIENT PRESSURE =/ ,F11.3,/ PSIA/)
C4210 FORMAT (/0 TIME/,35X,/COMPONENT MASS FLOW RATE (LB/SEC)/,
* 32X,/TEMPERATURE PRESSURE/ ,1/ (SEC)/ ,9(3X,A8),* (DEG F) (PSIA)/,/,lH)
C4304 FORMAT ('0 SOURCE TERM: HF LIQUID/ ,T60,
* /INCRE- DURATION MASS TEMPERATURE PRESSURE/)C
4305 FORMAT (/0 SOURCE TERM: HF VAPOR/ ,T60,* /INCRE- DURATION MASS TEMPERATURE PRESSURE')
C4307 FORMAT ('0 SOURCE TERM: UF6 LIQUID/ ,T60,
* 'INCRE- DURATION MASS TEMPERATURE PRESSURE/)C4308 FORMAT (/0 SOURCE TERM: UF6 VAPOR/ ,T60,
* /INCRE- DURATION MASS TEMPERATURE PRESSURE/)C
4310 FORMAT (T60,/ MENT (SEC) (LB) (DEG F) (PSIA)/)C
4320 FORMAT (lHO,T60,/ 1/,F11.1,F8.1,F11.3,/ LIQUID' ,I,* T60,/ 2',Fl1.1,F8.1,F11.3,/ LIQUID/ ,I,* T60,' 3',F11.1,F8.1,F11.3,/ LIQUID/ ,I,* T60,' 4/,F11.1,F8.1,F11.3,/ LIQUID/,/,
18
*C4330 FORMAT (lHO,T60,' l' ,F11.1,F8.1,2Fl1.3,1,
* T60,' 2',F11.1,F8.1,2F11.3,1,* T60,' 3',Fll.l,F8.1,2F11.3,1,* T60,' 4' ,Fl1.1,F8.1,2F11.3,1,* T60,' 5',Fl1.1,F8.1,2F11.3)
C4340 FORMAT (lHO,T60,' l',F11.1,F8.1,F11.3,' LIQUID' ,I,
* T60,' 2' ,F11.1,F8.1,F11.3,' LIQUID' ,I,* T60,' 3' ,F11.1,F8.1,F11.3,' LIQUID')
C4341 FORMAT ('
* T60,'C
4342 FORMAT ('* T60,'
C4343 FORMAT ('
* T60,'
FLASH BASIS: ISENTROPIC',4' ,F11.1,F8.1,Fl1.3,' LIQUID')
FLASH BASIS: ISENTHALPIC',4',F11.1,F8.1,F11.3,' LIQUID')
UF6 MOLECULAR WEIGHT =',F8.3,5' ,F11.1,F8.1,F11.3,' LIQUID')
C4350 FORMAT (lHO,T60,' l',Fl1.1,F8.1,2F11.3,1,
* T60,' 2',F11.1,F8.1,2F11.3,1,* T60,' 3',F11.1,F8.1,2F11.3)
C4351 FORMAT ('
* T60,'C4352 FORMAT ('
* T60,'C
4353 FORMAT ('* T60,'
FLASH BASIS: ISENTROPIC',4' ,F11.1,F8.1,2Fl1.3)
FLASH BASIS: ISENTHALPIC',4',F11.1,F8.1,2Fl1.3)
UF6 MOLECULAR WEIGHT =',F8.3,5',F11.1,F8.1,2Fll.3)
C4360 FORMAT (T60,' TOTAL',F9.1,F8.1)
C4370 FORMAT ('0 SOLIDS FORMED BY FLASHING UF6 LIQUID ARE ASSUMED',
* ' TO ACCUMULATE ON THE FLOOR.',I,' THESE SOLIDS ARE NOT',* 'INVOLVED IN ENERGY BALANCES ABOUT THE COMPARTMENT.')
C4380 FORMAT ('0 SOURCE TERM: SOURCE TERM MASS FLOW RATES,',
* ' TEMPERATURE, AND PRESSURE WERE READ FROM DATA FILE.')C
4400 FORMAT ('0 EXHAUST STREAM (FORCED DRAFT)',T60,* 'RESISTANCE TERM =',lPE11.3,' PSI-SEC**2/LB/FT**3')
C4410 FORMAT (F10.l,' REVERSE FLOW OCCURING')
C4500 FORMAT ('0 CONDENSATE FALLOUT' ,T60,'DEPOSITION VELOCITY =',
* F10.4,' FT/SEC' ,1,T60,'DEPOSITION AREA =',F10.O,' FT**2')C
4510 FORMAT ('0* I,'
C
TIME',35X,'COMPONENT MASS FLOW RATE (LB/SEC), ,(SEC)' ,9(3X,A8),I,lH )
19
4600 FORMAT ('0 CONDENSATE ACCUMULATED ON FLOOR')C
4610 FORMAT ('0 TIME',42X,'COMPONENT MASS (LB)' ,I,* ' (SEC)',9(3X,A8),I,lH)
C4700 FORMAT ('0 URANIUM AND HF RELEASE SUMMARY AND COMPARTMENT',
* ' CONCENTRATIONS')C
4710 FORMAT (lHO,T86,'COMPARTMENT CONCENTRATIONS' ,I,' TIME* 'CUMULATIVE MATERIAL RELEASED OR FORMED FROM RELEASED' ,* ' MATERIAL (LB)' ,T94, , (LB/FT**3) , ,I,' (SEC) ,* UF6 U02F2 TOTAL U HF HF FROM UF6',* 'TOTAL HF URANIUM HF',I,lH)
C4720 FORMAT (F10.l,5X,lP6Ell.3,5X,2E11.3)
CC***********************************************************************C
END
A.2 INDRFT - An Induced-Draft Compartment Model
C THIS PROGRAM MODELS A RELEASE OF UF6 OR HF INTO A COMPARTMENTC HAVING AN INDUCED DRAFT VENTILATION SYSTEM. NODE NUMBERS ANDC STREAM DEFINITIONS FOR THIS MODEL ARE AS FOLLOWS.CC 1 COMPARTMENTC 2 INLET AIRC 3 SOURCE TERMC 4 EXHAUST BLOWERC 5 CONDENSATE FALLOUTC 6 COMPARTMENT FLOORC 7 AMBIENTCC THE FOLLOWING VARIABLES ARE USED.CC COMMON BLOCK VARIABLESCC ILBMASSICC MASS (30,9) NODE MASS, LB, OR MASS FLOW RATE, LB/(DELT)C RH RELATIVE HUMI DITY, % (AS INPUT) OR FRACTI ONC ( INTERNAL)CC ICOMPTPICC TC (30) NODE TEMPERATURE, DEG FC PC (30) NODE PRESSURE, PSIAC TSURF (30) NODE HEAT TRANSFER SURFACE TEMPERATURE, DEG FCC IMOLWTICC ~OL (9) COMPONENT MOLECULAR WEIGHTS, LB/LB MOLE
20
CC /VOLUME/CC VOL (30) NODE VOLUME, FT**3C KRCOEF (30) RESISTANCE COEFFICIENT, --, OR RESISTANCE TERM,C RESISTANCE TERM, PSI-SEC**2/LB-FT**3C DPAREA (30) DEPOSITION AREA, FT**2C DEPVEL DEPOSITION VELOCITY, FT/SECCC /ENTHAL/CC H (30) NODE ENTHALPY, BTU, OR ENTHALPY RATE, BTU/(DELT)C QRATE (30) HEAT TRANSFER RATE, BTU/SEC OR BTU/(DELT)C QCOOL (30) COOLING RATE, BTU/HR (INPUT) OR BTU/SECC ( INTERNAL)C HTCOEF (30) HEAT TRANSFER COEFFICIENT, BTU/SEC-FT**2-DEG FC HTAREA (30) HEAT TRANSFER AREA, FT**2CC /ISTRMS/CC lIN (30,4) INLET STREAM NODE NUMBERC lOUT (30,4) OUTLET STREAM NODE NUMBERCC /CONTRL/CC AMINLN NATURAL LOG OF MINIMUM NUMBER ACCEPTED BY THEC COMPUTERC TIME CUMULATIVE SIMULATION TIME, SECC DELT TIME INTERVAL USED FOR TRANSIENT SIMULATION, SECC MAXTIM MAXIMUM SIMULATION TIME, SECC IFLAG FLAG TO CONTROL PRINTING OF OUTPUTC TRELS TOTAL RELEASE TIME, SECCC /POLYMRICC Cl WEIGHT FRACTION OF HF MONOMER TO TOTAL HF VAPORC C3 WEIGHT FRACTION OF HF TRIMER TO TOTAL HF VAPORC C6 WEIGHT FRACTION OF HF HEXAMER TO TOTAL HF VAPORC ~BHF MOLECULAR WEIGHT OF HF MONOMER, LB/LB MOLECC IMISCEL/CC ITYPE VARIABLE TO SPECIFY TYPE OF RELEASE, SEE CARD 5C SOURCE TOTAL MASS OF RELEASE, LBC ISEN VARIABLE TO SPECIFY ISENTROPIC OR ISENTHALPICC RELEASE, SEE CARD 5CC /RVFLOWCC TSTART (30) START OF REVERSE FLOW IN NODEC TSTOP (30) END OF REVERSE FLOW IN NODECC EQUIVALENCED VARIABLESC
UNDIMENSIONED VARIABLES
OTHER DIMENSIONED VARIABLES
ACFM (30)FLAREA (30)
CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCC
VOL
RATEMSOURCTSOURCTEMPPRESNAMETITLEDWGNUM
INODES
INOUT
IRELST
MWMWURANMRELSPTESTPRINTRATIO
MASS2DENSDELPUA
ICOUNTIRELSDELTATSOLIDS
Vi
1.,12
FRAC
IDEVHRATEDENUDENHFUF6REL
( 9)( 5)
(5)( 5)( 5)( 9)(10)
(6,4)
21
VOLUMETRIC FLOW RATE, FT**3IMINFLOW AREA FOR PRESSURE-DROP-CONTROLLEDNODE, FT**2
COMPONENT MASS RELEASE RATE, LB/SECINCREMENTAL SOURCE MASS, LBINCREMENTAL RELEASE TIME, SECTEMPERATURE OF INCREMENTAL SOURCE, DEG FPRESSURE OF INCREMENTAL SOURCE, PSIACOMPONENT IDENT IFI ERTITLE ARRAYPLOT NUMBER ARRAY
MAXIMUM NUMBER OF NODES ALLOWED BY CODING OFSUBROUTINESMAX IMUM NUMBER OF INLET STREAMS AND OUTLETSTREAMSNUMBER OF INCREMENTAL RELEASES IN TOTAL RELEASE(MAXIMUM OF 5)MOLECULAR WEIGHT, LB/LB MOLEMOLECULAR WEIGHT OF URANIUM, LB/LB MOLETOTAL MASS OF SOURCE MATERIAL RELEASED, LBVAPOR PRESSURE OF SOURCE, PSIAPRINT INTERVAL, SECRATIO OF MOLES OF WATER VAPOR TO TOTAL MOLES OFMOIST AIRMASS FLOW RATE THROUGH NODE 2, LB/(DELT)DENSITY, LB/FT**3PRESSURE DROP, PSIPRODUCT OF HEAT TRANSFER COEFICIENT AND AREA,BTU/SEC-DEG FCOUNTER TO CONTROL PRINTING OF OUTPUTCURRENT INCREMENT OF TOTAL RELEASESOURCE TERM INPUT INTERVAL, SECMASS FLOW RATE OF UF6 SOLIDS ONTO THE FLOOR,LB/(DELT)VOLUME OCCUPIED BY CONTENTS OF THE COMPARTMENTAT AMBIENT PRESSURE, FT**3MAXIMUM VOLUME TO BE RELEASED BY REVERSE FLOWTHROUGH NODE 2 OVER A SPECIFIC TIME INTERVAL,FT**3/(DELT)VOLUME FPACTION (-1.,12/1.,11) USED TO OBTAIN MASSFLOW AND ENTHALPY RATES WHEN LIMITING EXHAUSTRATE THROUGH NODE 2OUTPUT DEVICEENTHALPY RATE, BTU/SECCOMPARTMENT CONCENTRATION OF URANIUM, LB/FT**3COMPARTMENT CONCENTRATION OF HF, LB/FT**3CUMULATIVE t1ASS OF UF6 RELEASED TO THEATMOSPHERE, LB
22
FLAG IN ESTABLISHING INITIAL STEADY STATECONDITIONS ABOUT NODE 2
CUMULATIVE MASS OF U02F2 RELEASED TO THEATMOSPHERE, LBCUMULATIVE MASS OF URANIUM RELEASED TO THEATMOSPHERE, LBCUMULATIVE MASS OF HF RELEASED TO THEATMOSPHERE, LBCUMULATIVE MASS OF HF THAT CAN BE FORMED FRct1UF6 RELEASED TO THE ATMOSPHERE, LBCUMULATIVE MASS OF HF RELEASED TO OR FORMED INTHE ATMOSPHERE, LB
COMPRTDENTHLDPFLOWHCOEFFHUMIDPHFH20REMOVERESISTROOMSETRAYSSBL~
STERMTRBLOWVPRUF6
DENUF6EQTUF6FLASHHFPOLYHHFH20HUF6PHASESUF6ZUF6
CHECK
UOFREL
HFTOT
HFUF6
HFREL
UTOT
LOGICAL VARIABLES
CCCCCCCCCCCCCCCCC THE FOLLOWING SUBROUTINES ARE CALLED BY INDRFT.CCCCCCCCCCCCCCCCC THE FOLLOWING SUBROUTINES ARE ALSO REQUIRED.CCCCCCCCCCCC***********************************************************************CC INITIAL STATEMENTSC ==================C
CIMPLICIT REAL*8 (A-H,J-Z)
LOGICAL CHECKC
23
DIMENSION FLAREA(30), ACFM(30), RATE(9), MSOURC(5), TSOURC(5),* TEMP(5), PRES(5)
DIMENSION NAME(9), TITLE(10), DWGNUM(6,4)C
C
C
COMMON ILBMASSI MASS(30,9), RHCOMMON ICOMPTPI TC(30), PC(30), TSURF(30)COMMON IMOLWTI WMOL(9)COMMON IVOLUMEI VOL(30), KRCOEF(30), DPAREA(30), DEPVELCOMMON IENTHALI H(30), QRATE(30), QCOOL(30), HTCOEF(30),
* HTAREA(30)COMMON IISTRMSI IIN(30,4), IOUT(30,4)COMMON ICONTRLI AMINLN, TIME, DELT, MAXTIM, IFLAG, TRELSCOMMON IPOLYMRI Cl, C3, C6, WMBHFCOMMON IMISCELI ITYPE, SOURCE, ISENCOMMON IRVFLOW/ TSTART(30), TSTOP(30)
EQUIVALENCE (VOL(l),ACFM(l),FLAREA(l»
DATA NAME 18HAIR V, 8HH20 L, 8HH20 V, 8HHF L,* 8HHF V, 8HUF6 S, 8HUF6 L, 8HUF6 V, 8HU02F2 S I
CCALL SETRAY(INODES, INOUT)
CC NODE ASSIGNMENTC ===============C
IIN(l,l) = 2I IN(1 ,2) =3IIN(2,1) = 7IIN(4,1) =1IIN(5,1) = 1IIN(6,1) =5
CIOUT(l,l) =4IOUT(1,2) = 5IOUT(2,1) =1IOUT(5,1) =6
CC READ STATEMENTSC ===============CC ALL INPUT DATA EXCEPT THAT ON CARDS 1 AND 9 IS READ IN FREE FORMAT.C ON CARDS 1 AND 9, COUNT CHARACTERS STARTING IN COLUMN 1.CCC IC/ CARD 1. READ TITLE (MAXIMUM OF 80 CHARACTERS).C
READ (40,4000) TITLECCC /C/ CARD 2. READ AMBIENT TEMPERATURE (F), PRESSURE (PSIA), AND RELATIVEC HUMIDITY (~).
24
C
CREAD (40,*) TC(7), PC(7), RH
IF (RH.GT.l.DO) RH = RH/l.D2
READ COMPARTMENT TEMPERATURE (F), PRESSURE (PSIA), VOLUME(FT**3), AND FLOOR (DEPOSITION) AREA (FT**2). IF THECOMPARTMENT PRESSURE IS NOT KNOWN AND IS TO BE CALCULATED,SPECIFY A PRESSURE GREATER THAN OR EQUAL TO THE AMBIENTPRESSURE OR LESS THAN OR EQUAL TO ZERO.
READ (40,*) TC(l), PC(l), VOL(l), DPAREA(l)
CCC /C/ CARD 3.CCCCC
CCC /C/ CARD 4.CCCCCCCC
READ EXHAUST FLOW RATE (ACFM), INLET FLOW AREA (FT**2), ANDINLET RESISTANCE COEFFICIENT (--). IF THE PROGRAM IS TOCALCULATE THE RESISTANCE COEFFICIENT, A COMPARTMENTPRESSURE GREATER THAN OR EQUAL TO THE AMBIENT PRESSURE ORLESS THAN OR EQUAL TO ZERO MUST HAVE BEEN ENTERED, ANDAN INLET AREA AND RESISTANCE COEFFICIENT MUST BE GIVEN. ARESISTANCE COEFFICIENT COEFFICIENT OF 1.5 REPRESENTS ASUDDEN CONTRACTION FOLLOWED BY A SUDDEN EXPANSION.
READ (40,*) ACFM(4), FLAREA(2), KRCOEF(2)CCC /C/ CARD 5.CCCCCCCC
READ HEAT TRANSFER SURFACE AREA IN COMPARTMENT (FT**2),HEAT TRANSFER SURFACE TEMPERATURE (F), AND COOLING RATE(BTU/HR). A NEGATIVE COOLING RATE IMPLIES A HEATING RATE.WHILE THE VALUE OF THE SURFACE AREA IS NOT PARTICULARLYIMPORTANT BECAUSE THE PRODUCT OF THE SURFACE AREA AND THEHEAT TRANSFER COEFFICIENT TO BE CALCULATED WILL BECONSTANT, A SURFACE TEMPERATURE GREATER THAN THECOMPARTMENT TEMPERATURE MUST BE SPECIFIED.
CREAD (40,*) HTAREA(l), TSURF(l), QCOOL(l)
QCOOL(l) =QCOOL(1)/3.6D3CCC /C/ CARD 6.CCCCCCCC
READ SOURCE TYPE, NUMBER OF RELEASES, BASIS FOR FLASH, ANDMOLECULAR WEIGHT. SOURCE TYPE IS GIVEN BY THE FOLLOWING:
4 LIQUID HF5 VAPOR HF7 LIQUID UF6 (VAPOR SOURCE TERM GENERATED)
-7 LIQUID UF6 (VAPOR/SOLID SOURCE TERM GENERATED)8 VAPOR UF6
22 INPUT PROVIDED IN FOR22.DAT
CCCCCCCCCCCC
25
IF SOURCE TYPE IS SET EQUAL TO 22, SET NUMBER OF RELEASESTO ZERO. NO MORE THAN FIVE RELEASES MAY BE SPECIFIED, WHICHARE TO RUN CONSECUTIVELY. THE BASIS FOR THE FLASH IS GIVENBY THE FOLLOWING:
o ISENTROPIC1 ISENTHALPI C
THE DEFAULT MOLECULAR WEIGHT FOR UF6 IS 352.025; ENTER AVALUE LESS THAN 100 IF THAT VALUE IS ACCEPTABLE.
C
C
C
C
C
READ (40,*) ITYPE, IRELST, ISEN, MW
IF (MW.LT.l00.DO) GO TO 10
WMOL(9) = WMOL(9) - ~OL(6) +MWWMOL(6) ="""WMOL(7) =MWWMOL(8) =H-J
10 CONTINUE
MWURAN = WMOL(6) - 113.9900
IF (ITYPE. EQ. 22) GO TO 30CCC ICI CARD 7.CCCCCCCC
-- DO NOT USE "CARD 7" CARDS IF ITYPE = 22. --
READ FOR EACH INCREMENTAL RELEASE THE DURATION (SEC), MASS(LB), TEMPERATURE (DEG F), AND PRESSURE (PSIA). SPECIFY ASt~ SETS OF DATA AS THE NUMBER OF RELEASES (IRELST). IFTHE PRESSURE GIVEN IS LESS THAN OR EQUAL TO ZERO OR GREATERTHAN THE VAPOR PRESSURE, THE PRESSURE IS SET EQUAL TO THEVAPOR PRESSURE FOR THAT INCREMENT.
C
C
C
C
C
C
C
READ (40,*) (TSOURC(I), MSOURC(I), TEMP(I), PRES(I), I=l,IRELST)
TRELS = 0.00
MRELS = 0.00
DO 20 I20=1,IRELST
TRELS = TRELS + TSOURC(I20)
MRELS =MRELS + MSOURC(I20)
IF (ITYPE.EQ.5) CALL PHFH20(TEMP(I20), 1.00, 0.00, PTEST,* 0 •DO, O. DO )
IF (ITYPE.EQ.8) CALL VPRUF6(TEMP(I20), PTEST)
26
IF (PRES(I20).GT.PTEST .OR. PRES(I20).LE.0.DO)* PRES(I20) = PTEST
C20 CONTINUE
C30 CONTINUE
CCC /C/ CARD B. READ TIME INTERVAL FOR CALCULATIONS (SEC), DURATION OFC SIMULATION (SEC), AND PRINT INTERVAL (SEC).C
READ (40,*) DELT, MAXTIM, PRINTC
IFLAG = IDINT(PRINT/DELT+0.01DO)CCC /C/ CARD 9.CCCCCCCCCCC
-- THESE CARDS ARE OPTIONAL. --
READ DRAWING NUMBERS FOR PLOTS (LIMITED TO 20 CHARACTERS-THE LAST CHARACTER MUST BE A DOLLAR SIGN ($».
1ST CARD 9 = CUMULATIVE URANIUM RELEASED2ND CARD 9 = CUMULATIVE HF RELEASED3RD CARD 9 = URANI UM CONCENTRATI ON IN COMPARTMENT4TH CARD 9 = HF CONCENTRATION IN Cct1PARTMENT5TH CARD 9 = TEMPERATURE IN COMPARTMENT6TH CARD 9 = PRESSURE IN COMPARTMENT
DO 40 140=1,6C
READ (40,4010,END=50) (DWGNUM(140,1), 1=1,4)WRITE (49,4010) (DWGNUM(140,1), 1=1,4)
c40 CONTINUE
C50 CONTINUE
CWRITE (49,4020)
CC***********************************************************************CC STEADY STATE CONDITIONSC =======================CC SET STEADY-STATE CONDITIONS FOR THE COMPARTMENT, EXHAUST, AND INLETC AIR NODES.C
CALL HUMID(?, RH, RATIO)C
IF (PC(l).GE.PC(?) .OR. PC(l).LE.O.DO) PC(l) = PC(?)C
CHECK = .TRUE.
27
CVOL( 7) = 1. D9
CCALL ROOM(7, RATIO)
C60 CONTINUE
CCALL ROOM(l, RATIO)
C
C
C
C
C
C
C
C
C
C
CALL SSBLOW(4, RATIO)
MASS(2,1) =MASS(4,1)MASS(2,3) =MASS(4,3)
TC(2) =TC(7)PC(2) = PC(7)
IF (PC(1).LT.PC(7) .AND. CHECK) GO TO 70
IF (CHECK) CALL RESIST(2)
CHECK = .FALSE.
MASS2 =MASS(2,1) + MASS(2,3)
DENS = (MASS(7,1)+MASS(7,3»/VOL(7)
DELP = KRCOEF(2)*MASS2*MASS2/DENS/DELT/DELT
IF (DABS(PC(7)-PC(1)-DELP).LT.l.D-6.AND.PC(1).LT.PC(7»* GO TO 70
CPC(1) = PC( 7) - DELP
CGO TO 60
C70 CONTINUE
CKRCOEF(2) = O.DO
CCALL RESI ST( 2)
CCALL DENTHL(TC(2), PC (2), 2, H(2) )
CCALL HCOEFF(l)
CUA = HTCOEF(l) * HTAREA(l)
CC***********************************************************************CC TITLE BLOCKSC ============CC WRITE TITLE AND PROGRAM IDENTIFIER.
CDO 80 180=1,7
CIDEV = 40 + 180
C
CWRITE (IDEV,4030) TITLE
80 CONTINUECC WRITE NODE NAMES AND IMPORTANT CONSTANTS FOR EACH FILE.C
WRITE (41,4100) VOL(l), UA, TSURF(l), QCOOL(l)C
C
C
C
C
C
C
c
c
c
c
c
c
C
C
WRITE (42,4200) KRCOEF(2), TC(7), PC(?)
IF (ITYPE.EQ.4) WRITE (43,4304)IF (ITYPE.EQ.5) WRITE (43,4305)IF (IABS(ITYPE).EQ.7) WRITE (43,4307)IF (ITYPE.EQ.8) WRITE (43,4308)
IF (ITYPE.NE.22) WRITE (43,4310)
IF (ITYPE.EQ.4) WRITE (43,4320) (TSOURC(I), MSOURC(I),* TEMP(I), 1=1,5)
IF (ITYPE.EQ.5) WRITE (43,4330) (TSOURC(I), MSOURC(I),* TEMP(I), PRES(I), 1=1,5)
IF (IABS(ITYPE).EQ.7) WRITE (43,4340) (TSOURC(I), MSOURC(I),* TEMP(I), 1=1,3)
IF (IABS(ITYPE).EQ.7 .AND. ISEN.EQ.O) WRITE (43,4341) TSOURC(4),* MSOURC(4), TEMP(4)
IF (IABS(ITYPE).EQ.7 .AND. ISEN.EQ.1) WRITE (43,4342) TSOURC(4),* MSOURC(4), TEMP(4)
IF (IABS(ITYPE).EQ.7) WRITE (43,4343) WMOL(6), TSOURC(5),* MSOURC(5), TEMP(5)
IF (ITYPE.EQ.8) WRITE (43,4350) (TSOURC(I), MSOURC(I),* TEMP(I), PRES(I), 1=1,3)
IF (ITYPE.EQ.8 .AND. ISEN.EQ.O) WRITE (43,4351) TSOURC(4),* MSOURC(4), TEMP(4), PRES(4)
IF (ITYPE.EQ.8 .AND. ISEN.EQ.1) WRITE (43,4352) TSOURC(4),* MSOURC(4), TEMP(4), PRES(4)
IF (ITYPE.EQ.8) WRITE (43,4353) WMOL(6), TSOURC(5), MSOURC(5),* TEMP(5), PRES(5)
IF (ITYPE.NE.22) WRITE (43,4360) TRELS, MRELS
29
IF (ITYPE.EQ.7) WRITE (43,4370)C
IF (ITYPE.EQ.22) WRITE (43,4380)C
WRITE (44,4400) ACFM(4)C
WRITE (45,4500) DEPVEL, DPAREA(l)C
WRITE (46,4600)C
WRITE (47,4700)CC WRITE COLUMN HEADINGS.C
WRITE (41,4110) NAMEC
DO 90 190=2,4C
IDEV = 40 + 190C
WRITE (l DEV, 4210) NAMEC
90 CONTINUEC
WRITE (45,4510) NAMEC
WRITE (46,4610) NAMEC
WRITE (47,4710)CC***********************************************************************CC TRANSIENT ANALYSISC ==================CC BEGIN TRANSIENT ANALYSIS.C
TIME = 0.00C
ICOUNT = IFLAGC
IRELS = 1C
TRELS = 0.00CCC /C/ OPTIONAL SOURCE TERM INPUT: CARD 1. ENTER TIME INTERVAL FOR SOURCEC TERM INPUT (SEC).C
IF (ITYPE.EQ.22) READ (22,*) DELTATC
100 CONTINUEC
30
C EVALUATE SOURCE TERMC ====================C
IF (TIME.LT.TRELS) GO TO 140C
IF (ITYPE.NE.22) GO TO 120CCC /C/ OPTIONAL SOURCE TERM INPUT: CARD 2. ENTER INITIAL TIME FOR RELEASEC INTERVAL (SEC); MASS FLOW RATE (LB/SEC) FOR EACH OF THE NINEC COMPONENTS IN THE FOLLOWING ORDER: AIR, H20(L), H20(V),C HF(L), HF(V), UF6(S), UF6(L), UF6(V), U02F2; SOURCE TERMC TEMPERATURE FOR INTERVAL (DEG F); AND SOURCE TERM PRESSUREC FOR THE INTERVAL (PSIA).C
READ (22,*,END=140) TRELS, (RATE(I),I=1,9),TC(IIN(1,2)),* PC(IIN(1,2))
CDO 110 1110=1,9
CMASS(IIN(1,2),I110) = RATE(Ill0)*DELT
C110 CONTI NUE
CTRELS = TRELS + DELTAT
CGO TO 140
C120 CONTINUE
C
C
C
C
C
C
C
C
C
IF (IRELS.GT.IRELST) GO TO 140
TRELS = TSOURC(IRELS)
SOURCE = MSOURC(IRELS)
TC(3) = TEMP(IRELS)
PC(3) = PRES(IRELS)
CALL STERM(3, 1, SOLIDS)
TRELS = 0.00
DO 130 I130=1,IRELS
TRELS = TRELS + TSOURC(I130)C
130 CONTINUEC
IRELS = IRELS + 1C
140 CONTINUE
31
CIF (TIME.GE.TRELS) IIN(1,2) = INODES
CC EVALUATE FLOW RATESC ===================C
CCALL TRBLOW (4)
CALL DPFLOW(2)CC LIMIT REVERSE FLOW EXHAUST RATE THROUGH DOOR.C
C
C
C
C
C
C
C
C
IF (PC(1).LE.PC(7» GO TO 160
Vi = PC(1)*VOL(1)/PC(7)
V2 = Vi - ACFM(4)*DELT/6.Dl - VOL(l)
IF (V2.LT.0.DO) V2 = O.DO
FRAC = -V21V1
IF (DABS(FRAC*MASS(1,1».GE.DABS(MASS(2,1») WRITE (42,4220) TIME
IF (DABS(FRAC*MASS(1,1».GE.DABS(MASS(2,1») GO TO 160
DO 150 1150=1,9
MASS(2,1150) = FRAC*MASS(1,I150)C
150 CONTINUEC
H(2) = FRAC*H(l)C
C
C
TC( 2) = TC(1)
PC(2) = PC(l)
WRITE (42,4230) TIMEC
160 CONTINUECC CALCULATE DEPOSITION RATE.C
CCALL REMOVE(l, 5)
IF (ICOUNT.LT.IFLAG) GO TO 190CC OUTPUT NODE DATAC ================CC WRITE COMPARTMENT DATA.C
WRITE (41,4120) TIME, (MASS(1,I),I=1,9), TC(l), PC(l)
32
CC WRITE DATA FOR FLOWING STREAMS.C
C
C
C
DO 180 1180=2,5
IF (TIME.GE.TRELS .AND. I180.EQ.3) GO TO 180
DO 170 1170=1,9
RATE(I170) = MASS(I180,I170)/DELTC
170 CONTINUEC
IDEV = 40 + 1180C
CHRATE = H(I180)/DELT
IF (I180.LE.4) WRITE (IDEV,4120) TIME, RATE, TC(I180),* PC(I180)
IF (I180.GT.4) WRITE (IDEV,4120) TIME, RATEC
180 CONTINUECC WRITE MASSES OF CONDENSED MATERIALS ON FLOOR.C
WRITE (46,4120) TIME, (MASS(6,I),I=1,9)C
ICOUNT = 0CC WRITE SUMMARY DATA ON RELEASE.C
WRITE (47,4720) TIME, UF6REL, UOFREL, UTOT, HFREL, HFUF6, HFTOT,* DENU, DENHF
CC WRITE SUMMARY DATA FOR PLOTTING.C
IF (TIME.GT.TRELS) WRITE (48,*) TIME, UTOT, HFTOT, DENU, DENHF,* TC(l), PC(l)
C190 CONTI NUE
CIF (TIME.LE.60.DO.AND.TIME.LE.TRELS) WRITE (48,*) TIME, UTOT,
* HFTOT, DENU, DENHF, TC(l), PC(l)C
IF (TIME.GT.60.DO.AND.TIME.LE.TRELS.AND.l0*(ICOUNT/l0).EQ.ICOUNT)* WRITE (48,*) TIME, UTOT, HFTOT, DENU, DENHF, TC(l), PC(l)
CC EVALUATE COMPARTMENT CONDITIONSC ===============================C
TIME = TIME + DELTC
IF (TIMLGT .MAXTIM) STOPC
33
ICOUNT = ICOUNT + 1CC PERFORM MASS AND ENENGY BALANCE FOR THE COMPARTMENT.C
CALL COMPRT(l, 2, INODES)CC CALCULATE COMPARTMENT CCNCENTRATI ONS OF URANI lt1 AND HF.C
DENU = «MASS(1,6) + MASS(1,7) + MASS(1,8»JWMOL(6)* + MASS(1,9)IWMOL(9»*MWURANVVOL(1)
CDENHF = (MASS(1,4) + MASS(1,5»IVOL(1)
CC ACCUMULATE SOLID PARTICLES AND LIQUID DROPLETS ON THE FLOOR.C
CDO 200 1200=1,9
MASS(6,I200) = MASS(6,I200) + MASS(5,I200)C
200 CONTINUEC
IF (ITYPE.EQ.7 .AND. TIME.LE.TRELS) MASS(6,6) = MASS(6,6)* + SOLIDS
CC ACCUMULATE TOTAL MASS QUANTITIES OF URANIUM AND HF RELEASED TO THEC ATMOSPHERE.C
UF6REL = UF6REL + MASS(4,6) + MASS(4,7) + MASS(4,8)* + DABS(MASS(2,6) + MASS(2,7) + MASS(2,B»
C
C
C
C
C
C
UOFREL = UOFREL + MASS(4,9) + DABS(MASS(2,9»
UTOT = (UF6RELJWMOL(6) + UOFRELlWMOL(9»*MWURAN
HFREL = HFREL + MASS(4,4) + MASS(4,5)* + DABS(MASS(2,4) + MASS(2,5»
HFUF6 = 4.DO*UF6REL*WMOL(4)JWMOL(6)
HFTOT = HFREL + HFUF6
GO TO 100CC***********************************************************************CC FORMAT STATEMENTSC =================C
4000 FORMAT (10AB)C
4010 FORMAT (4A5)C
4020 FORMAT (6(lH$,/»C
4030 FORMAT ('1 TITLE: ',10A8,1,'0 DATA GENERATED BY INDRFT* 'AN INDUCED DRAFT VENTILATION SYSTEM TRANSIENT' ,* ' COMPARTMENT MODEL.')
C4100 FORMAT ('0 COMPARTMENT CONDITIONS' ,T60,'COMPARTMENT VOLUME
* Fll.0,' FT**2' ,1,T60,'U*A PRODUCT =',* lPEll.3,' BTU/SEC-DEG F' ,1,T60,'SURFACE TEMPERATURE =',* OPFll.l,' DEG F' ,1,T60,'COOLING RATE =',lPEll.3,* ' BTU/SEC')
C4110 FORMAT ('0 TIME' ,42X,'COMPONENT MASS (LB)' ,39X,
* 'TEMPERATURE PRESSURE' ,I,' (SEC)' ,9(3X,A8),* (DEG F) (PSIA)' ,1,1H
C4120 FORMAT (Fl0.1,lP9Ell.3,OP2Fl0.4)
C4200 FORMAT ('0 INLET AIR STREAM (INDUCED DRAFT)',T60,
* 'RESISTANCE TERM =',lPEll.3,' PSI-SEC**2/LB/FT**3',* I,T60,'AMBIENT TEMPERATURE =' ,OPF11.3,' DEG F' ,I,* T60,'AMBIENT PRESSURE =' ,Fll.3,' PSIA')
C4210 FORMAT ('0 TIME' ,35X,'COMPONENT MASS FLOW RATE (LB/SEC), ,
* 32X,'TEMPERATURE PRESSURE' ,I' (SEC)' ,9(3X,A8),* (DEG F) (PSIA)',I,lH )
-,- ,
C4220 FORMAT (F10.l,' REVERSE FLOW OCCURING')
C4230 FORMAT (Fl0.l,' REVERSE FLOW OCCURING FLOW RATES LIMITED')
C4304 FORMAT ('0 SOURCE TERM: HF LIQUID',T60,
* 'INCRE- DURATION MASS TEMPERATURE PRESSURE')C4305 FORMAT ('0 SOURCE TERM: HF VAPOR' ,T60,
* 'INCRE- DURATION MASS TEMPERATURE PRESSURE')C4307 FORMAT ('0 SOURCE TERM: UF6 LIQUID' ,T60,
* 'INCRE- DUPATION MASS TEMPERATURE PRESSURE')C4308 FORMAT ('0 SOURCE TERM: UF6 VAPOR' ,T60,
* 'INCRE- DURATION MASS TEMPERATURE PRESSURE')C
4310 FORMAT (T60,' MENT (SEC) (LB) (DEG F) (PSIA)')C
4320 FORMAT (lHO,T60,' l' ,Fl1.1,F8.1,Fll.3,' LIQUID' ,I,* T60,' 2' ,Fl1.l,F8.1,Fll.3,' LIQUID' ,I,* T60,' 3' ,Fl1.l,FB.1,F11.3,' LIQUID' ,I,* T60,' 4' ,Fll.1,F8.1,Fl1.3,' LIQUID',I,* T60,' 5',F11.1,F8.1,Fll.3,' LIQUID')
C4330 FORMAT (lHO,T60,' l' ,Fll.l,F8.1,2Fl1.3,1,
* T60,' 2' ,Fll.l,F8.1,2Fll.3,1,* T60,' 3' ,Fll.1,F8.1,2Fll.3,1,* T60,' 4' ,Fll.1,F8.1,2Fl1.3,1,* T60,' 5' ,F11.1,F8.1,2Fll.3)
35
C4340 FORMAT (1HO,T60,' l' ,F11.1,F8.1,F11.3,' LIQUID',I,
* T60,' 2',F11.1,F8.1,F11.3,' LIQUID' ,I,* T60,' 3',F11.1,F8.1,F11.3,' LIQUID')
C4341 FORMAT ('
* T60,'C4342 FORMAT ('
* T60,'C4343 FORMAT ('
* T60,'
FLASH BASIS: ISENTROPIC' ,4' ,F11.1,F8.1,F11.3,' LIQUID')
FLASH BASIS: ISENTHALPIC',4' ,Fl1.1,F8.1,Fl1.3,' LIQUID')
UF6 MOLECULAR WEIGHT =' ,F8.3,5',Fl1.1,F8.1,F11.3,' LIQUID')
C4350 FORMAT (lHO,T60,' l' ,Fll.l,F8.1,2Fll.3,1,
* T60,' 2',Fll.l,F8.1,2Fl1.3,1,* T60,' 3',F11.1,F8.1,2F11.3)C
4351 FORMAT ('* T60,'
C4352 FORMAT ('
* T60,'C4353 FORMAT ('
* T60,'
FLASH BASIS: ISENTROPIC',4',F11.1,F8.1,2F11.3)
FLASH BASIS: ISENTHALPIC',4' ,F11.1,F8.1,2Fl1.3)
UF6 MOLECULAR WEIGHT =',F8.3,5' ,Fl1.1,F8.1,2F11.3)
C4360 FORMAT (T60,' TOTAL',F9.1,F8.1)
C4370 FORMAT ('0 SOLIDS FORMED BY FLASHING UF6 LIQUID ARE ASSUMED',
* ' TO ACCUMULATE ON THE FLOOR.' ,I,' THESE SOLIDS ARE NOT',* 'INVOLVED IN ENERGY BALANCES ABOUT THE COMPARTMENT.')
C4380 FORMAT ('0 SOURCE TERM: SOURCE TERM MASS FLOW RATES,',
* ' TEMPERATURE, AND PRESSURE WERE READ FROM DATA FILE.')
TIME',42X,'COMPONENT MASS (LB)' ,I,(SEC)',9(3X,A8),I,lH)
C4400 FORMAT ('0
C4500 FORMAT ('0
* FlO.4,'C4510 FORMAT ('0
* I,'C
4600 FORMAT (' 0C
4610 FORMAT ('0* '
EXHAUST BLOWER',T60,'FLOW RATE =',F10.1,' ACFM')
CONDENSATE FALLOUT',T60,'DEPOSITION VELOCITY =',FT/SEC',I,T60,'DEPOSITION AREA =',FIO.O,' FT**2')
TIME',35X,'COMPONENT MASS FLOW RATE (LB/SEC), ,(SEC)',9(3X,A8),I,lH)
CONDENSATE ACCUMULATED ON FLOOR')
C4700 FORMAT ('0 URANIUM AND HF RELEASE SUMMARY AND COMPARTMENT',
* ' CONCENTRATIONS')C
4710 FORMAT (lHO,T86,'COMPARTMENT CONCENTRATIONS',I,' TIME* 'CUMULATIVE MATERIAL RELEASED OR FORMED FROM RELEASED',
36
* ' MATERIAL (LB)' ,T94,'(LB/FT**3)',I,' (SEC) "* UF6 U02F2 TOTAL U HF HF FROM UF6' ,* 'TOTAL HF URANIUM HF' ,1,1H )
C4720 FORMAT (Fl0.l,5X,lP6Ell.3,5X,2Ell.3)
CC***********************************************************************C
END
A.3 BATCH - A Oosed Compartment/Ventilation System Model
COMMON BLOCK VARIABLES
THE FOLLOWING VARIABLES ARE USED.
NODE VOLUME, FT**3
COMPONENT MOLECULAR WEIGHTS, LB/LB MOLE
NODE ENTHALPY, BTU, OR ENTHALPY RATE, BTU/(DELT)
NODE TEMPERATURE, DEG FNODE PRESSURE, PSIA
CLOSED COMPARTMENTAHB IENT CONDITIONSSOURCE TERMOPEN COMPARTMENT (FINAL PRESSURE =AHBI ENT PRESSURE)
(30,9) NODE MASS, LB, OR MASS FLOW RATE, LB/(DELT)( INTERNAL)
MASS
ICOMPTPI
TC (30)PC (30)
IMOLWTI
WMOL (9)
/vOLUMEI
VOL (30)
lENTHALl
H (30)
1234
ILBMASSI
C THIS PROGRAM MODELS A RELEASE OF UF6 OR HF INTO A CLOSED COMPARTMENTC OR A CONSTANT RELEASE OF UF6 OR HF INTO A CONSTANT VOLUME FLOW. INC THE LATTER CASE, THE REQUESTED COMPARTMENT VOLUME IS CONS IDERED AC VOLUMETRIC FLOW RATE BASED ON THE SAME TIME UNIT AS THE SOURCE TERM.C IF THE MODEL IS USED IN THE LATTER STEADY-STATE MODE, AN OPTION ISC AVAILABLE TO PERMIT THE EVALUATION OF THE FINAL TEMPERATURE AND PHASEC COMPOSITION AT AMBIENT PRESSURE (WHICH ASSUMES RELEASE TO THE AMBIENTC SURROUNDINGS). THIS MODEL MAKES USE OF SUBROUTINES DEVELOPED FORC TRANSIENT ANALYSIS OF UF6 AND HF RELEASES IN BUILDINGS. NODE NUMBERSC AND DEFINITIONS ARE AS FOLLOWS.CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCC
37
CC IISTRMSICC lIN (30,4) INLET STREAM NODE NUMBERC lOUT (30,4) OUTLET STREAM NODE NUMBERCC ICCNfRLICC AMINLN NATURAL LOG OF MINIMUM NUMBER ACCEPTED BY THEC COMPUTERC TIME CUMULATIVE SIMULATION TIME, SECC DELT TIME INTERVAL USED FOR TRANSIENT SIMULATION, SECC MAXTIM MAXIMUM SIMULATION TIME, SEC, EQUALS DELT FORC BATCH ANALYSISC IFLAG FLAG TO CONTROL PRINTING OF OUTPUTC TRELS TOTAL RELEASE TIME, SEC, EQUALS DELT FOR BATCHC ANALYSIS
CC IPOLYMRICC C1 WEIGHT FRACTION OF HF MONOMER TO TOTAL HF VAPORC C3 WEIGHT FRACTION OF HF TRIMER TO TOTAL HF VAPORC C6 WEIGHT FRACTION OF HF HEXAMER TO TOTAL HF VAPORC WMBHF MOLECULAR WEIGHT OF HF MONOMER, LB/LB MOLECC IMISCEUCC ITYPE VARIABLE TO SPECIFY TYPE OF RELEASE, SEE CARD 5C SOURCE TOTAL MASS OF RELEASE, LBC ISEN VARIABLE TO SPECIFY ISENTROPIC OR ISENTHALPICC RELEASE, SEE CARD 5CC OTHER DIMENSIONED VARIABLESCC NAME (9) COMPONENT IDENT IFIERC TITLE (6) TITLE ARRAYCC UNDIMENSIONED VARIABLESCC INODES MAXIMUM NUMBER OF NODES ALLOWED BY CODING OFC SUBROUTINESC INOUT MAXIMUM NUMBER OF INLET STREAMS AND OUTLETC STREAMSC RH RELATIVE HUMIDITY, % (AS INPUT) OR FRACTIONC ~ MOLECULAR WEIGHT, LB/lB MOLEC IWRITE CONTROL VARIABLE TO SPECIFY OUTPUT BASED ON THEC ASSUMPT ION OF AN OPEN COMPARTMENTC RATIO RATIO OF MOLES OF WATER VAPOR TO TOTAL MOLES OFC MOIST AIRC SOLIDS MASS FLOW RATE OF UF6 SOLIDS ONTO THE FLOOR,C LB/(DELT)C MSSTOT FINAL TOTAL MASS IN COMPARTMENT, LBC DENS DENSITY AT FINAL TEMPERATURE, PRESSURE, AND
38
VOLl~E (SPECIFIC VOLUME OF CONDENSATE ISNEGLECTED), LB/FT**3
COMPRTHUMIDMIXFLWROOMSETRAYSTERM
DENTHLDENUF6EQTUF6FLASHHFPOLYHHFH20HUF6PHASEPHFH20SUF6VPRUF6ZUF6
CCCC THE FOLLOWING SUBROUTINES ARE CALLED BY BATCH.CCCCCCCCC THE FOLLOWING SUBROUTINES ARE ALSO REQUIRED.CCCCCCCCCCCCCCC***********************************************************************CC INITIAL STATEMENTSC ==================C
IMPLICIT REAL*B (A-H,J-Z)C
DIMENSION NAME(9) , TITLE(6)C
COMMON /LBMASS/ MASS(30,9), DUMlCOMMON /COMPTP/ TC(30), PC(30), DUM2(30)COMMON /MOLWT/ WMOL(9)COMMON /VOLUME/ VOL(30), DUM3(61)COMMON /ENTHAL/ H(30), DUM4(120)COMMON /ISTRMS/ IIN(30,4), IOUT(30,4)COMMON ICONTRL/ AMINLN, TIME, DELT, MAXTIM, IFLAG, TRELSCOMMON IPOLYMR/ Cl, C3, C6, WMBHFCOMMON /MISCEL/ ITYPE, SOURCE, ISEN
CDATA NAME /8HAIR V ,BHH20 L ,BHH20 V ,BHHF L,
* 8HHF V ,BHUF6 S ,8HUF6 L ,BHUF6 V,* BHU02F2 S /
CC SET PARAMETERS.C
CALL SETRAY(INODES, INOUT)C
39
INOUT =1IFLAG =1I IN(1 ,1) = 3IIN(4,1) =1IOUT(l,l) = INODESlOUT( 4 , 1) = 2DELT = 6.D1MAXTIM = DELTTRELS =DELT
CC READ STAMENTSC =============CC BATCH IS WRITTEN FOR INTERACTIVE EXECUTION.CC ALL INPUT DATA EXCEPT THAT ON CARD 1 ARE READ IN FREE FORMAT.C ON CARD 1, COlNf CHARACTERS STARTING IN COLlJt1'.l 1.CC WARNING: OUTPUT APPEARS IN FOR06.DATC
WRITE (5,5000)CCC /C/ CARD 1.CC ENTER TITLE (MAXIMUM OF 48 CHARACTERS).C
CWRITE (5,5010)
READ (5,5015) (TITLE(I5015), 15015=1,6)CCC /C/ CARD 2.CC ENTER COMPARTMENT TEMPERATURE (F), PRESSURE (PSIA), ANDC VOLUME (FT**3).C
CWRITE (5,5020)
READ (5,*) TC(l), PC(l), VOL(l)CCC /C/ CARD 3.CC ENTER AMBIENT TEMPERATURE (F), PRESSURE (PSIA), AND RELATIVEC HUMIDITY (%)C
C
C
WRITE (5,5030)
READ (5,*) TC(2), PC(2), RH
40
RH = RH/1.D2
IF (ITYPE.EQ.4 .OR. ITYPE.EQ.5) GO TO 10
WRITE (5,5040)
READ (5,*) ITYPE, TC(3), PC(3)
ENTER SOURCE TYPE (4=HF LIQUID, 5=HF VAPOR, 7=UF6 LIQUID WITH VAPORSOURCE TERM AND SOLIDS IGNORED IN HEAT BALANCE, -7=UF6 LIQUID WITHVAPOR PLUS SOLID SOURCE TERM, B=UF6 VAPOR), TEMPERATURE (F), ANDPRESSURE (PSIA--A NEGATIVE PRESSURE OR A LIQUID RELEASE DEFAULTSTO THE VAPOR PRESSURE CORRESPONDING TO THE SOURCE TEMPERATURE).
C
C
CCC /C/ CARD 4.CCCCCCC
CCC /C/ CARD 5.CCENTER UF6 MOLECULAR WEIGHT (A VALUE LESS THAN 100 DEFAULTS TOC 352.025) AND BASIS FOR FLASH (O=ISENTROPIC, 1=ISENTHALPIC).C
WRITE (5,5050)C
READ (5,*) MW, ISENC
C
C
IF (MW.LT.1.D2) GO TO 10
WMOL(9) = WMOL(9) - WMOL(6) + MWWHOL(6) = MWWHOL(7) = MWWHOL( B) = t1.J
10 CCNTINUECCC /C/ CARD 6.CC ENTER MASS OF SOURCE TERM (LB).C
CWRITE (5,5060)
READ (5,*) SOURCECCC /C/ CARD 7.CC ENTER OUTPUT BASIS (l=CLOSED Cct1PARTMENT, 4=OPEN Cct1PARTMENT WITHC FINAL PRESSURE EQUAL TO AMBIENT PRESSURE).
41
c
cWRITE (5,5070)
READ (5,*) IWRITEcC***********************************************************************CC BATCH ANALYSISC ==============C
WRITE (6,6000) (TITLE( 16000) , 16000=1,6)CC EVALUATE INITIAL CONDITIONS.C
CALL HUMID(2, RH, RATIO)C
WRITE (6,6010)WRITE (6,6020) TC(2)WRITE (6,6030) PC(2)WRITE (6,6040) RH, RATIO
CCALL ROOM(l, RATIO)
CWRITE (6,6050)WRITE (6,6020) TC(l)WRITE (6,6030) PC(1)WRITE (6,6060) VOL(l)
CDO 20 120=1,9
CIF (MASS(1,I20).GT.0.DO) WRITE (6,6070) NAME(I20),
* MASS(1,I20)C
20 CONTINUECC El~LUATE SOURCE TERM.C
C
C
C
C
C
IF (ITYPE.EQ.4) WRITE (6,6090)IF (ITYPE.EQ.5) WRITE (6,6100)IF (IABS(ITYPE).EQ.7) WRITE (6,6110)IF (ITYPE.EQ.8) WRITE (6,6120)
WRITE (6,6020) TC(3)
CALL STERM(3, 1, SOLIDS)
IF (ITYPE.EQ.5.0R.ITYPE.EQ.8) WRITE (6,6030) PC(3)WRITE (6,6130) SOURCE
IF (IABS(ITYPE).EQ.7.0R.ITYPE.EQ.8) WRITE (6,6140) WHOL(6)
IF (IABS(ITYPE).EQ.7.AND.ISEN.EQ.0) WRITE (6,6150)IF (IABS(ITYPE).EQ.7.AND.ISEN.EQ.1) WRITE (6,6160)IF (ITYPE.EQ.8.Ar~D.ISEN.EQ.0) WRITE (6,6170)
C
C
C
C
C
42
IF (ITYPE.EQ.8.AND.ISEN.EQ.1) WRITE (6,6180)
IF (ITYPE.EQ.7) WRITE (6,6190) SOLIDS
IF (IABS(ITYPE).EQ.7) WRITE (6,6200) TC(3)IF (ITYPE.EQ.8) WRITE (6,6210) TC(3)
DO 30 130=1,9
IF (MASS(3,I30).GT.0.DO) WRITE (6,6070) NAME(I30),* MASS(3,I30)
30 CONTINUECC EVALUATE CLOSED COMPARTMENT FINAL CONDITIONS.C
CALL COMPRT(l, INOUT, INODES)C
IF (IWRITE.EQ.1) GO TO 40CC EVALUATE OPEN COMPARTMENT FINAL CONDITIONS.C
CALL MIXFLW(4, 1, INODES)C
40 CONTINUEC
C
C
C
C
C
c
C
c
C
IF (IWRITE.EQ.1) WRITE (6,6220)IF (IWRITE.EQ.4) WRITE (6,6230)
WRITE (6,6020) TC(IWRITE)WRITE (6,6030) PC(IWRITE)WRITE (6,6060) VOL(IWRITE)
MSSTOT = O.DO
DO 50 150=1,9
MSSTOT = MSSTOT + MASS(IWRITE,150)
IF (MASS(IWRITE,I50).GT.0.DO) WRITE (6,6070) NAME(150),* MASS(IWRITE,I50)
50 C~~TINUE
DENS = MSSTOT/VOL(IWRITE)
WRITE (6,6240) DENS
STOPCc***********************************************************************cC FORMAT STATEMENTSC =================
C5000 FORMAT (II, 41H
* II)
43
WARNING: OUTPUT APPEARS IN FOR06.DAT,
C5010 FORMAT (' ENTER TITLE (MAXIMUM OF 48 CHARACTERS).')
C5015 FORMAT (6A8)
C5020 FORMAT (46H ENTER COMPARTMENT TEMPERATURE (F), PRESSU,
* 14HRE (PSIA), AND, I, 20H VOLUME (FT**3).)C5030 FORMAT (46H ENTER AMBIENT TEMPERATURE (F), PRESSURE (,
* 19HPSIA), AND RELATIVE, I, 17H HUMIDI~( (~»
C5040 FORMAT (46H ENTER SOURCE TYPE (4=HF LIQUID, 5=HF VAPO,
* 2HR" 24H 7=UF6 LIQUID WITH VAPOR, I, llH SOURCE,* 16H TERM AND SOLIDS, 28H IGNORED IN HEAT BALANCE, -7,* 16H=UF6 LIQUID WITH, I, 10H VAPOR, 10H PLUS SOLI,* 49HD SOURCE TERM, 8=UF6 VAPOR), TEMPERATURE (F), AND,* I, 46H PRESSURE (PSIA--A NEGATIVE PRESSURE OR A ,* 6HLIQUID, 17H RELEASE DEFAULTS, I, 14H TO THE VA,* 12HPOR PRESSURE, 32H CORRESPONDING TO THE SOURCE TEM,* 10HPERATURE).)
C5050 FORMAT (46H ENTER UF6 MOLECULAR WEIGHT (A VALUE LESS ,
* 20HTHAN 100 DEFAULTS TO, I, 17H 352.025) AND,* 16H BASIS FOR FLASH, 24H (O=ISENTROPIC, l=ISENTH,* 7HALPIC).)
C5060 FORMAT (36H ENTER MASS OF SOURCE TERM (LB).)
C5070 FORMAT (46H ENTER OUTPUT BASIS (l=CLOSED COMPARTMENT,
* 24H 4=OPEN COMPARTMENT WITH, I, 17H FINAL PRESSU,* 11HRE EQUAL TO, 19H AMBIENT PRESSURE).)
C6000 FORMAT ('1 CASE:' ,6A8)
C6010 FORMAT ('- AMBIENT CONDITIONS',I,lH )
C6020 FORMAT (' TEMPERATURE
* 'DEG F')C
6030 FORMAT (' PRESSURE* 'PSIA')
, ,F13.3,5X,
, ,F13.3,5X,
C6040 FORMAT (' RELATIVE HUMIDITY ',2PFll.l,7X,
* '~' ,1,1H ,I,' WATER VAPOR MOIST AIR ',OPF15.5,* 3X,'MOLE/MOLE')
C6050 FORMAT ('0 INITIAL COMPARTMENT C~IDITIONS' ,1,1H )
C6060 FORMAT (' VOLUME ',Fl1.l,7X,
* 'FT**3',I,lH)C
44
6070 FORMAT (8X,~MASS OF ~ ,A8,11X,Fl1.1,7X,~LB~)
C6080 FORMAT (lH ,I,~ TOTAL ENTHALPY
* ~BTU~,I,lH )~ ,Fll .1 , 7X ,
C6090 FORMAT (~O SOURCE TERM: HF LI QU ID~ ,I , 1H )
C6100 FORMAT eo SOURCE TERM: HF VAPOR~,I,lH )
C6110 FORMAT (~O SOURCE TERM: UF6 LIQUID~,I,lH )
C6120 FORMAT (~o SOURCE TERM: UF6 VAPOR~ ,I ,1H )
C6130 FORMAT ( ~ TOTAL MASS OF SOURCE ~ ,Fll .1 ,7X ,
* ~LB~ ,1,1H )C6140 FORMAT (~ MOLECULAR WEIGHT ~ ,F13.3,5X,
* ~LB/LB MOLE~ ,1,1H )C
6150 FORMAT (~ BASIS FOR FLASHING OF LIQUID~,
* ~ ISENTROPIC~,I,lH )C
6160 FORMAT (~ BASIS FOR FLASHING OF LIQUID~,
* ISENTHALPIC~ ,1,1H )C6170 FORMAT (~
* ~
BASIS FOR EXPANSION OF VAPOR~,
ISENTROPIC~,I,lH )C6180 FORMAT (~ BASIS FOR EXPANSION OF VAPOR~,
* ~ ISENTHALPIC~,I,lH)
C6190 FORMAT (~ SOLID UF6 DUMPED ON FLOOR ~,F11.1,7X,
* ~LB~ ,I ,1HC6200 FORMAT (~ TEMPERATURE AFTER FLASHING ~,F13.3,5X,
* ~DEG F~,I,lH )C6210 FORMAT (~ TEMPERATURE AFTER EXPANSION~,F13.3,5X,
* ~DEG F~,I,lH )C
6220 FORMAT (~O FINAL CONDITIONS (CLOSED COMPARTMENT)~ ,1,1HC
6230 FORMAT (~O FINAL CONDITIONS (OPEN COMPARTMENT)~,I,lH )C
6240 FORMAT (~O DENSITY OF FINAL MIXTURE ~ ,F15.5,3X,* ~LB/FT**3~)
C
C***********************************************************************C
END
MODEL NUMBER SA 8A 12B 30B 48X 48Y
VALUE OF ICYL 1 2 3 4 5 6
DATA TOTM / 55.DO, 255.DO, 460.00, 5020.00, 21030.00, 27560.00/OATA TOTV /0.28400, 1. 31900, 2.3800, 26.00, 108.900, 142.7DO/DATA CYLO / 5.00, 8.00, 12.00, 29.00, 48.00, 48.00/OATA CYLL /24.9900, 45.3400, 36.3600, 68.0200, 103.9900, 136.2700/DATA HOLR /1.37500, 1.37500, 1.375DO, 9.00, 17.DO, 17.DO/DATA HOLO /0.375DO, 0.37500, 0.37500, 0.875DO, 0.87500, 0.875DO/
45
A.4 CYLIND - A Cylinder Release Model
C THIS PROGRAM CALCULATES THE MASS FLOW RATE FROM A UF6 CYCLINDERC TO THE SURROUNDINGS TI1ROIIGH EITHER A BREACH OR HOLE IN THEC CYLINDER OR THROUGH A PIGTAIL CONSISTING OF A KNOWN LENGTH OFC PIPE AND FIXTURES. THE PROGRAM AND ALL SUBROUTINES ARE WRITTENC IN DOUBLE PRECISION.CC***********************************************************************CC INITIAL STATEMENTSC ==================C
IMPLICIT REAL*8 (A-H,J-Z)CC COMMON BLOCKS TRANSFER INFORMATION ON THE STATE OF UF6 ANDC ON THE OPTIONS TO BE USED.C
COMMON /ICQMONI ISEN,IPIG,IBRCH,IGEXITCOMMON /CONCYL/ PCYL,TCYL,XVCYL,XLCYL,MWCOMMON /CONENT/ PENT,TENT,XVENT,XLENT,VNTBARCOMMON /GMTRY / PIGRAYCOMMON /CONIN / PIN,TIN,XVIN,XLINCOMMON /CONVOL/ PVOL,TVOL,XVOL,XLVOLCOMMON /PARAM / VOL,DELT,QCOMMON /MASS / MSFLRT,MIN,MTOTCOMM~1 /CYLIND/ DIACYL,LCYL,RHOLE,DHOLE,ALPHA,IVERTCOMMON /TRIPLEI TTRIPL,PTRIPL
CDIMENSION TITLE(16)DIMENSION PIGRAY(99,3),0~(99)
OIMENSION TOTM(6) ,TOTV(6) ,CYLO(6),CYLL(6) ,HOLR(6),HOLD(6)DIMENSION DWGNUM(4,4)
CC THE FOLLOWING OATA STATEMENTS PROVIOE OEFAULT VALUES FOR VARIABLESC REQUIREO BY THE SUBROUTINE LEVEL. THE USER MAY SPECIFY A COMPLETEC SET OF VALUES BY SPECIFYING ICYL = 0 THEN ENTERING THE REQUIREOC INFORMATION ON THE FOLLOWING LINE OF INPUT.CCCCC
CC ANY PROGRAM USING THE BREACH AND PIGTAIL SUBROUTINES OR THEC LIQUIO LEVEL ANO MASS/O~ERGY BALANCE SUBROUTINES USED HEREC MUST SUPPLY SIMILAR DATA AND TRANSFER BLOCK COMMON STATEMENTS.C
46
C READ STATEMENTSC ===============CCC /C/ CARD 1. READ TITLE (LIMITED TO 80 CHARACTERS).C
READ (20,2000) TITLECCC /C/ CARD 2.CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCC
READ FLASH BASIS, CYLINDER TYPE, CYLINDER ORIENTATION,AND NUMBER OF ELEMENTS IN RELEASE PATHWAY.
FLASH BASIS (ISEN)
o ISENTROPIC1 ISENTHALPIC
ISEN = 1 IS RECOMMENDED SINCE THE FLASHING PROCESS WASASSUMED TO BE ISENTHALPIC IN THE DERIVATION OF THECORRELATION USED IN THE SUBROUTINE PIPSYS FOR PRESSUREDROP IN A PIPE.
CYLINDER TYPE (ICYL)
o USER SPECIFIED1 TYPE SA CYLINDER2 TYPE SA CYLINDER3 TYPE 12B CYLINDER4 TYPE 30B CYLINDER (2.5 TON)5 TYPE 48X CYLINDER (10 TON)6 TYPE 48Y CYLINDER (14 T~~)
IF A NEGATIVE VALUE OF ICYL IS READ (-1, -2, -3, -4, -5,-6), THE USER MAY SUBSEQUENTLY SPECIFY A TOTAL MASS OF UF6DIFFERENT FROM THE DEFAULT VALUE (SEE CARD 4).
CYLINDER ORIENTATION (IVERT)
-1 CYLINDER STANDS ON END -- RELEASE FROM TOP ENDo CYLINDER LIES ON SIDE -- RELEASE FROM END1 CYLINDER STANDS ON END -- RELEASE FROM BOTTOM END
NUMBER OF ELEMENTS IN RELEASE PATHWAY (IPIG)
IF IPIG = 2, THE RELEASE PATHWAY IS A BREACH IN THECYLINDER. IF THE RELEASE PATHWAY IS A PIPING SYSTEM, IPIGIS GREATER 1HAN 2.
READ (20,*) ISEN, ICYL, It...'ERT, IPIGC
IF(ICYL.GE.-6.AND.ICYL.LE.6) GO TO 10c
47
WRITE (5,500) ICYLC
STOPC
10 CONTINUEC
IF (IABS(ICYL).GT.O) GO TO 20CCC ICI CARD 3.CCCCCC
-- USE THIS CARD ONLY IF ICYL = 0 --
READ MASS OF UF6 IN THE CYLINDER (LB); VOLUME (FT**3),INTERNAL DIAMETER (IN), AND INTERNAL LENGTH (IN) OF THECYLINDER; RADIUS FROM THE CYLINDER CENTERLINE TO THE VALVE(BREACH) (IN); AND THE VALVE (BREACH) DIAMETER (IN).
READ (20,*) MTOT, VOL, DIACYL, LCYL, RHOLE, DHOLEC
GO TO 30C
20 CCNrINUEC
MTOT =TOTM(IABS(ICYL»VOL =TOTV(IABS(ICYL»DIACYL = CYLD(IABS(ICYL»LCYL =CYLL(IABS(ICYL»RHOLE = HOLR(IABS(ICYL»DHOLE = HOLD(IABS(ICYL»
CCC ICI CARD 4. -- USE THIS CARD ONLY IF ICYL IS NEGATIVE -CC READ MASS OF UF6 IN CYLINDER (LB).C
CIF (ICYL.LT.O) READ (20,*) MTOT
30 CONTINUECCC IC/ CARD 5.CCCCCCCCCCC
READ PRESSURE (PSIA), TEMPERATURE (DEG F), LIQUID MASSFRACTION OF THE NONVAPOR FRACTION (--), MOLECULAR WEIGHT(LB/LB MOLE), AND THE ANGLE MEASURED FROM A VERTICAL VECTORPASSING THROUGH THE CENTER OF THE END AND A VECTOR FROM THECENTER OF THE END AND THE ENTRANCE TO THE RELEASE PATHWAY(DEG). IF PRESSURE IS SPECIFIED AS ZERO AND/OR TEMPERATUREIS SPECIFIED AS NONZERO, THEN THE PRESSURE WILL BE SET EQUALTO THE VAPOR PRESSURE. IF PRESSURE IS SPECIFIED AS NONZEROAND TEMPERATURE IS SPECIFIED AS ZERO, THEN THE EQUILIBRIUMTEMPERATURE CORRESPONDING TO THE SPECIFIED PRESSURE WILL BECALCULATED. IF THE TRIPLE POINT TEMPERATURE IS SPECIFIED(147.306561 DEG F), THEN A NONZERO VALUE FOR THE LIQUID MASS
CCCCCC
48
FRACTION OF THE NONVAPOR FRACTION CAN BE SPECIFIED;OTHERWISE, THE VALUE READ AS INPUT WILL BE SET BY THEPROGRAM TO THE APPROPRIATE VALUE. THE DEFAULT VALUE FORMOLECULAR WEIGHT IS 352.025 -- IF THIS VALUE IS ACCEPTABLE,A ZERO MAY BEPECIFIED FOR THIS VARIABLE.
READ (20,*) PVOL, TVOL, XLVOL, MW, ALPHACC CHECK SPECIFIED VALUES OF PVOL AND TVOL. TERMINATE EXECUTION IF ANC ERROR IS FOUND; OTHERWISE, CALCULATE THE APPROPRIATE VAPOR PRESSUREC OR EQUILIBRIUM TEMPERATURE.C
IF (PVOL.GE.O.DO.AND.TVOL.GE.O.DO.AND.(PVOLtTVOL).GT.O.DO)* GO TO 40
CWRITE(5,510) PVOL, TVOL
CSTOP
C40 CONTINUE
CIF (TVOL.GT.O.DO) CALL VPRUF6 (TVOL,PVOL)
CIF (TVOL.EQ.O.DO) CALL EQTUF6 (PVOL,TVOL)
CC SET THE TRIPLE POINT CONDITIONS AND CHECK THE VALUE OF THEC LIQUID/SOLID SPLIT.C
PTRIPL = 22.04226474DOC
TTRIPL =147.306561DOC
IF (TVOL.LT.TTRIPL) XLVOL = O.DOC
IF (TVOL.GT.TTRIPL) XLVOL = 1.DOC
IF (XLVOL.GE.O.DO.AND.XLVOL.LE.l.DO) GO TO 50C
WRITE (5,520) XLVOLC
STOPC
50 CONTINUEC
IF (MW.EQ.O.DO) MW = 352.025DOC
IF (IPIG.GT.2) GO TO 60CCC /C/ CARD 6. -- USE THIS CARD ONLY IF IPIG = 2 -CC READ AMBIENT PRESSURE (PSIA). A ZERO VALUE DEFAULTS TOC 14.7 PSIA.
49
CREAD (20,*) PAMB
CC SET UP ELEMENTS OF PIGRAY FOR A BREACH CALCULATION.C
C
C
C
C
CC
PIGRAY(l,l) = 1.00PIGRAY(1,2) = 0.500PIGRAY(1,3) = DHOLE/12.DO
PIGRAY(2,1) = 2.DOPIGRAY(2,2) = 1.DOPIGRAY(2,3) =14.7DO
IF (PAMB.GT.O.DO) PIGRAY(2,3) = PAMB
GO TO 80
60 CONTINUE
C /C/ CARD 7.CCCCCCCCCCCCCCCCCCCCCCCCCCCCCC
-- USE ONLY IF IPIG IS GREATER THAN 2 --
READ AS MANY CARDS AS THE VALUE OF IPIG TO SPECIFY THEPIPING SYSTEM. EACH CARD CONTAINS (1) A VALUE SPECIFYINGELEMENT TYPE, (2) ELEMENT LENGTH (FT) OR RESISTANCECOEFFICIENT (--), AND (3) DIAMETER (IN), EXCEPT FOR THE LASTCARD. THE THIRD VALUE ON THE LAST OF THE "CARD 7" CARDS ISTHE AMBIENT PRESSURE (PSIA).
ELEMENT TYPE (PIGRAY(I,1»
1 SPECIFIES A PIPE SEGMENT (EXCEPT FIRST -CARD 7" WHEREIT SPECIFIES THE ENTRANCE)
2 SPECIFIES A PIPING SYSTEM FEATURE (SUDDEN EXPANSI~~,
VALVE, BEND, ETC.) FOR WHICH A RESISTANCE COEFFICIENTIS SUPPLIED
3 SPECIFIES A SUDDEN CONTRACTION FOR WHICH A RESISTANCECOEFFICIENT IS SUPPLIED
RESISTANCE COEFFICIENT (PIGRAY(I,2»
THIS VALUE MUST BE CALCULATED BY THE USER.
DIAMETER (PIGRAY(I,3»
(NOTE: PIGRAY(IPIG,3) IS THE EXHAUST PRESSURE, PSIA.)
FOR A SUDDEN CONTRACTION, SPECIFY THE DOWNSTREAM DIAMETERFOI.LOW ING THE CONTRACTI ON . FOR A SUDDEN EXPANS ION, SPEC IFYTH.: UPSTREAM DIAMETER BEFORE THE EXPANS ION.
DO 70 170 ~ 1,IPIGC
50
READ (20,*) (PIGRAY(I70,I), 1=1,3)CC CONVERT DIAMETER FROM INCHES TO FEET FOR EACH ELEMENT OF THEC PIGTAIL WHICH HAS A DIAMETER VALUE.C
C
C
C
IF (I70.LT.IPIG) PIGRAY(I70,3) = PIGRAY(I70,3)/12.DO
70 CONTINUE
80 CONTINUE
PFIN = PIGRAY(IPIG,3)CCC IC/ CARD 8. READ SIMULATION TIME INTERVAL (SEC) AND MAXIMUMC SIMULATION TIME (SEC).C
READ (20,*) DELT, MAXTIMCCC IC/ CARD 9.CCCCCCCCCCCC
-- THESE CARDS ARE OPTIONAL --
ENTER DRAWING NUMBERS (LIMITED TO 20 CHARACTERS--THE LASTCHARACTER MUST BE A DOLLAR SIGN ($». THESE NUMBERS AREENTERED IN A FILE FOR CYLPLT PROCESSING.
1ST CARD 9 = PHASE MASSES AND TOTAL MASS OF UF6 INSIDECYLINDER
2ND CARD 9 = PHASE AND TOTAL MASS RELEASE RATES FROMCYLINDER
3RD CARD 9 = TEMPERATURE AND PRESSURE INSIDE CYLINDER4TH CARD 9 = EXHAUST TEMPERATURE
DO 90 190=1,4C
READ (20,2010,END=100) (DHGNL~(I90,I), 1=1,4)WRITE (31,2010) (DHGNUM(I90,I), 1=1,4)
C90 CONTINUE
C100 C~JTINUE
CWRITE(31,2020)
CC***********************************************************************CC INITIAL CONDITIONSC ==================CC DENUF6 WILL CALCULATE DENSITIES OF UF6 PHASES IN THE CYLINDERC
CALL DENUF6 (TVOL,PVOL,t1H,DENSOL,DENLIQ,DENVAP)
51
CC THE VAPOR MASS FRACTION IN THE CYLINDER CAN NOW BE DETERMINEDC
XVOL = (VOL/MTOT - XLVOL/DENLIQ - (l.DO-XLVOL)/DENSOL)* l(l.DO/DENVAP - XLVOL/DENLIQ - (l.DO-XLVOL)/DENSOL)
CC THIS ARGUMENT TO THE LEVEL SUBROUTINE SAVES PREVIOUS VALUES OFC LIQUID LEVEL FOR USE AS INITIAL GUESSES. IT IS INITIALLY SET EQUALC TO CYLINDER DIAMETER.C
VLFACE = DIACYLCC THIS DRIVER ROUTINE DOES NOT CONSIDER AN INLET STREAM TO THEC CYLINDER. THE LEVEL AND INTMEB SUBROUTINES ARE WRITTEN TOC HANDLE SUCH A STREAM. THEREFORE SET MASS OF THE STREAM TOC ZERO AND OTHER STREAM PARAMETERS TO MATCH THE CYLINDERC CCJ-ITENTS.C
MIN = O.DOC
PIN = PVOLC
TIN =TVOLC
XVIN = XVOLC
XLIN = XLVOLC
ITRIPL = 0CC SET TIME STEP AND HEAT TRANSFERC
DELTSM = O.DOC
Q = O.DOC
WRITE (30,3000) TITLEC
WRITE (30,3010)C
WRITE (22,2200) DELTC
C***********************************************************************CC TRANSIENT ANALYSISC ==================C
110 CONTINUECC FROM THIS POINT ON THE PROGRAM SOLVES EACH TIME STEP USINGC VALUES FROM THE PREVIOUS STEP AI\ID FROM THE MASS AI\ID ENERGYC BALANCE ABOUT THE CYLINDER. STARTING VALUES FOR THE STREAMC LEAVING THE CYLINDER DURING THE COMING TIME STEP ARE INPUT ANDC THE LEVEL SUBROUTINE IS CALLED IF NEEDED TO MODIFY THESE
52
C PARAMETERS AS REQUIRED. TCYL IS ALWAYS EQUAL TO TVOL, BUTC XVCYL, XLCYL, AND PCYL MAY BE CHANGED AS THE VAPOR/LIQUIDC INTERFACE DROPS.C
XVCYL =1.DOC
XLCYL = XLVOLC
PCYL = PVOLC
TCYL =TVOLCC PHASE INTERFACE LEVELC =====================C
IF (IVERT.NE.-l) CALL LEVEL (DENVAP,VLFACE)CC BREACH FLOW RATE ANALYSISC =========================CC THE BREACH SUBROUTINE CALCULATES A MASS VELOCITY AND A SET OFC CONDITIONS FOLLOWING THE ENTRANCE PRESSURE DROP. THOSEC CONDITIONS ARE TRANSFERRED TO PIPSYS IF THE PIGTAILC SUBROUTINE IS CALLED.C
IF (DELTSM.GT.O.DO .AND. IPIG.GT.2) GO TO 120C
CALL BREACH (G)CC THE BREACH SUBROUTINE HAS CALCULATED A MAXIMUM VALUE OF MASSC VELOCITY.C
IF(IPIG.EQ.2) GO TO 130CC PIPING SYSTEM FLOW RATE ANALYSISC ================================CC THE PIGTAIL SUBROUTINE CALCULATES NEW VALUES OF G FOR RELEASESC OF UF6 THROUGH PIGTAILS CONSISTING OF LENGTHS OF PIPE ANDC FIXTURES SUCH AS ELBOWS AND VALVES.C
120 CONTINUEC
CIF (TCYL.EQ.TTRIPL .AND. XVCYL.EQ.1 .AND. ITRIPL.EQ.l) GO TO 130
CALL PIPSYS (G)CC SET BASIS FOR SUBSEQUENT EVALUATIONS OF G IN PIPSYS.C
IBRCH = 3CC SET FLAG FOR SKIPPING CALL TO PIPSYS.C
ITRIPL = 0
53
CIF (TCYL.EQ.TTRIPL .AND. XVCYL.EQ.1.DO) ITRIPL = 1
C130 CONTINUE
CC OUTPUT DATAC ===========CC PHASE COMPOSITION INSIDE CYLINDERC
MSOL = MTOT*(l.DO - XVOL)*(l.DO - XLVOL)MLIQ =MTOT*(l.DO - XVOL)*XLVOLMVAP =MTOT*XVOL
CC PHASE COMPOSITION ENTERING RELEASE PATHWAYC
PHASE = 'IF (XVCYL.EQ.1.DO) PHASE = ' VAPOR'IF (XVCYL.LT.l.DO.AND.XVCYL.GT.O.DO.AND.XLCYL.EQ.l.DO)
* PHASE = 'LIQ-vAP'IF (XVCYL.LT.1.DO.AND.XVCYL.GT.0.DO.AND.XLCYL.LT.1.DO.
* AND.XLCYL.GT.O.DO) PHASE = '3-PHASE'IF (XVCYL.EQ.0.DO.AND.XLCYL.EQ.1.DO) PHASE = 'LIQUID'IF (XVCYL.EQ.0.DO.AND.XLCYL.LT.1.DO.AND.XLCYL.GT.0.DO)
* PHASE = 'SOL-LIQ'CC CONDITIONS OF UF6 EXHAUSTED AT FINAL PRESSUREC
CALL FLASH (TVOL,PVOL,MW,XVCYL,XLCYL,PFIN,ISEN,XVFIN,XLFIN,TFIN)C
MSFLRT = G*(PIGRAY(1,3)**2)*3.14159DO/4.DO
MSSRTS =MSFLRT*(l.DO - XVFIN)*(l.DO - XLFIN)MSSRTL =MSFLRT*(l.DO - XVFIN)*XLFINMSSRTV =MSFLRT*XVFIN
CC BASIS FOR FLOW RATE CALCULATIONC
BASIS = 'CHOKE'IF (IPIG.EQ.2.AND.IBRCH.EQ.2) BASIS = ' PDC 'IF (IPIG.GT.2.AND.IGEXIT.EQ.2) BASIS = ' PDC '
CC OUTPUT TO TERMINAL FOR MONITORING PROGRESS OF PROGRAM EXECUTIONC
WRITE (5,530) DELTSM,MTOT,MSFLRTCC PROGRAM OUTPUTC
WRITE (30,3020) DELTSM,MSOL,MLIQ,MVAP,MTOT,TVOL,PVOL ,PHASE ,* PCYL,BASIS,MSSRTS,MSSRTL,MSSRiV,MSFLRT,PFIN,TFIN
CC OUTPUT TO DATA FILE FOR INPUT TO FODRFT OR INDRFTC
WRITE (22,2210) DELTSM,MSSRTS,MSSRTL,MSSRTV,TFIN,PFIN
54
CC CYL INDER INTERNAL MASS AND ENERGY BALANCEC =========================================C
CALL INTMEBC
DELTSM = DELTSM+DELTC
CALL DENUF6 (TVOL,PVOL,MW,DENSOL,DENLIQ,DEt~P)
CIF (TVOL.LT.TTRIPL .OR. MTOT.LT.(MSFLRT*DELT).OR.
* DELTSM.GE.MAXTIM) STOPC
GO TO 110CC***********************************************************************CC FORMAT STATEMENTSC =================C
500 FORMAT(' VALUE OF ICYL =1,13,* I NOT RECOGNIZED -- EXECUTION TERMINATED. I)
C
C
C
510 FORMAT ( I
***
520 FORMAT( I
* I
* I
PVOL =',F8.3,' AND TVOL =',F8.3,' NOT ALLOWED __ 1,/,
EITHER PVOL OR TVOL MUST BE GREATER THAN 0 __1,/,NEITHER PVOL OR TVOL CAN BE LESS THAN 0 __ 1,/,
EXECUTION TERMIt~TED./)
TRIPLE POINT SPECIFIED __ 1,/,
SPECIFIED VALUE OF XLVOL =',F6.2,' OUT OF BOUNDS __1,/,
EXECUTION TERMINATED/)
530 FORMAT (3F15.5)C
2000 FORMAT(16A5)C
2010 FORMAT (4A5)C
2020 FORMAT(4(lH$,/»C
2200 FORMAT (lPE15.7)C
2210 FORMAT (lPE15.7,' 0 0 0 0 0 ',3E15.7,' 0 ',2E15.7)C
3000 FORMAT(lHl,T22,/TITLE: ',16A5)C
3010 FORMAT(/O ******* CONDITI~~ OF UF6 IN C~~AINMENT/,
* I ******* PATHWAY INLET ********* CONDITION OF / ,* I UF6 EXHAUSTED **********1 ,/,T76,/FLOW' ,/,1 TIME *****1,* 1***** MASS (LB)/,* I ********** TEMP PRES RELEASE PRES RATE ****1 ,* I RELEASE RATE (LB/SEC) **** TEMP PRES/,/,' (SEC)/,* SOLID LIQUID VAPOR TOTAL (DEG F) (PSIA)',* PHASE (PSIA) BASIS SOLID LIQUID VAPOR TOTAL / ,
* (DEG F)
55
(PSIA) ~ ,I ,1H )C
3020 FORMAT(F7.0,1X,4FB.1,2FB.3,2X,A7,FB.3,2X,A5,1X,6FB.3)CC***********************************************************************C
END
A.5 COMPLT - A Plotting Program for FODRFT and INDRFT Results
C THIS PROGRAM PLOTS OUTPUT FROM FODRFT AND INDRFT.CC THIS PROGRAM USES DISSPLA (VERSION 9.0) SUBROUTINES FOR PLOTTING.C DISSPLA IS A PRODUCT OF INTEGRATED SOFTWARE SYSTEMS CORPORATION OFC SAN DIEGO, CALIFORNIA. DOCUMENTATION WAS COPYRIGHTED IN 19B1.CC***********************************************************************CC INITIAL STATEMENTSC ==================C
CIMPLICIT REAL*4 (A-H,J-Z)
DIMENSION TIME(1000), UTOT(1000), HFTOT(1000), DENU(1000),* DENHF(1000), T(1000), P(1000)
DIMENSION DWGNUM(6,4), NUMBER(4)CC***********************************************************************CC READ STATEMENTSC ===============C
IMAX = 0CC CODING BETWEEN 810 CONTINUE" AND "30 CONTINUE" READS AND DEVELOPSC DATA FOR PLOTTINGC
10 CONTINUEC
IMAX = IMAX + 1CC INPUT IS READ FROM AN ~FORMATTED OUTPUT FILE GENERATED BY EITHERC FODRFT OR INDRFT.C
C
C
C
READ (4B,*,END=30) TIME(IMAX), UTOT(IMAX), HFTOT(IMAX),* DENU(IMAX), DENHF(IMAX), T(IMAX), P(IMAX)
IF (DENU(IMAX).LT.1.E-20) DENU(IMAX) = 1.E-20IF (DENHF(IMAX).LT.1.E-20) DENHF(IMAX) = 1.E-20
IF (IMAX.GT.1) GO TO 20
DLtlAX = DENU(1)
56
DUMIN = DENU(l)C
DHFMAX = DENHF(l)DHFMIN = DENHF(l)
CTMAX =Hl)THIN = T(l)
cPMAX = P(1)PHIN = pel)
cGO TO 10
C20 CCNTINUE
CIF (DENU(IMAX).GT.DUHAX) DUMAX = DENU(IMAX)IF (DENU(IMAX).LT.DUMIN) DlttlN = DENU( lMAX)
c
c
c
c
c
IF (DENHF(IMAX).GT.DHFMAX) DHFMAX = DENHF(IMAX)IF (DENHF(IMAX).LT.DHFMIN) DHFMIN = DENHF(IMAX)
IF (T(IMAX).GT.TMAX) TMAX =T(IMAX)IF (T(IMAX).LT.TMIN) TMIN = T(IMAX)
IF (POMAX).GT.PMAX) PMAX = P(IMAX)IF (P(IMAX).LT.PMIN) PMIN = P(IMAX)
GO TO 10
30 CONTINUEcC READ DRAWING NUMBERS.C
C
C
C
C
C
C
C
C
DO 40 140=1,6
READ (49,4900) (DWGNUM(140,1), 1=1,4)
40 CONTINUE
lMAX = lMAX - 1
TIMMAX =TIME(IMAX)
UMAX =UTOT(IMAX)
HFMAX = HFTOT(IMAX)
DUMIN =AMAX1(DUMIN,5.07E-B)
DHFMIN =AMAX1(DHFMIN,6.24E-B)C
c***********************************************************************CC PLOTTING COMMANDS
57
C =================C
CALL COMPRSC
DO 80 180=1,6CC SET UP AXES.C
CALL RESET('ALL')CALL NOBRDRCALL GRACE (0.)CALL AREA2D(S.,S.)CALL FRAMECALL DUPLXCALL XREVTKCALL YREVTKCALL YAXANG(O.O)
C
C
C
CALL MXIALF('STANDARD','!')CALL MX2ALF('L/CSTD' ,'@')CALL MX3ALF('INSTRUCTION' ,'&')
CALL XINTAXCALL XNAME ('CUMULATIVE TIME OF TRANSIENT@ (SEC)!$' ,100)CALL AXSPLT (O.,TIMMAX,S.,XORIG,XSTEP,XAXIS)XMAX = XORIG + XSTEP*XAXIS
IF(I80.EQ.3.0R.180.EQ.4) GO TO SOCC PLOT LINEAR AXES FOR PLOTS 1, 2, S, AND 6.C
IF (l80. EQ.l)
* 100)IF (I80.EQ.l)
CIF (180.EQ.2)IF (l80 .EQ .2)
C
CALL YNAME ('CUMULATIVE URANIUM RELEASED@ (LB)!$',
CALL AXSPLT (0.,~1AX,5.,YORIG,YSTEP,YAXIS)
CALL YNAME ('CUMULATIVE HF RELEASED@ (LB)!$' ,100)CALL AXSPLT (O.,HFMAX,S.,YORIG,YSTEP,YAXIS)
IF (I80.EQ.S) CALL YNAME* ('TEMPERATURE IN COMPARTMENT@ (&EH.S@0&EXHX!F@)!$',100)
IF (180.EQ.S) CALL AXSPLT (TMIN,TMAX,S.,YORIG,YSTEP,YAXIS)C
IF (180.EQ.6) CALL YNAME ('PRESSURE IN COMPARTMENT@ (PSIA)!$',* 100)
IF (I80.EQ.6) CALL AXSPLT (PMIN,PMAX,5.,YORIG,YSTEP,YAXIS)C
YMAX = YORIG + YSTEP*YAXISC
CALL YINTAXCALL GRAF (XORIG,XSTEP,XMAX,YORIG,YSTEP,YMAX)
CGO TO 60
CSO CONTINUE
58
CC PLOT SEMI LOG AXES FOR PLOTS 3 AND 4.C
CALL YTICKS (0)CALL YAXEND ('NOENDS')CALL RESET ('YINTAX')CALL RESET ('YNAME')CALL GRAF (XORIG,XSTEP,XMAX,O,l,l)CALL RESET ('YAXEND')CALL YTICKS(l)
CIF (I80.EO.3) CALL ALGPLT (DUMIN,DUMAX,5.,YORIG,YCYCLE)IF (I80.EQ.3) CALL YLGAXS (YORIG,YCYCLE,5.,
* 'URANIUM CONCENTRATION IN COMPARTMENT@ (LB/FT&EH.8@3&EXHX@)!$',* 100,0,0)
CIF (I80.EO.4) CALL ALGPLT (DHFMIN,DHFMAX,5.,YORIG,YCYCLE)IF (I80.EQ.4) CALL YLGAXS (YORIG,YCYCLE,5.,
* 'HF CONCENTRATION IN COMPARTMENT@ (LB/FT&EH.8@3&EXHX@)!$',* 100,0,0)
C60 CONTINUE
CCALL THKCRV (0.05)CALL NOCHEK
CC PLOT 1. CUMULATIVE URANIUM RELEASED (LB) VS CUMULATIVE TIME OFC TRANSIENT (SEC).C
IF (I80.EO.l) CALL CURVE (TIME,UTOT,IMAX,O)CC PLOT 2. CUMULATIVE HF RELEASED (LB) VS CUMULATIVE TIME OF TRANSIENTC (SEC).C
IF (I80.EQ.2) CALL CURVE (TIME,HFTOT,IMAX,O)CC PLOT 3. URANI LIM CONCENTRATI ON IN COMPARTMENT (LB/FT**3) VSC CUMULATIVE TIME OF TRANSI ENT (SEC).C
IF (I80.EO.3) CALL CURVE (TIME,DENU,IMAX,O)CC PLOT 4. HF CONCENTRATION IN COMPARTMENT (LB/FT**3) VS CL~ULATIVE
C TIME OF TRANSIENT (SEC).C
IF (I80.EO.4) CALL CURVE (TIME,DENHF,IMAX,O)CC PLOT 5. TEMPERATURE IN COMPARTMENT (DEG F) VS CUMULATIVE TIME OFC TRANSIENT (SEC).C
IF (I80.EO.5) CALL CURVE (TIME,T,IMAX,O)CC PLOT 6. PRESSURE IN COMPARTMENT (PSIA) VS CUMULATIVE TIME OFC TRANS IENT (SEC).C
59
IF (I80.EQ.6) CALL CURVE (TIME,P,IMAX,O)CC DRAWING NUMBERS.C
DO 70 170=1,4C
C
C
C
C
C
C
NUMBER(I70)=DWGNUM(I80,I70)
70 CONTINUE
CALL HEIGHT (0.1)CALL MESSAG (NUMBER,lOO,3.2,5.1)
CALL ENDPL(O)
80 C(l>.lTINUE
CALL DONEPL
STOPCc***********************************************************************CC FORMAT STATEMENTSC =================C
4900 FORMAT (4AS)CC***********************************************************************C
END
A.6 CYLPLT - A Plotting Program for CYLIND Results
C THIS PROGRAM PLOTS OUTPUT FROM CYLIND.CC THIS PROGRAM USES DISSPLA (VERSION 9.0) SUBROUTINES FOR PLOTTING.C DISSPLA IS A PRODUCT OF INTEGRATED SOFTWARE SYSTEMS CORPORATION OFC SAN DIEGO, CALIFORNIA. DOCUMENTATION WAS COPYRIGHTED IN 1981.CC***********************************************************************CC INITIAL STATEMENTSC ==================C
IMPLICIT REAL*4 (A-H,J-Z)C
DIMENSION TIME(1000), MSOL(1000), MLIQ(1000), MTOT(lOOO),* TCYL(1000), PCYL(lOOO), MSSRTS(1000), MSSRTL(lOOO),* MSFLRT(1000), TFIN(lOOO), BSLNX(2), BSLNY(2), AX(2),* AY(2), BX(2), BY(2), CX(2), CY(2), DX(2), DY(2)
DIMENSION DWGNUM(4,4), NUMBER(4)C
60
C***********************************************************************CC READ STATEMENTSC ===============CC THE FOLLOWING DO LOOP BYPASSES HEADINGS IN THE INPUT FILE WHICH ISC THE PRIMARY CYLIND OUTPUT FILE.C
DO 10 110=1,6C
READ (30,3010) IDUMC
10 CONTINUEC
IMAX = 0CC CODING BETWEENC TO BE PLOTTED.C
20 C~TINUE
C
-20 CONTINUE" AND -40 CONTINUE- READS OR DEVELOPS DATA
IMAX = IMAX + 1C
READ (30,3020,END=40) TIME(IMAX), MSOL(IMAX), MLIQ(IMAX),* MTOT(IMAX), TCYL(IMAX), PCYL(IMAX), MSSRTS(IMAX),* MSSRTL(IMAX), MSFLRT(IMAX), PFIN, TFIN(IMAX)
CMLIQ(IMAX) = MSOL(IMAX) + MLIQ(IMAX)
CMSSRTL(IMAX) = MSSRTS(IMAX) + MSSRTL(IMAX)
CIF (IMAX.NE.1) GO TO 30
CTMIN = TFIN(IMAX)TMAX = TFIN(IMAX)
CGO TO 20
C30 CONTINUE
CIF (TFIN(IMAX).LT.TMIN) TMIN = TFIN(IMAX)IF (TFIN(IMAX).GT.TMAX) TMAX = TFlN( IMAX)
CGO TO 20
C40 CONTINUE
CC READ DRAWING NUMBERS.C
DO 50 150=1,4C
READ (31,3110 ) (DWGNUM(I50,I), 1=1,4)C
50 CONTINUE
61
CIMAX = IMAX - 1
CBSLNX(l) = O.BSLNX(2) = TIME(IMAX)BSLNY(l) = o.BSLNY(2) = o.
CC***********************************************************************CC PLOTTING COMMANDSC =================C
CALL COMPRSC
DO 160 1160=1,4CC SET UP AXES.C
CALL RESET ('ALL')CALL NOBRDRCALL GRACE (0.)CALL AREA2D(5.,5.)CALL FRAMECALL DUPLX
CCALL XREVTKCALL YREVTKCALL YAXANG(O.O)
CCALL MX1ALF('STANDARD' ,'!')CALL MX2ALF('L/CSTD' ,'@')CALL MX3ALF('INSTRUCTION' ,'&')
CCALL INTAXS
CCALL XNAME ('CUMULATIVE TIME OF TRANSIENT@ (SEC)!$' ,100)CALL AXSPLT (0.,TIME(IMAX),5.,XORIG,XSTEP,XAXIS)XMAX = XORIG + XSTEP*XAXIS
CIF (I160.NE.1) GO TO 60
CCALL YNAME ('MASS OF UF&LH.8@6&LXHX! IN CYLINDER@ (LB)!$' ,100)CALL AXSPLT (O.,MTOT(1),5.,YORIG,YSTEP,YAXIS)
CGO TO 90
C60 CONTINUE
CIF (I160.NE.2) GO TO 70
CCALL YNAME ('MASS RELEASE RATE OF UF&LH.8@6&LXHX@ (LB/SEC)!$' ,100)CALL AXSPLT (0.,MSFLRT(1),5.,YORIG,YSTEP,YAXIS)
c
62
GO TO 90C
70 Ce:t-JTINUEC
C
C
C
C
C
C
C
C
C
C
C
C
C
IF (I160.NE.3) GO TO SO
CALL YNAME (/UF&LH.S@6&LXHX! TEMPERATURE IN CYLINDER@* (&EH.5@0&EXHX!F@)!$' ,100)
CALL AXSPLT (TCYL(IMAX) ,'TCYL(1) ,5. ,YORIG,YSTEP,YAXIS)
GO TO 90
SO CCflITINUE
CALL YNAME (/UF&LH.S@6&LXHX! EXHAUST TEMPERATURE@* (&EH.5@0&LXHX!F@)!$' ,100)
IF (ABS(TMAX-TMIN).LT.l.) TMIN =FLOAT(IFIX(TMIN»IF (ABS(TMAX-TMIN).LT.l.) TMAX =FLOAT(IFIX(TMAX + 2.»
CALL AXSPLT (TMIN,TMAX,5.,YORIG,YSTEP,YAXIS)
90 Ce:t-JTINUE
~1AX =YORIG + YSTEP*YAXIS
CALL GRAF (XORIG,XSTEP,XMAX,YORIG,YSTEP,YMAX)
XFACT = (XMAX-XORIG)/5.YFACT = (YMAX-YORIG)/5.
CALL THKCRV (0.03)
CALL NOCHEK
IF (I160.NE.l) GO TO 100CC PLOT 1. MASS OF UF6 IN CYLINDER (LB) VS CUMULATIVE TIME OF TRANSIENTC (SEC).C
CALL CURVE (TIME,MTOT,IMAX,O)CALL RESET ('THKCRV/)
CCALL DOTCALL CURVE (TIME,MLIQ,IMAX,O)
CCALL CI-tmOTCALL CURVE (TIME,MSOL,IMAX,O)CALL RESET (/CHNDOT/)
CCALL SHDPAT (45350)CALL SHDCRV (BSLNX, BSl}IY, 2, TIME, MSOL, IMAX)CALL SHDPAT (135190)CALL SHDCRV (TIME, MSOL, IMAX , TIME, MLIQ, IMAX)
63
CALL SHDPAT (45590)CALL SHDCRV (TIME, MLIQ, IMAX , TIME, MTOT, IMAX)
CGO TO 110
C100 CONTINUE
CIF (I160.NE.2) GO TO 120
CC PLOT 2. MASS RELEASE RATE OF UF6 (LB/SEC) VS CUMULATIVE TIME OFC TRANSIENT (SEC).C
CALL CURVE (TIME,MSFLRT,IMAX,O)CALL RESET ('THKCRV')
cCALL DOTCALL CURVE (TIME,MSSRTL,IMAX,O)
CCALL CHNDOTCALL CURVE (TIME,MSSRTS,IMAX,O)CALL RESET ('CHNDOT')
CCALL SHDPAT (45350)CALL SHDCRV (BSLNX, BSLNY,CALL SHDPAT (135190)CALL SHDCRV (TIME, MSSRTS,CALL SHDPAT (45590)CALL SHDCRV (TIME, MSSRTL,
C110 CONTI NUE
CC LEGEND FOR PLOTS 1 AND 2.C
AX(l) = 2.5*XFACTAX(2) = 3.4*XFACTAY(1) = 4.90*YFACTAY(2) =AY(l)
CBX(l) = AX (1 )BX(2) =AX(2)BY(l) = 4.62*YFACTBY(2) =BY(1)
CCX(1) = AX (1 )CX(2) =AX(2)CY(1) = 4.34*YFACTCY(2) =CY(l)
CDX(l) =AX(l)DX(2) =AX(2)DY(1) = 4. 06*YFACTDY(2) = DY(1)
C
2, TIME, MSSRTS, IMAX)
IMAX , TIME, MSSRTL, IMAX)
IMAX , TIME, MSFLRT, IMAX)
CALL THKCRV (0.03)
64
CALL CURVE (AX, AY, 2, 0)CALL RESET (/THKCRV/)CALL CURVE (DX, DY, 2, 0)CALL DOTCALL CURVE (BX, BY, 2, 0)CALL CHNDOTCALL CURVE (CX, CY, 2, 0)
CCALL RESET (/CHNDOT/)
CCALL SHDPAT (45350)CALL SHDCRV (DX, DY, 2, CX, CY, 2)CALL SHDPAT (135190 )CALL SHDCRV (CX, CY, 2, BX, BY, 2)CALL SHDPAT (45590)CALL SHDCRV (BX, BY, 2, AX, AY, 2)
CCALL MESSAG (/UF&LH.B@6&LXHX! VAPOR$/,100,3.5,4.69)CALL MESSAG (/UF&LH.B@6&LXHX! LIQUID$/,100,3.5,4.41)CALL MESSAG (/UF&LH.B@6&LXHX! SOLID$/,100,3.5,4.13)
CGO TO 140
C120 CONTINUE
CIF (I160.NE.3) GO TO 130
CC PLOT 3. CURVE 1: TEMPERATURE IN CYLINDER (DEG F) VS CUMULATIVE TIMEC OF TRANSIENT (SEC).C
CALL CURVE (TIME,TCYL,IMAX,O)CC LEGEND FOR PLOT 3 (CURVE 1).C
AX(l) = 2.5*XFACTAX(2) = 3.4*XFACTAY(l) = 4.79*YFACT + YORIGAY(2) =AY(1)
CCALL CURVE (AX, AY, 2, 0)
CCALL MESSAG (/TEMPERATURE$/ ,100,3.5,4.72)
CC PLOT 3. CURVE 2: VAPOR PRESSURE OF UF6 IN CYLINDER (PSIA) VSC CUMULATIVE TIME OF TRANSIENT(SEC).C
CALL AXSPLT (PCYL(IMAX),PCYL(1),5.,YORIG,YSTEP,YAXIS)C
YMAX =YORIG + YSTEP*YAXISC
CALL YGRAXS (YORIG,YSTEP,YMAX,5.,/VAPOR PRESSURE OF* UF&LH.B@6&LXHX! IN CYLINDER@ (PSIA)!$/,-100,5.,O.)
CCALL CI-t-lDOT
65
CCALL CURVE (TIME,PCYL,IMAX,O)
CC LEGEND FOR PLOT 3 (CURVE 2).C
AY(l) = 4. 61*(YMAX-YORIG)/5. + YORIGAY(2) = AY(l)
CCALL CURVE (AX, AY, 2, 0)
CCALL MESSAG ('PRESSURE$',100,3.5,4.51)
CGO TO 140
C130 CONTINUE
CC PLOT 4. EXHAUST TEMPERATURE (DEG F) VS CL~ULATIVE TIME OF TRANSIENTC (SEC).C
CALL CURVE (TIME,TFIN,l~~V.~O)
cCALL MESSAG ('EXHAUST PRESSURE$' ,100,3.0,4.72)CALL MESSAG (' = $' ,100,3.0,4.51)CALL REALNO (PFIN,2,'ABL~','ABUT')
CALL MESSAG ('@ PSIA!$' ,100,'ABUT','ABUT')C
140 CONTINUECC DRAWING NUMBERS.C
DO 150 1150=1,4C
NUMBER(I150) = DWGNUM(I160,I150)C
150 CONTINUEC
CALL HEIGHT (0.1)CALL MESSAG (NUMBER, 100, 3.2, 5.1)
CCALL ENDPL(O)
C160 CONTINUE
CCALL DONEPL
CSTOP
CC***********************************************************************CC FORMAT STATEMENTSC =================C
3010 FORMAT (11)C
66
3020 FORMAT (F7.0,lX,2F8.1,8X,F8.1,2F8.3,25X,2F8.3,8X,3F8.3)C
3110 FORMAT (4A5)CC**********************************************~k***********************c
END
Appendix BLISTINGS OF SUBROUTINES
This appendix contains listings of all subroutines required by the main programs, FODRFT,INDRFT, BATCH, and CYLIND. These subroutines are arranged alphabetically by subroutinename. Several UF6 physical properties subroutines described in the text but not required by theaforementioned main programs are also included in this appendix. Table B.I is a summary ofSTOPs that may occur during execution of programs using these subroutines. Note that subroutinescalled by COMPLT and CYLPLT are DISSPLA version 9.0 subroutines.·
·For information on DISSPLA, contact Integrated Software Systems Corporation, 10505 Sorrento Valley Road, SanDiego, CA, 92121.
Table B.l. Causes for program termination
STOP Subroutine Cause
STOPOI COMPRT 100 iterations without temperature-enthalpyconvergence in compartment
STOP02 INTMEB New estimate of temperature inside cyclinderexceeds 250°F (upper limit based on DOEregulations, see Table 8) or is less thanthe triple point when UF6 condensate isknown to be liquid
STOP03 INTMEB 20 iterations without temperature-enthalpyconvergence; UF6 condensate is liquid
STOP04 INTMEB 20 iterations without temperature-enthalpyconvergence; UF6 condensate is solid
STOP05 INTMEB New estimate of temperature inside cyclinderis less than O°F (arbitrary lower limit)or is greater than the triple point whenUF6 condensate is known to be solid
STOP06 LEVEL 100 iterations without convergence on UF6
vapor-liquid interface level (not bounded)
STOP07 LEVEL 100 iterations without convergence on UF6
vapor-liquid interface level (bounded)
STOPII LEVEL UF6 solid-vapor interface level above hole
STOP12 LEVEL HF-H20 equilibrium partitioning did notconverge in 100 iterations
STOP13 PIPSYS Pressure drop-pipe length calculation did notconverge within 100 iterations
STOP14 PIPSYS Pressure drop calculation across a contractiondid not converge within 100 iterations
STOP15 STERM ITYPE (release type identifier) not recognized
67
68
B.1 BREACH
SUBROUTINE BREACH (G)
INPUT VARIABLES, VALUES PROVIDED BY CALLING PROGRAM.
INTERNAL VARIABLES, USED ONLY IN BREACH AND ITS SUBROUTINES.
EPSLN IS A CONVERGENCE CRITERION ALSO SET HERE AND PASSEDTHROUGH THE LABELED BLOCK COMMON /CNSTNT/.
ALPHA, BETA, DELTA, GAMMA ARE CONSTANTS USED IN DIFFERENTFORMS OF THE BASIC PRESSURE DROP EQUATION RELATING CHANGEIN PRESSURE TO MASS VELOCITY AND TO SPECIFICVOLUME. THEY ARE SET IN BREACH AND PASSED TO THE CALLINGPROGRAM FOR USE IN OTHER SUBROUTINES THROUGH THE LABELEDBLOCK COMMON /CNSTNT/.
INTERMEDIATE PRESSURE, PRESSURE-DROP-CONTROLLEDFLOW, PSIAINTERMEDIATE TEMPERATURE, PDC FLOW, DEGREES FVAPOR MASS FRACTI~~ AT INTERMEDIATE CONDITIONSIN PDC FLOWMASS FRACTION OF THE NON-VAPOR PHASE WHICH ISLIQUID AT INTERMEDIATE CONDITIONS IN PDC FLOW
INDEX FOR CONSTANT ENTROPY/CONSTANT ENTHALPYISEN=O, ASSUME CONSTANT ENTROPY FLASHISEN=l, ASSUME CONSTANT ENTHALPY FLASH
NUMBER OF ELEMENTS IN RELEASE PAT~Y:
IPIG=2, PATHWAY IS A BREACH OR HOLE.IPIG>2, PATHWAY IS A PIPE AND FIXTURE SYSTEM.
ARRAY OF VALUES DESCRIBING THE RELEASE PATHWAY.EACH PATHWAY ELEMENT CORRESPONDS TO ONE ROW OFTHE ARRAY. SPECIAL VALUES INCLUDEPIGRAY(IPIG,3), THE AMBIENT PRESSURE IN PSIA.PIGRAY IS MORE FULLY DESCRIBED IN THECALLING PROGRAM AND INPUT DATA FILES.PRESSURE OF MASS ENTERING RELEASE PATHWAY, PSIATEMPERATURE OF MASS ENTERING PATHWAY, DEGREES FPRESSURE IN PSIA AND TEMPERATURE IN DEGREES F,RESPECTIVELY, FOR THE TRIPLE POINT CONDITION,INPUT FROM THE CALLING PROGRAMVAPOR MASS FRACTION ENTERING PATHWAYMASS FRACTION OF THE NON-VAPOR MASSWHICH IS LIQUID ENTERING PATHWAYMOLECULAR WEIGHT OF UF6, LB MASS/LB-MOLE
XLI NT
IPIG
ISEN
PINT
PI GRAY
XVCYLXLCYL
TINTXVINT
PCYLTCYLPTRIPL,TTRIPL
CC THIS SUBROUTINE CALCULATES THE MASS VELOCITY, IN UNITS OF LBS/SEC/C FT**2, OF UF6 ESCAPING FROM A VESSEL THROUGH A BREACH OR HOLE IN THEC VESSEL WALL. THE INSIDE TEMPERATURE (DEG F) AND PRESSURE (PSIA), THEC OUTSIDE PRESSURE (PSIA), AND THE INITIAL MASS FRACTIONS OF VAPOR,C LIQUID, AND SOLID UF6 ARE KNOWN. THE MASS VELOCITY IS CALCULATED.CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCC
69
* * * * * * * * * * * * * * * * * * * * * * * * * * * * * ** NOTE! PRESSURE-DROP-CONTROLLED MASS VELOCITY (PDC G) ** IS A FUNCTION OF CONDITIONS IN THE CYLINDER, ** INTERMEDIATE CONDITIONS, AND AMBIENT CONDITIONS. ** CHOKED FLOW G IS DETERMINED BY MATCHING CRITERIA FOR ** PDC G FROM CYLINDER CONDITIONS TO THE CHOKED FLOW ** CONDITIONS WITH THE CHOKED FLOW EQUATION, WHICH ** RELATES MAXIMUM G TO THE DERIVATIVE OF PRESSURE WITH ** RESPECT TO SPECIFIC VOLUME AT CHOKED FLOW CONDITIONS. ** THE SMALLER VALUE, PDC G OR CHOKED FLOW G, IS THEN ** OUTPUT AS THE BREACH MASS VELOCITY. ** * * * * * * * * * * * * * * * * * * * * * * * * * * * * *
MASS VELOCITY THROUGH THE HOLE, LB MASS/S/FT**2
TEMPERATURE IN DEGREES F CORRESPONDING TO THEINTERMEDIATE OR CHOKED FLOW CONDITIONSPRESSURE IN PSIA CORRESPONDING TO THEINTERMEDIATE OR CHOKED FLOW CONDITIONSVAPOR MASS FRACTION AT Ti, PiMASS FRACTION OF THE NON-vAPOR PHASE AT Ti, PiWHICH IS LIQUIDSPECIFIC VOLUME AT Ti, Pi
DENSITIES OF VAPOR, LIQUID, AND SOLID,RESPECTIVELY, AT INTERMEDIATE CONDITIONS,LB MASS/FT**3SPECIFIC VOLUME OF MASS IN RELEASE PATHWAY ATINTERMEDIATE CONDITIONS, FT**3/LB MASSINTEGER VARIABLE WHICH CONTROLS PROGRAM FLOWUPPER AND LOWER LIMITS ON PRESSURE IN PSIAFOR INTERVAL HALVING SEARCH TECHNIQUEPRESSURE IN PSIA ONLY SLIGHTLY LOWER THANTHE CHOKED FLOW PRESSURE. THE SMALL PRESSUREDIFFERENCE AND THE CORRESP~~DING SMALLDIFFERENCE IN SPECIFIC VOLUME ARE USED TOAPPROXIMATE THE DERIVATIVE OF PRESSURE WITHRESPECT TO SPECIFIC VOLUME AT CHOKED FLOWCONDITIONS.TEMPERATURE IN DEGREES F CORRESPONDING TO P2VAPOR MASS FRACTION CORRESPONDING TO P2MASS FRACTION OF THE NON-VAPOR PHASE WHICH ISLIQUID AT P2, T2SPECIFIC VOLUME IN FT**3/LB MASS CORRESPONDINGTO P2CHOKED FLOW MASS VELOCITY, LB MASS/S/FT**2,EVALUATED AT CURRENT GUESS FOR Pi, Ti CONDITIONSPRESSURE IN PSIA PREDICTED WHEN CHOKED FLOW MASSVELOCITY IS USED IN PDC FLOW EQUATION BETWEENCYLINDER CONDITIONS AND Pi, Ti CONDITIONS. WHENGMAX CORRESPONDS TO Pi, Ti CONDITIONS, PCHECKEQUALS Pi.
ViBAR
G
Pi
V2BAR
GMAX
PCHECK
XViXLi
RHOVI,RHOLI,RHOSI
VIBAR
Ti
ICHECKPUPPER,
PLOWERP2
T2XV2XL2
CCCCCCCCCCCCCCCCCCCCCCCCCCCCCC OUTPUT VARIABLES, VALUES SET BY BREACH FOR CALLING PROGRAM.CCCCCCCCCCCCCCCCCCCCCCCC
70
INDEX OUTPUT CHARACTERIZING BREACH MASS VELOCITY=1, CHOKED FLOW CONTROLS THE MASS VELOCITY=2, PDC FLOW CC~TROLS THE MASS VELOCITY
IBRCHCCCCC THIS SUBROUTINE IS WRITTEN IN DOUBLE PRECISION. ALL INTEGER VARIABLEC NAMES START WITH II'.C
IMPLICIT REAL*8 (A-H,J-Z)CC NAMED COMMON BLOCKS TRANSFER MOST INPUTS FROM THE CALLING PROGRAM ANDC MOST OUTPUTS CALCULATED BY THE BREACH SUBROUTINE.C
COMMON IICOMON/ ISEN, IPIG, IBRCH, IGEXITCOMMON IGMTRY I PIGRAYCOMMON ICONCYLI PCYL,TCYL,XVCYL,XLCYL,MWCOMMON ICONENTI Pl,Tl,XV1,XL1,V1BARCOMMON ICNSTNTI ALPHA, BETA, DELTA, GAMMA,EPSLNCOMMON ITRIPLEI TTRIPL,PTRIPL
CC AN ARRAY IS DIMENSIONED WHICH CONTAINS DESCRIPTIVE VALUES FOR THEC RELEASE PATHWAY, MODELED AS AN INFINITESIMAL LENGTH BETWEEN ENT~~CE
C AND EXIT PRESSURE LOSSES.C
DIMENSION PIGRAY(99,3)CC FOUR RELATED CONSTANTS ARE USED IN THE VARIOUS PRESSURE DROPC CORRELATIONS.C
ALPHABETADELTAGAt11A
=4633.100=ALPHA*4.DO/3.DO=ALPHA*2.DO=ALPHA*4.DO
CC DEFINE A SMALL NUMBER FOR CONVERGENCE TOLERANCE.C
EPSLN = 1.D-6(;
C AN INTERMEDIATE PRESSURE INSIDE THE BREACH IS CALCULATED.C
PINT = (PCYL*2.DO+PIGRAY(IPIG,3))/3.DOCC IN THE PRESENCE OF LIQUID, THIS INTERMEDIATE PRESSURE MUST BEC AT OR ABOVE THE TRIPLE POINT. ADJUST PINT UPWARD IF NECESSARY.C
IF (XVCYL.NE.l.DO.AND.* XLCYL.NE.O.DO.AND.* PINT.LT.PTRIPL) PINT = PTRIPL
CC AT THIS PRESSURE A FLASH CALCULATION IS MADE TO DETERMINE THEC INTERMEDIATE TEMPERATURE AND MASS FRACTIONS.r"
CALL FLASH (TCYL,PCYL,MW,XVCYL,XLCYL,PINT,ISEN,* XVINT,XLINT,TINT)
C
71
C CALCULATE THE INTERMEDIATE SPECIFIC VOLUME.CC THE DENSITIES OF EACH PHASE ARE REQUIRED.C
CALL DENUF6 (TINT,PINT,MW,RHOSI,RHOLI,RHOVI)C
VIBAR =XVINT/RHOVI+(l.DO-XVINT)*XLINT/RHOLI* +(l.DO-XVINT)*(l.DO-XLINT)/RHOSI
CC CALCULATE THE MASS VELOCITY LIMITED BY PRESSURE DROP.C
G = SQRT(DELTA*(PCYL-PIGRAY(IPIG,3))/l.5DO/VIBAR)CC THE t1ASS VELOCITY MIGHT BE LIMITED BY CHOKED FLOW. EQUATION 119 MAYC BE USED TO EVALUATE THE CHOKED FLOW MASS VELOCITY. USE THEC INTERMEDIATE CONDITIONS AS FIRST GUESSES FOR THE CHOKED FLOWC CONDITIONS. ONCE THE CHOICE BETWEEN PDC FLOW AND CHOKED FLOW ISC MADE, THE STORAGE LOCATIONS FIRST DEFINED HERE WILL BE UPDATED WITHC THE CORRECT BREACH CONDITIONS FOR OUTPUT TO THE CALLING PROGRAM.C
T1PiXViXL1V1BAR
=TINT= PINT= XVINT= XLINT= \,,JI BAR
CC THE ITERATION BELOW CLOSES TO A VALUE OF P1 EQUAL TO PCHECK. THEC METHOD USED IS CHANGED AS REQUIRED FROM DIRECT SUBSTITUTION TOC INTERVAL HALVING TO REGULA FALSI. THE FOLLOWING PARAMETERS AREC INITIALIZED FOR BOOKKEEPING IN THE ITERATION.CC INDICES FOR PROGRAM LOGIC CONTROLC
ICHECK = 0IPLUS = 0
CC UPPER AND LOWER BOUNDS ON PRESSURE FOR INTERVAL HALVING.C
CCALL VPRUF6 (TCYL, PCYLEQ)
PUPPER = PCYLEQPLOWER = O.DO
CC UPPER AND LOWER BOUNDS ON PRESSURE FOR REGULA FALSI.C
PUCHK =O.DOPLCHK =O.DO
C10 CONTINUE
CC THE PROGRAM BEGINS THE DETERMINATION OF GMAX, THE CHOKED FLOW MASSC VELOCITY, BY SETTING A SMALL (APROXIMATELY INFINITESIMAL) PRESSUREC DIFFERENCE, STARTING FROM THE MOST RECENT GUESS FOR THE CHOKED FLOWC PRESSURE.
72
CP2 =Pl-l.D-3
CC AT THIS PRESSURE A FLASH CALCULATION IS MADE TO DETERMINE THEC DIFFERENTIAL TEMPERATURE AND MASS FRACTIONS.CC FLASH BASIS FOR CHOKE FLOW CONDITION IS ISENTROPIC.C
ISNGMX = 0C
CALL FLASH (Tl,Pl,MW,XV1,XL1,P2,ISNGMX,XV2,XL2,T2)CC CALCULATE THE DIFFERENTIAL SPECIFIC VOLUME. THE DENSITIES OF EACHC PHASE ARE REQUIRED.C
CALL DENUF6 (T2,P2,MW,RHOS2,RHOL2,RHOV2)C
V2BAR =XV2/RHOV2+(1.DO-XV2)*XL2/RHOL2* +(1.DO-XV2)*(1.DO-XL2)/RHOS2
CC THE CHOKED FLOW MASS VELOCITY CORRESPONDING TO THE LATEST GUESSES FORC CHOKED FLOW TEMPERATURE AND PRESSURE IS CALCULATED.C
GMAX = SQRT(ALPHA*(PI-P2)/(V2BAR-VIBAR»CC A CHECK IS REQUIRED TO SEE IF THE GUESSED PRESSURE FOR CHOKED FLOWC CORRESPONDS TO THE PDCPRESSURE CALCULATED USING GMAX, THE CYLINDERC PRESSURE, AND THE SPECIFIC VOLUME AT THE GUESSED PRESSURE. WHEN THEC GUESSED PRESSURE AND THE PDC PRESSURE DIFFER BY LESS THAN SOMEC TOLERANCE CRITERION, THE CLCULATION OF GMAX IS COMPLETE.C
PCHECK = PCYL-(GMAX**2.DO*V1BAR/GAMMA)C
IF (PCHECK.GT.PCYLEQ) PCHECK = PCYLEQC
IF (DABS(PCHECK-P1).LT.(100.DO*EPSLN)* .OR.DABS(PUPPER-P1).LT.(EPSLN» GO TO 40
CC IF THE MAXIMUM MASS VELOCITY FOR CHOKED FLOW IS NOT COMPATIBLE WITHC THE PREVIOUSLY CALCULATED CHOKED FLOW CONDITIONS, AN ITERATION ISC NECESSARY TO FIND THE ACTUAL CHOKED FLOW CONDITIm~S OF PRESSURE,C TEMPERATURE, AND MASS VELOCITY.C
IF (PCHECK.GT.Pl) GO TO 20C
ICHECK =1C
C
C
C
IF (PCHECK.GT.O.DO.AND.PLCHK.GT.O.DO) ICHECK = 3
20 CONTINUE
IF (ICHECK.GT.O) GO TO 60
PLOWER = P1
73
PLCHK = PCHECKPi = PCHECK
C30 CONTINUE
CCALL FLASH (TCYL,PCYL,MW,XVCYL,XLCYL,Pl,ISEN,XV1,XL1,Tl)
CCALL DENUF6(Tl,Pl,MW,RHOS1,RHOLi,RHOV1)
CV1BAR =XV1/RHOV1+(1.DO-XV1)*XLl/RHOLl
* +(1.DO-XV1)*(1.DO-XL1)/RHOSlC
GO TO 10C
40 C~TINUE
CC NOW THAT THE CHOKED FLOW MASS VELOCITY HAS BEEN CALCULATED THE LOWERC OF THE TWO VALUES FOR MASS VELOCITY WILL BE RETURNED TO THE CALLINGC PROGRAM.C
IF (GMAX-G) 50,120,120C
50 CONTINUECC CHOKED FLOW CONTROLS THE MASS VELOCITY. THE CHOKED FLOW CONDITIONSC ARE THE INTERMEDIATE CONDITIONS, SO Pi, ETC., NEED NOT BE CHANGED.C
G = GMAXC
IBRCH =1C
GO TO 130C
60 CONTINUEC
IF (ICHECK.GT.l) GO TO 70C
PUPPER = PiPUCHK = PCHECK
CPi = (PUPPER+PLOWER)/2.DO
CICHECK =2
CGO TO 80
C70 CONTINUE
CIF (I CHECK. GT. 2) GO TO 90
CPLOWER =PiPLCHK =PCHECK
CPi = (PLOWER+PUPPER)/2.DO
74
C80 CONTINUE
CGO TO 30
C90 CONTINUE
CIF (P1.GT.PCHECK) GO TO 100
CPLOWER =PiPLCHK = PCHECK
CIF (ICHECK.EQ.4) IPLUS =1
CICHECK =4
CGO TO 110
C100 CONTINUE
CPUPPER =PiPUCHK = PCHECK
C110 CONTINUE
CPi = (PUPPER*PLCHK-PLOWER*PUCHK)
* /(PUPPER+PLCHK-PLOWER-PUCHK)c
P1PLUS = 2.DO*P1-PLOWERC
IF (IPLUS.EQ.1.AND.P1PLUS.LT.PUPPER) Pi = P1PLUSC
IPLUS = 0C
GO TO 30C
120 CONTINUECC PDC FLOW CONTROLS THE MASS VELOCITY. THE INTERMEDIATE CONDITIONS AREC THE BREACH CONDITIONS. Pi, ETC., ARE RESET FOR OUTPUT.C
T1 = TINTP1 = PINTXVi =XVINTXLi = XLINTV1BAR =VIBAR
CIBRCH = 2
C130 CONTINUE
RETURNEND
75
D.2 COMPRT
SUBROUTINE COMPRT (IC, INOUT, INODES)
COMMON BLOCK VARIABLES
THE FOLLOWING VARIABLES ARE USED.
ESTIMATED FINAL TEMPERATURE, DEG FDIFFERENCE BETWEEN ENTHALPY AT ESTIMATED FIt~L
TEMPERATURE AND THE ACTUAL FINAL ENTHALPY, BTUHEAT RELEASED BY REACTION, BTUFINAL ENTHALPY, BTUINDEX FOR ITERATION VARIABLES T AND HDIFCOUNTER TO LIMIT NUMBER OF ITERATIONSABSOLUTE TEMPERATURE, DEG R
COMPONENT MASS OR MASS RATE, LB OR LB/(DELT)NODE TEMPERATURE, DEG FNODE PRESSURE, PSIAHEAT TRANSFER SURFACE TEMPERATURE, DEG FCOMPONENT MOLECULAR WEIGHT, LB/LB MOLENODE VOLUME, FT**3NODE ENTHALPY OR ENTHALPY RATE, BTU ORBTU/(DELT)HEAT TRANSFER RATE TO COMPARTMENT ATMOSPHEREFROM HEAT TRANSFER SURFACES, BTU/(DELT)COOLING RATE, BTU/SECHEAT TRANSFER COEFFICIENT, BTU/SEC-FT**2-DEG FSURFACE AREA FOR HEAT TRANSFER, FT**2INLET STREAM NODE N~1BERS
OUTLET STREAM NODE NUMBERSNATURAL LOG OF MINIMUM NUMBER ACCEPTABLE TO THECOMPUTERCUMULATIVE TIME OF TRANSIENT SIMULATION, SECTIME INTERVAL FOR TRANSIENT SIMULATION, SEC
NODE NUMBER OF COMPARTMENTMAXIMUM NUMBER OF THE NUMBER OF INLET STREAMSAND THE NUMBER OF OUTLET STREAMS (LESS THAN OREQUAL TO 4)MAXIMUM NUMBER OF NODES ALLOWED, CORRESPONDINGTO THE NULL VECTOR
( 3)( 3)
(30)(30 )(30)(30,4)(30,4)
(30)
(30,9)(30 )(30)(30)( 9)( 30)(30)
THDIF
QRATE
QCOOLHTCOEFHTAREAIINlOUTAMINLN
INODES
HRXNHAVAILITEMPI COUNTTR
ICINOUT
TIMEDELT
MASSTCPCTSURFWMOLVOLH
INTERNAL VARIABLES
INPUT VARIABLES
CC THIS SUBROUTINE PERFORMS A MASS AND ENERGY BALANCE FOR NODE IC. ITC DETERMINES THE TEMPERATURE, PRESSURE, AND PHASE COMPOSITION AT THEC END OF A TIME STEP. THE MASS AND ENERGY OF INLET AND OUTLET STREAMSC ARE ADDED OR SUBTRACTED TO THE MASS AND ENERGY OF THE COMPARTMENTC NODE, THEN COMPONENTS WITHIN THE NODE ARE ALLOWED TO REACT BEFORE THEC FINAL CONDITIONS ARE EVALUATED.CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCC
76
THE FOLLOWING SUBROUTINES ARE ALSO REQUIRED TO USE COMPRT.
VAPOR PRESSURE OF UF6, PSIAMAXIMUM AMOUNT OF UF6 THAT CAN BE CONTAINED ASVAPOR IN THE COMPARTMENT VOLUME AT THE ASSUMEDTEMPERATURE BASED ON THE VAPOR PRESSURE OF UF6MOLES OF AIRMOLES OF WATER VAPORMOLES OF HF VAPOR BASED ON THE EFFECTIVEMOLECULAR WEIGHT OF THE POLYMERIZED VAPORMOLES O~ UF6 VAPORTOTAL MOLES OF VAPOR IN THE COMPARTMENTTOTAL PRESSURE IN THE COMPARTMEtiT, PSIAENTHALPY AT THE ESTIMATED FINAL TEMPERATURE, BTUAPPROXIMATE SLOPE OF HDIF VS T, BTU/DEG F
DENTHLPHASEVPRUF6
DENUF6HFPOLYHHFH20HUF6PHFH20ZUF6
PUF6MAXVAP
NAIRNH20NHF
NUF6NTOTPTOTHTESTM
CCCCCCCCCCCCCCC THE FOLLOWING SUBROUTINES ARE CALLED BY COMPRT.CCCCCCCCCCCCCC
IMPLICIT REAL*8 (A-H,J-Z)C
DIMENSION T(3), HDIF(3)C
COMMON ILBMASSI MASS(30,9), DUMlCOMMON ICOMPTPI TC(30), PC(30), TSURF(30)COMMON IMOLWTI WMOL(9)COMMON /vOLUMEI VOL(30), DUM2(61)COMMON IENTHALI H(30), QRATE(30), QCOOL(30), HTCOEF(30),
* HTAREA(30)COMMON IISTRMSI IIN(30,4), IOUT(30,4)COMMON ICONTRLI AMINLN, TIME, DELT, DUM3, IDUM1, DUM4
CC SUM INLET AND OUTLET STREAM MASSES AND ENTHALPIES FOR THE TIME STEP.C
DO 20 120 =1,INOUTC
IF «IIN(IC,I20)+IOUT(IC,I20».EQ.(2*INODES» GO TO 30c
DO 10 110 =1,9
10 CctITINUE
C
C *MASS(IC,Il0) =MASS(IC,Il0) + MASS(IIN(IC,I20),Il0)
- MASS(IOUT(IC,I20),Il0)
77
C
C
C
H(IC) = H(IC) + H(IIN(IC,I20» - H(IOUT(IC,I20»
20 CONTINUE
30 CONTINUE
C
CC PLACE ALL COMPONENTS IN THE VAPOR PHASE.C
MASS(IC,3) =MASS(IC,2) + MASS(IC,3)MASS(IC,5) =MASS(IC,4) + MASS(IC,5)MASS(IC,8) =MASS(IC,6) + t1ASS(IC,7) + MASS(IC,8)
MASS(IC,2) = 0.00MASS(IC,4) =0.00MASS(IC,6) = 0.00MASS(IC,7) = 0.00
CC REACT UF6 WITH H20 TO THE EXTENT POSSIBLE.CC UF6(V) + 2 H20(V) --> U02F2(S) + 4 HF(V)CC HRXN = 25,199 BTU/LB MOLE H20 AT 77 F AND 1 ATMC
HRXN = O.DOC
IF (MASS(IC,8).EQ.0.DO.OR.MASS(IC,3).EQ.0.DO) GO TO 50·C
IF «MASS(IC,8)/MASS(IC,3».LT.(WMOL(8)/(2.DO*WMOL(3»» GO TO 40CC THE FOLLOWING MASS AND ENERGY BALANCE IS BASED ON H20 CONTROLLING THEC EXTENT OF REACTION.C
C
C
C
C
MASS(IC,8) =MASS(IC,8) - MASS(IC,3)*HMOL(8)/(2.DO*WMOL(3»MASS(IC,9) =MASS(IC,9) + MASS(IC,3)*WMOL(9)/(2.DO*WMOL(3»MASS(IC,5) =MASS(IC,5) + t1ASS(IC,3)*2.DO*~~OL(4)/WMOL(3)
HRXN = 25.199D3*MASS(IC,3)/WMOL(3)
MASS(IC,3) =O.DO
GO TO 50
40 Crn~TINUE
CC THE FOLLOWING MASS AND ENERGY BALANCE IS BASED ON UF6 CONTROLLING THEC EXTENT OF REACTION.C
MASS(IC,3) = MASS(IC,3) - MASS(IC,8)*2.DO*WMOL(3)/WMOL(8)MASS(IC,9) =MASS(IC,9) + MASS(IC,8)*WMOL(9)/HMOL(8)MASS(IC,5) = MASS(IC,5) + MASS(IC,8)*4.DO*WMOL(4)/~~OL(8)
CHRXN = 50.398D3*MASS(IC,8)/WMOL(8)
C
CMASS(IC,8) = 0.00
50 CONTINUE
78
CC EVALUATE HEAT TRANSFER TO THE COMPARTMENT ATMOSPHERE FROM HOTC SURFACES.C
QRATE(IC) = HTCOEF(IC)*HTAREA(IC)*(TSURF(IC) - TC(IC»*OELTCC CALCULATE THE TOTAL ENTHALPY IN THE COMPARTMENT AT THE END OF THEC TIME STEP.C
HAVAIL = HRXN + H(IC) + QRATE(IC) - (QCOOL(IC)*OELT)CC BEGIN ITERATIVE PROCEDURE TO FIND FINAL TEMPERATURE, PRESSURE, ANDC PHASE COMPOSITIONS. TEMPERATURE IS VARIED UNTIL ENTHALPY AGREES WITHC HAVAIL.C
ITEMP =1C
C
C
C
C
T(ITEMP) =TC(IC)
HDIF(2) = 0.00
ICOUNT = 0
60 CONTINUE
ICOUNT = ICOLNT + 1
C
CC PLACE ALL COMPONENTS IN THE VAPOR PHASE.C
MASS(IC,3) =t1ASS(IC,2) + MASS(IC,3)MASS(IC,5) =MASS(IC,4) + MASS(IC,5)MASS(IC,8) =MASS(IC,6) + MASS(IC,7) + MASS(IC,B)
MASS(IC,2) = 0.00MASS(IC,4) = 0.00MASS(IC,6) = 0.00MASS(IC,7) = 0.00
CTR =T(ITEMP) + 459.6700
CC DETERMINE IF At{Y UF6 C~~OENSES.
C
C
C
C
C
IF (MASS(IC,8).LE.0.DO) GO TO 70
CALL VPRUF6 (T(ITEMP), PUF6)
MAXVAP =WMOL(B)*PUF6*VOL(IC)/l0.73DO/TR
IF (MASS(IC,8).LE.MAXVAP) GO TO 70
IF (T(ITEMP).GT.147.306561DO) MASS(IC,7) =MASS(IC,B) - MAXVAP
79
CIF (T(ITEMP).LE.147.306561DO) MASS(IC,6) =MASS(IC,8) - MAXVAP
CMASS(IC,8) =MAXVAP
C70 CONTINUE
CC DETERMINE IF HF AND/OR H20 CONDENSE.C
C
C
IF (MASS(IC,3).EQ.0.DO.AND.MASS(IC,5).EQ.0.DO) GO TO 80
CALL PHASE (T(ITEMP), IC)
80 CONTINUECC ESTIMATE FINAL COMPARTMENT PRESSURE.C
C
C
NAIR =MASS(IC,l)/WMOL(l)NH20 =MASS(IC,3)/WMOL(3)NHF =MASS(IC,5)IWMOL(5)NUF6 =MASS(IC,B)/WMOL(8)
NTOT =NAIR + NH20 + NHF + NUF6
PTOT = NTOT*10.73DO*TR/VOL(IC)CC EVALUATE ENTHALPY CORRESPONDING TO ESTIMATED TEMPERATURE AND COMPAREC TO HAVAIL.C
CALL DENTHL (T(ITEMP), PTOT, IC, HTEST)C
C
C
HDIF(ITEMP) = HTEST - HAVAIL
IF (DABS(HDIF(ITEMP».LT.DMAX1(1.D-3,DABS(HAVAIL*1.D-3»)* GO TO 140
IF (ICOUNT.EQ.I00) STOPOlCC ESTIMATE NEW TEMPERATURE TO COI'frINUE ITERAT ION.C
C
C
C
C
C
C
IF (ITEMP.EQ.3) GO TO 120IF (ITEMP.EQ.2) GO TO 100
IF (HDIF(1).LT.0.DO.AND.HDIF(2).GT.0.DO) GO TO 110
IF (HDIF(l).GT.O.DO) GO TO 90
ITEMP = 2
T(2) =T(l) + 5.DO
GO TO 60
90 COI'frINUE
80
CT(2) = T(l)HDIF(2) = HDIF(l)T(1) = T(2) - 5.DO
CGO TO 60
C100 CONTINUE
CIF (HDIF(2).GT.0.DO) GO TO 110
CHDI F(1) = HDIF(2)T( 1) = T(2)T(2) = T(1) + 5.DO
CGO TO 60
C110 CONTINUE
CITEMP = 3
CM = (HDIF(2) - HDIF(1»/(T(2) - T(l»)T(3) =T(2) - HDIF(2)/M
CGO TO 60
C120 CONTINUE
CIF «T(2) - T(1»).LT.l.D-3) GO TO 140
CIF (HDIF(3).GT.0.DO) GO TO 130
CHDIF(l) = HDIF(3)T(l) = T(3)
CGO TOllO
C130 CONTINUE
CHDIF(2) = HDIF(3)T(2) = T(3)
CGO TOllO
C140 CONTINUE
CC THE MATERIAL AND ENERGY BALANCE HAS BEEN CLOSED FOR COMPARTMENT IC.C
TC(IC) =T(ITEMP)PC(IC) = PTOTH(I C) = HAVAI L
CRETURN
CEND
81
B.3 CPUF6
SUBROUTINE CPUF6 (TF, PSIA, MW, CPSOL, CPLIQ, CPVAP, CVVAP,* C~OCV)
CC THIS SUBROUTINE CALCULATES THE CONSTANT PRESSURE HEAT CAPACITIES OFC UF6 SOLID, LIQUID, AND VAPOR, AS WELL AS THE CONSTANT VOLUME HEATC CAPACITY AND THE HEAT CAPACITY RATIO FOR THE VAPOR. THE FOLLOWINGC VARIABLES ARE USED.C
THE HEAT CAPACITY CORRELATIONS ARE BASED ON INFORMATION IN R. DEWITT,"URANIUM HEXAFLUORIDE: A SURVEY OF THE PHYSICO-CHEMICAL PROPERTIES,"GAT-280, GOODYEAR ATOMIC CORP., PORTSMOUTH, OHIO, JAN. 29, 1960,PAGES 56 - 64. THE HEAT CAPACITY OF THE VAPOR GIVEN BY THE CORRELATION IN GAT-280 IS FOR A PRESSURE OF 1 ATM. THE VAPOR CORRELATIONGIVEN BELOW HAS BEEN MODIFIED USING THE MAGNUSON EQUATION OF STATE(SEE GAT-280, PAGES 97 - 101) AND THE DEPARTURE FUNCTION CORRELATIONSGIVEN IN R. C. REID, J. M. PRAUSNITZ, AND T. K. SHERWOOD, THEPROPERTIES OF GASES AND LIQUIDS, 3RD ED., MCGRAW-HILL BOOK COMPANY,1977, PAGE 93, SO THAT BOTH SATURATED AND UNSATURATED VAPOR HEATCAPACITIES CAN BE CALCULATED.
TEMPERATURE, DEG FABSOLUTE TEMPERATURE, DEG RTR**2PRESSURE, PSIAMOLECULAR WEIGHT, LB MASS/LB MOLECONSTANT PRESSURE HEAT CAPACITY OF THE SOLID,BTU/LB MASS-DEG FCONSTANT PRESSURE HEAT CAPACITY OF THE LIQUID,BTU/LB MASS-DEG FCONSTANT PRESSURE HEAT CAPACITY OF THE VAPOR,BTU/LB MASS-DEG FCONSTANT VOLUME HEAT CAPACITY OF THE VAPOR,BTU/LB MASS-DEG FHEAT CAPACITY RATIOVAPOR COMPRESSIBILITY FACTOR AT TF AND PSIAVAPOR COMPRESSIBILITY FACTOR AT TF AND 14.696 PSIA
CVVAP
CPLIQ
CPVAP
ZUF6
TFTRTRSQPSIAMWCPSOL
CPTOCVZPSIAZlATMZTZP
CCCCCCCCCCCCCCCCCCCC THE FOLLOWING SUBROUTINE IS CALLED.CCCCCCCCCCCCCCC
IMPLICIT REAL*8 (A-H,J-Z)C
TR =TF + 459.67DOC
TRSQ =TR**2CC THE HEAT CAPACITY OF THE SOLID IS GIVEN BY THE FOLL~~ING CORRELATIONC WHICH IS ACCURATE WITHIN 1~ BETWEEN -10 DEG F AND THE TRIPLE POINTC (147.3 DEG F).
82
CCPSOL = ( -5.70531D-2 + 2.55019D-4*TR
* + ( 9.64563D3/TRSQ ) ) * ( 3.52D2/MWCC THE HEAT CAPACITY OF THE LIQUID IS GIVEN BY THE FOLLOWING CORRELATIONC WHICH IS REPORTED TO HAVE AN ACCURACY OF 0.6% BETWEEN 147.3 AND 206.3C DEG F.C
CPLIQ = ( 5.10057D-2 + 1.02633D-4*TR* + ( 6.13934D3/TRSQ ) ) * ( 3.52D2/MW
CC CALCULATE THE VAPOR COMPRESSIBILITY FACTOR AT 14.696 PSIA AND ATC "PSIA" AS I.JELL AS ZP AND ZT AT "PSIA."C
CALL ZUF6 (TF, 14.696DO, ZlATM, O.ODO, O.ODO)C
CALL ZUF6 (TF, PSIA, ZPSIA, ZP, ZT)CC THE CONSTANT PRESSURE HEAT CAPACITY OF THE VAPOR IS GIVEN BY THEC FOLLOWING CORRELATION.C
CPVAP
***
= (9.21307D-2 + 1.25253D-5*TR- ( 2.95171D3/TRSQ )+ 3.0939D-3 * ( (4.DO*ZPSIA-3.DO*ZPSIA**2)- (4.DO*ZlATM-3.DO*ZlATM**2) ) ) * ( 3.52D2/MW
CC THE CONSTANT VOLUME HEAT CAPACITY OF THE VAPOR IS GIVEN BY THEC FOLLOWING CORRELATION.C
ClJVAP = CPVAP - ( 1.9872DO * ZT**2 )/( MW * ZP )CC THE HEAT CAPACITY RATIO FOR THE VAPOR IS GIVEN BYC
CPTOCV = CPVAP / CVVAPC
RETURNC
END
B.4 DENTHL
SUBROUTINE DENTHL (T, P, I, H)
VAPORVAPORt1ONOMER IC VAPORlJAPORSOLID
AIRH20HFUF6U02F2
CC THIS SUBROUTINE DETERMINES THE ENTHALPY OF A MIXTURE AT A GIVENC TEMPERATURE WITH RESPECT TO A REFERENCE TEMPERATURE OF 77 F ANDC THE FOLL~~ING REFERENCE STATES:CCCCCCC
83
ENTHALPY OF A MULTI COMPONENT MIXTURE WITHRESPECT TO THE REFERENCE TEMPERATURE AND STATES,BTU OR BTU/(DELT)
MOLECULAR WEIGHT OF HF MONOMER, LB/LB MOLE
COMPONENT MASS OR MASS FLOW RATE WITHIN A NODE,LB (COMPARTMENT) OR LB/(DELT) (STREAM)COMPONENT MOLECULAR WEIGHT, LB/LB MOLEWEIGHT FRACTION OF HF MONOMER TO HF VAPORWEIGHT FRACTI~~ OF HF TRIMER TO HF VAPORWEIGHT FRACTION OF HF HEXAMER TO HF VAPOR
ENTHALPY OF AIR WITH RESPECT TO THE REFERENCETEMPERATURE AND STATE, BTU OR BTU/(DELT)ENTHALPY OF HF AND H20 WITH RESPECT TO THEREFERENCE TEMPERATURE AND STATES, BTU ORBTU/( DELT)COMBINED MASS OF LIQUID HF AND LIQUID H20, LBOR LB/(DELT)COMBINED MASS OF HF VAPOR AND H20 VAPOR, LBOR LBI(DELT)WEIGHT FRACTION OF HF LIQUID IN A LIQUID MIXTUREOF HF AND H20WEIGHT FRACTI~~ OF HF VAPOR IN A VAPOR MIXTUREOF HF AND H20ENTHALPY OF THE HF-H20 LIQUID PHASE, BTU ORBTU/(DELT)ENTHALPY OF THE HF-H20 VAPOR PHASE, BTU ORBTU/(DELT)COMBINED MASS OF HF AND H20, LB OR LB/(DELT)WEIGHT FRACTION OF HF LIQUID AND VAPOR IN A TWO
TEMPERATURE, DEG FTOTAL PRESSURE, PSIANODE NUMBER
( 9)
(30,9)
HA
HFH20V
HMX
HFH20L
H
HMXLT
TPI
MASS
WMBHF
I-t1XVT
WHFL
WHFV
WMOLClC3C6
HFH20TWHFTOT
******************************************************************* ** WARNING! THIS SUBROUTINE RESETS THE VALUES OF Cl, C3, AND ** C6. BE SURE THAT SUBSEQUENT CODING YIELDS APPROPRIATE VALUES ** OF Cl, C3, AND C6 FOR LATER USE. ** *******************************************************************
OUTPUT VARIABLE
INPUT VARIABLES
INTERNAL VARIABLES
COMMON BLOCK VARIABLES
CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCC
C THE FOLLOWING VARIABLES ARE USED:CCCCC
OTHER SUBROUTINES REQUIRED TO USE DENTHL ARE:
PHASE MIXTURE OF HF AND H20REFERENCE ENTHALPY FOR THE HF-H20 SYSTEM,BTUOR BTU/(DELT)COMBINED MASS OF UF6 SOLID, LIQUID, AND VAPOR,ILB OR LB/(DELT)ENTHALPY OF SOLID UF6, BTU OR BTU/(DELT)ENTHALPY OF LIQUID UF6, BTU OR BTU/(DELT)ENTHALPY OF VAPOR UF6, BTU OR BTU/(DELT)REFERENCE ENTHALPY FOR UF6, BTU OR BTU/(DELT)ENTHALPY OF UF6 WITH RESPECT TO THE REFERENCETEMPERATURE AND STATE, BTU OR BTU/(DELT)ENTHALPY OF U02F2 WITH RESPECT TO THE REFERENCETEMPERATURE AND STATE, BTU OR BTU/(DELT)
HHFH20HUF6
DENUF6VPRUF6ZUF6
~77
UF6TOT
HUF2
H6STH6LTH6VTH6V77HHUF6
CCCCCCCCCCCCCCC SUBROUTINES CALLED BY DENTHL ARE:CCCCCCCCCC
IMPLICIT REAL*8 (A-H,J-Z)C
COMMON I LBMASS I MASS(30,9)COMMON I MOLWT I WMOL(9)COMMON I POLYMR I Cl, C3, C6, WMBHF
CC CALCULATE THE ENTHALPY OF AIR WITH RESPECT TO THE REFERENCEC TEMPERATURE AND STATE.C
HA =MASS(I,1)*0.24073DO*(T-77.DO)CC CALCULATE THE ENTHALPY OF THE HF-H20 SYSTEM WITH RESPECT TO THEC REFERENCE TEMPERATURE AND STATES.C
HMX = 0.00C
C
C
C
C
c
C
HFH20L =MASS(I,2) + MASS(I,4)HFH20V =MASS(I,3) + MASS(I,5)
IF «HFH20L+HFH2OV) .LE. 0.00) GO TO 30
IF (HFH20L.LE.0.DO) GO TO 10
WHFL =MASS(I,4)/HFH20L
10 CONTINUE
IF (HFH2OV.LE.0.DO) GO TO 20
85
WHFV =MASS(I,5)/HFH2OVC
20 CONTINUEC
CALL HHFH20 (T,WHFL,WHFV,HMXLT,HMXVT)C
HFH20T = HFH20L + HFH20VC
C
C
C
C
WHFTOT = (MASS(I,4) + MASS(I,5»/HFH20T
C1 = 1.00C3 = 0.00C6 = 0.00
CALL HHFH20 (77.DO,0.DO,WHFTOT,O.DO,HMXV77)
HMX = (HFH20L*HMXLT + HFH20V*HMXVT) - HFH20T*HMXV77
30 CONTINUECC CALCULATE THE ENTHALPY OF UF6 WITH RESPECT TO THE REFERENCEC TEMPERATURE AND STATE.C
UF6TOT =MASS(I,6) + MASS(I,7) + MASS(I,8)C
CALL HUF6 (T,P,WMOL(8),H6ST,H6LT,H6VT)C
CALL HUF6 (77.DO,14.696DO,WMOL(8),O.DO,O.DO,H6V77)C
HHUF6 = (MASS(I,6)*H6ST* + MASS(I,7)*H6LT + MASS(I,8)*H6VT)* -UF6TOT*H6V77
CC CALCULATE THE ENTHALPY OF U02F2 WITH RESPECT TO THE REFERENCEC TEMPERATURE AND STATE.C
HUF2 =MASS(I,9)*0.0821DO*(T-77.DO)CC CALCULATE THE ENTHALPY FOR NODE I WITH RESPECT TO THE REFERENCEC TEMPERATURE AND STATES.C
H = HA + HMX + HHUF6 + HUF2C
RETURNC
END
D.5 DENUF6
SUBROUTINE DENUF6 (TF, PSIA, MW, DENSOL, DENLIQ, DENVAP)CC THIS SUBROUTINE CALCULATES THE DENSITIES OF UF6 SOLID, LIQUID, ANDC VAPOR. THE FOLLOWING VARIABLES ARE USED.
86
TEMPERATURE, DEG FABSOLUTE TEMPERATURE, DEG RPRESSURE, PSIAMOLECULAR WEIGHT, LB MASS/LB MOLECOMPRESSIBILITY FACTOR FOR THE VAPORDENSITY OF SOLID, LB MASS/FT**3DENSITY OF LIQUID, LB MASS/FT**3DENSITY OF VAPOR, LB MASS/FT**3
TFTRPSIAMWZDENSOLDENLIQDENVAP
CCCCCCCCCCC THE DENSITY CORRELATIONS USED ARE BASED ON R. DEWITT, ·URANIUMC HEXAFLUORIDE: A SURVEY OF THE PHYSICO-CHEMICAL PROPERTIES,· GAT-280,C GOODYEAR ATOMIC CORP., PORTSMOUTH, OHIO, JAN. 29, 1960, PAGES 17 C 24. A CORRELATION FOR SOLID DENSITY, BASED ON TABLE 7 OF GAT-280C (EXCLUDING PRELIMINARY VALUES), WAS DERIVED BY W. R. WILLIAMS.C
CIMPLICIT REAL*8 (A-H,J-Z)
TR =TF + 459.6700CC THE DENSITY OF THE SOLID IS GIVEN BY THE FOLLOWING CORRELATION WHICHC IS BASED ON DATA REPORTED OVER THE TEMPERATURE RANGE OF 69 TO 145C DEG F.C
DENSOL = ( 3.300D2 - 1.800D-1*TF ) * ( MW / 3.5202 )CC THE DENSITY OF THE LIQUID IS GIVEN BYC
DENLIQ = ( 2.506D2 - ( 1.241D-1 + 2.620D-4 * TF ) * TF )* * ( MW / 3.52D2 )
CC EVALUATE THE COMPRESSIBILITY FACTOR FOR UF6 VAPOR.C
CALL ZUF6 (TF, PSIA, Z, ZP, ZT)CC THE DENSITY OF THE VAPOR IS GIVEN BYC
DENVAP = ( MW * PSIA * Z ) / ( 10.7300 * TRC
RETURNC
END
B.6 DPFLOW
SUBROUTINE DPFLOW (IC)CC THIS SUBROUTINE EVALUATES THE MASS FLOW THROUGH A PRESSURE-DROP-C C~~TROLLED PATHWAY ~)ER A TIME STEP DELT. THE ENTHALPY CHANGE ASSOCIC ATED WITH THIS MASS FLOW IS ALSO DETERMINED. IF REVERSE FLOW OCCURSC (WITH RESPECT TO THE NORMAL DIRECTION OF FLlli~), THEN THE MASS ISC TAKEN FROM THE PROPER NODE AND THE INDIVIDUAL COMPONENTS ARE ASSIGNEDC NEGATIVE VALUES.
87
COMMON BLOCK VARIABLES
THIS SUBROUTINE USES THE FOLLOWING VARIABLES:
NOTE THAT THIS SUBROUTINE IDENTIFIES THE TIME WHEN REVERSE FLOWBEGINS AND WHEN IT ENDS. PREVIOUS FLOW REVERSAL START AND STOP TIMESFOR A NODE ARE OVERWRITTEN AS SUBSEQUENT REVERSALS OCCUR.
NODE NUMBER FOR STREAM BEING EVALUATED
LOGICAL VARIABLE USED IN DETERMINING TSTART ANDTSTOPPRESSURE DIFFERENCE BETWEEN NORMAL INLET ANDOUTLET NODES, PSIACTUAL INLET NODE TO STREAMTOTAL MASS CONTAINED IN ACTUAL INLET NODE, LBDENSITY OF ACTUAL INLET STREAM, LB/FT**3TOTAL MASS FLOW RATE THROUGH STREAM, LB/(DELT)RATIO OF MASS FLOW THROUGH STREAM NODE TO TOTALMASS IN ACTUAL INLET NODE -- A POSITIVE VALUECORRESPONDS TO NORMAL FLOW AND A NEGATIVE VALUETO REVERSE FLOW
COMPONENT NODE MASS OR MASS FLOW RATE, LB(COMPARTMENT) OR LB/(DELT) (STREAM)NODE TEMPERATURE, DEG FNODE PRESSURE, PSIACOMPARTMENT NODE VOLUME, FT**3RESISTANCE TERM, PSI-SEC**2/LB-FT**3NODE ENTHALPY OR ENTHALPY RATE, BTU ORBTU/(DELT)NODE INPUT STREAM NUMBERNODE OUTPUT STREAM NUMBERMINIMUM NATURAL LOG ACCEPTED BY THE COMPUTERTIME AT WHICH MASS AND ENTHALPY RATES ARE BEINGDETERMINED, SECTIME INTERVAL USED IN TRANSIENT SIMULATION, SECTIME AT WHICH FLOW REVERSAL BEGINS, SECTIME AT WHICH FLOW REVERSAL ENDS, SEC
IC
MASS (30,9)
TC (30)PC (30)VOL (30)KRCOEF (30)H (30)
lIN (30,4)lOUT (30,4)AMINLNTIME
DELTTSTART (30)TSTOP (30 )
INTERNAL VARIABLES
CHECK (30)
DELP
INLETMASSlDENSMASS2FRAC
INPUT VARIABLE
CC THE TOTAL MASS FLOW RATE IS ESTABLISHED USING A RESISTANCE TERMC EVALUATED IN THE SUBROUTINE RESIST.CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCC
IMPLICIT REAL*8 (A-H,J-Z)C
LOGICAL CHECK(30)C
COMMON ILBMASSI MASS(30 ,9), DUMlCOMMON ICOMPTPI TC(30), PC(30), DUM2(30)
C
88
COMMON /vOLUMEI VOL(30), KRCOEF(30), DUM3(31)Cot1'1ON IENTHAU H( 30), DUM4(120)COMMON IISTRMSI IIN(30,4), IOUT(30,4)COMMON ICONTRLI AM INLN, TIME, DELT, DUM5 , IDUM1, Dl.tI6COMMON IRVFLOWI TSTART(30), TSTOP(30)
IF (TIME.EQ.O.DO) CHECK(IC) = .TRUE.CC DETERMINE PRESSURE DIFFERENCE ACROSS STREAM NODE, ACTUAL INLET NODE,C AND THE TOTAL MASS CONTAINED IN THE ACTUAL INLET NODE.C
DELP = PC(IIN(IC,l» - PC(IOUT(IC,l»C
INLET = IIN(IC,l)C
C
C
C
C
IF (DELP.LT.O.DO) INLET = 10UT(IC,1)
MASSi = O.DO
DO 10 110=1,9
MASSi = MASSi + MASS(INLET,li0)
10 CONTINUECC DETERMINE INLET DENSITY AND TOTAL MASS FLOW RATE THROUGH THE STREAMC NODE.C
CDENS = MASSi/vOL(INLET)
MASS2 = DSQRT(DABS(DELP)*DENS/KRCOEF(IC»*DELTCC DETERMINE COMPONENT MASS FLOW RATES, STREAM ENTHALPY RATE, AND STREAMC TEMPERATURE AND PRESSURE.C
IF (DELP.LT.O.DO) MASS2 = - MASS2C
FRAC = MASS2/MASS1C
DO 20 I20 =1 ,9C
MASS(IC,120) = MASS(INLET,120)*FRACC
20 CONTINUEC
H(IC) = H(INLET)*FRACTC(IC) = TC(INLET)PC(IC) = PC(INLET)
CC CHECK FOR REVERSE FLOW.C
IF (DELP.GE.O.DO) GO TO 30C
IF (DELP.LT.O.DO.AND.CHECK(IC» WRITE (5,100) IC, TIME
89
CIF (DELP.LT.O.DO.AND.CHECK(IC» TSTART(IC) =TIME - DELT
CHECK(IC) = .FALSE.C
RETURNC
30 CONTINUEC
C
IF (.NOT.CHECK(IC» WRITE (5,110) IC, TIMEIF (.NOT.CHECK(IC» TSTOP(IC) = TIME - DELT
CHECK(IC) = .TRUE.C
RETURNC
100 FORMAT ( ,C
110 FORMAT ( ,C
END
REVERSE FLOW OCCURING IN NODE',13,' AT' ,F10.5,' SEC.')
NORMAL FLOW RESUMES IN NODE' ,13,' AT' ,Fl0.5,' SEC.')
B.7 EQTUF6
SUBROUTINE EQTUF6 (PSIA, TF)
PRESSURE, PSIAESTIMATED PRESSURE, PSIAESTIMATED PRESSURE, PSIAESTIMATED PRESSURE, PSIATEMPERATURE, DEG FESTIMATED TEMPERATURE, DEG FESTIMATED TEMPERATURE, DEG FESTIMATED TEMPERATURE, DEG FACCURACY REQUIRED OF P3 RELATIVE TO PSIADIFFERENCE BETWEEN Pl AND PSIADIFFERENCE BETWEEN P2 AND PSIADIFFERENCE BETWEEN P3 AND PSIASLOPE OF F =M*T + B
F2F3M
PSIAPiP2P3TFT1T2T3LIMITF1
CC THIS SUBROUTINE CALCULATES THE EQUILIBRIUM TEMPERATURE, TF,C CORRESPONTING TO A GIVEN PRESSURE, PSIA. THE FOLLOWING VARIABLES AREC USED.CCCCCCCCCCCCCCC
IMPLICIT REAL*8 (A-H,J-Z)CC THE ACCURACY REQUIRED OF P3 RELATIVE TO PSIA IS GIVEN BY LIMIT.C
LIMIT = PSIA/l.D8CC THE INITIAL GUESS OF TF, WHICH IS Tl, IS BASED ON THE CORRELATIONC FOR VAPOR PRESSURE USED BETWEEN 147.3 AND 240 DEG F (22.04 ANDC 87.91 PSIA).C
C
90
T1 =( -4.6680703 / (OLOG(PSIA) - 12.160000) ) - 367.533DO
IF (PSIA.GE.22.04226474DO) GO TO 40CC THE FOLLOWING SEQUENCE OF EQUATIONS, THROUGH STATEMENT 40, GIVES THEC EQUILBRIUM TEMPERATURE FOR A PRESSURE LESS THAN 22.04 PSIA.CC A SECOND ESTIMATED TEMPERATURE IS ALSO REQUIRED.C
T2 =T1 + 1.0DOC
IF (T2.GT.147.306561DO) T2 =147.306561C
10 CONTINUECC CALCULATE VAPOR PRESSURES CORRESPONDING TO T1 AND T2.C
CALL VPRUF6 (T1, P1)CALL VPRUF6 (T2, P2)
C20 CONTINUE
CC EVALL~TE T3, AN IMPROVEO ESTIMATE OF TF.C
Fl =P1 - PSIAF2 = P2 - PSIAM = ( F2 - Fl ) / ( T2 - T1 )T3 =T2 - F2/M
CC CHECK ACCURACY OF T3 BY CHECKING ACCURACY OF P3.C
C
C
C
C
C
C
C
C
C
C
CALL VPRUF6 (T3, P3)
F3 = P3 - PSIA
IF (DABS(F3).LT.LIMIT) GO TO 30
T1 = T2T2 = T3P1 = P2P2 = P3
GO TO 20
30 CONTINUE
TF = T3
RETURN
40 CONTINUE
IF (PSIA.GT.87.9133385200) GO TO 50
91
C THE ESTIMATED TEMPERATURE, Tl, CORRESPONDS TO TF BETWEEN 147.3 ANDC 240 DEG F (22.04 AND 87.91 PSIA).C
TF = T1C
RETURNC
50 CONTINUEC
IF (PSIA.GT.135.4039894DO) GO TO 60CC THE FOLLOWING SEQUENCE OF EQUATIONS, THROUGH STATEMENT 60, GIVES THEC EQUILBRIUM TEMPERATURE FOR PRESSURES BETWEEN 87.91 AND 135.4 PSIA.CC CHECK Tl TO ENSURE THAT IT DOES NOT EXCEED 275.8 DEG F. A SECONDC ESTIMATED TEMPERATURE IS ALSO REQUIRED.C
IF (T1.GT.275.8DO) Tl = 275.8C
T2 =Tl + 0.200CC RETURN TO 10 TO EVALUATE TF CORRESPONTING TO PSIA.C
GO TO 10C
60 CONTINUECC THE FOLLOWING EQUATION GIVES TF FOR PRESSURES EXCEEDING 135.4039894C PSIA (276 DEG F).C
TF = ( -6.9761103 / (DLOG(PSIA) - 13.7627DO) ) - 511.866DOC
RETURNC
END
D.8 FLASH
INPUT VARIABLES:
INITIAL TEMPERATURE, DEG FINITIAL PRESSURE, PSIAMOLECULAR WEIGHT, LB MASS/LB MOLEINITIAL VAPOR MASS FRACTION
TINITPINITMWXVINIT
SUBROL~INE FLASH (TINIT, PINIT, MW, XVINIT, XLINIT, PFIN, ISEN,* XVFIN, XLFIN, TFIN)
CC THIS SUBROUTINE DETERMINES THE VAPOR MASS FRACTION FOR A GIVEN FINALC PRESSURE BASED ON THE INITIAL TEMPERATURE, PRESSURE, VAPOR MASSC FRACT ION, AND LI QU10 MASS FRACTI ON OF THE NON-VAPOR FRACT ION AS WELLC AS WHETHER THE FLASH IS ISENTROPIC OR ISENTHALPI C. THE FOLLOWINGC VARIABLES ARE USED.CCCCCCC
92
************************************************************ ** WARNING! PINIT MUST BE GREATER THAN OR EQUAL TO PFIN. ** ************************************************************
INTERNAL VARIABLES:
OUTPUT VARIABLES:
BTU/LB MASS
VALUES OF THE FUNCTION F =M*T + B CORRESPONDINGTO Tl, T2, AND T3
THE FUNCTION F CORRESPONDS TO THE TEST VALUEMINUS THE AVERAGE VALUE OF THE PROPERTY.
TEST ENTROPIES CORRESPONDING TO Tl, T2, AND T3
TEST ENTHALPIES CORRESPONDING TO Tl, T2, AND T3
TEST TEMPERATURES
CALCULATES UF6 ENTROPIESCALCULATES TEMPERATURE CORRESPONDING TO A GIVENVAPOR PRESSURE
ENTHALPY OF THE SOLID, BTU/LB MASSENTHALPY OF THE LIQUID, BTU/LB MASSENTHALPY OF THE VAPOR, BTU/LB MASSAVERAGE ENTHALPY OF THE INITIAL MIXTURE,
ENTROPY OF THE SOLID, BTU/LB MASS-DEG FENTROPY OF THE LIQUID, BTU/LB MASS-DEG FENTROPY OF THE VAPOR, BTU/LB MASS-DEG FAVERAGE ENTROPY OF THE INITIAL MIXTURE,BTU/LB MASS-DEG F
FINAL VAPOR MASS FRACTIONFINAL LI QU ID MASS FRACT ION OF THE NON-VAPOR FRACT IONFINAL TEMPERATURE, DEG F
SLOPE OF THE FUNCTION FACCURACY REQUIRED IN ESTIMATING THE AVERAGE PROPERTYIN SELECTING THE FINAL TEMPERATUREMAXIMUM TEMPERATURE A SUBCOOLED LIQUID CAN ATTAIN ATTHE FINAL PRESSURE, DEG F
INITIAL LIQUID MASS FRACTION OF THE NON-VAPOR FRACTIONFINAL PRESSURE, PSIAVARIABLE SPECIFYING BASIS FOR FLASH CALCULATION
ISEN =0, ISENTROPIC FLASHISEN = 1, ISENTHALPIC FLASH
Hi, H2, H3
HSOLHLIQHVAPHAVG
SUF6EQTUF6
Sl, S2, S3
F1, F2, F3
SSOLSLIQSVAPSAVG
MLIMIT
XVFINXLFINTFIN
TMAX
T1, T2, T3
XLI NITPFINISEN
CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCC THE FOLLOWING SUBROUTINES ARE USED.CCCC
93
CALCULATES UF6 ENTHALPIES
DENUF6VPRUF6ZUF6
HUF6CCC THE FOLLOWING SUBROUTINES ARE ALSO REQUIRED.CCCCC
IMPLICIT REAL*8 (A-H,J-Z)CC A THREE PHASE INITIAL RELEASE CAN ONLY EXIST AT THE TRIPLE POINT;C THEREFORE, XLINIT EQUALS 1 OR 0 EXCEPT AT THE TRIPLE POINT.C
IF (TINIT.GT.147.306561DO) XLINIT = 1.0DOIF (TINIT.LT.147.306561DO) XLINIT = O.ODO
CC SELECT BASIS FOR FLASH CALCULATION.C
IF (ISEN.EQ.l) GO TO 40CC CALCULATE THE AVERAGE ENTROPY OF THE INITIAL MIXTURE.C
CALL SUF6 (TINIT, PINIT, MW, SSOL, SLIQ, SVAP)C
SAVG =XVINIT*SVAP + (l.DO-XVINIT)*XLINIT*SLIQ* + (l.DO-XVINIT)*(l.DO-XLINIT)*SSOL
CC CALCULATE THE FINAL VAPOR MASS FRACTION ASSUMING AN EQUILIBRIUMC FLASH.C
CALL EQTUF6 (PFIN, TFIN)c
CALL SUF6 (TFIN, PFIN, MW, SSOL, SLIQ, SVAP)C
IF (TFIN.GE.147.306561DO) XVFIN = (SAVG-SLIQ)/(SVAP-SLIQ)IF (TFIN.LT.147.306561DO) XVFIN = (SAVG-SSOL)/(SVAP-SSOL)
CIF (XVFIN.GE.O.ODO) GO TO 10
CC A VALUE OF ~)FIN LESS THAN ZERO IMPLIES A SUBCOOLED CONDENSED PHASEC IS RELEASED. SINCE THERE IS CURRENTLY NO PRESSURE DEPENDENCE FORC LIQUID ENTROPY, TFIN =TINIT.C
XLFIN =XLINITXVFIN = O.ODOTFIN =TINIT
CRETURN
C10 CONTINUE
cC THE COND~~SED PHASE RELEASED WITH THE VAPOR IS LIQUID IF THE FINALC TEMPERATURE IS GREATER THAN OR EQUAL TO THE TRIPLE POINT TEMPERATURE.C
94
IF (TFIN.GE.147.30656100) XLFIN = 1.000IF (TFIN.LT.147.306561DO) XLFIN = 0.000
CIF (XVFIN.LE.l.DO) RETURN
CC A VALUE OF XVFIN GREATER THAN 1 IMPLIES THAT THE FINAL FORM OF THEC RELEASE IS A SUPERHEATED VAPOR. THE FOLLOWING SEQUENCE OF EQUATIONSC THROUGH 40 EVALUATES THE FINAL TEMPERATURE OF A SUPERHEATED VAPORC HAVING PFIN AS THE FINAL PRESSURE.C
LIMITSlT1T2
= SAVG / 1.0B= SVAP=TFIN=Tl + 1.00
C
C
C
C
C
C
C
C
C
C
C
C
CALL SUF6 (T2, PFIN, MW, 0.000, 0.000, S2)
20 CONTINUE
Fl = Sl - SAVGF2 = S2 - SAVGM = ( F2 - Fl ) / ( T2 - Tl )T3 = T2 - F2IM
CALL SUF6 (T3, PFIN, MW, 0.000, 0.000, S3)
F3 = S3 - SAVG
IF (DABS(F3).LT.LIMIT) GO TO 30
T1 = T2T2 = T3Sl = S2S2 = S3
GO TO 20
30 CONTINUE
XVFIN = 1.00TFIN = T3
RETURN
40 CONTINUECC CALCULATE THE AVERAGE ENTHALPY OF THE INITIAL MIXTURE.C
CALL HUF6 (TINIT, PINIT, t~l, HSOL, HLIQ, HVAP)C
HAVG = ~JINIT*HVAP + (1.00-XVINIT)*XLINIT*HLIQ* + (1.DO-XVINIT)*(1.00-XLINIT)*HSOL
CC CALCULATE THE FINAL VAPOR MASS FRACTION ASSL~ING AN EQUILIBRIUM
95
C FLASH.C
CALL EQTUF6 (PFIN, TFIN)C
TM.4X =TFINC
CALL HUF6 (TFIN, PFIN, MW, HSOL, HLIQ, HVAP)C
IF (TFIN.GE.147.306561DO) XVFIN = (HAVG-HLIQ)/(HVAP-HLIQ)IF (TFIN.LT.147.306561DO) XVFIN = (HAVG-HSOL)/(HVAP-HSOL)
CIF (XVFIN.GE.O.ODO) GO TO 70
CC A VALUE OF XVFIN LESS THAN ZERO IMPLIES A SUBCOOLED PHASE ISC RELEASED.C
XLFIN = XLINITXVFIN = O.ODO
CC IF XLINIT EQUALS ZERO, THAN THE SUBCOOLED PHASE IS SOLID.C
TFIN =TINITC
IF (XLINIT.EQ.O.DO) RETURNCC IF XLINIT IS NOT EQUAL TO ZERO, THEN A SUBCOOLED LIQUID IS RELEASED.C THE FOLLOWING SEQUENCE OF EQUATIONS THROUGH 60 DETERMINES THE FINALC TEMPERATURE OF A SUBCOOLED LIQUID HAVING PFIN AS THE FINAL PRESSURE.C
XLFIN = 1. 000LIMIT = HAVG I 1.08T1 = TMAXHi = HLIQT2 = TINIT
CCALL HUF6 (T2, PFIN, MW, 0.000, H2, 0.000)
C50 CONTINUE
CFl = Hi - HAVGF2 = H2 - HAVGM = ( F2 - Fi ) I ( T2 - Tl )T3 =T2 - F2/M
CIF (T3.GT.TMAX) T3 = (TMAX + DMAXl(Ti,T2»/2.DOIF (T3.LT.TINIT) T3 = (TINIT + DMINi(Ti,T2»/2.DO
CCALL HUF6 (T3, PFIN, MW, 0.000, H3, 0.000)
CF3 = H3 - HAVG
CIF (DABS(F3).LT.LIMIT) GO TO 60
CIF «DMAXi(Tl,T2,T3) - DMINi(Tl,T2,T3».LT.i.D-3) GO TO 60
96
CT1 =T2T2 = T3Hl = H2H2 = H3
CGO TO 50
C60 CCNfINUE
CTFIN = T3
CRETURN
C70 CONTINUE
CC THE CONDENSED PHASE RELEASED WITH THE VAPOR IS LIQUID IF THE FINALC TEMPERATURE IS GREATER THAN OR EQUAL TO THE TRIPLE POINT TEMPERATURE.C
C
IF (TFIN.GE.147.306561DO) XLFIN =1.000IF (TFIN.LT.147.306561DO) XLFIN = 0.000
IF (XVFIN.LE.l.DO) RETURNCC A VALUE OF XVFIN GREATER THAN 1 IMPLIES THAT THE FINAL FORM OF THEC RELEASE IS A SUPERHEATED VAPOR. THE FOLLOWING SEQUENCE OF EQUATIONSC THROUGH THE. END OF THE SUBROUTINE EVALUATES THE FINAL TEMPERATUREC OF A SUPERHEATED VAPOR HAVING PFIN AS THE FINAL PRESSURE.C
LIMIT = HAVG / 1.08Hl = HVAPT1 = TFINT2 =Tl + 1.00
CCALL HUF6 (T2, PFIN, MW, 0.000, 0.000, H2)
C80 CONTINUE
CFl = Hl - HAVGF2 = H2 - HAVGM = ( F2 - Fl ) / ( T2 - Tl )T3 = T2 - F2/M
CCALL HUF6 (T3, PFIN, MW, 0.000, 0.000, H3)
CF3 = H3 - HAVG
CIF (DABS(F3).LT.LIMIT) GO TO 90
CT1 =T2T2 =T3Hl = H2H2 = H3
C
97
GO TO 80C
90 CONTINUEC
XVFIN =1.DOTFIN =T3
CRETURN
CEND
B.9 HCOEFF
SUBROUTINE HCOEFF (I C)
C~1ON BLOCK VARIABLES
THE FOLLOWING VARIABLES ARE USED.
NODE NUMBER OF THE COMPARTMENT FOR WHICH THEHEAT TRANSFER COEFFICIENT IS BEING CALCULATED
COMPONENT MASS IN A NODE, LB (FOR COMPARTMENTNODES), OR LB/(DELT) (FOR STREAM NODES)NODE TEMPERATURE, DEG FNODE PRESSURE, PSIAHEAT TRANSFER SURFACE TEMPERATURE, DEG FTOTAL ENTHALPY OR ENTHALPY RATE, BTU ORBTU/( DELT)AMOUNT OF HEAT ADDED TO A NODE TO MAINTAIN AC~~STANT TEMPERATURE UNDER NORMAL STEADY STATECONDITI~~S, BTU/SECCOOLING RATE, BTU/SECHEAT TRANSFER COEFFICIENT, BTU/SEC-FT**2-DEG FSURFACE AREA FOR HEAT TRANSFER, FT**2t~TURAL LOG OF THE MINIMUM NUMBER ACCEPTED BYTHE COMPUTERTIME INTERVAL USED FOR THE TRANSIENT SIMULATION,SECINLET STREAM NODE NUMBER
IC
MASS (30,9)
TC (30)PC (30)TSURF (30)H (30)
QRATE (30)
QCOOL (30)HTCOEF (30)HTAREA (30)AMINLN
DELT (30)
lIN (30,4)
INPUT VARIABLES
CC THIS SUBROUTINE DETERMINES THE HEAT TRANSFER COEFFICIENT GIVEN THEC ENTHALPIES OF THE INLET STREAMS AND THE COMPARTMENT, THE MASSES INC THE INLET STREAMS AND THE COMPARTMENT, THE COOLING RATE AND THE TIMEC STEP, AND THE AREA AND TEMPERATURE OF HEAT TRANSFER SURFACES. THEC HEAT TRANSFER COEFFICIENT IS BASED ON HEATING UP THE MASS BROUGHT INC BY THE INLET STREAMS TO THE TEMPERATURE OF THE COMPARTMENT ATMOSPHEREC UNDER NORMAL STEADY STATE CONDITIONS. THE TEMPERATURES USED INC EVALUATING THE HEAT TRANSFER COEFFICIENT ARE THE ROOM TEMPERATUREC (NOT THE INLET STREAM TEMPERATURES) AND THE HEAT TRANSFER SURFACEC TEMPERATURES.CCCCCCCCCCCCCCCCCCCCCCCCCCCC
98
CC
ECCCCC
INTERNAL VARIABLES
MASSICMASS1MASS2MASS3MASS4
TOTAL MASS IN COMPARTMENT NODE IC,TOTAL MASS RATE IN INLET STREAM 1,TOTAL MASS RATE IN INLET STREAM 2,TOTAL MASS RATE IN INLET STREAM 3,TOTAL MASS RATE IN INLET STREAM 4,
LBLB/(DELT)LB/(DELT)LB/(DELT)LB/(DELT)
C
C
C
C
C
IMPLICIT REAL*8 (A-H,J-Z)
COMMON ILBMASSI MASS( 30,9), DUM1COMMON ICOMPTPI TC(30), PC(30), TSURF(30)COMMON IENTHALI H(30), QRATE(30), QCOOL(30), HTCOEF(30),
* HTAREA( 30)COMMON ICONTRLI AMINLN, DUM2, DELT, DUM3, IDUM1, DUM4COMMON IISTRMSI IIN(30,4), IDUM2(120)
MASSIC = 0.00MASS1 = O.DOMASS2 = 0.00MASS3 = 0.00MASS4 = 0.00
DO 10 110=1,9
MASSIC = MASSIC + MASS(IC,I10)MASS1 =MASS1 + MASS(IIN(IC,1),I10)MASS2 = MASS2 + t1ASS(IIN(IC,2),I10)MASS3 = MASS3 + MASS(IIN(IC,3),I10)t1ASS4 = MASS4 + MASS(IIN(IC,4),I10)
10 CONTINUEC
QRATE(I C)
*-k
CHTCOEF(IC)
CRETURN
CEND
= (H(IC)*(MASS1 + MASS2 + MASS3 + MASS4)/MASSIC- (H(IIN(IC,1» + H(IIN(IC,2» + H(IIN(IC,3»+ H(IIN(IC,4») + QCOOL(IC)*DELT)/DELT
= QRATE(IC)/HTAREA(IC)/(TSURF(IC) - TC(IC»
B.10 HFPOLY
SUBROUTINE HFPOLY (TF, PHF, MW, C1C3C6)CC THIS SUBROUTINE IS BASED ON INFORMATION PRESENTED IN JOHN M.C BECKERDITE, DAVID R. POWELL, AND EMORY T. ADAMS, JR., "SELF-ASSOCICATION OF GASES. 2. THE ASSOCIATION OF HYDROGEN FLUORIDE," J. CHEM.C ENG. DATA 1983, 28, 287-293. THE EQUILIBRIUM COEFFICIENTS USED BELOWC WERE DEVELOPED FROM STRO~1EIER AND BRIEGLEB/S DATA (SEE TABLE III).
99
THIS VARIABLE IS GENERALLY .TRUE. EXCEPT, FOR EXAMPLE,WHEN ONLY THE MOLECULAR WEIGHT IS REQUIRED IN PHFH20 TOESTABLISH THE AZEOTROPIC MOLE FRACTION OF HF IN THE HFH20 SYSTEM; IN THAT CASE, A CHANGE IN THE VALUES OFCl, C3, AND C6 WOULD MESS UP OTHER CALCULATIONS.
FUNCTION OF PHF AND ESTIMATED Pl THAT MUST CONVERGE TOZERO TO OBTAIN THE AVERAGE MOLECULAR WEIGHT OF HF VAPORDERIVATIVE OF F WITH RESPECT TO Pl
TEMPERATURE, DEG FABSOLUTE TEMPERATURE, DEG RPARTIAL PRESSURE OF HF, PSIACONVERGENCE LIMIT FOR PRESSURE, PSIAVERAGE MOLECULAR WEIGHT OF HF, LB/LB MOLEMOLECULAR WEIGHT OF HF MONOMER, LB/LB MOLEEQUILIBRIUM COEFFICIENT FOR TRIMER, PSIA**-2EQUILIBRIUM COEFFICIENT FOR HEXAMER, PSIA**-5PRESSURE OF HF MONOMER, PSIAPRESSURE-MOLECULAR WEIGHT PRODUCT FOR HF MONOMERPRESSURE-MOLECULAR WEIGHT PRODUCT FOR HF TRIMERPRESSURE-MOLECULAR WEIGHT PRODUCT FOR HF HEXAMERSUM OF PRESSURE-MOLECULAR WEIGHT PRODUCTSMASS FRACTION OF MONOMER TO TOTAL HF, LB MONOMER/LB HF
VAPORMASS FRACTION OF TRIMER TO TOTAL HF, LB TRIMER/LB HF
VAPORMASS FRACTION OF HEXAMER TO TOTAL HF, LB HEXAMER/LB HF
VAPOR
DFDP
F
C1C3C6 A LOGICAL VARIABLE TO INDICATE WHETHER EXISTING VALUESOF Cl, C3, AND C6 SHOULD BE CHANGED
.TRUE. PERMITS VALUES TO BE CHANGED
.FALSE. RETAINS EXISTING VALUES
C6
C3
TFTRPHFPLIMITMWIr-lMBHFK3K6PlP1MWlP3MW3P6J'1.J6PMWSUMCl
CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCC
c
C THE FOLLOWING VARIABLES ARE USED.CCC
IMPLICIT REAL*B(A-H,K-Z)C
LOGICAL C1C3C6C
COMMON /POLYMRI Cl, C3, C6,WMBHFC
MW =WMBHFC
IF (.NOT.C1C3C6) GO TO 10C
Cl = 1.DOC3 = 0.00C6 = O.DO
C10 CONTINUE
C
100
IF (PHF.LT.l.D-5) RETURNC
PLIMIT = PHF*1.D-6TR =TF + 459.67DOK3 = DEXP(23884.0DO/TR - 51.2393DO)K6 =DEXP(40319.6DO/TR - 87.7927DO)Pi = PHF
C20 CONTINUE
CF = PHF - Pi - K3*Pl**3 - K6*Pl**6IF (DABS(F).LT.PLIMIT) GO TO 30DFDP = -l.DO - 3.DO*K3*Pl**2 - 6.DO*K6*Pl**5Pi = Pi - F/DFDP
CGO TO 20
C30 CONTINUE
CP1MWl =WMBHF*PlP3MW3 = 3.DO*WMBHF*K3*Pl**3P6MW6 =6.DO*WMBHF*K6*Pl**6PMHSUM = P1MWl + P3MW3 + P6MW6MW = PMWSUMlPHF
CIF (.NOT.C1C3C6) GO TO 40
CCl = P1MW1/PMWSUMC3 = P3MW3/PMWSlJ1C6 = P6MW6/PMWSUM
C40 CONTINUE
CRETURNEND
B.ll HHFH20
SUBROUTINE HHFH20 (TF, WHFL, WHFV, HL, HV)
TEMPERATURE, DEG FWEIGHT FRACTION HF IN LIQUID, LB HF/LB HF-H20 LIQ MIXWEIGHT FRACTION HF IN VAPOR, LB HF/LB HF-H20 VAP MIXENTHALPY OF HF-H20 LIQUID MIXTURE, BTU/LB LIQ MIXENTHALPY OF HF-H20 VAPOR MIXTURE, BTU/LB VAP MIXMASS HF TRIMER TO MASS OF HF, LB TRIMER/LB HF VAPORMASS HF HEXAMER TO MASS OF HF, LB HEXAMERILB HF VAPORWHFL**2
TFWHFLWHFVHLHVC3POLYC6POLYWHFLSQ
CC THIS SUBROUTINE CALCULATES THE ENTHALPIES OF LIQUID AND VAPORC MIXTURES OF HF AND H20 GIVEN THE TEMPERATURE AND THE WEIGHT MASSC FRACTION OF HF IN EACH PHASE. THE FOLLOWING VARIABLES ARE USED.CCCCCCCCCC
101
IMPLICIT REAL*8 (A-H,J-Z)
COMMON /POLYMR/ DUM1,C3POLY,C6POLY,DUM2
Al,A2,A3,A4,A5 CONSTANTS IN EQUATIONS FOR LIQUID ENTHALPYB1,B2,B3,B4,B5 LINEAR CONSTANTS IN EQUATIONS FOR LIQUID
ENTHALPYC2,C3,C4,C5 QUADRATIC CONSTANTS IN EQUATIONS FOR LIQUID
ENTHALPY
CCCCCCCCCCCCC
C
H20,H60,H80,H90,HI00
M20,M60,M80,M90
LIQUID ENTHALPY AT 20, 60, 80, 90, AND100 WT %, RESPECTIVELY, BTU/LB HF-H20MIXTURE
SLOPE OF H-WHFL CURVE AT 20, 60, 80, AND90 WT %
CC THE FOLLOWING SEQUENCE OF EQUATIONS THROUGH "50 CONTINUE" EVALUATEC THE ENTHALPY OF HF-H20 LIQUID MIXTURES. THE EQUATIONS ARE BASED ONC A PLOT OF ENTHALPY VS CONCENTRATION AS A FUNCTI~~ OF TEMPERATUREC WHICH WAS SENT TO W. REID WILLIAMS BY BRIAN C. ROGERS OF ALLIEDC CHEMICAL, SOLVAY, NY, IN A LETTER DATED JULY 26, 1983. THE EQL~TIONS
C WERE DEVELOPED BY W. R. WILLIAMS.C
WHFLSQ =WHFL*WHFLC
Al = -32.252DO + O.99783DO*TFBl = -357.75DO - 0.969DO*TF + 0.0013DO*TF**2
CIF (WHFL.GT.0.2DO) GO TO 10
CC THE FOLLOWING EQUATION IS APPLICABLE FOR WHFL BETWEEN 0.0 AND 0.2.C
HL = A1 + B1*WHFLC
GO TO 50C
10 CONTINUEC
H20 =Al + B1*0.2DOH60 = -179.68DO + 0.63569DO*TF + 5.8429D-4*TF**2M20 = B1C2 = (H20 - H60 + 0.4DO*M20) / (-0.16DO)B2 =M20 - O.4DO*C2A2 =H20 - 0.2DO*B2 - 0.04DO*C2
CIF (WHFL.GT.0.6DO) GO TO 20
CC THE FOLLOWING EQUATION IS APPLICABLE FOR WHFL BETWEEN 0.2 AND 0.6.C
HL =A2 + B2*WHFL + C2*WHFLSQC
GO TO 50C
102
20 CONTINUEC
H80 = -159.26DO + 0.7985DO*TFM60 = B2 + 1.2DO*C2C3 = (H60 - H80 + 0.2DO*M60) / (-0.04DO)B3 =M60 - 1.2DO*C3A3 = H60 - 0.6DO*B3 - 0.36DO*C3
CIF (WHFL.GT.0.8DO) GO TO 30
CC THE FOLLOWING EQUATION IS APPLICABLE FOR WHFL BETWEEN 0.6 AND 0.8.C
HL =A3 + B3*WHFL + C3*WHFLSQC
GO TO 50C
30 CONTINUEC
H90 =-111.54DO + 0.67057*TFM80 = B3 + 1.6DO*C3C4 = (H80 - H90 + 0.lDO*M80) / (-O.OlDO)B4 =M80 - 1.6DO*C4A4 = H80 - 0.8DO*B4 - 0.64DO*C4
CIF (WHFL.GT.0.9DO) GO TO 40
CC THE FOLLOWING EQUATION IS APPLICABLE FOR WHFL BETWEEN 0.8 AND 0.9.C
HL =A4 + B4*WHFL + C4*WHFLSQC
GO TO 50C
40 CONTINUEC
H100 = -23.3142DO + 0.870283DO*TFM90 = B4 + 1.8DO*C4C5 = (H90 - Hl00 + O.lDO*M90) / (-O.OlDO)B5 =M90 - 1.8DO*C5A5 =H90 - 0.9DO*B5 - 0.81DO*C5
CC THE FOLLOWING EQUATION IS APPLICABLE FOR WHFL BETWEEN 0.9 AND 1.0C
HL =A5 + B5*WHFL + C5*WHFLSQC
50 CONTINUECC THE FOLLOWING EQUATION FOR THE ENTHALPY OF A VAPOR MIXTURE OF HF ANDC H20 WAS DERIVED BY W. R. WILLIAMS FROM THE ABOVE CITED PLOT AND FRctlC INFORMATION PRESENTED IN JOHN M. BECKERDITE, DAVID R. POWELL, ANDC EMORY T. ADAMS, JR., "SELF-ASSOCIATION OF GASES. 2. THE ASSOCIATIONC OF HYDROGEN FLUORIDE," J. CHEM. ENG. DATA 1983, 28, 287-293.C
HV = (1051.0DO + 0.472DO*TF) - (376.0DO + 0.136DO*TF* + 790.642DO*C3POLY + 667.358DO*C6POLY)*WHFV
103
CRETURN
CEND
B.12 HUF6
SUBROUTINE HUF6 (TF, PSIA, MW, HSOL, HLIQ, HVAP)
THE FOLLOWING SUBROUTINES ARE CALLED.
THE ENTHALPY CORRELATIONS ARE BASED OF INFORMATION FOUND IN R.DEWITT, ·URANIUM HEXAFLUORIDE: A SURVEY OF THE PHYSICO-CHEMICALPROPERTIES, II GAT-280, GOODYEAR ATOMIC CORP., PORTSMOUTH, OHIO, JAN.29, 1960, PAGES 65 - 67. THE CORRELATIONS REPORTED IN GAT-280 FOR THEENTHALPIES OF THE SOLID AND LIQUID ARE FOR SATURATED CONDITIONS, ANDTHE ENTHALPY OF THE VAPOR IS BASED ON A PRESSURE OF 1 ATM. THE LIQUIDENTHALPY CORRELATION WAS MODIFIED FOR SUPERSATURATED CONDITIONS (PSIAGRAETER THAN VPSIA) ASSUMING AN INCOMPRESSIBLE LIQUID. THE VAPORENTHALPY CORRELATI ON WAS MODI FI ED USING THE MAGNUSON EQUATI ON OFSTATE (SEE GAT-280, PAGES 97 - 101) AND THE DEPARTURE FUNCTIONCORRELATIONS GIVEN IN R. C. REID, J. M. PRAUSNITZ, AND T. K.SHERWOOD, THE PROPERTIES OF GASES AND LIQUIDS, 3RD ED., MCGRAW-HILLBOOK COMPANY, 1977, PAGE 93, SO THAT BOTH SATURATED AND UNSATURATEDVAPOR ENTHALPIES CAN BE CALCULATED.
TEMPERATURE, DEG FABSOLUTE TEMPERATURE, DEG R(DEG R)**2PRESSURE, PSIAVAPOR PRESSURE CORRESPONDING TO TF, PSIAMOLECULAR WEIGHT, LB MASS/LB MOLEENTHALPY OF THE SOLID, BTU/LB MASSENTHALPY OF THE LIQUID, BTU/LB MASSENTHALPY OF THE VAPOR, BTU/LB MASSDENSITY OF THE LIQUID, LB MASS/FT**3VAPOR COMPRESSIBILITY FACTOR AT TF AND PSIAVAPOR COMPRESSIBILITY FACTOR AT TF AND 14.696 PSIA
DENUF6VPRUF6ZUF6
TFTRTRSQPSIAVPSIAMWHSOLHLIQHVAPDENLIQZPSIAZlATM
CC THIS SUBROUTINE CALCULATES THE ENTHALPIES OF UF6 SOLID, LIQUID, ANDC VAPOR. THE FOLLOWING VARIABLES ARE USED.CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCC
CIMPLICIT REAL*8 (A-H,J-Z)
TR =TF + 459.67DOC
TRSQ =TR**2CC THE ENTHALPY OF THE SOLID IS GIVEN BY THE FOLLOWING CORRELATION WHICH
104
C IS ACCURATE WITHIN 0.01% FROM 17 DEG F TO THE TRIPLE POINT (147.3C DEG F).C
HSOL = ( 50.446000 - 5.70531D-2*TR + 1.27509D-4*TRSQ* - ( 9.64563D3/TR ) ) * ( 3.52D2/MW )
CC CALCULATE THE DENSITY OF THE LIQUID AND THE VAPOR PRESSURE.C
CALL DENUF6 (TF, PSIA, MW, O.ODO, DENLIQ, O.ODO)C
CALL VPRUF6 (TF, VPSIA)CC THE ENTHALPY OF THE LIQUID IS GIVEN BY THE FOLLOWING CORRELATIONC WHICH IS REPORTED TO HAVE AN ACCURACY WITHIN 0.01% [OVER THE ASSUMEDC RANGE OF 147.3 TO 206.3 DEG F] FOR THE SATURATED LIQUID.C
HLIQ =( 30.6133DO + 5.10057D-2*TR + 5.13165D-5*TRSQ* - ( 6.13934D3/TR )* + ( 1.82628D-1 * ( PSIA - VPSIA ) / DENLIQ )* * ( 3.52D2IMW )
CC CALCULATE THE VAPOR COMPRESSIBILITY AT 14.696 PSIA AND AT apSIA.·C
CALL ZUF6 (TF, 14.696DO, ZlATM, O.ODO, O.ODO)C
CALL ZUF6 (TF, PSIA, ZPSIA, O.ODO, O.ODO)CC THE ENTHALPY OF THE VAPOR IS GIVEN BY THE FOLLOWING CORRELATION.C
HVAP**
CRETURN
CEND
= ( 43.2614DO + 9.21307D-2*TR + 6.26265D-6*TRSQ+ ( 2.95171D3/TR )+ 3.0939D-3 * TR * (ZPSIA - ZlATM) ) * ( 3.52D2/MW )
B.13 HUMID
SUBROUTINE HUMID (IC, RH, RATIO)
THE FOLLOWING VARIABLES ARE USED.
NODE NUMBER OF VECTOR HAVING TEMPERATURE ANDPRESSURE REQUIRED FOR CALCULATING RATIORELATIVE HUMIDITY CORRESPONDING TO TEMPERATUREAND PRESSURE OF NODE IC
RH
IC
INPUT VARIABLES
CC THIS SUBROUTINE CALCULATES THE RATIO OF MOLES OF WATER VAPOR IN HUMIDC AIR TO THE TOTAL MOLES OF AIR PLUS WATER VAPOR.CCCCCCCCCC
105
C OUTPUT VARIABLECC RATIO RATIO OF MOLES OF WATER VAPOR TO TOTAL MOLES OFC MOIST AIRCC COMMON BLOCK VARIABLESCC TC (30) NODE TEMPERATURE, DEG FC PC (30) NODE PRESSURE, PSIACC INTERNAL VARIABLESCC WHFL WEIGHT FRACTION OF HF IN HF-H20 CONDENSATEC PH20 VAPOR PRESSURE OF H20, PSIACC THE FOLLOWING SUBROUTINE IS REQUIRED.CC PHFH20CC THE SUBROUTINE HFPOLY IS CALLED BY PHFH20, BUT IT IS NOT CALLED INC CALCULATING PH20 FOR THIS SUBROUTINE.C
IMPLICIT REAL*8 (A-H,J-Z)C
C
C
C
C
C
COMMON /COMPTP/ TC(30), PC(30), DUM1(30)
WHFL = 0.00
CALL PHFH20 (TC(IC), WHFL, 0.00, 0.00, PH20, 0.00)
RATIO = RH*PH20/PC(IC)
RETURN
END
B.14INTMEB
SUBROUTINE ItfTMEBCC THIS SUBROUTINE DETERMINES THE FINAL STATE (PRESSURE, TEMPERATURE,C MASS FRACTIONS IN EACH PHASE) OF UF6 IN A CONTROL VOLUME GIVEN THEC INITIAL STATES OF INLET AND OUTLET STREAMS AND OF THE MASS IN THEC VOLUME AT THE BEGINNING OF A TIME STEP DURING WHICH MASS AND ENERGYC ARE ASSUMED TO FLOW AT CONSTANT RATES.C
IMPLICIT REAL*8 (A-H,J-Z)CC COMMON BLOCKS TRANSFER DATA BETWEEN INTMEB AND THE DRIVER.C
COMMON /ICOMON/ ISEN,IPIG,IBRCH,IGEXITCOMMON /CONCYL/ PCYL,TCYL,XVCYL,XLCYL,MWCOMMON /CONIN / PIN,TIN,XVIN,XLIN
106
C
COMMON ICONVOLI PVOL,TVOL,XVOL,XLVOLCOMMON IPARAM I VOL,DELT,QCOMMON /MASS I MOUT,MIN,MTOTCOMM~~ /TRIPLEI TTRIPL,PTRIPL
DIMENSION HARRAY(3,3),HVECTR(3)CC THE ARRAY FOR ENTHALPIES OF MATERIAL AT TIME T IS FILLEDC
CALL HUF6(TVOL,PVOL,MW,HARRAY(1,3),HARRAY(1,2),HARRAY(1,1»CALL HUF6( TIN, PIN,MW,HARRAY(2,3),HARRAY(2,2),HARRAY(2,1»CALL HUF6(TVOL,PVOL,MW,HARRAY(3,3),HARRAY(3,2),HARRAY(3,1»
C~~ =
* MTOT*(HARRAY(3,1)*XVOL + HARRAY(3,2)*(1.DO-XVOL)*XLVOL* + HARRAY(3,3)*(1.DO-XVOL)*(1.DO-XLVOL»*+(MIN*(HARRAY(2,1)*XVIN + HARRAY(2,2)*(1.DO-XVIN)*XLIN* + HARRAY(2,3)*(1.DO-XVIN)*(1.DO-XLIN»*-MOUT*(HARRAY(l,l)*XVCYL + HARRAY(1,2)*(1.DO-XVCYL)*XLCYL* + HARRAY(1,3)*(1.DO-XVCYL)*(1.DO-XLCYL»*+ Q)*DELT
cMTOT =MTOT + DELT*(MIN-MOUT)
CC FIRST ASSUME A FINAL CONDITION AT THE TRIPLE POINTC
CALL HUF6 (TTRIPL,PTRIPL,MW,HVECTR(3),HVECTR(2),HVECTR(1»c
CALL DENUF6(TTRIPL,PTRIPL,MW,DENSOL,DENLIQ,DENVAP)
ITER8R = 0
MSOL =MTOT-MVAP-MLIQ
IF (MLIQ.LT.O.DO) GO TO 50IF (MSOL.LT.O.DO) GO TO 20
OLDSOL =MSOLOLDT =TTRIPL
= ~OT/(HVECTR(2)-HVECTR(3»
-MTOT*HVECTR(3)/(HVECTR(2)-HVECTR(3»-MVAP*(HVECTR(1)-HVECTR(3»/(HVECTR(2)-HVECTR(3»
= DENVAP*( VOL*DENLIQ*DENSOL*(HVECTR(2)-HVECTR(3»tMTOT*(DENSOL*HVECTR(3)-DENLIQ*HVECTR(2»+HTOT*(DENLIQ-DENSOL»
I( DENLIQ*DENSOL*(HVECTR(2)-HVECTR(3»+DENVAP*DENLIQ*(HVECTR(1)-HVECTR(2»-DENVAP*DENSOL*(HVECTR(1)-HVECTR(3»)
TVOL =TTRIPLPVOL = PTRIPLXVOL =MVAPIMTOT
M~P
*****
MLIQ
**
c
c
c
C
C
C
C
107
CIF (MLIQ.EQ.O.DO.AND.MSOL.EQ.O.DO) GO TO 10
CXLVOL =MLIQ/(MLIQfMSOL)
CRETURN
C10 CONTINUE
CXLVOL = 1.DO
CRETURN
CC FOLLOWING CODE SEGMENTS ARE CALLED WHEN FINAL CONDITIONSC DO NOT MATCH THE TRIPLE POINT.C
20 CONTINUECC FINAL TEMPERATURE IS ABOVE TRIPLE POINT. NO SOLID IS PRESENT.C
XLVOL =1.DOC
30 CONTINUEC
CALL HUF6 (TVOL,PVOL,MW,HVECTR(3) ,HVECTR(2) ,HVECTR(l»C
CALL DENUF6(TVOL,PVOL,MW,DENSOL,DENLIQ,DENVAP)C
~JAP = DENVAP*( VOL*DENLIQ*DENSOL*(HVECTR(2)-HVECTR(3»* tMTOT*(DENSOL*HVECTR(3)-DENLIQ*HVECTR(2»* fHTOT*(DENLIQ-DENSOL»* /( DENLIQ*DENSOL*(HVECTR(2)-HVECTR(3»* fDENVAP*DENLIQ*(HVECTR(1)-HVECTR(2»* -DENVAP*DENSOL*(HVECTR(1)-HVECTR(3»)
CMLIQ = HTOT/(HVECTR(2)-HVECTR(3»
* -MTOT*HVECTR(3)/(HVECTR(2)-~)ECTR(3»
* -MVAP*(HVECTR(1)-HVECTR(3»/(HVECTR(2)-HVECTR(3»C
MSOL =MTOT-MVAP-MLIQC
XVOL =MVAP/MTOTC
C
C
C
C
IF (DABS(MSOL).LT.l.D-6) RETURN
IF (MSOL.GT.O.DO) GO TO 40
OLDSOL =MSOLOLDT = TVOLTVOL = HITVOLMSOL = HIMSOL
40 CONTINUE
C
C
C
C
C
C
C
108
NEWT =TVOL - MSOL*(TVOL-OLDT)/(MSOL-OLDSOL)
IF (NEWT.GT.250.DO.OR.NEWT.LT.TTRIPL) STOP02
ITER8R =1 + ITER8R
IF (ITER8R.GT.20) STOP03
HIMSOL =MSOLHITVOL =TVOLTVOL =NEWT
CALL VPRUF6(TVOL,PVOL)
GO TO 30
50 CONTINUECC FINAL TEMPERATURE IS BELOW TRIPLE POINT. NO LIQUID IS PRESENT.C
XLVOL = O.DOTVOL =TTRIPL - 10.DO
C
CCALL VPRUF6(TVOL,PVOL)
60 CONTINUE
CALL HUF6 (TVOL,PVOL,MW,HVECTR(3),HVECTR(2),HVECTR(1»
CALL DENUF6(TVOL,PVOL,MW,DENSOL,DENLIQ,DENVAP)
C
C
C
C
MVAP
*****
MLIQ
**
= DENVAP*( VOL*DENLIQ*DENSOL*(HVECTR(2)-HVECTR(3»+MTOT*(DENSOL*HVECTR(3)-DENLIQ*HVECTR(2»+HTOT*(DENLIQ-DENSOL»
I( DENLIQ*DENSOL*(HVECTR(2)-HVECTR(3»+DENVAP*DENLIQ*(HVECTR(1)-HVECTR(2»-DENVAP*DENSOL*(HVECTR(1)-HVECTR(3»)
= HTOT/(HVECTR(2)-HVECTR(3»-MTOT*HVECTR(3)/(HVECTR(2)-HVECTR(3»-MVAP*(HVECTR(1)-HVECTR(3»/(HVECTR(2)-HVECTR(3»
C
C
C
C
C
C
MSOL =MTOT-MVAP-MLIQ
XVOL =MVAPIMTOT
IF (DABS(MLIQ).LT.l.D-6) RETURN
IF (MLIQ.GT.O.DO) GO TO 80
OLDLI Q = MLI QOLDT = TVOL
IF (ITER8R.GT.0.DO) GO TO 70
109
CTVOL = TVOL - 10.00
C
CCALL VPRUF6(TVOL,PVOL)
GO TO 60C
70 CCNfINUEC
OLDT = TVOLOLDLIQ = MLIQTVOL = LOTVOLMLIQ =LOMLIQ
C80 CONTINUE
CITER8R = 1 + ITER8R
CIF (ITER8R.GT.20) STOP04
CNEWT = TVOL + MLIQ*(OLDT-TVOL)/(MLIQ-OLDLIQ)
C
C
C
C
C
C
IF (NEWT.GT.TTRIPL.OR.NEWT.LT.O.DO) STOP05
LOMLI Q = MLI QLOTVOL = TVOLTVOL = NEWT
CALL VPRUF6(TVOL,PVOL)
GO TO 60
RETURN
END
B.15 LEVEL
SUBROUTINE LEVEL (DENVAP, VLFACE)CC THIS SUBROUTINE CALCULATES THE LEVEL OF THE PHASE INTERFACE WITHC RESPECT TO THE BOTTOM OF A Cm~TAINMENT VOLUME AND W.R.T. A BREACHC OR PIPE SYSTEM ENTRANCE. THE CODE THEN DETERMINES THE MASS FRACTIONSC OF VAPOR, LIQUID, AND SOLID WHICH LEAVE THE CONTAINMENT AND THEC PRESSURE OF THE RELEASE, IF DIFFERENT FROM THE SATURATION PRESSURE.CC THE TOTAL MASS IN CONTAINMENT IS INPUT ALONG WITH THE TOTAL VOLUME,C SATURATION PRESSURE AND TEMPERATURE, AND THE MASS FRACTIONS OF EACHC PHASE PRESENT. ALSO INPUT ARE THE Cm~TAINMENT PARAMETERS OF LENGTHC AND DIAMETER, THE BREACH PARAMETERS OF HOLE DIAMETER AND DISTANCE OFC THE HOLE CENTER FROM THE CONTAINMENT CENTER. THE C~~TAINMENT ISC MODELED AS A CYLINDER WITH THE HOLE IN ~~E END AND THE CYLINDERC ORIENTATION (UPRIGHT OR ON ITS SIDE) IS ALSO INPUT.
110
INTERNAL VARIABLES USED BY THE LEVEL SUBROUTINE
OUTPUT VARIABLES, VALUES RETUP~ED TO CALLING PROGRAM.
VAPOR MASS FRACTIONOF MATERIAL ENTERING RELEASE PATHWAY.PRESSURE OF MATERIALENTERING RELEASE PATHWAY, PSIA
DENSITY OF ~~POR, LB MASS/FT**3HEIGHT ABOVE CYLINDER BOTTOM OF VAPOR-LIQUIDINTERFACE, INMASS FRACTION OF VAPOR IN CYLINDERTOTAL MASS IN CYLINDER, LB MASSTOTAL VOLUME ENCLOSED IN CYLINDER, FT**3DIAMETER OF CYLINDER, INLENGTH OF CYLINDER, INLENGTH OF RAY FROM CENTER OF CYLINDERTO CENTER OF HOLE, INDIAMETER OF HOLE, IN
IVERT
WOLVOL2,
VVOL2RADIANISPLIT
DENLS
DHOLE
ALPHA ANGLE BETWEEN VERTICAL UPWARD RAY AND RAY FROMCENTER OF CYLINDER TO CENTER OF HOLE, DEGREESVOLUME OF VAPOR IN CYLINDER, FT**3TOTAL VOLUME AND VAPOR VOLUME IN CYLINDER,RESPECTIVELY, IN**3ANGLE AS DEFINED FOR ALPHA, RADIANS=0, VAPOR-LIQUID INTERFACE IS ABOVE (BELOW) HOLE=1, VAPOR-LIQUID INTERFACE COINCIDES WITH HOLE=0, CYLINDER LIES ON SIDE=1, CYLINDER STANDS ON END, HOLE ON BOTTOM
ITER8R INDEX USED TO CONTROL NUMBER OF ITERATIONSAl,A2,A3 OLD, CURRENT, AND NEW RESULTS FOR VLFACEG1,G2,G3 OLD, CURRENT, AND NEW GUESSES FOR VLFACEOLDVLF STORAGE LOCATION FOR PREVIOUS VALUE OF VLFACE.HINTER DEPTH OF LIQUID ABOVE BOTTOM OF HOLE, INYVCYL VAPOR VOLUME FRACTION
OF MATERIAL ENTERING RELEASE PATHWAY.DENSITY OF THE MASS FRACTION WHICH IS NOT VAPOR,LB MASS/FT**3
DENVAPVLFACE
XVCYL
XVOLMTOTVOLDIACYLLCYLRHOLE
PCYL
CC INPUT VARIABLES, VALUES PROVIDED BY CALLING PROGRAM.CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCC
IMPLICIT REAL*8 (A-H,J-Z)CC C~1MON BLOCKS TRANSFER MOST OF THE INPUT ~~D OUTPUT VALUES.C
C~1MON /CONCYL/ PCYL,TCYL,XVCYL,XLCYL,MWCOMMON /CONVOLI PVOL,TVOL,XVOL,XLVOLCOMMON /PARAM I VOL,DELT,QCOMMON IMASS I MSFLRT,MIN,MTOTCOMMON ICYLINDI DIACYL,LCYL,RHOLE,DHOLE,ALPHA,IVERT
C
111
C CALCULATE THE VOLUME OF VAPOR IN THE CYLINDER.C
VVOL =XVOL*MTOT/DENVAPCC VOL AND VVOL ARE IN CUBIC FEET. CONVERT TO CUBIC INCHES.c
VOL2 =VOL*1728.DOC
VVOL2 =VVOL*1728.DOCC ALPHA IS IN DEGREES. USE EQUIVALENT ANGLE IN RADIANS.C
RADIAN =ALPHA*3.14159DO/180.DOCC AN INTEGER INDEX IS SET TO ZERO FOR A VAPOR-LIQUID INTERFACE ABOVEC THE TOP OF THE HOLE OR BELOW THE BOTTOM OF THE HOLE. IF THE VAPORC LIQUID INTERFACE IS FOUND TO COINCIDE WITH THE HOLE, THE INDEX WILLC BE RESET TO 1.C
ISPLIT = 0cC IF THE HOLE IS AT THE BOTTOM OF A CYLINDER STANDING ON END, THEC VAPOR-LIQUID INTERFACE CAN BE CALCULATED DIRECTLY. THE PROGRAM WILLC SKIP DOWN TO THAT SECTION.C
IF (IVERT.EQ.1) GO TO 70CC CALCULATE VAPOR-LIQUID INTERFACE. START WITH THE VALUE OF VLFACEC PASSED FROM THE CALLING PROGRAM. THEN EVALUATE VLFACE USING THEC PREVIOUS VALUE AS A GUESS.C
C
C
C
C
C
C
ITER8R = 0
Ai = 0.00
G1 = 0.00
A2 = 0.00
G2 = 0.00
A3 = 0.00
G3 = 0.00C
10 CONTINUEC
OLDVLF =VLFACEC
VLFACE = DIACYL/2.DO*(1.DO + DCOS(3.14159DO*LCYLIVOL2* *(VVOL2/LCYL + (VLFACE - DIACYL/2.DO)* *DSQRT(VLFACE*DIACYL - VLFACE**2»»
CC IF VLFACE CONVERGES STOP THE ITERATION.
112
CIF (DABS(VLFACE-OLDVLF).LT.l.D-6) GO TO 60
CITER8R = ITER8R + 1
CC IF VLFACE DOES NOT CONVERGE STOP EXECUTION.C
IF (ITER8R.GT.I00) STOP06C
C
C
IF (VLFACE.GT.OLDVLF.AND.Gl.GT.Al) GO TO 20
Gl = OLDVLF
Al = VLFACEC
GO TO 10C
20 CONTINUECC A REGULA FALSIC
SCHEME DETERMINES FURTHER GUESSES FOR VLFACE.
C
C
C
C
G2 = OLDVLF
A2 = VLFACE
30 CONTINUE
G3 = (G2*(AI-A2)-A2*(GI-G2»* I( (AI-A2) - (GI-G2»
A3 = DIACYL/2.DO*(1.DO + DCOS(3.14159DO*LCYLfiJOL2* *(VVOL2ILCYL + (G3 - DIACYL/2.DO)* *DSQRT(G3*DIACYL - 63**2»»
CC IF A3 CONVERGES STOP THE ITERATION.C
IF (DABS(A3-G3).LT.l.D-6) GO TO 50C
ITER8R = ITER8R + 1CC IF A3 DOES NOT CCNVERGE STOP EXECUTION.C
IF (ITER8R.GT.I00) STOPO?CC THIS MODIFIED REGULA FALSI SELECTS WHICH OF THE TWO PREVIOUS GUESSESC TO REPLACE WITH THE NEW GUESS. BY THIS MEANS THE REGULA FALSI IS .C ALWAYS USED FOR INTERPOLATION, SPEEDING CONVERGENCE.C
C
C
C
IF (G3.LT.A3) GO TO 40
A2 = A3
G2 = G3
113
GO TO 30C
40 CONTINUEC
Ai =A3C
Gl = G3C
GO TO 30C
50 CONTINUECC HEIGHT OF THE VAPOR-LIQUID INTERFACE IS DETERMINED. THE LAST PAIR OFC GUESS AND RESULT IS STORED AS OLDVLF AND VLFACE, RESPECTIVELY.C
VLFACE =A3C
OLDVLF =G3C
60 CONTINUECC NOW CALCULATE THE DEPTH OF LIQUID ABOVE THE BOTTOM OF THE HOLE.C
HINTER =VLFACE - (DIACYL/2.DO + RHOLE*DCOS(RADIAN)* - DHOLE/2.DO)
CC HINTER NEGATIVE MEANS VAPOR-LIQUID INTERFACE IS BELOW BOTTOM OF HOLE;C A VAPOR RELEASE OCCURS. SINCE THE CALLING PROGRAM HAS ALREADYC INITIALIZED A VAPOR RELEASE, LEVEL RETURNS WITHOUT FURTHERC CALCULATION.C
IF (HINTER.LE.O.DO) GO TO 100CC THE LIQUID LEVEL IS ABOVE THE BOTTOM OF THE HOLE. IF IT IS ABOVE THEC TOP OF THE HOLE, THE RELEASE WILL CONTAIN NO VAPOR. CALCULATE THEC INTERFACE LEVEL FOR A PRESSURE CORRECTION.C
VLFACE = HINTER - DHOLE/2.DOC
IF (HINTER.GE.DHOLE) GO TO 80CC THE LIQUID LEVEL COINCIDES WITH THE HOLE LEVEL. CALCULATE THE VAPORC VOLUME FRACTION AND SET ISPLIT TO 1.C
YVCYL = (ACOS(S~GL(2.DO*HINTER/DHOLE-1.DO»
* -4.DO/DHOLE**2*(HINTER-DHOLE/2.DO)* *DSQRT(DHOLE*HINTER-HINTER**2»/3.14159DO
CISPLIT = 1
C70 CONTINUE
CC CALCULATE DEPTH OF LIQUID IN VERTICAL CYLINDER.C
114
VLFACE = LCYL*VVOLIVOLC
80 CONTINUECC SET XVCYL TO ZERO AND CALCULATE THE DENSITY OF THE NON-VAPOR t1ASSC FRACTION.C
XVCYL = O.DOC
DENLS =MTOT*(l.DO-XVOL)/(VOL-VVOL)C
IF (ISPLIT.NE.l) GO TO 90CC IF THE LIQUID LEVEL COINCIDES WITH THE LEVEL OF THE HOLE THE VAPORC MASS FRACTION OF THE RELEASE IS RECALCULATED. VLFACE IS SET TO ZEROC SO THAT THE PRESSURE OF THE RELEASE WILL EQUAL THE SATURATI~1
C PRESSURE.C
XVCYL = YVCYL*DENVAP/DENLS* l(l.DO - YVCYL + YVCYL*DENVAP/DENLS)
CVLFACE = O.DO
C90 CONTINUE
CC CALCULATE RELEASE PRESSURE. NO CORRECTION IF VLFACE IS ZERO.C
PCYL = PVOL + VLFACE*DENLS/1728.DOC
100 CONTI NUEC
VLFACE = OLDVLFCC THIS SUBROUTINE CANNOT PROVIDE REASONABLE RESULTS IF THE UF6 GOESC SOLID BEFORE THE INTERFACE DROPS BELOW THE BOTTOM OF THE HOLE. CHECKC FOR THIS RESULT AND STOP IF A PROBLEM IS ENCOUNTERED.C
IF (XLCYL.EQ.O.DO.AND.XVCYL.NE.l.DO) STOPllC
RETURNC
END
B.16 MIXFLW
SUBROUTINE MIXFLW (IC, INLET, INODES)CC *********************************************************************C * *C * WARNING! THIS SUBROUTINE USES THE NULL VECTOR (NODE 30) FOR *C * INTERMEDIATE STORAGE. NODE 30 VALUES ARE RESET TO THOSE VALUES *C * ASSIGNED BY THE SUBROUTINE SETPAY. *C * *
115
COMMON BLOCK VARIABLES
THE FOLLOWING SUBROUTINE IS CALLED BY MIXFLW.
THE FOLLOWING SUBROUTINES ARE ALSO REQUIRED.
THE FOLLOWING VARIABLES ARE USED IN THIS SUBROUTINE.
TEMPORARY STORAGE VARIABLE
COMPONENT MASS FLOW RATE, LBI (DELT)NODE TEMPERATURE, DEG FNODE PRESSURE, PSIAVOLUMETRIC FLOW RATE THROUGH STREAM NODE,FT**3IMINNODE ENTHALPY RATE, BTU/(DELT)NODE INPUT STREAM NUMBERNODE OUTPUT STREAM NUMBERMINIMUM NATURAL LOG ACCEPTED BY THE COMPUTERTIME INTERVAL USED IN TRANSIENT SIMULATION, SEC
NODE NUMBER REPRESENTING COMBINED STREAMNUMBER OF STREAMS TO BE MIXED (MAXIMUM OF 4)MAXIMUM NUMBER OF NODES ALLOWED BY THE SET OFSUBROUTINES OF WHICH THIS SUBROUTINE IS A PART,CORRESPONDS TO THE NULL VECTOR NODE NUMBER
COMPRT
DENTHLDENUF6HFPOLYHHFH20HUF6PHASEPHFH20VPRUF6ZUF6
(30)(30,4)(30,4)
(30,9)(30)(30)(30)
IOUTMP
HI INlOUTAMINLNDELT
ICINLETINODES
MASSTCPCACFM
INTERNAL VARIABLE
INPUT VARIABLES
THIS SUBROUTINE COMBINES UP TO 4 INLET STREAMS AND DETERMINES THEOUTLET PHASE COMPOSITION AND TEMPERATURE AT A GIVEN FINAL PRESSURE.IF REACTIVE COMPONENTS ARE IN THE STREAMS, THEY ARE ALLOWED TOREACT TO THE EXTENT OF THE LIMITING REACTANT. ALL INLET STREAMS MUSTBE BLOWER NODES.
C *********************************************************************CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCC
IMPLICIT REAL*8 (A-H,J-Z)C
COMMON ILBMASSI MASS(30,9), DUMl
116
COMMON ICOMPTPI TC(30), PC(30), DUM2(30)COMMON /vOLUMEI ACFM(30), DUM3(61)COMMON IENTHAU H(30), DlJ14(120)COMMON IISTRMSI IIN(30,4), IOUT(30,4)CotflON ICONTRU AMINLN, DlJ15, DELT, DUM6, IDUM1, DUM7
CC SPECIFY INITIAL ESTIMATES OF MIXED STREAM TEMPERATURE AND VOLUMEC FLOW RATE.C
C
C
C
C
C
C
C
IF (TC(IC).EQ.O.DO) TC(IC) = TC(IIN(IC,l»
IF (ACFM(IC).GT.O.DO) GO TO 20
ACFM(I C) = O. DO
DO 10 I10=1,INLET
ACFM(IC) = ACFM(IC) + ACFM(IIN(IC,I10»
10 CONTINUE
20 CONTINUE
ACFM(IC) = ACFM(IC)*DELT/6.D1CC SET NODE IC COMPONENT MASS AND ENTHALPY RATES TO ZERO AND TEMPORARI LYC SET THE OUTLET NODE OF NODE IC TO THE NULL VECTOR.C
C
C
C
C
C
DO 30 130=1,9
MASS(IC,I30) = O.DO
30 CONTINUE
H(I C) = O. DO
IOUTMP = IOUT(IC,l)
IOUT (I C, 1) = 30CC COMBINE STREAMS TO OBTAIN COMPONENT MASS AND ENTHALPY RATES, THENC RESET OUTLET STREAM NODE FOR NODE IC.C
CALL COMPRT (I C, INLET, INODES)C
IOUT(IC,l) = IOUTMPCC SET "NULL VECTOR" VALUES TO BEGIN ITERATION TO OBTAIN MIXED STREAMC PHASE COMPOSITION AND TEMPERATURE AS WELL AS VOLUME FLOW RATE WHICHC CORRESPOND TO THE OUTLET PRESSURE.C
CACFM(30) = ACFM(IC)*PC(IC)/PC(IOUT(IC,l»
H(30) = H(IC)
117
CTC(30) = TCnC)
C
C
C
C
C
C
C
c
C
DO 40 140=1,9
MASS(30,I40) = MASS(IC,I40)
40 CONTINUE
50 CONTINUE
CALL COMPRT (30, 1, INODES)
IF (DABS(PC(30) - PC(IOUT(IC,1»).LT.l.D-4) GO TO 60
ACFM(30) = ACFM(30)*PC(30)/PC(IOUT(IC,1»
GO TO 50
60 CONTINUECC TRANSFER TEMPORARY VALUES STORED IN THE NULL VECTOR TO NODE VECTORC IC, THEN RESET NULL VECTOR VALUES.C
DO 70 170=1,9C
MASS n C, I70 ) = MASS( 30, 170)MASS (30 , I70 ) = 0.00
C70 CONTINUE
CPCn C) = PC(30)PC(30) = 0.00
CTCnC) = TC(30)TC(30) = 0.00
CH(30) = 0.00
CACFM( IC) = 6.Dl*ACFM(30)/DELTACFM(30) = 0.00
CRETURN
CEND
B.17 PHASE
SUBROUTINE PHASE (TF, IC)cC THIS SUBROUTINE CALCULATES THE PHASE COMPOSITION OF THE HF-H20 SYSTEMC IN A COMPARTMENT. THE FOLLOWING VARIABLES ARE USED.C
118
LNPHF1, LNPHF2 LN(PHF) AT I AND I + 1
IJ INDEX CONTROLLING PHASE ITERATION SCHEMEICOUNT COUNTER FOR PHASE ITERATION SCHEME
COEFFICIENTS FOR LN(PHF) =AITR + B
TEMPERATURE, DEG FABSOLUTE TEMPERATURE, DEG RNUMBER OF NODE BEING EVALUATEDMASS OF COMPONENT IN NODE, LBMASS OF WATER IN NODE, LBMASS OF HF IN NODE, LBCOMBINED MASS OF H20 AND HF IN NODE, LBMASS OF HF AND H20 VAPOR IN NODE, LBCOMPONENT MOLECULAR WEIGHT, LB/LB MOLEESTIMATED MOLECULAR WEIGHT OF HF VAPOR, LB/LB MOLEVOLUME OF NODE, FT**3WEIGHT FRACTION OF HF IN THE HF-H20 LIQUID CONDENSATE,LB HF LIQ/LB HF-H20 LIQ MIXWEIGHT FRACTION OF HF IN THE HF-H20 VAPOR MIXTURE,LB HF VAP/LB HF-H20 VAP MIXWEIGHT FRACTION HF IN THE HF-H20 SYSTEM, LB HF/LB HF+H20WEIGHT FRACTION OF HF IN AN HF-H20 MIXTURE OF AZEOTROPICCOMPOSITION, LB HF/LB HF-H20 MIXWEIGHT FRACTION OF HF IN THE LIQUID REQUIRED TO YIELDPHF BASED ON THE CONCENTRAT ION OF HF ASSUMED TO BEVAPOR ONLY, LB HF LIQUID/LB HF-H20 LIQ MIXPARTIAL VAPOR PRESSURE OF HF, PSIAPARTIAL VAPOR PRESSURE OF H20, PSIAVAPOR PRESSURE OF THE HF-H20 SYSTEM, PSIAMOLE FRACTION OF HF IN THE HF-H20 VAPOR SYSTEM, MOLES HFVAPORIMOLES HF-H20 VAPOR MIXTUREMOLES OF HF-H20 VAPOR MIXTURE, MOLES/LB PLUMEPARTIAL PRESSURE OF HF-H20 VAPOR MIXTURE RESULTING FROMNVAP, VOLUME, AND TR, PSIAPCALC - PSUMPRESSURE CONVERSION FACTOR FROM TORR TO PSIAMINIMUM NATURAL LOG ACCEPTED BY COMPUTERLN(PHF/PCONV)
WHF
A, B
WHFV
WHFTOTAZEOTR
HFPOLYPHFH20
PDIFPCONVAMINLNLNPHF
PHFPH20PSUMYHF
NVAPPCALC
TFTRICMASSMSSH20MSSHFMSSTOTMSSVAPWMOLMWVOLWHFL
CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCC THE FOLLOWING SUBROUTINES ARE CALLED.CCCC
IMPLICIT REAL*B (A-H,J-Z)C
DIMENSION WHFL(3), PDIF(3)DIMENSION A(20), B(20)
CCOMMON /LBMASS/ MASS(30,9), DUMlCOMM~~ /VOLUME/ VOL(30), DUM2(61)C~1M~~ /MOLWT/ WMOL(9)
119
COMMON ICONTRLI AM INLN, OUM3, OUM4 (2), IOUM1, OUM5C
DATA A 1-1068900,-1053600,-1064700,-1067500,-1046000,-1036200,* -9779.500,-8917.700,-8188.200,-7770.000,-7575.000,-7411.400,* -7315.700,-7163.400,-6984.300,-6459.700,-6269.700,-5891.700,* -5849.800,-5641.0001
CDATA B 117.68000,18.06900,18.79300,19.40900,19.59500,19.95100,
* 19.42900,18.94800,18.25600,17.97500,18.05400,18.17800,* 18.36500,18.45700,18.49200,17.85700,17.81200,17.39100,* 17.55500,17.364001
CTR =TF + 459.6700PCONV =14.69600/7.602
CMSSHF = MASS(IC,4) + MASS(IC,5)MSSH20 =MASS(IC,2) + MASS(IC,3)MSSTOT =MSSHF + MSSH20
CWHFTOT = MSSHF/MSSTOT
CC THE FOLLOWING SECTION EVALUATES THE WEIGHT FRACTION OF HF IN THEC LIQUIO, WHF, REQUIREO TO YIELO PHF BASEO ON THE ASSUMPTION THAT ALLC HF IS IN THE VAPOR PHASE. IF THE REQUIREO WHF IS GREATER THAN ONE,C CONOENSATION WILL OCCUR. IF WHF IS LESS THAN OR EQUAL TO ONE, PSUMC CORRESPONOING TO WHF IS CALCULATEO ANO COMPAREO TO PHF + PH20 EVALUC ATEO ASSUMING ALL HF ANO H20 IS IN THE VAPOR PHASE. IF PSUM IS LESSeTHAN PHF + PH20, CONOENSATION WILL OCCUR.C
10 CONTINUEC
PHF =MSSHF*TR*10.73DOIVOL(IC)IWMOL(5)C
CALL HFPOLY (TF, PHF, MIN, .TRUE.)C
C
C
C
C
C
C
C
IF (DABS(MW-WMOL(5».LT.1.D-4) GO TO 20
WMOL(5) = (MW + WMOL(5»/2.00
GO TO 10
20 CONTINUE
WMOL(5) = MW
PH20 =MSSH20*TR*10.73001V0L(IC)IWMOL(3)
LNPHF =AMINLN
IF (PHF.GT.O.DO) LNPHF = DLOG(PHF/PCONV)CC THE FOLLOWING EQUATION APPLIES FOR WHF BETWEEN 0.00 ANO 0.05.C
WHF = PHF*0.05DO/PCONV/DEXP(A(1)ITR + B(l»
120
CIF (WHF.LT.0.05DO) GO TO 40
CC THE FOLLOWING SET OF ITERATIVE EQUATIONS IS APPLICABLE BETWEEN 0.05C AND 1.00. IF WHF IS FOUND TO BE GREATER THAN 1 ON THE INTERATION 19,C CONDENSATION OCCURS.C
DO 30 130 =1,19C
LNPHFl =A(I30)/TR + B(I30)LNPHF2 =A(I30+1)/TR + B(I30+1)
40 CONTINUE
50 CONTINUE
IF (WHF.GT.l.DO) GO TO 50
IF (PSUH.LT.(PHF+PH20» GO TO 50
= 0.05DO*«LNPHF - LNPHF1)/(LNPHF2 - LNPHF1)+ DFLOAT(I30»
WHF
MASS(IC,5) =MSSHFMASS(IC,4) = O.DOMASS(IC,3) =MSSH20MASS(IC,2) = O.DO
RETURN
CALL PHFH20 (TF, WHF, O.DO, O.DO, O.DO, PSUM)
*IF (WHF.GE.(0.05DO*DFLOAT(I30».AND.WHF.LE.
* (0.05DO*DFLOAT(I30+1») GO TO 40
30 CONTINUE
C
C
C
C
C
C
C
C
C
C
CC IF CONDENSATION OCCURS, THE FOLLOWING SECTION EVALUATES THEC EQUILIBRIUM VAPOR PHASE COMPOSITION AT TF.C
IF (MSSHF.EQ.0.DO.OR.MSSH20.EQ.0.DO) GO TO 60C
AZEOTR = 0.3826DOC
IF (DABS(AZEOTR-WHFTOT).GE.l.D-6) GO TO 70CC THE FOLLOWING SECTION EVALUATES THE VAPOR CONCENTRATION AT THEC AZETROPE OR FOR A PURE COMPONENT.C
60 CONTINUEC
CALL PHFH20 (TF,WHFTOT,YHF,PHF,PH20,PSUM)C
IF (MSSHF.GT.O.DO) CALL HFPOLY (TF,PHF,WMOL(5),.TRUE.)
121
CMASS(IC,5) = PHF*VOL(IC)*WMOL(5)/10.73DO/TRMASS(IC,4) =MSSHF-MASS(IC,5)MASS(IC,3) =PH20*VOL(IC)*WMOL(3)/10.73DO/TRMASS(IC,2) =MSSH20-MASS(IC,3)
CRETURN
C70 CONTINUE
CICOUNT = 0
CWHFL(l) =AZEOTR + DSIGN(1.D-6,(WHFTOT-AZEOTR»WHFL(2) =WHFTOT
CIJ = 1
CGO TO 90
C80 CONTINUE
CIJ = 2
C90 CONTINUE
CCALL PHFH20 (TF,WHFL(IJ),YHF,PHF,PH20,PSUM)
CCALL HFPOLY (TF,PHF,WMOL(5),.TRUE.)
CWHFV =YHF*WMOL(5)/(YHF*WMOL(5) + (l.DO - YHF)*WMOL(3»
CMSSVAP = (MSSH20*WHFL(IJ) - MSSHF*(l.DO - WHFL(IJ»)
1 / (WHFL(IJ) - WHFV)C
C
C
C
NVAP =MSSVAP*WHFV/WMOL(5) + MSSVAP*(l.DO - WHFV)/WMOL(3)
PCALC = NVAP*10.73DO*TR,/vOL(IC)
PDIF(IJ) = PCALC - PSUM
IF (IJ - 2) 80,100,110C
100 CONTINUEC
ICO~~T = ICOUNT + 1C
IJ = 3C
C
C
C
M = (PDIF(2) - PDIF(1»/(WHFL(2) - WHFL(l»
WHFL(3) =WHFL(2) - PDIF(2)/M
IF «PDIF(1)-PDIF(2».GE.PSUM) WHFL(3) = (WHFL(l) + WHFL(2»/2.DO
122
GO TO 90C
110 CONTI NUEC
IF (DABS(PDIF(3».LT.(PSUM*1.D-3» GO TO 140C
IF (ICOUNT.EQ.l00) STOP12C
IF (PDIF(3» 120,140,130C
120 CONTINUEC
WHFL(2) =WHFL(3)PDIF(2) = PDIF(3)
CGO TO 100
C130 CONTINUE
CWHFL(l) =WHFL(3)PDIF(l) = PDIF(3)
CGO TO 100
C140 CONTINUE
CMASS(IC,5) =MSSVAP*WHFVMASS(IC,4) =MSSHF-MASS(IC,5)MASS(IC,3) =MSSVAP*(l.DO - WHFV)MASS(lC,2) =MSSH20-MASS(IC,3)
CRETURN
CEND
B.18 PHFH20
SUBROUTINE PHFH20 (TF, WHFL, YHF, PHF, PH20, PSUM)
TEMPERATURE, DEG FTEMPERATURE, DEG RWEIGHT FRACTION OF HF IN THE LIQUID HF-H20 MIXTURE,LB HF LIQ/LB HF-H20 LIQ MIXMOLE FRACTION OF HF IN THE VAPOR HF-H20 MIXTURE,MOLES HF VAPOR/MOLES HF-H20 VAPORPARTIAL VAPOR PRESSURE OF HF, PSIAPARTIAL VAPOR PRESSURE OF H20, PSIAVAPOR PRESSURE OF THE HF-H20 VAPOR MIXTURE, PSIA
YHF
PHFPH20PSUM
TFTRWHFL
CC THIS ROUTINE CALCULATES THE MOLE FRACTION OF HF IN THE VAPOR PHASE OFC THE HF-H20 SYSTEM AS WELL AS THE PARTIAL VAPOR PRESSURES OF HF ANDC H20 AND THEIR SUM GIVEN THE TEMPERATURE IN DEG F AND THE WEIGHTC FRACTION OF HF IN THE LIQUID PHASE. THE FOLLOWING VARIABLES ARE USED.CCCCCCCCCC
123
IMPLICIT REAL*8 (A-H,J-Z)
LNPHF1, LNPHF2 LN(PHF) EVALUATEO AT Ii ANO 1211, 12 INOICES FOR EVALUATING PHF (12 = Ii + 1)
OIMENSION A(20), 8(20)
COMMON ICONTRLI AMINLN
PCONV CO~jERSION FACTOR FROM TORR TO PSIA, PSIA/TORR
A, B COEFFICIENTS FOR LN(PHF) =A/TR + 8
LN(PHF)MINIMUM NATURAL LOG ACCEPTEO 8Y COMPUTERMOLECULAR WEIGHT OF HF VAPOR AT THE AZEOTROPE,LB/LB MOLEAZEOTROPIC WEIGHT FRACTION OF HF IN THE HF-H20 SYSTEMPARTIAL tJAPOR OF HF AT THE AZEOTROPIC COMPOSITIONPARTIAL VAPOR OF H20 AT THE AZEOTROPIC COMPOSITIONPHFAZ + PH20AZ
AZEOTRPHFAZPH20AZPAZEOT
LNPHFAMINLNMWAZ
C
C
CCCCCCCCCCCCCCCC
C
C
C
DATA A 1-1068900,-1053600,-1064700,-1067500,-1046000,-1036200,* -9779.500,-8917.700,-8188.200,-7770.000,-7575.000,-7411.400,* -7315.700,-7163.400,-6984.300,-6459.700,-6269.700,-5891.700,* -5849.800,-5641.0001
DATA B 117.68000,18.06900,18.79300,19.40900,19.59500,19.95100,* 19.42900,18.94800,18.25600,17.97500,18.05400,18.17800,* 18.36500,18.45700,18.49200,17.85700,17.81200,17.39100,* 17.55500,17.364001
TR =TF + 459.6700C
PCONV = 14.69600/7.602CC THE FOLLOWING SEQUENCE OF EQUATIONS THROUGH "30 CONTINUE" EVALUATESC THE PARTIAL VAPOR PRESSURE OF HF. THESE EQUATIONS ARE BASEO ON A PLOTC OF PARTIAL VAPOR PRESSURE OF HF VS TEMPERATURE AS A FUNCTION OFC WEIGHT FRACTION OF HF IN THE LIQUIO PHASE. THIS PLOT WAS PROVIOEO TOC W. REIO WILLIAMS BY BRIAN C. ROGERS OF ALLIEO CHEMICAL, SOLVAY, NY,C IN A LETTER OATEO JULY 26, 1983. THE EQUATIONS WERE OERIVEO BY W. R.C WILLIAMS.C
PHF =0.000C
IF (WHFL.LE.(OEXP(AMINLN+6.00») GO TO 30C
11 = IOINT(WHFL/O.0500)C
IF (Il.EQ.20) Ii =19C
12 = 11 + 1C
C
C
C
C
IF (Il.EQ.O) GO TO 10
LNPHFl =A(Il)ITR + B(Il)
10 CONTINUE
LNPHF2 =A(I2)ITR + B(I2)
IF (Il.EQ.O) GO TO 20
1~
CC THE FOLLOWING EQUATION APPLIES FOR WHFL BETWEEN 0.05 AND 1.00.C
LNPHF = LNPHFl + (LNPHF2 - LNPHF1)*(WHFL/0.05 - DFLOAT(Il»C
PHF =PCONV*DEXP(LNPHF)C
GO TO 30C
20 CONTINUECC THE FOLLOWING EQUATION APPLIES FOR WHFL BETWEEN 0.00 AND 0.05.C
PHF = (WHFL/0.05DO)*PCONV*DEXP(LNPHF2)C
30 CONTINUECC THE FOLLOWING SEQUENCE OF EQUATIONS THROUGH "60 CONTINUE" EVALL~TES
C A PSUEDO PARTIAL VAPOR PRESSURE FOR H20. THE EQUATIONS ARE BASED ONC THE VAPOR PRESSURE OF WATER GIVEN IN R. C. REID, J. H. PRAUSNITZ, ANDC T. K. SHERWOOD, THE PROPERTIES OF GASES AND LIQUIDS, 3RD ED., HCGRAWC HILL BOOK COMPANY, 1977, PP. 629 AND 632, AN ESTIMATED VALUE OF THEC PARTIAL VAPOR PRESSURE OF H20 AT THE AZEOTROPE, AND THE REQUIREMENTC THAT PH20 = 0 AT WHFL =1. THE EQUATIONS USED BELOW WERE DERIVED BYC W. R. WILLIAMS.CC THE FOLLOWING EQUATION GIVES THE VAPOR PRESSURE OF H20.C
PH20 = PCONV*DEXP(18.3034DO - 6869.5900/(TF + 376.6400»C
IF (WHFL.EQ.O.DO) GO TO 50CC THE FOLLOWING SEQUENCE OF EQUATIONS ESTIMATES THE PARTIAL VAPORC PRESSURE OF H20 AT THE AZEOTROPE.C
LNPHFl =A(7)/TR + B(7)C
LNPHF2 =A(8)ITR + B(8)C
AZEOTR =0.382600C
LNPHF =LNPHFl + (LNPHF2 - LNPHF1)*(AZEOTR - 0.3500)/0.0500C
PHFAZ = PCONV*OEXP(LNPHF)C
**************************************************************** ** WARNING: THE VALUE OF MASS VELOCITY, G, IS CONSTANT ONLY *
125
C IN THE FOLLOWING CALL TO HFPOLY, THE LOGICAL VARIABLE C1C3C6 ISC SPECIFIED AS .FALSE. SINCE PREVIOUS ESTIMATES OF Cl, C3, AND C6C SHOULD NOT BE CHANGED.C
CALL HFPOLY (TF, PHFAZ, MWAZ, .FALSE.)C
YHF = (AZEOTR/MWAZ)/(AZEOTRIMWAZ + (l.DO - AZEOTR)/18.016DO)C
PH20AZ = (l.DO - YHF)*PHFAZlYHFC
IF (WHFL.GT.0.3826DO) GO TO 40CC THE FOLLOWING EQUATIONS APPLY FOR WHFL BETWEEN 0.0 AND THE AZEOTROPE.C
PAZEOT = PHFAZ + PH20AZC
PSUM = PH20 + (PAZEOT - PH20)*WHFL/AZEOTRC
PH20 = PSUM - PHFC
GO TO 60C
40 CONTINUECC THE FOLLOWING EQUATION APPLIES FOR WHFL BETWEEN THE AZEOTROPE AND 1.C
PH20 = PH20AZ*«1.DO - WHFL)/(l.DO - AZEOTR»**3C
50 CONTINUEC
PSUM = PHF + PH20C
60 CONTINUEC
YHF = PHF/PSUMC
RETURNC
END
B.19 PIPSYS
SUBROUTINE PIPSYS(G)CC THE PIPSYS SUBROUTINE RECALCULATES THE MASS VELOCITY AS IT MOVES Drn~
C THE LENGTH OF THE PIPE AND FIXTURE SYSTEM. THE INITIAL MASS VELOCITYC SUPPLIED TO PIPSYS CORRESPONDS TO THE ENTRANCE EFFECT PRESSURE DROP.C THE TRUE MASS VELOCITY MUST BE LESS THAN OR EQUAL TO THIS FIGURE. SOC A NEW GUESS OF MASS VELOCITY IS CALCULATED.CCCC
126
C * IF THE PIPING SYSTEM DIAMETER IS CONSTANT. HOWEVER, *C * MASS FLOW RATE IS CONSTANT. THESE VALUES ARE RELATED *C * THROUGH PIPE DIAMETERS. THE VALUE GFEAT IS CALCULATED *C * WHEN A MASS VELOCITY POTENTIALLY DIFFERENT FROM THE *C * INITIAL G CAN BE EXPECTED FOR A PARTICULAR DOWNSTREAM *C * FEATURE. *C * *C ***************************************************************C
C
C
C
C
IMPLICIT REAL*8 (A-H,J-Z)
COMMON IICOMONI ISEN, IPIG, IBRCH, IGEXITCOMMON /CONCYL/ PCYL,TCYL,XVCYL,XLCYL,MWCOMMON ICONENTI PENT,TENT,XVENT,XLENT,VNTBARCOMMON IGMTRY 1 PIGRAYCOMMON ICNSTNTI ALPHA,BETA,DELTA,GAMMA,EPSLNCOMMON ITRIPLEI TTRIPL,PTRIPL
DIMENSION PIGRAY(99,3),CONRAY(99,6)
TWELTH = 1.DO/12.DO
REYNMX = 1. 1504CC THE IGEXIT SWITCH CONTROLS THE CALCULATION OF THE EXIT. AT A VALUEC OF IGEXIT=2 THE EXIT IS KNOWN TO BE CONTROLLED BY PRESSURE DROP ANDC THE FURTHER CALCULATI~~ OF GMAX VALUES SHOULD BE SUPPRESSED.C
IGEXIT = 1CC TO BEGIN THE PIPE SYSTEM CALCULATION, A GUESS FOR G ONE-HALF THEC VALUE ENTERED AS PIPSYS WAS CALLED (WHICH MIGHT BE A CHOKE FLOWC VALUE) IS USED IN CALCULATING THE ENTRY PRESSURE DROP. A NEW GMAX FORC CHOKE FLOW IS THEN DETERMINED AND IF THIS VALUE IS LESS THAN THEC ASSUMED G, THE ASSUMED G IS REDUCED BEFORE ENTRY CONDITIONS AREC RECALCULATED.C
CONRAY(IPIG,l) = PIGRAY(IPIG,3)CC SET UPPER AND LOWER BOL~DS ON G AND MAKE FIRST GUESS.C
CONRAY(IPIG,5) = 1.010
IF (IBRCH.LT.3) C~~RAY(IPIG,5) = GC
C
C
C
CONRAY(IPIG,6) = 0.00
IF (IBRCH.LT.3) G
10 CONTINUE
= G/2.DO
CC ON RETURNING TO THIS POINT IN THE SUBROUTINE (I.E., 10 CONTINUE), THEC VALUE OF G HAS BEEN ADJUSTED AND THE ENTIRE PIPE SYST~1 CALCULATIONC IS REPEATED STARTING WITH THE ENTRANCE EFFECT.
127
C
C
C
C
C
C
C
IF ( (CONRAY(IPIG,5)-CONRAY(IPIG,6» I (CONRAY(IPIG,5)+* CONRAY(IPIG,6» .LT.EPSLN) GO TO 200
20 CONTINUE
PENT =PCYL-PIGRAY(1,2)*G**2/DELTA*VNTBAR
CALL FLASH (TCYL,PCYL,MW,XVCYL,XLCYL,PENT,ISEN,XVENT,XLENT,TENT)
CALL DENUF6(TENT,PENT,MW,RHOS,RHOL,RHOV)
OLOVBR = VNTBAR
VNTBAR =XVENT/RHOV+(l.DO-XVENT)*XLENT/RHOL* +(l.DO-XVENT)*(l.DO-XLENT)/RHOS
CC A NEW SET OF ENTRANCE CONDITIONS BASED ON THE NEW VALUE OF MASSC VELOCITY HAS BEEN COMPUTED.C
IF (DABS(VNTBAR-OLDVBR).GT.(EPSLN» GO TO 20C
P2 = PENT-l.D-3CC EVALUATE GMAX BASED ON ISENTROPIC EXPANSION.C
ISNGMX = 0C
CALL FLASH (TENT, PENT, MW, XVENT, XLENT, P2, ISNGMX,* XV2, XL2, T2)
CCALL DENUF6(T2,P2,MW,RHOS,RHOL,RHOV)
CV2BAR =XV2/RHOV+(1.DO-XV2)*XL2/RHOL
* +(1.DO-XV2)*(1.DO-XL2)/RHOSC
GMAX = DSQRT(ALPHA*(PENT-P2)/(V2BAR-VNTBAR»C
IF (GMAX.LE.G) GO TO 180CC LOAD THE FIRST ROW OF CONRAY.C
CONRAY( 1,1) = PENTCONRAY(1 ,2) =TENTCONRAY(1,3) =XVENTCONRAY(1,4) = XLENTCONRAY(1,5) = VNTBARCONRAY(1,6) = GMAX
CIFEAT = 2
C30 CONTINUE
CIF (IFEAT.EQ.IPIG) GO TO 150
128
CGO TO (40,100,130), IDINT(PIGRAY(IFEAT,l»
C40 CONTINUE
CC THE PIPE SOLVER STARTS HERE BY LIMITING THE TOTAL NUMBER OF STEPS TOC THE PRESSURE DIFFERENCE BETWEEN THE BEGINNING OF THE PIPE AND THEC SURROLNDINGS. IN LATER PASSES THE TOTAL PRESSURE DROP CONSIDEREDC WILL BE UPDATED. EACH STEP INCLUDES A CALCULATION OF THE PIPE LENGTHC CORRESPONDING TO AN INCREMENTAL PRESSURE DROP OF ABOUT ONE PSI.C
DELTAP = CONRAY«IFEAT-l),l)-CONRAY(IPIG,l)CC THE TRIPLE POINT PRESSURE MUST NOT BE INCLUDED IN DELTAP IF FLASHINGC FLOW IS OCCURING.C
IF (CONRAY«IFEAT-l),l).GT.PTRIPL .AND.* CONRAY(IPIG,l).LT.PTRIPL .AND.* CONRAY«IFEAT-1),3).NE.1.DO)* DELTAP = CONRAY«IFEAT-l),l)-PTRIPL
CIF (DELTAP.LE.O.DO) GO TO 180
CICON =1
C50 CONTINUE
CIDELP = IDINT(DELTAP)
C
CIF (IDELP.EQ.O) IDELP =1
DELP = DELTAP/DFLOAT(IDELP)Pi = CONRAY«IFEAT-l),i)Tl =CONRAY«IFEAT-i),2)XVi = CONRAY«IFEAT-i),3)XLi = CONRAY«IFEAT-i),4)V1BAR = CONRAY«IFEAT-i),5)DLSUM = 0.00
CC ADJUST THE MASS VELOCITY BASED ON THE ENTRANCE DIAMETER TO THEC CURRENT DIAMETER.C
GFEAT = G*(PIGRAY(1,3)**2)/(PIGRAY(IFEAT,3)**2)C
DO 80 180 = 1,IDELPC
P2 = Pl-DELPC
60 CONTINUEC
PAVG = (P2+Pl)/2.DOC
CALL FLASH (TCYL,PCYL,MW,XVCYL,XLCYL,P2,ISEN,XV2,XL2,T2)C
129
CALL DENUF6(T2,P2,MW,RHOS,RHOL,RHOV)C
V2BAR =XV2/RHOV + (1.DO-XV2)*XL2/RHOL* +(1.DO-XV2)*(1.DO-XL2)/RHOS
CCALL FLASH (TCYL,PCYL,MW,XVCYL,XLCYL,PAVG,ISEN,XVAVG,XLAVG,TAVG)
CCALL DENUF6(TAVG,PAVG,MW,RHOS,RHOL,RHOV)
CVBRAVG =XVAVG/RHOV + (l.DO-XVAVG)*XLAVG/RHOL
* +(1.DO-XVAVG)*(1.DO-XLAVG)/RHOSC
CALL VISUF6(TAVG,PAVG,MW,VISL,VISV)C
VIS = (VISV*XVAVG/RHOV + VISL*(l.DO-XVAVG)*XLAVG/RHOL)/VBRAVGC
REYN =3600.DO*PIGRAY(IFEAT,3)*GFEAT/VISC
BFACTR =1.D25C
IF (REYN.GT.1.D3) BFACTR = (37580.DO/REYN)**16C
AFACTR = O.DOC
IF (REYN.GT.1.D3) AFACTR = (2.457DO** DLOG(1.DO/«7.DO/REYN)**0.9DO + (0.27DO*EPSOD»»**16
CC THE EQUATION FOR FRICTION FACTOR IS OF A TYPE WHICH LEADS TO AN ERRORC MESSAGE IF REYN IS TOO LARGE. LIMITING REYN WILL NOT AFFECT THISC CALCULATION AT THIS POINT. THIS PROBLEM IS SIMPLY A MACHINEC LIMITATION.C
IF (REYN.GT.REYNMX) REYN =REYNMXC
FFACTR = 2.DO*«8.DO/REYN)**12* + (1.DO/(AFACTR+BFACTR)**1.5DO»**TWELTH
CDELTAL = (4633.1DO*(P1-P2) + GFEAT**2*(V1BAR-V2BAR»1
* (2.DO*FFACTR*GFEAT**2*(VB~)G)/PIGRAY(IFEAT,3)
* + 32.174DO*DSIN(THETA)/(VBRAVG»C
C
C
IF (DELTAL.LE.O.DO .AND. IGEXIT.EQ.2) WRITE (5,500) IFEAT
IF (DELTAL.LE.O.DO) GO TO 180
DLSUM = DLSUM + DELTALCC EVALUATE GMAX BASED ON ISENTROPI C EXPANSION.C
P3 = P2-1.D-3C
ISNGMX = 0C
CALL FLASH (T2, P2, MW, XV2, XL2, P3, ISNGMX,
130
* XV3, XL3, T3)C
CALL DENUF6(T3,P3,MW,RHOS,RHOL,RHOV)C
V3BAR =XV3/RHOV+(1.DO-XV3)*XL3/RHOL* +(1.DO-XV3)*(1.DO-XL3)/RHOS
CGMAX = DSQRT(ALPHA*(P2-P3)/(V3BAR-V2BAR»
C
C
C
C
C
C
C
C
C
C
IF (GMAX.LE.GFEAT .AND. DLSUM.LT.(PIGRAY(IFEAT,2)-0.01DO) .AND.* IGEXIT.EQ.2) WRITE (5,510) IFEAT
IF (GMAX.LE.GFEAT .AND. DLSUM.LT.(PIGRAY(IFEAT,2)-O.Ol»* GO TO 180
IF (DABS(DLSUM-PIGRAY(IFEAT,2».LT.l.D-2) GO TO 90
IF (DLSUM.LT.PIGRAY(IFEAT,2) .AND. ICON.EQ.l) GO TO 70
IF (ICON.EQ.100) STOP13
IF (ICON.EQ.l) PUPPER = PiIF (ICON.EQ.i) PLa~ER = P2
IF (DLSUM.GT.PIGRAY(IFEAT,2) .AND. ICON.GT.l) PLOWER = P2IF (DLSUM.LT.PIGRAY(IFEAT,2) .AND. ICrn~.GT.i) PUPPER = P2
P2 = (PUPPER + PLOWER)/2.DO
ICON = ICON + 1
DLSUM = DLSUM - DELTALC
GO TO 60C
70 CONTINUEC
Pi = P2T1 = T2Xl)1 = X'V2XLi =XL2ViBAR =V2BAR
C80 CONTINUE
CGO TO 180
C90 COt,lTINUE
CC PRESSURE DROP EVALL~TED FOR TOTAL LENGTH OF CURRENT FEATURE. CHOKEC FLOW DOES NOT OCCUR IN THE CURRENT FEATURE.C
CONRAY(IFEAT,l) = P2CONRAY(IFEAT,2) = T2
131
CONRAY(IFEAT,3) =XV2CONRAY(IFEAT,4) =XL2CONRAY(IFEAT,5) =V2BARCONRAY(IFEAT,6) =GMAX*PIGRAY(IFEAT,3)**2/PIGRAY(IFEAT,1)**2
CIFEAT = IFEAT + 1
CC FINISHED WITH PIPE ELEMENT.C
GO TO 30C
100 CONTINUECC EXPANSIONS AND FITTINGS FOR WHICH PRESSURE DROP MUST BE CALCULATEDC ARE HANDLED BY THIS SECTION OF PROGRAMMING.CC ADJUST THE MASS VELOCITY BASED ON THE ENTRANCE DIAMETER TO THEC CURRENT DIAMETER.C
C
C
C
C
GFEAT = G*(PIGRAY(1,3)**2)/(PIGRAY(IFEAT,3)**2)
CONRAY(IFEAT,l) = CONRAY«IFEAT-l),l)* - PIGRAY(IFEAT,2) * GFEAT**2/DELTA* * CONRAY«IFEAT-l),5)
CALL FLASH (TCYL,PCYL,MW,XVCYL,XLCYL,CONRAY(IFEAT,l),ISEN,* CONRAY(IFEAT,3),CONRAY(IFEAT,4),CONRAY(IFEAT,2»
CALL DENUF6 (CONRAY(IFEAT,2),CONRAY(IFEAT,1),MW,RHOS,RHOL,RHOV)
CONRAY(IFEAT ,5) = CONRAY(IFEAT ,3)/RHOV* + (1.DO-CONRAY(IFEAT,3»*CONRAY(IFEAT,4)/RHOL*+ (1.DO-CONRAY(IFEAT,3»*(1.DO-CONRAY(IFEAT,4»/RHOS
CC FOR A SUDDEN EXPANSION, A GMAX VALUE NEED NOT BE CALCULATED. GMAXC FOR THE PREVIOUS ELEMENT IS PLACED IN THE CONDITIONS ARRAY.C
IF (PIGRAY«IFEAT+1),3).GT.PIGRAY(IFEAT,3) .AND.* (IFEAT+1).LT.IPIG) GO TO 120
C110 CONTINUE
CP2 = CONRAY(IFEAT,1)-1.D-3
CC EVALUATE GMAX BASED ON ISENTROPI C EXPANSION.C
ISNGMX = 0C
C
C
CALL FLASH (CONRAY(IFEAT,2), CONRAY(IFEAT,l), MW,* CONRAY(IFEAT,3), CONRAY(IFEAT,4), P2, ISNGMX, XV2, XL2, T2)
CALL DENUF6(T2,P2,MW,RHOS,RHOL,RHOV)
V2BAR =XV2/RHOV+(1.DO-XV2)*XL2IRHOL
C
132
* + (1.DO-XV2)*(1.DO-XL2)/RHOS
GMAX = DSQRT(ALPHA*(CONRAY(IFEAT,1)-P2)/* (V2BAR-CONRAY(IFEAT,5)))
CC IF GHAX IS SMALLER THAN G, THE CALCULATION MUST BE RESTARTED AT AC NEW, LOWER VALUE OF G.C
IF (GMAX.LE.GFEAT) GO TO 180C
120 CONTINUEC
C
C
C
CONRAY(IFEAT,6) = GMAX*PIGRAY(IFEAT,3)**2/PIGRAY(1,3)**2
IF (PIGRAY«IFEAT+l),3).GT.PIGRAY(IFEAT,3) .AND.* (IFEAT+l).LT.IPIG) CONRAY(IFEAT,6) = CONRAY«IFEAT-l),6)
IFEAT = IFEAT+l
GO TO 30C
130 CONTINUECC CONTRACTIONS IN THE PIPE SYSTEM ARE HANDLED BY THIS SECTION OF THEC PROGRAM. SINCE THE PRESSURE DROP IS A FUNCTION OF DOWNSTREAMC CONDITIONS, AN ITERATION IS REQUIRED. INITIALLY THE SPECIFIC VOLUMEC UPSTREAM IS ASSUMED TO HOLD DOWNSTREAM. THEN A NEW GUESS IS COMPUTED.C
ICON =1C
CONRAY(IFEAT,5) =CONRAY«IFEAT-l),5)CC ADJUST THE MASS VELOCITY BASED ON THE ENTRANCE DIAMETER TOC THE CURRENT DIAMETER.C
GFEAT = G*(PIGRAY(1,3)**2)/(PIGRAY(IFEAT,3)**2)C
140 CONTINUEC
CONRAY(IFEAT,l) =CONRAY«IFEAT-l),l)* - PIGRAY(IFEAT,2)*(GFEAT**2)/DELTA* * CONRAY(IFEAT,5)
C
C
C
C
C
CALL FLASH (TCYL,PCYL,MW,XVCYL,XLCYL,CONRAY(IFEAT,l),ISEN,* CONRAY(IFEAT,3),CONRAY(IFEAT,4),CONRAY(IFEAT,2))
CALL DENUF6 (CONRAY(IFEAT,2),CONRAY(IFEAT,1),MW,RHOS,RHOL,RHOV)
OLDCON =CONRAY(IFEAT,5)
CONRAY(IFEAT,5) = CONRAY(IFEAT,3)/RHOV* + (1.DO-CONRAY(IFEAT,3))*CONRAY(IFEAT,4)/RHOL* + (1.DO-CONRAY(IFEAT,3))*(1.DO-CONRAY(IFEAT,4))/RHOS
133
ICON = ICON + 1C
C
C
IF (ICON.GT.100) STOP14
IF (DABS(CONRAY(IFEAT,5)-OLDCON).GT.EPSLN) GO TO 140
GO TO 110C
150 CONTINUECC EVALUATION OF PRESSURE DROP ALONG THE PIPING SYSTEM FOR THE CURREtfrC VALUE OF G IS COMPLETE EXCEPT FOR THE EXHAUST PRESSURE DROP.C
DELTAP = PIGRAY(IPIG,2)*GFEAT**2*CONRAY«IPIG-1),5)/DELTACC DETERMINE WHETHER THE CURRENT VALUE OF G IS AN UPPER OR LOWER LIMIT.C
IF (CONRAY«IPIG-l),l) - DELTAP - PIGRAY(IPIG,3» 170, 190, 160C
160 CONTINUECC RESET LOWER BOUND ON G AND INCREASE MASS VELOCITY.C
C~~RAY(IPIG,6) = GC
C
C
G = (G + CONRAY(IPIG,5»/2.DO
IF (CONRAY(IPIG,5).EQ.1.D10) G = CONRAY(IPIG,6)/0.98DO
GO TO 10CC RESET UPPER BOUND AND REDUCE MASS VELOCITY.C
170 CONTINUEC
IGEXIT = 2C
180 CONTINUEC
CONRAY(l PI G, 5) = GC
CG = (G+ CONRAY(IPIG,6»/2.DO
IF (CONRAY(IPIG,6).EQ.0.DO .AND. IBRCH.EQ.3)* G =CONRAY(IPIG,5)*0.98DO
CGO TO 10
C190 CONTINUE
CIGEXIT = 2
C200 CONTINUE
C
134
RETURNC
500 FORMAT (' ',/,' WARNING! CHOKE FLOW PREDICTED IN FEATURE',* 13,/,' AFTER PRESSURE-DROP-CONTROLLED FLOW ESTABLISHED',* ' FOR PIPING SYSTEM (DELTAL.LE.O).')
C510 FORMAT (' ',/,' WARNING! CHOKE FLOW PREDICTED IN FEATURE',
* 13,/,' AFTER PRESSURE-DROP-CONTROLLED FLOW ESTABLISHED',* ' FOR PIPING SYSTEM (ISENTROPIC FLASH).')
END
B.20 REMOVE
SUBROUTINE REMOVE (IC, IREMOV)
COMMON BLOCK VARIABLES
OTHER SUBROUTINES REQUIRED ARE:
THE FOLLOWING VARIABLES ARE USED.
THE FOLLOWING SUBROUTINE IS CALLED.
REMOVAL FRACTION (VOLUME BASIS)
NODE NUMBER OF COMPARTMENT FROM WHICH CONDENSATEIS BEING REMOVED BY FALL OUTNODE NUMBER OF REMOVAL STREAM
COMPONENT MASS REMOVAL RATE, LB/(DELT), ORCOMPONENT MASS IN COMPARTMENT, LBNODE VOLUME, FT**3DEPOSITION AREA, FT**2DEPOSITI~~ VELOCITY, FT/SECMINIMUM NATURAL LOG ACCEPTED BY COMPUTERTIME INTERVAL FOR TRANSIENT SIMULATION, SECNODE TEMPERATURE, DEG FNODE PRESSURE, PSIAENTHALPY RATE, BTU/ (DELT)
DENUF6HHFH20HUF6
DENTHL
(30,9)
(30)(30)
(30 )(30)(30)
RMFRAC
MASS
IREt'10V
IC
VOLDPAREADEPVELAMINLNDELTTCPCH
INTERNAL VARIABLE
INPUT VARIABLES
CC THIS SUBROUTINE DETERMINES THE MASSES OF CONDENSED PHASES REMOVED BYC DEPOSITION FROM A ROOM.CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCC
CCC
C
135
VPRUF6ZUF6
IMPLICIT REAL*8 (A-H,J-Z)
COMMON ILBMASSI MASS(30,9), DUMlCOMMON IVOLUMEI VOL(30), DUM2(30), DPAREA(30), DEPVELCCM10N ICONTRLI AMINLN, DUM3, DELT, DUM4, IDUM1, DUM5COMMON ICOMPTPI TC(30), PC(30), DUM6(30)COMMON IENTHALI H(30), DUM7(120)
CC CALCULATE THE REMOVAL FRACTION WHICH IS BASED ON THE VOLUME FROMC WHICH CONDENSATES CAN BE REMOVED DURING THE TIME INTERVAL USEDC FOR THE TRANSIENT ANALYSIS DIVIDED BY THE TOTAL VOLUME OF THEC COMPARTMENT. THE FIRST VOLUME IS THE PRODUCT OF THE DEPOSITIONC VELOCITY, THE DEPOSITION AREA, AND THE TIME INTERVAL.C
RMFRAC =DEPVEL*DPAREA(IC)*DELTIVOL(IC)CC APPLY THE REMOVAL FRACTION, RMFRAC, TO CONDENSED PHASES CONTAINEDC IN NODE IC.C
MASS(IREMOV,l) = O.DOMASS(IREMOV,2) =MASS(IC,2)*RMFRACMASS(IREMOV,3) = O.DOMASS(IREMOV,4) =MASS(IC,4)*RMFRACMASS(IREMOV,5) =O.DOMASS(IREMOV,6) =MASS(IC,6)*RMFRACMASS(IREMOV,7) =MASS(IC,7)*RMFRACMASS(IREMOV,8) = O.DOMASS(IREMOV,9) =MASS(IC,9)*RMFRAC
CC SET THE TEMPERATURE AND PRESSURE OF THE REMOVAL STREAM TO THAT OF THEC SOURCE NODE, THEN CALCULATE THE ENTHALPY RATE OF THE REMOVAL STREAM.C
TC(IREMOV) =TC(IC)PC(IREMOV) = PC(IC)
C
C
C
CALL DENTHL (TC(IREMOV), PC(IREMOV), IREMOV, H(IREMOV»
RETURN
END
B.21 RESIST
SUBROUTINE RESIST (IC)CC THIS SUBROUTINE EVALUATES THE RESISTENCE TERM FOR THE RELATIONSHIPC DELP = KRCOEF*MASS-FLOW-RATE**2/DENSITY. THE MASS FLOW RATE FOR THEC TIME STEP DELT MUST HAVE ALREADY BEEN CALCULATED BEFORE THISC SUBROUTINE IS CALLED UNLESS A RESISTANCE COEFFICIENT FOR THE STREAMC HAS BEEN ENTERED.
136
CROSS-SECTIONAL AREA FOR FLOW, FT**2
STREAM NODE FOR WHICH RESISTANCE TERM IS TO BEEVALUATED
NODE INPUT STREAM NUMBERNODE OUTPUT STREAM NUMBERMINIMUM NATURAL LOG ACCEPTED BY THE COMPUTERTIME INTERVAL USED IN TRANSIENT SIMULATION, SEC
ABSOLUTE PRESSURE DIFFERENCE ACROSS NODE, PSITOTAL MASS IN INLET NODE, LBTOTAL MASS FLOW RATE IN STREAM NODE, LB/(DELT)DENSITY OF MATERIAL FLOWING INTO THE STREAMNODE, LB/FT**3
COMPONENT NODE MASS OR MASS FLOW RATE, LB(COMPARTMENT) OR LB/(DELT) (STREAM)NODE TEMPERATURE, DEG FNODE PRESSURE, PSIACOMPARTMENT NODE VOLUME, FT**3RESISTANCE COEFFICIENT (INPUT), --, ORRESISTANCE TERM (OUTPUT), PSI-SEC**2/LB-FT**3
AS A RESISTANCE TERM, KRCOEF IS A COMBINATIONOF THE RESISTANCE TERM, THE CROSS-SECTIONALAREA OF FLOW, AND CONVERSION FACTORS.
(30,4)(30,4)
MASS (30,9)
TC (30)PC (30)VOL (30)KRCOEF (30)
NOTE:
IC
FLAREA (30)
I INlOUTAMINLNDELT
DELPMASSiMASS2DENS
IMPLICIT REAL*B (A-H,J-Z)
DIMENSION FLAREA(30)
EQUIVALENCED VARIABLE
COMMON BLOCK VARIABLES
INTERNAL VARIABLES
INPUT VARIABLE
C
CC THE FOLLOWING VARIABLES ARE USED IN THIS SUBROUTINE:CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCC
C
C
C
COMMON /LBMASS/ MASS(30,9), DUMlCOMMON /COMPTP/ TC(30), PC(30), DUM2(30)COMMON /VOLUME/ VOL(30), KRCOEF(30), DUM3(31)COMMON /ISTRMS/ IIN(30,4), IOUT(30,4)COMMON /CONTRL/ AMINLN, DUM4, DELT, DUM5, IDUM1, DUM6
EQUIVALENCE (VOL(l), FLAREA(l»
IF (KRCOEF(IC).LE.O.DO) GO TO 10CC IF A POSITIVE RESISTANCE COEFFICIENT HAS BEEN ENTERED, FOR EXAMPLE, A
137
C VALUE OF 1.5 CORRESPONDING TO A SUDDEN CONTRACTION FOLLOWED BY AC SUDDEN EXPANSION, THE RESISTANCE TERM IS EVALUATED USING THE FOLLOWC ING EQUATION.C
KRCOEF(IC) = KRCOEF(IC)/FLAREA(IC)/FLAREA(IC)/9266.1DOC
RETURNC
10 CONTINUECC THE REMAINDER OF THIS SUBROUTINE EVALUATES A COEFFICIENT WHICHC INCORPORATES THE RESISTANCE COEFFICIENT, FLOW AREA, AND CONVERSIONC FACTORS INDIRECTLY BY USING INITIAL STEADY STATE CONDITIONS OF MASSC FLOW RATE AND PRESSURE DROP.C
CDELP = PC(IIN(IC,l)) - PC(IOUT(IC,l))
MASSl = O.DOMASS2 = O.DO
C
C
C
DO 20 120=1,9
MASSl = MASSl + MASS(IIN(IC,1),I20)MASS2 =MASS2 + MASS(IC,I20)
20 CONTINUEC
CDENS =MASS1/VOL(IIN(IC,1))
KRCOEF(IC) = DELP*DENS*DELT*DELTIMASS2/MASS2C
RETURNC
END
B.22 ROOM
SUBROUTINE ROOM (IC, RATIO)
COMMON BLOCK VARIABLES
THE FOLLOWING VARIABLES ARE USED.
NUMBER OF NODE BEING INITIALIZEDRATIO OF THE MOLES OF WATER VAPOR TO THE TOTALNL~BER OF MOLES OF MOIST AIR
(30,9) NODE COMPONENT MASS, LB
ICRATIO
MASS
INPUT VARIABLES
CC THIS SUBROUTINE EVALUATES THE INITIAL MASSES AND ENTHALPIES IN NODESC WHICH REPRESENT ROOMS.CCCCCCCCCCCC
138
THE FOLLOWING SUBROUTINES ARE ALSO REQUIRED.
LB/LB MOLE
NODE TEMPERATURE, DEG FNODE PRESSURE, PSIACOMPONENT MOLECULAR WEIGHT,NODE ENTHALPY, BTUNODE VOLUME, FT**3
TOTAL MOLES OF MOIST AIR IN NODEMOLES OF WATER VAPOR IN NODEMOLES OF DRY AIR IN NODE
DENTHL
DENUF6HHFH20HUF6lJPRUF6ZUF6
(30)(30)(9)(30)(30)
NTOTNH20NAIR
TCPCWMOLHVOL
INTERNAL VARIABLES
CCCCCCCCCCCCC THE FOLLOWING SUBROUTINE IS CALLED.CCCCCCCCCCC
C
C
IMPLICIT REAL*B (A-H,J-Z)
COMMON /LBMASS/ MASS(30,9), DUMlCOMMON /COMPTP/ TC(30), PC(30), DUM2(30)COMMON /MOLWT/ WMOL(9)C~1ON /ENTHAL/ H(30), DUM3(120)COMMON /VOLUME/ VOL(30), DUM4(61)
NTOT = PC(IC)*VOL(IC)/10.73DO/(TC(IC) + 459.67DO)C
NH20 = RATIO*NTOTNAIR =NTOT - NH20
C
C
C
MASS(IC,3) = NH20*WMOL(3)MASS(IC,l) =NAIR*WMOL(l)
CALL DENTHL(TC(IC), PC(IC), IC, H(IC»
RETURNC
END
B.23 SETRAY
SUBROUTINE SETRAY (INODES, INOUT)CC THIS SUBROUTINE IS USED TO INITIALIZE VALUES IN THE VARIOUS ARRAYSC NEEDED FOR TRANSIENT COMPARTM~~T ANALYSIS.C
139
COMMON BLOCK VARIABLES
EQUIVALENCED VARIABLES
BLOWER FLOW RATE, FT**3IMINFLOW AREA FOR PRESSURE DROP CONTROLLED FLOW,FT**2
NUMBER OF NODES AVAILABLE IN THE TRANSIENTCOMPARTMENT MODEL (NOTE: NODE 30 IS THE NULLVECTOR)NUMBER OF INPUT AND NUMBER OF OUTPUT STREAMSALLOWED IN THE TRANSIENT COMPARTMENT MODEL
NODE COMPONENT MASS, LB, OR NODE Cot1PONENT FLOWRATE, LB/(DELT)FRACTIONAL RELATIVE HUMIDITY, -NODE TEMPERATURE, DEG FNODE PRESSURE, PSIANODE HEAT TRANSFER SURFACE TEMPERATURE, DEG FCOMPONENT MOLECULAR WEIGHTS, LB/LB MOLENODE VOLUME, FT**3RESISTANCE COEFFICIENT, --, OR RESISTENCE TERM,PSI-SEC**2/LB-FT**2DEPOSITION AREA, FT**2DEPOSITION VELOCITY, FT/SECNODE ENTHALPY, BTU, OR NODE ENTHALPY RATE,BTU/(DELT)HEAT TRANSFER RATE, BTU/(DELT)COOLING RATE, BTU/(DELT)HEAT TRANSFER COEFFICIENT, BTU/SEC-FT**2-DEG FHEAT TRANSFER AREA, FT**2NODE INLET STREAMSNODE OUTLET STREAMSNATURAL LOG OF THE MINIMUM NUMBER ACCEPTED BYTHE COMPUTERCUMULATIVE TIME OF THE TRANSIENT SIMULATION, SECTIME INCREMENT FOR THE TRANSIENT SIMULATION, SECMAXIMUM CUMULATIVE TIME OF THE SIMULATION, SECCONTROL VARIABLE FOR PRINTING OUTPUTTOTAL RELEASE TIME, SECWEI GHT FRACTION OF MONOMER TO HF VAPORWEIGHT FRACTION OF TRIMER TO HF VAPORWEIGHT FRACTION OF HEXAMER TO HF VAPOREFFECTIVE MOLECULAR WEIGHT OF HF VAPOR,LB/LB MOLETYPE OF RELEASETOTAL MASS OF RELEASED MATERIAL, LBCONTROL VARIABLE IDENTIFYING BASIS FOR UF6LIQUID FLASH OR VAPOR EXPANSION
INOUT
INODES
MASS (30,9)
RHTC (30)PC (30)TSURF (30)WMOL (9)
VOL (30)KRCOEF (30)
DPAREA (30)DEPVELH (30)
QRATE (30)QCOOL (30)HTCOEF (30)HTAREA (30)IIN (30,4)lOUT (30,4)AMINLN
TIMEDELTMAXTIMIFLAGTRELSC1C3C6WMBHF
ITYPESOURCEISEN
ACFM (30)FLAREA (30)
OUTPUT VARIABLES
C THE FOLLOWING VARIABLES ARE USED.CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCC
C
C
C
140
IMPLICIT REAL*8 (A-H,J-Z)
DIMENSION ACFM(30), FLAREA(30)
COMMON ILBMASSI MASS(30,9) , RHCOMMON ICOMPTPI TC(30), PC(30), TSURF(30)COMMON IMOLWTI WMOL(9)COMMON /vOLUMEI VOL(30), KRCOEF(30), DPAREA(30), DEPVELCOMMON lENTHAll H(30), QRATE(30), QCOOL(30), HTCOEF(30),
* HTAREA(30)COMMON IISTRMSI IIN(30,4), IOUT(30,4)COMMON ICONTRLI AMINLN, TIME, DELT, MAXTIM, IFLAG, TRELSCOMMON IPOLYMRI Cl, C3, C6, WMBHFCOMMON IMISCELI ITYPE, SOURCE, ISEN
CEQUIVALENCE (VOL(l), ACFM(l), FLAREA(l»
CAMINLN =-88.00
CINODES =30INOUT =4
CC MOLECULAR WEIGHTS.C
WMOL(1) =28.96600WMOL(2) =18.01600WMOL(3) =WMOL(2)WMOL(4) = 20.00800WMOL(5) = WMOL(4)WMOL(6) = 352.02500WMOL(?) = WHOL(6)WMOL(8) =WMOL(6)WMOL(9) = 308.02500
CWMBHF = 1oI'10L(4)
CDO 30 I30=1,INOOES
CDO 10 110=1,9
CMASS(I30,I10) = 0.00
C10 CONTINUE
C
C
VOL (130) = O. DOH(l30) =0.00QRATE(I30) = 0.00QCOOL(I30) =0.00HTCOEF(I30) = 0.00VOL (130 ) = O. DOKRCOEF(I30) = 0.00DPAREA(I30) = 0.00
141
C
C
DO 20 I20=1,INOUT
IIN(I30,I20) = INODESIOUT(I30,I20) = INODES
20 CONTINUEC
30 CONTINUEC
DEPVEL = 0.033DOC
RETURNC
END
B.24 SSBLOW
SUBROUTINE SSBLOW (IC, RATIO)
COMM~~ BLOCK VARIABLES
THE FOLLOWING VARIABLES ARE USED:
STREAM NODE NUMBERRATIO OF MOLES OF WATER VAPOR TO TOTAL MOLES OFMOIST AIR
ABSOLUTE TEMPERATURE, DEG RTOTAL MOLE FLrn~ RATE, MOLE/(DELT)
COMPONENT NODE MASS OR MASS FLOW RATE, LB(COMPARTMENT) OR LB/(DELT) (STREAM)NODE TEMPERATURE, DEG FNODE PRESSURE, PSIACOMPONENT MOLECULAR WEIGHTS, LB/LB MOLEVOLUMETRIC FLOW RATE THROUGH STREAM NODE,FT**3/MINENTHALPY RATE, BTU/(DELT)NODE INPUT STREAM NUMBERNODE OUTPUT STREAM NUMBERMINIMUM NATUPAL LOG ACCEPTED BY THE COMPUTERTIME AT WHICH FLOW RATE IS BEING EVALUATED, SECTIME INTER~~L USED IN TRANSIEt~ SIMULATION, SEC
(30)(30,4)(30,4)
(30)(30 )( 9)(30)
(30,9)MASS
ICRATIO
TRNTOT
TCPCWMOLACFM
HlINlOUTAtv!!:~LN
TIMEDELT
INTERNAL VARIABLES
INPUT VARIABLES
CC THIS SUBROUTINE EVALUATES THE STEADY-STATE COMPONENT MASS FLOW RATESC RESULTING FROM THE FLOW OF MOIST AIR THROUGH A CONSTANT VOLUME BLOWERC GIVEN THE RATIO OF WATER VAPOR TO AIR AND WATER. FOR STEADY STATEC CONDITIONS, THE TEMPERATURE AND PRESSURE OF NODE IC SHOULD BE THAT OFC THE NODE SERVING AS THE INLET TO NODE IC.CCCCCCCCCCCCCCCCCCCCCCCCCCCCC
DENTHL
HHFH20HUF6DENUF6VPRUF6ZUF6
OTHER SUBROUTINES REQUIRED (BECAUSE OF DENTHL) ARE:
142
Ce THE FOLLOWING SUBROUTINE IS CALLED BY DENTHL:eCCCeCCCCCC
IMPLICIT REAL*8 (A-H,J-Z)e
COMMON /LBMASSI MASS(30,9), DUMlCOMMON ICOMPTPI TC(30), PC(30), DUM2(30)COMMON IMOLWTI WMOL(9)COMMON IVOLUMEI ACFM(30), DUM3(61)COMMON IENTHALI H(30), DUM4(120)COMMON IISTRMSI IIN(30,4), IOUT(30,4)COMMON ICONTRLI AMINLN, TIME, DELT, DUM5, IDUM, DUM6
C
C
C
C
C
C
C
TC(IC) =TC(IIN(IC,l»PC(IC) = PC(IIN(IC,l»
TR =TC(IC) + 459.6700
NTOT = PC(IC)*ACFM(IC)*DELT/l0.73DO/TR/6.Dl
MASS(IC,3) = RATIO*NTOT*WMOL(3)MASS(IC,l) = (1.00 - RATIO)*NTOT*WMOL(l)
CALL DENTHL (TC(IC), PC(IC), IC, H(IC»
RETURN
END
B.25 STERM
SUBROUTINE STERM (IC, ICMAIN, SOLIDS)cC THIS SUBROUTINE EVALUATES A STEADY STATE RELEASE RATE BASED ON THEC INITIAL PRESSURE OF THE MAIN COMPARTMENT ~ID, FOR UF6 RELEASES,C WHETHER THE RELEASE IS ISENTROPIC OR ISENTHALPI C.CC THE FOLLOWING VARIABLES ARE USED.CC INPUT VARIABLEScCC
IeICMAIN
NODE NUMBER FOR SOURCENODE NUMBER OF COMPARTMENT IN WHICH SOURCE IS
143
CCCCCC
OUTPUT VARIABLE
SOLIDS
LOCATED
MASS FLOW RATE OF UF6 SOLIDS BEING DEPOSITED ONFLOOR, LB/(DELT)
SOLIDS DUMPED TO FLOORSOLIDS AIRBORNE
ISENTROPIC FLASHISENTHALPIC FLASH
HF LIQUIDHF VAPORUF6 LIQUID,UF6 LIQUID,UF6 VAPOR
o1
457
-78
WEIGHT FRACTION OF HF IN HF-H20 CONDENSATEVAPOR PRESSURE OF HF, PSIAINITIAL UF6 VAPOR MASS FRACTIONINITIAL UF6 LIQUID MASS FRACTION IN THE UF6CONDENSED FRACTIONFINAL UF6 VAPOR MASS FRACTIONFINAL UF6 LIQUID MASS FRACTION IN THE UF6CONDENSED FRACTIONFINAL TEMPERATURE OF FLASHED UF6 CORRESPONDINGTO THE PRESSURE OF THE MAIN COMPARTMENT, DEG FVAPOR PRESSURE OF UF6, PSIA
COMPONENT MASS FLOW RATE, LB/(DELT)NODE TEMPERATURE, DEG FNODE PRESSURE, PSIACOMPONENT MOLECULAR WEIGHTNODE ENTHALPY RATE, BTU/(DELT)MINIMUM NATURAL LOG ACCEPTED BY THE COMPUTERINTERVAL OF TIME USED FOR TRANSIENT SIMULATION,SECTOTAL TIME OF RELEASE, SECRELEASE TYPE INENTIFIER
TOTAL MASS OF SOURCE, LBBASIS FOR FLASH OF UF6 LIQUID
(30,9)(30 )(30)(9)(30)
DENTHLFLASHHFPOLYPHFH20VPRUF6
PUF6
SOURCEISEN
XVFINXLFIN
TRELSITYPE
WHFLPHFXVINITXLINIT
MASSTCPCWMOLHAMINLNDELT
TFIN
COMMON BLOCK VARIABLES
INTERNAL VARIABLES
CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCC THE FOLLOWING SUBROUTINES ARE CALLED BY THIS SUBROUTINE.CCCCCCC
DENUF6EQTUF6HHFH20HUF6SUF6ZUF6
144
C THE FOLLOWING SUBROUTINES ARE ALSO REQUIRED TO EXECUTE THISC SUBROUTINE.CCCCCCCC
IMPLICIT REAL*8 (A-H,J-Z)C
C
C
COMMON ILBMASSI MASS(30,9) , DUM1COMMON ICOMPTPI TC(30), PC(30), DUM2(30)COMMON IMOLWTI WMOL(9)COMMON IENTHALI H(30), DUM3(120)COMMON ICONTRLI AMINLN, DL~4, DELT, DUM5, IDUM, TRELSCOMMON IMISCELI ITYPE, SOURCE, ISEN
SOLIDS = O.DO
MASS(IC,IABS(ITYPE» = SOURCE*DELTITRELSCC SOURCE TERM FOR HF LIQUID.C
IF (ITYPE.EQ.4) GO TO 40CC SOURCE TERM FOR HF VAPOR. IF THE ENTERED SOURCE PRESSURE IS LESSC THAN ZERO OR GREATER THAN THE VAPOR PRESSURE CORRESPONDING TO THEC SOURCE TERMPERTURE, THE SOURCE PRESSURE IS SET EQUAL TO THE VAPORC PRESSURE.C
IF (ITYPE.NE.5) GO TO 10C
WHFL = 1.00C
CALL PHFH20 (TC(IC), WHFL, 0.00, PHF, 0.00, 0.00)C
IF (PHF.LT.PC(IC).OR.PC(IC).LT.O.DO) PC(IC) = PHFC
CALL HFPOLY (TC(IC), PC(IC), WMOL(5), .TRUE.)C
GO TO 40C
10 CONTINUECC SOURCE TERM FOR UF6 LIQUID. UF6 LIQUID IS FLASHED TO THE INITIALC PRESSURE OF THE COMPARTMENT. IF ITYPE = 7, ONLY THE VAPOR FRACTION ISC UTILIZED AS A SOURCE TERM FOR THE COMPARTMENT, WHILE THE SOLIDSC FRACTION IS ACCUMULATED ON THE FLOOR. IF ITYPE = -7, BOTH SOLID ANDC VAPOR ARE INCORPORATED INTO THE SOURCE TERM.C
IF (IABS(ITYPE).NE.7) GO TO 20C
C
C
C
C
C
C
C
C
C
C
145
CALL VPRUF6 (TC(IC), PC(IC»
XVINIT = O. DOXLINIT =1. DO
CALL FLASH (TC(IC), PC(IC), WMOL(7), XVINIT, XLINIT, PC(ICMAIN),* ISEN, XVFIN, XLFIN, TFIN)
MASS(IC,8) = MASS(IC,7)*XVFIN
SOLIDS =MASS(IC,7) - MASS(IC,8)
IF (ITYPE.EQ.-7) MASS(IC,6) = SOLIDSIF (ITYPE.EQ.-7) SOLIDS = O.DO
MASS(IC,7) = O.DO
TC(IC) =TFIN
PC(IC) = PC(ICMAIN)
GO TO 40
20 Ce:t-ITINUECC SOURCE TERM FOR UF6 VAPOR. IF THE ENTERED SOURCE PRESSURE IS LESSC THAN OR EQUAL TO ZERO OR GREATER THAN THE VAPOR PRESSUREC CORRESPONDING TO THE SOURCE TERMPERTURE, THE SOURCE PRESSURE IS SETC EQUAL TO THE VAPOR PRESSURE.C
IF (ITYPE.NE.8) GO TO 30C
C
C
C
C
C
C
C
C
CALL VPRUF6 (TC(IC), PUF6)
IF (PUF6.LT.PC(IC).OR.PC(IC).LE.0.DO) PC(IC) = PUF6
GO TO 40
30 CONTINUE
WRITE (5,500) ITYPE
STOP15
40 CONTINUE
CALL DENTHL (TC(IC), PC(IC), IC, H(IC»
RETURNC
500 FORMAT (11,5X,'ITYPE =',31,' NOT RECOGNIZED.',II)C
END
146
B.26 SUF6
SUBROUTINE SUF6 (TF, PSIA, MW, SSOL, SLIQ, SVAP)
THE FOLLOWING SUBROUTINE IS CALLED.
THE ENTROPY CORRELATIONS ARE BASED ON INFORMATION IN R. DEWITT,·URANIUM HEXAFLUORIDE: A SURVEY OF THE PHYSICO-CHEMICAL PROPERTIES,"GAT-280, GOODYEAR ATOMIC CORP., PORTg10UTH, OHIO, JAN. 29, 1960,PAGES 67 - 70. THE ENTROPY OF THE VAPOR GIVEN BY THE CORRELATION INGAT-280 IS FOR A PRESSURE OF 1 ATM. THE VAPOR CORRELATION GIVEN BELOWHAS BEEN MODIFIED USING THE MAGNUSON EQUATION OF STATE (SEE GAT-280,PAGES 97 - 101) AND THE DEPARTURE FUNCTION CORRELATIONS GI~EN INR. C. REID, J. M. PRAUSNITZ, AND T. K. SHERWOOD, THE PROPERTIES OFGASES AND LIQUIDS, 3RD ED., MCGRAW-HILL BOOK COMPANY, 1977, PAGE 93,SO THAT BOTH SATURATED AND UNSATURATED VAPOR ENTROPIES CAN BECALCULATED.
TEMPERATURE, DEG FABSOLUTE TEMPERATURE, DEG RLN(TR)TR**2PRESSURE, PSIAMOLECULAR WEIGHT, LB MASS/LB MOLEENTROPY OF THE SOLID, BTU/LB MASS-DEG FENTROPY OF THE LIQUID, BTU/LB MASS-DEG FENTROPY OF THE VAPOR, BTU/LB MASS-DEG FVAPOR COMPRESSIBILITY FACTOR AT TF AND PSIAVAPOR COMPRESSIBILITY FACTOR AT TF AND 14.696 PSIA
SSOL
TFTRLNTRTRSQPSIAMW
SUQSVAPZPSIAZlATM
ZUF6
CC THIS SUBROUTINE CALCULATES THE ENTROPIES OF UF6 SOLID, LIQUID, ANDC VAPOR. THE FOLLOWING VARIABLES ARE USED.CCCCCCCCCCCCCCCCCCCCCCCCCCCCC
CIMPLICIT REAL*8 (A-H,J-Z)
TR =TF + 459.67DOLNTR = DLOG(TR)TRSQ = TR*'k2
CC THE ENTROPY OF THE SOLID IS GIVEN BY THE FOLL(~ING CORRELATION WHICHC IS ACCURATE WITHIN 0.01% BETWEEN 32 DEG F AND THE TRIPLE POINT (147.3C DEG F).C
SSOL = ( 3.93535D-l - 5.70531D-2*LNTR + 2.55019D-4*TR* - ( 4.82282D3/TRSQ ) ) * ( 3.52D2/MW )
cC THE ENTROPY OF THE LIQUID IS GIVEN BY THE FOLLOWING CORRELATION WHICHC IS REPORTED TO HAVE AN ACCURACY OF 0.01% [OVER AN ASSUMED RANGE OFC 147.3 TO 206.3 DEG F).C
SLIQ = ( -1.72963D-1 + 5.10057D-2*LNTR + 1.02633D-4*TR* - ( 3.06967D3/TRSQ ) ) * ( 3.52D2/MW )
147
CC CALCULATE THE VAPOR COMPRESSIBILITY FACTOR AT 14.696 PSIA AND ATC ·PSIA.·C
CALL ZUF6 (TF, 14.696DO, ZlATM, O.ODO, O.ODO)CALL ZUF6 (TF, PSIA, ZPSIA, O.ODO, 0.000)
SVAP***
CRETURN
CEND
CC THE ENTROPY OF THE VAPOR IS GIVEN BY THE FOLLOWING CORRELATION.C
= ( -3.327040-1 + 9.21307D-2*LNTR + 1.25237D-5*TR+ ( 1.47586D3/TRSQ ) + 3.09390-3 * (ZPSIA - ZlATM)+ 1.0313D-3 * DLOG( (l.DO - ZlATM) / (1.00 - ZPSIA) ) )* ( 3.52D2/MW )
D.27 THCUF6
THE FOLLOWING SUBROUTINES ARE CALLED.
TEMPERATURE, DEG FABSOLUTE TEMPERATURE, OEG RPRESSURE, PSIAMOLECULAR WEIGHT, LB MASS/LB MOLETHERMAL CONDUCTIVITY OF THE SOLID, BTU/HR-FT-DEG FTHERMAL CONDUCTIVITY OF THE LIQUID, BTU/HR-FT-OEG FTHERMAL CONDUCTIVITY OF THE VAPOR, BTU/HR-FT-DEG FHEAT CAPACITY OF THE LIQUID, BTU/LB MASS-DEG FDENSITY OF THE LIQUID, LB MASS/FT**3
CPUF6DENUF6
TFTRPSIAMWTHCSOLTHCLIQTHCVAPCPLIQDENLIQ
SUBROUTINE THCUF6 (TF, PSIA, MW, THCSOL, THCLIQ, THCVAP)CC THIS SUBROUTINE CALCULATES THE THERMAL CONDUCTIVITY OF UF6 SOLID,C LIQUID, AND VAPOR. THE FOLLOWING VARIABLES ARE USED.CCCCCCCCCCCCCCCC
IMPLICIT REAL*8 (A-H,J-Z)C
TR =TF + 459.67DOCC THE THERMAL CONDUCTIVITY OF THE SOLID IS BASED ON DATA OBTAINED FROMC E. J. BARBER (PERSONAL COMMUNICATION, JULY 13, 1983). ASSUMING AC LINEAR RELATIONSHIP BETWEEN THERMAL CONDUCTIVITY AND TEMPERATURE,C THE THERMAL CONDUCTIVITY OF THE SOLID IS GIVEN BYC
THCSOL =2.586D-l + 6.084D-4*TFCC CALCULATE THE HEAT CAPACITY AND THE DENSITY OF THE LIQUID.C
148
CALL CPUF6 (TF, PSIA, MW, O.ODO, CPLIQ, O.ODO, O.ODO, O.ODO)C
CALL DENUF6 (TF, PSIA, MW, O.ODO, DENLIQ, O.ODO)CC THE THERMAL C~~DUCTIVITY OF THE LIQUID IS BASED ON A SINGLE VALUEC REPORTED IN R. DEWITT, "URANIUM HEXAFLUORIDE: A SURVEY OF THEC PHYSICO-CHEMICAL PROPERTIES," GAT-2BO, GOODYEAR ATOMIC CORP.,C PORTSMOUTH, OHIO, JAN. 29, 1960, PAGE 46. ASSUMING A GENERAL FORM OFC VARIOUS PREDICTIVE CORRELATIONS FOR THERMAL CONDUCTIVITY OF A LIQUID,C WHICH IS K = B * CP * (DEN**1.33) I TR, THE COEFFICIENT B WASC DETERMINED. THUS, AN APPROXIMATE CORRELATION FOR LIQUID THERMALC CONDUCTIVITY IS GIVEN BYC
THCLIQ = 3.2470-1 * CPLIQ * ( DENLIQ**(4.DO/3.DO) ) I TRCC THE THERMAL CONDUCTIVITY OF THE VAPOR IS BASED ON GAT-2BO, PAGES 44 C 46, AND IS GIVEN BYC
THCVAP = 3.26BD-3 * ( 1.0DO + 2.52D-3*TF )C
RETURNC
END
B.28 TRBLOW
SUBROUTINE TRBLOW (IC)
EQUIVALENCED VARIABLE
COMMON BLOCK VARIABLES
THE FOLLOWING VARIABLES ARE USED:
STREAM NODE NUMBER
COMPONENT NODE MASS OR MASS FLOW RATE, LB(COMPARTMENT) OR LB/(DELT) (STREAM)NODE TEMPERATURE, DEG FNODE PRESSURE, PSIACOMPONENT MOLECULAR WEIGHTS, LB/LB MOLEVOLUMETRIC FLOW RATE THROUGH BLOWER, FT**3/MINENTHALPY OR ENTHALPY RATE, BTU OR BTU/(DELT)MINIMUM NATURAL LOG ACCEPTED BY THE COMPUTERTIME INTERVAL USED IN TRANSIENT SIMULATION, SECNODE INPUT STREAM NUMBERNODE OUTPUT STREAM NUMBER
(30,9)
(30,4)(30,4)
(30)(30)(9)(30)(30)
IC
MASS
TCPCJoI10LACFMHAMINLNDELTI INlOUT
INPUT VARIABLE
CC THIS SUBROUTINE EVALUATES THE TRANSIENT MASS FLOW RATES FOR AC CONSTANT VOLUME BLOWER REPRESENTED BY NODE IC WHICH DRAWS FROM AC COMPARTMENT REPRESENTED BY NODE IIN(IC,l).CCCCCCCCCCCCCCCCCCCCCC
149
DIMENSION VOL(30)
IMPLICIT REAL*B (A-H,J-Z)
CCCCCCCC
C
VOL (30)
INTERNAL VARIABLE
FRAC
COMPARTMENT NODE VOLUME, FT**3
RATIO OF BLOWER VOLUME FLOW RATE-TIME INTERVALPRODUCT TO INLET NODE VOLUME
C
C
C
COMMON /LBMASS/ MASS(30,9), DUM1COMMON /COMPTP/ TC(30), PC(30), DUM2(30)COMMON /MOLWT/ WMOL(9)COMMON /VOLUME/ ACFM( 30), DUM3( 61)COMMON /ENTHAL/ H(30), DUM4(120)COI'1'1ON /CONTRU AMINLN, DUM5, DELT, DUM6, IDUM1, DUI'17COMMON /ISTRMS/ IIN(30,4), IOUT(30,4)
EQUIVALENCE (VOL(l),ACFM(l»
C
C
C
FRAC = ACFM(IC)*DELT/6.D1/vOL(IIN(TC,1»
DO 10 110=1,9
MASS(IC,I10) = FRAC*MASS(IIN(IC,1),I10)
10 CONTINUEC
C
H(IC) =FRAC*H(IIN(IC,l»TC(IC) =TC(IIN(IC,l»PC(IC) = PC(IIN(IC,l»
RETURNC
END
B.29 VISUF6
SUBROUTINE VISUF6 (TF, PSIA, MW, VISLIQ, VISVAP)
THE FOLLOWING SUBROUTINE IS CALLED.
TEMPERATURE, DEG FABSOLUTE TEMPERATURE, DEG RPRESSURE, PSIAMOLECULAR WEIGHT, LB/LB MOLELIQUID VISCOSITY, LB MASS/FT-HRVAPOR VISCOSITY, LB MASS/FT-HR
TFTRPSIAMWVISLIQVISVAP
CC THIS SUBROUTINE CALCULATES THE VISCOSITIES OF UF6 LIQUID AND VAPOR.C THE FOLLOWING VARIABLES ARE USED.CCCCCCCCC
150
CC VPRUF6CC THE VISCOSITY CORRELATIONS ARE BASED ON INFORMATION FROM R. DEWITT,C ·URANIUM HEXAFLUORID: A SURVEY OF THE PHYSICO-CHEMICAL PROPERTIES,"C GAT-280, GOODYEAR ATOMIC CORP., PORTSMOUTH, OHIO, JAN. 29, 1960,C PAGES 38 - 44. THE VAPOR VISCOSITY CORRELATION WAS FITTED TO DATAC REPORTED IN GAT-280 BY W. R. WILLIAMS.C
CIMPLICIT REAL*8 (A-H,J-Z)
TR =TF + 459.6700CC THE VISCOSITY OF THE LIQUID IS GIVEN BY THE FOLLOWING CORRELATIONC WHICH IS BASED ON DATA RANGING FROM 158 TO 410 DEG F. THE SUM OF THEC TERMS IN THE EXPONENTIAL IS CORRECT BASED ON THE DATA OF BLATTC REPORTED BY DEWITT IN TABLE 25.C
VISLIQ = 0.40400 * DEXP( (9.9702 + 4.1D-2*PSIA)/TR )CC THE VISCOSITY OF THE VAPOR BASED ON DATA RANGING FROM 104 TO 392C DEG F ISGIVEN WITHIN 0.6% BY THE FOLLOWING CORRELATION.C
VISVAP = 1.1920-4 * TR**0.9305DOC
RETURNC
END
B.30 VPRUF6
SUBROUTINE VPRUF6 (TF, PSIA)
TEMPERATURE, DEG FPRESSURE, PSIAPRESSURE, PSIAPRESSURE, PSIA
TFPSIAPlP2
C
CC THIS SUBROUTINE CALCULATES THE VAPOR PRESSURE OF UF6. THE FOLLOWINGC VARIABLES ARE USED.CC
CCCC THE VAPOR PRESSURE CORRELATIONS USED ARE BASED ON R. DEWITT, ·URANIUMC HEXAFLUORIDE: A SURVEY OF THE PHYSICO-CHEMICAL PROPERTIES,· GAT-280,C GOODYEAR ATOMIC CORP., PORTSMOUTH, OHIO, JAN. 29, 1960, PAGE 81.C
IMPLICIT REAL*8 (A-H,J-Z)C
IF (TF.GE.147.306561DO) GO TO 10CC THE VAPOR PRESSURE OF UF6 OVER THE SOLID FROM 32 DEG F TO THE TRIPLEC POINT AT 147.3 DEG F IS GIVEN BYC
PSIA = DEXP ( 10.444300 + 9.64233D-3*TF - ( 3.9074103 /
151
* ( TF + 298.149DO ) ) )C
RETURNC
10 CONTINUECC DEWITT RECOMMENDS 2 CORRELATIONS FOR THE VAPOR PRESSURE OF UF6 OVERC THE LIQUID. THE FIRST, WHICH IS GIVEN BELOW BY P1, GIVES GOOD AGREEC MENT (0.03%) FROM THE TRIPLE POINT TO 240.8 DEG F. THE SECOND, WHICHC IS GIVEN BELOW BY P2, AGREES WITHIN 0.3% ON AVERAGE BETWEEN THEC 240.8 DEG F AND THE CRITICAL POINT. P2 EXCEEDS THE TABULATED VALUESC OF VAPOR PRESSURE FROM 240.8 DEG F TO ABOUT 276 DEG F. BY USING AC WEIGHTED AVERAGE OF Pi AND P2 OVER THIS RANGE, A BETTER AGREEMENTC WITH TABULATED VALUES IS OBTAINED, AS WELL AS A CONTINUOUS FUNCTIONC FOR VAPOR PRESSURE.C
P1 = DEXP ( 12.1600DO - ( 4.66807D3 / ( TF + 367.533DO ) ) )P2 = DEXP ( 13.7627DO - ( 6.97611D3 / ( TF + 511.866DO ) ) )
CIF (TF. GE. 2.40D2) GO TO 20
CC THE VAPOR PRESSURE OF UF6 OVER THE LIQUID FROM THE TRIPLE POINT TOC 240 DEG F IS GIVEN BYC
PSIA = P1C
RETURNC
20 CONTINUEC
IF (TF.GE.2.76D2) GO TO 30CC THE VAPOR PRESSURE OF UF6 OVER THE LIQUID FROM 240 TO 276 DEG F ISC GIVEN BYC
PSIA = ( (2.76D2 - TF)*P1 + (TF - 2.40D2)*P2 )/ 3.6D1C
RETURNC
30 CONTINUECC THE VAPOR PRESSURE OF UF6 OVER THE LIQUID FROM 276 DEG F TO THEC CRITICAL POINT IS GIVEN BYC
PSIA = P2C
RETURNC
END
152
B.31 ZUF6
SUBROUTINE ZUF6 (TF, PSIA, Z, ZP, ZT)
ZP = Z - P (DZ/DP), EVALUATED FOR CONSTANT TZT = Z + T (DZ/DT), EVALUATED FOR CONSTANT P
THE COMPRESSIBILITY FACTOR IS BASED ON THE EQUATION OF STATE FOR UF6PROPOSED BY D. W. MAGNUSON CITED BY R. DEWITT, "URANIUM HEXAFLUORIDE:A SURVEY OF THE PHYSICO-CHEMICAL PROPERTIES,· GAT-280, GOODYEARATOMIC CORP., PORTSMOUTH, OHIO, JAN. 29, 1960, PAGES 24 AND 97 - 101.
TEMPERATURE, DEG FABSOLUTE TEMPERATURE, DEG R(DEG R)**3PRESSURE, PSIACOMPRESSIBILITY FACTOR
TFTRTCUBEPSIAZ
CC THIS SUBROUTINE CALCULATES THE COMPRESSIBILITY FACTOR OF UF6 AS WELLC AS THE QUANTITIES ZP AND ZT. THE FOLLOWING VARIABLES ARE USED.CCCCCCCCCCCCCCC
IMPLICIT REAL*8 (A-H,J-Z)C
TR =TF + 459.67DOTCUBE = TR**3
CZ =TCUBE I ( TCUBE + 4.8923D5*PSIA
CZP = ( 2.0DO - Z ) * ZZT = ( 4.0DO - 3.0DO*Z ) * Z
CRETURN
CEND
Appendix CEXAMPLE PROBLEM OUTPUT
Output for Examples I (Cases 1 through 4), 2 (Cases 1 and 3), 3 (Cases I through 3), 4(Cases 1 through 4), and 5 are included in this appendix. Output for Examples 1, 2, and 3 wereproduced by CYLIND. Output for Example 4, Cases 1 and 3, as well as Example 5, were producedby FODRFT and for Example 4, Cases 2 and 4, by INDRFT. Example problems are described inChapter 5. Output for Examples 2 (Case 2) and 6 from CYLIND and BATCH, respectively, areincluded in Chapter 5 as are selected plots produced by COMPLT and CYLPLT.
153
TITL
E:EX
.1,
CASE
1.10
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3.78
019
20.
0.0
8851
.215
4.4
9005
.619
7.67
349
.449
LIUI
D50
.987
CHOK
E2.
898
0.00
03.
268
6.16
614
.700
133.
780
1980
.0.
084
77.5
158.
186
35.7
197.
562
49.3
69LI
UID
50.8
31CH
OKE
2.89
60.
000
3.26
26.
158
14.7
0013
3.78
020
40.
0.0
8104
.416
1.8
8266
.219
7.44
749
.286
LIUI
D50
.670
CHOK
E2.
893
0.00
03.
256
6.15
014
.700
133.
780
2100
.0.
077
31.7
165.
578
97.2
197.
327
49.1
99LI
QUID
50.5
07CH
OKE
2.89
10.
000
3.25
06.
141
14.7
0013
3.78
021
60.
0.0
7359
.616
9.2
7528
.819
7.20
249
.109
LIQU
ID50
.339
CHOK
E2.
888
0.00
03.
244
6.13
214
.700
133.
780
2220
.0.
069
88.1
172.
871
60.9
197.
071
49.0
15LI
QUID
50.1
67CH
OKE
2.88
60.
000
3.23
76.
123
14.7
0013
3.78
022
80.
0.0
6617
.117
6.4
6793
.519
6.93
548
.918
LIQU
ID49
.990
CHOK
E2.
883
0.00
03.
230
6.11
314
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133.
780
2340
.0.
062
46.8
179.
964
26.7
196.
792
48.8
15LI
QUID
49.8
08CH
OKE
2.88
00.
000
3.22
36.
103
14.7
0013
3.78
024
00.
0.0
5877
.118
3.5
6060
.619
6.64
248
.708
LIQU
ID49
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CHOK
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877
0.00
03.
215
6.09
214
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133.
780
2460
.0.
055
08.1
186.
956
95.0
196.
484
48.5
95LI
QUID
49.4
26CH
OKE
2.87
40.
000
3.20
76.
081
14.7
0013
3.78
025
20.
0.0
5139
.819
0.4
5330
.219
6.31
748
.476
LIQU
ID49
.224
CHOK
E2.
871
0.00
03.
198
6.06
914
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133.
780
Ex.
1,Ca
se1
(con
tinue
d)
2580
.0.
047
72.3
193.
849
66.1
196.
140
48.3
50LI
QUID
49.0
15CH
OKE
2.86
70.
000
3.18
96.
056
14.7
0013
3.78
026
40.
0.0
4405
.619
7.1
4602
.719
5.95
148
.217
LIQU
ID48
.796
CHOK
E2.
863
0.00
03.
180
6.04
314
.700
133.
780
2700
.0.
040
39.7
200.
442
40.1
195.
750
48.0
74LI
QUID
48.5
67CH
OKE
2.85
60.
000
3.16
76.
023
14.7
0013
3.78
027
60.
0.0
3675
.120
3.6
3878
.719
5.53
547
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LIQU
ID48
.327
CHOK
E2.
844
0.00
03.
147
5.99
114
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133.
780
2820
.0.
033
12.6
206.
735
19.3
195.
303
47.7
59LI
QUID
48.0
73CH
OKE
2.83
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000
3.12
65.
957
14.7
0013
3.78
028
80.
0.0
2952
.120
9.7
3161
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5.05
147
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LIQU
ID47
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CHOK
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817
0.00
03.
104
5.92
114
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133.
780
2940
.0.
025
94.0
212.
728
06.6
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47.3
90LI
QUID
47.5
18CH
OKE
2.80
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000
3.08
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883
14.7
0013
3.78
030
00.
0.0
2238
.221
5.5
2453
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4.47
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LIQ-
vAP
47.1
79CH
OKE
2.76
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000
3.04
05.
801
14.7
0013
3.78
030
60.
0.0
1887
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7.9
2105
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4.07
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VAPO
R46
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000
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366
2.36
614
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978
3120
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81.4
182.
219
63.6
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706
37.7
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POR
37.7
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1.90
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3180
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49.5
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POR
30.8
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485
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3240
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27.7
132.
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POR
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01.
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3360
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0.89
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3420
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2.9
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722
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VAPO
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PDC
0.00
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60.
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14.7
0014
7.00
334
80.
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307
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POR
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0.00
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0014
7.00
336
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989
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147.
307
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POR
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3660
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R22
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0.00
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0014
7.00
337
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577.
961
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307
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POR
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3780
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VAPO
R22
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0.00
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0014
7.00
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934
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1152
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R22
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POC
0.00
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000
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896
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0014
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1
3960
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9.9
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307
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00.
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147.
003
TITL
E:EX
.1,
CASE
2.10-T~
CYL,
SHEA
RED
VALV
EAT
9O'
CLOC
K,UF
6AT
200
F
******
*C~ITJ~
OFUF
6IN
COOA
ltt1EN
T***
****
PAT~Y
INLE
T***
******
C~DITl~
orUF
6EX
WillS
TED
HH
HH
HrL
lJ4TIM
E**
****
****
MASS
(LB)
****
****
**TE
MPPR
ESRE
LEAS
EPR
ESRA
TE***
*REL
EASE
RATE
(LBI
SEC)
****
TEMP
PRES
(SEC
)SO
LID
LIQU
IDVA
POR
TOTA
L(D
EGF)
(PSI
A)PI¥
%SE
(PSI
A)BA
SIS
SOLI
DLI
QUID
VAPO
RTO
TAL
(DEG
F)(P
SIA)
O.0.
021
003.
426
.621
030.
020
0.00
051
.152
LIQU
ID53
.179
CHOK
E2.
944
0.00
03.
390
6.33
414
.700
133.
780
60.
0.0
2061
9.2
30.7
2064
9.9
199.
949
51.1
14LI
QUID
53.0
39CH
OKE
2.94
30.
000
3.38
76.
331
14.7
0013
3.78
012
0.0.
020
235.
234
.920
270.
119
9.89
651
.075
LIQU
ID52
.901
CHOK
E2.
942
0.00
03.
384
6.32
714
.700
133.
780
180.
0.0
1985
1.5
39.0
1989
0.5
199.
843
51.0
36LI
QUID
52.7
66CH
OKE
2.94
10.
000
3.38
26.
323
14.7
0013
3.78
024
0.0.
019
468.
043
.219
511.
119
9.78
950
.996
LIQU
ID52
.632
CHOK
E2.
940
0.00
03.
379
6.31
914
.700
133.7
BO30
0.0.
019
084.
747
.319
132.
019
9.73
450
.955
LIQU
ID52
.501
CHOK
E2.
939
0.00
03.
376
6.31
514
.700
133.
780
360.
0.0
1870
1.7
51.4
1875
3.1
199.
678
SO.91
4LI
QUID
52.3
71CH
OKE
2.93
80.
000
3.37
36.
311
14.7
0013
3.78
042
0.0.
018
318.
955
.618
374.
519
9.62
050
.871
LIQU
ID52
.241
CHOK
E2.
937
0.00
03.
370
6.30
714
.700
133.
780
480.
0.0
1793
6.4
59.7
1799
6.1
199.
562
50.8
28LI
QUID
52.1
12CH
OKE
2.93
60.
000
3.36
76.
302
14.7
0013
3.78
054
0.0.
017
554.
163
.817
617.
919
9.S0
350
.785
LIQU
ID51
.984
CHOK
E2.
934
0.00
03.
364
6.29
814
.700
133.
780
600.
0.0
1717
2.2
67.8
1724
0.0
199.
442
50.7
40LI
QUID
51.8
57CH
OKE
2.93
30.
000
3.36
16.
294
14.7
0013
3.78
066
0.0.
016
790.
571
.916
862.
419
9.38
150
.695
LI~ID
51.7
29CH
OKE
2.93
20.
000
3.35
76.
289
14.7
0013
3.78
072
0.0.
016
409.
076
.016
485.
019
9.31
850
.648
LIID
51.6
02CH
OKE
2.93
10.
000
3.35
46.
285
14.7
0013
3.78
078
0.0.
016
027.
980
.016
107.
919
9.25
350
.601
LIQU
ID51
.474
CHOK
E2.
930
0.00
03.
351
6.28
014
.700
133.
780
840.
0.0
1564
7.0
84.1
1573
1.1
199.
188
50.5
53LI
QUID
51.3
46CH
OKE
2.92
80.
000
3.34
76.
275
14.7
0013
3.78
090
0.0.
015
266.
588
.115
354.
619
9.12
150
.S03
LIQU
ID51
.218
CHOK
E2.
927
0.00
03.
344
6.27
114
.700
133.
780
960.
0.0
1488
6.2
92.1
1497
8.4
199.
052
50.4
53LI
QUID
51.0
89CH
OKE
2.92
60.
000
3.34
06.
266
14.7
0013
3.78
0~ 0
110
20.
0.0
1450
6.3
96.1
1460
2.4
198.
982
50.4
02LI
QUID
50.9
60CH
OKE
2.92
40.
000
3.33
66.
259
14.7
0013
3.78
0<
:1)
1080
.0.
014
126.
710
0.1
1422
6.9
198.
910
50.3
49LI
QUID
SO.8
30CH
OKE
2.91
50.
000
3.32
46.
239
14.7
0013
3.78
011
40.
0.0
1374
8.4
104.
113
852.
619
8.83
750
.295
LIQU
ID50
.699
CHOK
E2.
906
0.00
03.
312
6.21
814
.700
133.
780
1200
.0.
013
371.
410
8.1
1347
9.5
198.
762
50.2
40LI
QUID
50.5
68CH
OKE
2.89
80.
000
3.30
06.
198
14.7
0013
3.78
012
60.
0.0
1299
5.6
112.
013
107.
619
8.68
550
.184
LIQU
ID50
.436
CHOK
E2.
889
0.00
03.
288
6.17
714
.700
133.
780
1320
.0.
012
621.
111
5.9
1273
6.9
198.
607
50.1
27LI
QUID
50.3
04CH
OKE
2.88
10.
000
3.27
66.
157
14.7
0013
3.78
013
80.
0.0
1224
7.8
119.
812
367.
519
8.52
750
.069
LIQU
IDSO
.170
CHOK
E2.
872
0.00
03.
264
6.13
614
.700
133.
780
1440
.0.
011
875.
712
3.6
1199
9.3
198.
444
50.0
09LIQ~
SO.00
9CH
OKE
2.82
80.
000
3.23
26.
060
14.7
0013
3.78
015
00.
0.0
1150
8.4
127.
411
635.
719
8.34
049
.933
LIQ-
VAP
49.9
33CH
OKE
1.23
80.
000
2.64
83.
887
14.7
0013
3.78
015
60.
0.0
1127
4.7
127.
811
402.
519
6.94
248
.923
VAPO
R48
.923
CHOK
E0.
000
0.00
02.
462
2.46
214
.700
195.
786
1620
.0.
011
130.
312
4.5
1125
4.8
193.
642
46.6
01VA
POR
46.6
01CH
OKE
0.00
00.
000
2.35
22.
352
14.7
0019
2.55
016
80.
0.0
1099
2.5
121.
211
113.
719
0.43
544
.425
VAPO
R44
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CHOK
E0.
000
0.00
02.
249
2.24
914
.700
189.
404
1740
.0.
010
860.
711
8.0
1097
8.8
187.
317
42.3
85VA
POR
42.3
85CH
OKE
0.00
00.
000
2.15
22.
152
14.7
0018
6.34
518
00.
0.0
1073
4.8
114.
910
849.
718
4.28
640
.471
VAPO
R40
.471
CHOK
E0.
000
0.00
02.
060
2.06
014
.700
183.
369
1860
.0.
010
614.
311
1.8
1072
6.1
181.
337
38.6
73VA
POR
38.6
73PD
C0.
000
0.00
01.
959
1.95
914
.700
180.
475
1920
.0.
010
499.
710
8.8
1060
8.5
178.
490
36.9
95VA
POR
36.9
95PD
C0.
000
0.00
01.
860
1.86
014
.700
177.
679
1980
.0.
010
391.
010
5.9
1049
6.9
175.
748
35.4
33VA
POR
35.4
33PD
C0.
000
0.00
01.
766
1.76
614
.700
174.
985
2040
.0.
010
287.
810
3.2
1039
1.0
173.
106
33.9
76VA
POR
33.9
76PD
C0.
000
0.00
01.
678
1.67
814
.700
172.
389
2100
.0.
010
189.
710
0.5
1029
0.2
170.
562
32.6
17VA
POR
32.6
17PD
C0.
000
0.00
01.
595
1.59
514
.700
169.
889
2160
.0.
010
096.
697
.910
194.
516
8.11
331
.348
VAPO
R31
.348
PDC
0.00
00.
000
1.51
71.
517
14.7
0016
7.48
022
20.
0.0
1000
8.0
95.5
1010
3.5
165.
754
30.1
63VA
POR
30.1
63PD
C0.
000
0.00
01.
443
1.44
314
.700
165.
161
2280
.0.
099
23.8
93.1
1001
6.9
163.
484
29.0
55VA
POR
29.0
55PD
C0.
000
0.00
01.
373
1.37
314
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162.
928
2340
.0.
098
43.7
90.9
9934
.616
1.30
028
.019
VAPO
R28
.019
PDC
0.00
00.
000
1.30
61.
306
14.7
0016
0.77
924
00.
0.0
9767
.588
.798
56.2
159.
198
27.0
49VA
POR
27.0
49PD
C0.
000
0.00
01.
243
1.24
314
.700
158.
711
2460
.0.
096
95.0
86.7
9781
.715
7.17
726
.141
VAPO
R26
.141
PDC
0.00
00.
000
1.18
31.
183
14.7
0015
6.72
225
20.
0.0
9626
.084
.797
10.7
155.
233
25.2
91VA
POR
25.2
91PD
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7.00
3
TITL
E:EX
.1,
CASE
3.10
-T(}
ICY
L,SH
EARE
DVA
lVE
AT12
O'Cl
OCK,
UF'6
AT20
0F'
******
*C(
}IDIT
l(}l
OF'U
F'6IN
COOA
IttlE
NT***
****
PAHI
¥tYIN
lET
~~~~~~~~~
COND
ITI(}
IOF
'UF
6EX
HAUS
TED
~~~~*~~~*~
FL~
TIME
~~*~~~*~~*
MASS
(LB)
~****~***~
TEMP
PRES
RELE
ASE
PRES
RATE
****R
ELEA
SERA
TE(L
BISE
C)***
*TE
MPPR
ES(S
EC)
SOLI
DLI
QUID
VAPO
RTO
TAL
(DEG
F)(P
SIA)
PI¥lS
E(P
SIA)
BASI
SSO
LID
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I0VA
POR
TOTA
L(D
EGF)
(PSI
A)
O.0.
021
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426
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665.
514
7.30
722
.042
VAPO
R22
.D42
PDC
0.00
00.
000
0.89
60.
896
14.7
0014
7.00
352
80.
4093
.510
462.
356
.014
611.
814
7.30
722
.042
VAPO
R22
.042
POC
O.DDD
D.DDD
D.89
60.
896
14.70
D14
7.D03
534D
.41
76.5
1032
5.2
56.4
1455
8.0
147.
307
22.0
42VA
POR
22.M
2PD
CO.D
OOO.O
DO0.
896
0.89
614
.700
147.
003
5400
.42
59.5
1018
8.0
56.7
1450
4.2
147.
307
22.0
42VA
POR
22.M
2PO
C0.
000
0.00
00.
896
0.89
614
.70D
147.
003
Ex.
1,eas~
3(continu~d)
5460
.43
42.5
1005
0.8
57.1
1445
0.4
147.
307
22.0
42VA
POR
22.0
42PD
t0.
000
0.00
00.
896
0.89
614
.700
147.
003
5520
.44
25.5
9913
.757
.514
396.
614
7.30
722
.042
VAPO
R22
.042
poe
0.00
00.
000
0.89
60.
896
14.7
0014
7.00
355
80.
4508
.597
76.5
57.9
1434
2.9
147.
307
22.0
42VA
POR
22.0
42po
e0.
000
0.00
00.
896
0.89
614
.700
147.
003
5640
.45
91.5
9639
.458
.214
289.
114
7.30
722
.042
VAPO
R22
.042
poe
0.00
00.
000
0.89
60.
896
14.7
0014
7.00
357
00.
4674
.595
02.2
58.6
1423
5.3
147.
307
22.0
42VA
POR
22.0
42PD
t0.
000
0.00
00.
896
0.89
614
.700
147.
003
5760
.47
57.5
9365
.159
.014
181.
514
7.30
722
.042
VAPO
R22
.042
poe
0.00
00.
000
0.89
60.
896
14.7
0014
7.00
358
20.
4840
.592
27.9
59.4
1412
7.8
147.
307
22.0
42VA
POR
22.0
42po
e0.
000
0.00
00.
896
0.89
614
.700
147.
003
5880
.49
23.5
9090
.759
.714
074.
014
7.30
722
.042
VAPO
R22
.042
poe
0.00
00.
000
0.89
60.
896
14.7
0014
7.00
359
40.
5006
.589
53.6
60.1
1402
0.2
147.
307
22.0
42VA
POR
22.0
42po
e0.
000
0.00
00.
896
0.89
614
.700
147.
003
6000
.50
89.5
8816
.460
.513
966.
414
7.30
722
.042
VAPO
R22
.042
POC
0.00
00.
000
0.89
60.
996
14.7
0014
7.00
360
60.
5172
.586
79.3
60.9
1391
2.6
147.
307
22.0
42VA
POR
22.0
42PD
t0.
000
0.00
00.
896
0.89
614
.700
147.
003
6120
.52
55.5
8542
.161
.313
858.
914
7.30
722
.042
VAPO
R22
.042
poe
0.00
00.
000
0.89
60.
896
14.7
0014
7.00
361
80.
5338
.584
04.9
61.6
1380
5.1
147.
307
22.0
42VA
POR
22.0
42po
e0.
000
0.00
00.
896
0.89
614
.700
147.
003
6240
.54
21.5
9267
.862
.013
751.
314
7.30
722
.042
VAPO
R22
.042
poe
0.00
00.
000
0.89
60.
896
14.7
0014
7.00
363
00.
5504
.581
30.6
62.4
1369
7.5
147.
307
22.0
42VA
POR
22.0
42po
e0.
000
0.00
00.
896
0.89
614
.700
147.
003
6360
.55
87.5
7993
.562
.813
643.
814
7.30
722
.042
VAPO
R22
.042
poe
0.00
00.
000
0.89
60.
896
14.7
0014
7.00
364
20.
5670
.578
56.3
63.1
1359
0.0
147.
307
22.0
42VA
POR
22.0
42po
e0.
000
0.00
00.
896
0.89
614
.700
147.
003
6480
.57
53.5
7719
.263
.513
536.
214
7.30
722
.042
VAPO
R22
.042
poe
0.00
00.
000
0.89
60.
896
14.7
0014
7.00
365
40.
5836
.575
82.0
63.9
1348
2.4
147.
307
22.0
42VA
POR
22.0
42po
e0.
000
0.00
00.
896
0.89
614
.700
147.
003
6600
.59
19.5
7444
.864
.313
428.
614
7.30
722
.042
VAPO
R22
.042
poe
0.00
00.
000
0.89
60.
896
14.7
0014
7.00
366
60.
6002
.573
07.7
64.7
1337
4.9
147.
307
22.0
42VA
POR
22.0
42po
e0.
000
0.00
00.
896
0.89
614
.700
147.
003
6720
.60
85.5
7170
.565
.013
321.
114
7.30
722
.042
VAPO
R22
.042
poe
0.00
00.
000
0.89
60.
896
14.7
0014
7.00
3....
6780
.61
68.5
7033
.465
.413
267.
314
7.30
722
.042
VAPO
R22
.042
poe
0.00
00.
000
0.89
60.
896
14.7
0014
7.00
30
") ....69
40.
6251
.668
96.2
65.8
1321
3.5
147.
307
22.0
42VA
POR
22.0
42po
e0.
000
0.00
00.
896
0.89
614
.700
147.
003
6900
.63
34.6
6759
.066
.213
159.
814
7.30
722
.042
VAPO
R22
.042
poe
0.00
00.
000
0.89
60.
896
14.7
0014
7.00
369
60.
6417
.666
21.9
66.5
1310
6.0
147.
307
22.0
42VA
POR
22.0
42po
e0.
000
0.00
00.
896
0.99
614
.700
147.
003
7020
.65
00.6
6484
.766
.913
052.
214
7.30
722
.042
VAPO
R22
.042
PDt
0.00
00.
000
0.89
60.
896
14.7
0014
7.00
370
80.
6583
.663
47.6
67.3
1299
8.4
147.
307
22.0
42VA
POR
22.0
42po
e0.
000
0.00
00.
896
0.89
614
.700
147.
003
7140
.66
66.6
6210
.467
.712
944.
614
7.30
722
.042
VAPO
R22
.042
poe
0.00
00.
000
0.89
60.
896
14.7
0014
7.00
3
TITL
E:EX
.1,
CASE
4.10
-TON
CYL,
SHEA
RED
VALV
EAT
6O'
CLOC
K,UF
6AT
250
F
****
***
COND
ITIO
NOF
UF6
INCO
NTAI
t-t1EN
T***
****
PATH
-IAY
INLE
T**
****
***
COND
ITIO
NOF
UF6
EXHA
USTE
D**
****
****
FUJ4
TIME
****
****
**MA
SS(L
B)**
****
****
TEMP
PRES
RELE
ASE
PRES
RATE
****
RELE
ASE
RATE
(LBI
SEC)
****
TEMP
PRES
(SEC
)SO
LID
LIQU
IDVA
POR
TOTA
L(D
EGF)
(PSI
A)PH
ASE
(PSI
A)BA
SIS
SOLI
DLI
QUID
VAPO
RTO
TAL
(DEG
F)(P
SIA)
O.0.
021
007.
622
.421
030.
025
0.00
099
.709
LIQU
ID10
3.97
6CH
OKE
3.77
60.
000
6.93
410
.710
14.7
0013
3.78
060
.0.
020
351.
935
.520
387.
424
9.85
099
.525
LIQU
ID10
3.58
6CH
OKE
3.77
50.
000
6.92
110
.696
14.7
0013
3.78
012
0.0.
019
697.
148
.619
745.
724
9.69
699
.335
LIQU
ID10
3.21
3CH
OKE
3.77
30.
000
6.90
710
.681
14.7
0013
3.78
018
0.0.
019
043.
361
.519
104.
824
9.53
799
.141
LI~UID
102.
849
CHOK
E3.
772
0.00
06.
894
10.6
6514
.700
133.
780
240.
0.0
1839
0.4
74.5
1846
4.9
249.
373
98.9
41LI
UID
102.
488
CHOK
E3.
770
0.00
06.
879
10.6
5014
.700
133.
780
300.
0.0
1773
8.6
87.3
1782
5.9
249.
205
98.7
35LI
QUID
102.
129
CHOK
E3.
769
0.00
06.
865
10.6
3314
.700
133.
780
360.
0.0
1708
7.8
100.
117
187.
924
9.03
198
.522
LIQU
ID10
1.77
0CH
OKE
3.76
70.
000
6.85
010
.617
14.7
0013
3.78
042
0.0.
016
438.
111
2.8
1655
0.9
248.
851
98.3
04LI
QUID
101.
407
CHOK
E3.
765
0.00
06.
834
10.5
9914
.700
133.
780
480.
0.0
1578
9.6
125.
415
915.
024
8.66
598
.077
LIQU
ID10
1.04
2CH
OKE
3.76
30.
000
6.81
810
.582
14.7
0013
3.78
054
0.0.
015
142.
113
7.9
1528
0.1
248.
473
97.8
44LI
QUID
100.
671
CHOK
E3.
761
0.00
06.
802
10.5
6314
.700
133.
780
600.
0.0
1449
5.9
150.
414
646.
324
8.27
397
.602
LIQU
ID10
0.29
5CH
OKE
3.75
90.
000
6.78
510
.544
14.7
0013
3.78
066
0.0.
013
850.
916
2.71
4013
.624
8.06
697
.351
LIQU
ID99
.911
CHOK
E3.
757
0.00
06.
767
10.5
2414
.700
133.
780
720.
0.0
1320
7.2
175.
013
382.
224
7.85
197
.091
LIQU
ID99
.520
CHOK
E3.
755
0.00
06.
749
10.5
0414
.700
133.
780
780.
0.0
1256
4.8
187.
212
751.
924
7.62
696
.820
LIQU
ID99
.120
CHOK
E3.
753
0.00
06.
730
10.4
8214
.700
133.
780
840.
0.0
1192
3.8
199.
212
123.
024
7.39
296
.538
LIQU
ID98
.709
CHOK
E3.
750
0.00
06.
710
10.4
6014
.700
133.
780
900.
0.0
1128
4.3
211.
111
495.
424
7.14
796
.244
LIQU
ID98
.286
CHOK
E3.
748
0.00
06.
689
10.4
3714
.700
133.
780
960.
0.0
1064
6.2
223.
010
869.
224
6.89
195
.936
LIQU
ID97
.850
CHOK
E3.
745
0.00
06.
667
10.4
1214
.700
133.
780
.... 0')
1020
.0.
010
009.
823
4.7
1024
4.5
246.
621
95.6
13LI
QUID
97.4
00CH
OKE
3.74
20.
000
6.64
510
.387
14.7
0013
3.78
0~
1080
.0.
093
75.1
246.
296
21.3
246.
337
95.2
74LI
QUID
96.9
33CH
OKE
3.73
90.
000
6.62
110
.360
14.7
0013
3.78
011
40.
0.0
8742
.125
7.6
8999
.724
6.03
794
.917
LIQU
ID96
.447
CHOK
E3.
730
0.00
06.
586
10.3
1614
.700
133.
780
1200
.0.
081
11.9
268.
883
80.7
245.
719
94.5
39LI
QUID
95.9
41CH
OKE
3.72
00.
000
6.54
710
.266
14.7
0013
3.78
012
60.
0.0
7484
.927
9.8
7764
.824
5.38
194
.139
LIQU
ID95
.412
CHOK
E3.
709
0.00
06.
506
10.2
1414
.700
133.
780
1320
.0.
0686
1.3
290.
671
51.9
245.
021
93.7
14LI
QUID
94.8
56CH
OKE
3.69
70.
000
6.46
310
.160
14.7
0013
3.78
013
80.
0.0
6241
.130
1.2
6542
.324
4.63
593
.259
LIQU
ID94
.270
CHOK
E3.
686
0.00
06.
418
10.1
0414
.700
133.
780
1440
.0.
056
24.5
311.
559
36.1
244.
219
92.7
71LI
QUID
93.6
48CH
OKE
3.67
30.
000
6.37
110
.045
14.7
0013
3.78
015
00.
0.0
5011
.832
1.5
5333
.424
3.76
892
.243
LIQU
ID92
.984
CHOK
E3.
661
0.00
06.
321
9.98
214
.700
133.
780
1560
.0.
044
03.2
331.
247
34.5
243.
274
91.6
68LI
QUID
92.2
71CH
OKE
3.64
70.
000
6.26
89.
915
14.7
0013
3.78
016
20.
0.0
3799
.034
0.5
4139
.624
2.72
991
.036
LIQU
ID91
.497
CHOK
E3.
633
0.00
06.
210
9.84
314
.700
133.
780
1680
.0.
031
99.6
349.
435
48.9
242.
121
90.3
34LI
QUID
90.6
47CH
OKE
3.61
80.
000
6.14
89.
765
14.7
0013
3.78
017
40.
0.0
2605
.435
7.7
2963
.024
1.43
089
.541
LIQU
ID89
.701
CHOK
E3.
572
0.00
06.
030
9.60
214
.700
133.
780
1800
.0.
020
21.7
365.
323
86.9
240.
639
88.6
39LI
Q-VA
P88
.639
CHOK
E3.
319
0.00
05.
789
9.10
814
.700
133.
780
1860
.0.
014
72.0
368.
418
40.4
238.
883
86.6
78VA
POR
86.6
78CH
OKE
0.00
00.
000
4.20
34.
203
14.7
0023
6.83
219
20.
0.0
1308
.527
9.7
1588
.221
2.77
761
.307
VAPO
R61
.307
CHOK
E0.
000
0.00
03.
042
3.04
214
.700
211.
301
1980
.0.
011
90.3
215.
414
05.7
190.
643
44.5
64VA
POR
44.5
64CH
OKE
0.00
00.
000
2.25
52.
255
14.7
0018
9.60
920
40.
0.0
1101
.716
8.7
1270
.417
1.76
633
.254
VAPO
R33
.254
PDt
0.00
00.
000
1.63
41.
634
14.7
0017
1.07
221
00.
0.0
1036
.513
5.8
1172
.315
6.34
025
.772
VAPO
R25
.772
PDC
0.00
00.
000
1.15
81.
158
14.7
0015
5.89
821
60.
26.3
957.
711
8.9
1102
.814
7.30
722
.042
VAPO
R22
.042
PDC
0.00
00.
000
0.89
60.
896
14.7
0014
7.00
322
20.
109.
382
0.6
119.
310
49.1
147.
307
22.0
42VA
POR
22.0
42PD
C0.
000
0.00
00.
896
0.89
614
.700
147.
003
2280
.19
2.3
683.
411
9.6
995.
314
7.30
722
.042
VAPO
R22
.042
PDC
0.00
00.
000
0.89
60.
896
14.7
0014
7.00
323
40.
275.
354
6.2
120.
094
1.5
147.
307
22.0
42VA
POR
22.0
42PD
C0.
000
0.00
00.
896
0.89
614
.700
147.
003
2400
.35
8.3
409.
112
0.4
887.
714
7.30
722
.042
VAPO
R22
.042
poe
0.00
00.
000
0.89
60.
896
14.7
0014
7.00
324
60.
441.
327
1.9
120.
883
4.0
147.
307
22.0
42VA
POR
22.0
42PD
C0.
000
0.00
00.
896
0.89
614
.700
147.
003
2520
.52
4.3
134.
812
1.1
780.
214
7.30
722
.042
VAPO
R22
.042
PDC
0.00
00.
000
0.89
60.
896
14.7
0014
7.00
3
TITL
E:EX
.2,
CASE
1.RE
LEAS
EFR
OM8"
BREA
CHIN
SIDE
OF14
-TCY
L(A
SHO
LEIN
END)
TIME (SEC
) O. 10.
20.
30.
40.
50.
60.
70.
80.
90.
100.
110.
120.
130.
140.
150.
160.
170.
180.
190.
200.
210.
220.
230.
240.
250.
260.
270.
280.
290.
300.
310.
320.
330.
340.
350.
360.
370.
380.
390.
400.
410.
420.
******
*C(J.
IDIT
I(NOF
UF6
INCC
NTAl
tflENT
******
*PA
TIIoIA
YIN
LET
••••
••••
••MA
SS(L
B)••
••••
••••
TEMP
PRES
RELE
ASE
PRES
SOLI
DLI
QUID
~POR
TOTA
L(D
EGF)
(PSI
A)PH
ASE
(PSI
A)
0.0
2585
0.6
49.4
2590
0.0
190.
000
44.1
36LI
QUID
48.6
870.
025
510.
752
.625
563.
318
9.96
744
.114
LIQU
ID48
.604
0.0
2517
0.9
55.8
2522
6.7
189.
934
44.0
93LI
QUID
48.5
210.
024
831.
359
.024
890.
318
9.90
144
.070
LIQU
ID48
.439
0.0
2449
1.8
62.2
2455
3.9
189.
867
44.0
48LI
QUID
48.3
570.
024
152.
465
.424
217.
818
9.83
344
.025
LIQU
ID48
.276
0.0
2381
3.2
68.6
2388
1.7
189.
798
44.0
03LI
QUID
48.1
950.
023
474.
171
.823
545.
818
9.76
343
.979
LIQU
ID48
.115
0.0
2313
5.1
74.9
2321
0.1
189.
728
43.9
56LI
QUID
48.0
350.
022
796.
378
.122
874.
518
9.69
243
.932
LIQU
ID47
.955
0.0
2245
7.7
81.3
2253
9.0
189.
655
43.9
08LI
QUID
47.8
750.
022
119.
284
.522
203.
718
9.61
843
.883
LIQU
ID47
.795
0.0
2178
0.9
87.6
2186
8.5
189.
581
43.8
59LI
QUID
47.7
160.
021
442.
790
.821
533.
518
9.54
343
.834
LIQU
ID47
.636
0.0
2110
4.7
93.9
2119
8.6
189.
504
43.8
08LI
QUID
47.5
570.
020
766.
897
.120
863.
918
9.46
543
.782
LIQU
ID47
.477
0.0
2042
9.1
100.
220
529.
318
9.42
543
.756
LIQU
ID47
.398
0.0
2009
1.6
103.
420
194.
918
9.38
543
.730
LIQU
ID47
.318
0.0
1975
4.2
106.
519
860.
718
9.34
443
.703
LIQU
ID47
.238
0.0
1941
7.0
109.
619
526.
618
9.30
243
.675
LIQU
ID47
.158
0.0
1908
0.0
112.
719
192.
718
9.26
043
.648
LIQU
ID47
.078
0.0
1874
3.1
115.
818
859.
018
9.21
743
.620
LIQU
ID46
.998
0.0
1840
6.5
118.
918
525.
418
9.17
443
.591
LIQU
ID46
.917
0.0
1807
0.0
122.
018
192.
018
9.13
043
.562
LIQU
ID46
.836
0.0
1773
3.7
125.
117
858.
818
9.08
543
.532
LIQU
ID46
.755
0.0
1739
7.6
128.
217
525.
818
9.03
943
.502
LIQU
ID46
.673
0.0
1706
1.6
131.
317
192.
918
8.99
243
.472
LIQU
ID46
.591
0.0
1672
5.9
134.
416
860.
318
8.94
543
.441
LIQU
ID46
.509
0.0
1639
0.4
137.
416
527.
818
8.89
743
.409
LIQU
ID46
.426
0.0
1605
5.0
140.
516
195.
518
8.84
843
.377
LIQU
ID46
.342
0.0
1571
9.9
143.
515
863.
418
8.79
843
.345
LIQU
ID46
.258
0.0
1538
5.0
146.
615
531.
618
8.74
743
.311
LIQU
ID46
.174
0.0
1505
0.3
149.
615
199.
918
8.69
543
.277
LIQU
ID46
.089
0.0
1471
5.8
152.
614
868.
418
8.64
243
.243
LIQU
ID46
.003
0.0
1438
1.5
155.
614
537.
218
8.58
843
.207
LI~UID
45.9
170.
014
047.
515
8.6
1420
6.1
188.
533
43.1
72LI
UID
45.8
300.
013
713.
716
1.6
1387
5.3
188.
476
43.1
35LI
UID
45.7
420.
013
380.
116
4.6
1354
4.7
188.
419
43.0
97LI
QUID
45.6
530.
013
046.
716
7.6
1321
4.3
188.
360
43.0
59LI
QUID
45.5
640.
012
713.
617
0.6
1288
4.2
188.
300
43.0
20LI
QUID
45.4
730.
012
380.
817
3.5
1255
4.3
188.
239
42.9
80LI
QUID
45.3
820.
012
048.
217
6.5
1222
4.7
188.
176
42.9
39LI
QUID
45.2
890.
011
715.
917
9.4
1189
5.3
188.
111
42.8
98LI
QUID
45.1
96
FUll
RATE
BASI
S
CHOK
ECH
OKE
CHOK
ECH
OKE
CHOK
ECH
OKE
CHOK
ECH
OKE
CHOK
ECH
OKE
CHOK
ECH
OKE
CHOK
ECH
OKE
CHOK
ECH
OKE
CHOK
ECH
OKE
CHOK
ECH
OKE
CHOK
ECH
OKE
CHOK
ECH
OKE
CHOK
ECH
OKE
CHOK
ECH
OKE
CHOK
ECH
OKE
CHOK
ECH
OKE
CHOK
ECH
OKE
CHOK
ECH
OKE
CHOK
ECH
OKE
CHOK
ECH
OKE
CHOK
ECH
OKE
CHOK
E
••••
••••
•C(
J.IDI
TI(N
OFUF
6EX
HAUS
TED
••••
••••
•****
*REL
EASE
RATE
(LBI
SEC)
****
TEMP
PRES
SOLI
DLI
QUID
~POR
TOTA
L(D
EGF)
(PSI
A)
16.3
960.
000
17.2
7533
.671
14.7
0013
3.78
016
.392
0.00
017
.266
33.6
5814
.700
133.
780
16.3
880.
000
17.2
5633
.645
14.7
0013
3.78
016
.384
0.00
017
.247
33.6
3114
.700
133.
780
16.3
800.
000
17.2
3833
.618
14.7
0013
3.78
016
.376
0.00
017
.228
33.6
0414
.700
133.
780
16.3
720.
000
17.2
1833
.590
14.7
0013
3.78
016
.367
0.00
017
.208
33.5
7614
.700
133.
780
16.3
630.
000
17.1
9833
.562
14.7
0013
3.78
016
.359
0.00
017
.188
33.5
4714
.700
133.
780
16.3
540.
000
17.1
7833
.532
14.7
0013
3.78
016
.350
0.00
017
.168
33.5
1714
.700
133.
780
16.3
450.
000
17.1
5733
.502
14.7
0013
3.78
016
.340
0.00
017
.147
33.4
8714
.700
133.
780
16.3
360.
000
17.1
3633
.472
14.7
0013
3.78
016
.331
0.00
017
.125
33.4
5614
.700
133.
780
16.3
260.
000
17.1
1433
.440
14.7
0013
3.78
016
.321
0.00
017
.102
33.4
2414
.700
133.
780
16.3
160.
000
17.0
9133
.407
14.7
0013
3.78
016
.311
0.00
017
.079
33.3
9014
.700
133.
780
16.3
060.
000
17.0
6833
.374
14.7
0013
3.78
016
.301
0.00
017
.056
33.3
5614
.700
133.
780
16.2
950.
000
17.0
4433
.339
14.7
0013
3.78
016
.290
0.00
017
.031
33.3
2114
.700
133.
780
16.2
840.
000
17.0
1933
.303
14.7
0013
3.78
016
.279
0.00
017
.006
33.2
8514
.700
133.
780
16.2
730.
000
16.9
9333
.266
14.7
0013
3.78
016
.267
0.00
016
.980
33.2
4714
.700
133.
780
16.2
610.
000
16.9
6633
.228
14.7
0013
3.78
016
.255
0.00
016
.953
33.2
0814
.700
133.
780
16.2
490.
000
16.9
3933
.188
14.7
0013
3.78
016
.243
0.00
016
.925
33.1
6814
.700
133.
780
16.2
360.
000
16.9
1033
.147
14.7
0013
3.78
016
.230
0.00
016
.896
33.1
2614
.700
133.
780
16.2
230.
000
16.8
8133
.104
14.7
0013
3.78
016
.217
0.00
016
.865
33.0
8214
.700
133.
780
16.2
100.
000
16.8
5033
.059
14.7
0013
3.78
016
.203
0.00
016
.834
33.0
3614
.700
133.
780
16.1
950.
000
16.8
1833
.013
14.7
0013
3.78
016
.188
0.00
016
.801
32.9
8914
.700
133.
780
16.1
800.
000
16.7
8432
.964
14.7
0013
3.78
016
.173
0.00
016
.767
32.9
3914
.700
133.
780
16.1
650.
000
16.7
4932
.914
14.7
0013
3.78
0
.... ~
Ex.
2,Ca
se1
(con
tinue
d)
430.
0.0
1138
3.8
182.
311
566.
218
8.04
542
.855
LIQU
ID45
.101
CHOK
E16
.157
0.00
016
.731
32.8
8714
.700
133.
780
440.
0.0
1105
2.0
185.
311
237.
318
7.97
842
.811
LIQU
ID45
.006
CHOK
E16
.148
0.00
016
.712
32.8
6014
.700
133.
780
450.
0.0
1072
0.5
188.
210
908.
718
7.90
842
.766
LIQU
ID44
.908
CHOK
E16
.140
0.00
016
.693
32.8
3314
.700
133.
780
460.
0.0
1038
9.3
191.
010
580.
318
7.83
742
.720
LIQU
ID44
.810
CHOK
E16
.131
0.00
016
.673
32.8
0414
.700
133.
780
470.
0.0
1005
8.4
193.
910
252.
318
7.76
342
.672
LIQU
ID44
.710
CHOK
E16
.122
0.00
016
.653
32.7
7514
.700
133.
780
480.
0.0
9727
.819
6.8
9924
.618
7.68
842
.624
LIQU
ID44
.609
CHOK
E16
.113
0.00
016
.633
32.7
4514
.700
133.
780
490.
0.0
9397
.519
9.6
9597
.118
7.61
042
.574
LIQU
ID44
.505
CHOK
E16
.103
0.00
016
.611
32.7
1414
.700
133.
780
500.
0.0
9067
.520
2.5
9270
.018
7.53
142
.522
LIQU
ID44
.401
CHOK
E16
.093
0.00
016
.590
32.6
8314
.700
133.
780
510.
0.0
8737
.920
5.3
8943
.118
7.44
842
.469
LIQU
ID44
.294
CHOK
E16
.083
0.00
016
.567
32.6
5014
.700
133.
780
520.
0.0
8408
.620
8.1
8616
.618
7.36
342
.414
LIQU
ID44
.185
CHOK
E16
.072
0.00
016
.544
32.6
1614
.700
133.
780
530.
0.0
8079
.621
0.8
8290
.518
7.27
542
.358
LIQU
ID44
.074
CHOK
E16
.062
0.00
016
.520
32.5
8114
.700
133.
780
540.
0.0
7751
.121
3.6
7964
.718
7.18
442
.300
LIQU
ID43
.961
CHOK
E16
.050
0.00
016
.495
32.5
4514
.700
133.
780
550.
0.0
7422
.921
6.3
7639
.218
7.09
042
.239
LIQU
ID43
.846
CHOK
E16
.039
0.00
016
.469
32.5
0814
.700
133.
780
560.
0.0
7095
.121
9.1
7314
.118
6.99
242
.177
LI~UID
43.7
28CH
OKE
16.0
270.
000
16.4
4332
.469
14.7
0013
3.78
057
0.0.
067
67.7
221.
869
89.4
186.
891
42.1
12LI
UID
43.6
07CH
OKE
16.0
140.
000
16.4
1532
.429
14.7
0013
3.78
058
0.0.
064
40.7
224.
466
65.1
186.
785
42.0
44LI
QUID
43.4
83CH
OKE
16.0
010.
000
16.3
8632
.387
14.7
0013
3.78
059
0.0.
061
14.2
227.
163
41.3
186.
675
41.9
74LI
QUID
43.3
55CH
OKE
15.9
870.
000
16.3
5732
.344
14.7
0013
3.78
060
0.0.
057
88.1
229.
760
17.8
186.
560
41.9
01LI
QUID
43.2
24CH
OKE
15.9
730.
000
16.3
2632
.299
14.7
0013
3.78
061
0.0.
054
62.5
232.
356
94.8
186.
440
41.8
24LI
QUID
43.0
89CH
OKE
15.9
580.
000
16.2
9332
.251
14.7
0013
3.78
062
0.0.
051
37.5
234.
953
72.3
186.
314
41.7
44LI
QUID
42.9
50CH
OKE
15.9
430.
000
16.2
5932
.202
14.7
0013
3.78
063
0.0.
048
12.9
237.
450
50.3
186.
182
41.6
60LI
QUID
42.8
06CH
OKE
15.9
260.
000
16.2
2332
.150
14.7
0013
3.78
0~
640.
0.0
4488
.923
9.9
4728
.818
6.04
341
.572
LIQU
ID42
.656
CHOK
E15
.909
0.00
016
.186
32.0
9514
.700
133.
780
~65
0.0.
041
65.5
242.
344
07.9
185.
895
41.4
79LI
QUID
42.5
01CH
OKE
15.8
910.
000
16.1
4632
.037
14.7
0013
3.78
066
0.0.
038
42.7
244.
740
87.5
185.
739
41.3
80LI
QUID
42.3
38CH
OKE
15.8
710.
000
16.1
0431
.976
14.7
0013
3.78
067
0.0.
035
20.6
247.
137
67.7
185.
573
41.2
75LI
QUID
42.1
69CH
OKE
15.8
510.
000
16.0
6031
.911
14.7
0013
3.78
068
0.0.
031
99.2
249.
434
48.6
185.
395
41.1
63LI~ID
41.9
91CH
OKE
15.8
290.
000
16.0
1231
.841
14.7
0013
3.78
069
0.0.
028
78.6
251.
631
30.2
185.
204
41.0
43LI
ID41
.803
CHOK
E15
.805
0.00
015
.961
31.7
6614
.700
133.
780
700.
0.0
2558
.825
3.8
2812
.518
4.99
740
.914
LIQU
ID41
.603
CHOK
E15
.779
0.00
015
.907
31.6
8614
.700
133.
780
710.
0.0
2239
.825
5.9
2495
.718
4.77
240
.773
LIQU
ID41
.391
CHOK
E15
.751
0.00
015
.847
31.5
9814
.700
133.
780
720.
0.0
1921
.825
7.9
2179
.718
4.52
640
.619
LIQU
ID41
.162
CHOK
E15
.721
0.00
015
.782
31.5
0214
.700
133.
780
730.
0.0
1605
.025
9.7
1864
.718
4.25
240
.450
LIQU
ID40
.913
CHOK
E15
.687
0.00
015
.710
31.3
9714
.700
133.
780
740.
0.0
1289
.326
1.4
1550
.718
3.94
640
.260
LIQU
ID40
.640
CHOK
E15
.644
0.00
015
.625
31.2
6914
.700
133.
780
750.
0.0
975.
026
3.0
1238
.018
3.59
740
.045
LIQU
ID40
.335
CHOK
E15
.546
0.00
015
.480
31.0
2614
.700
133.
780
760.
0.0
663.
526
4.3
927.
818
3.19
339
.797
LIQU
ID39
.989
CHOK
E15
.436
0.00
015
.315
30.7
5114
.700
133.
780
770.
0.0
355.
026
5.3
620.
318
2.71
239
.503
LIQ-
vAP
39.5
03CH
OKE
15.1
510.
000
15.0
2330
.174
14.7
0013
3.78
0
TIM
E(S
EC) O. 60.
120.
180.
240.
300.
360.
420.
480.
540.
600.
660.
720.
TITL
E:EX
.2,
rASE
3.RE
LEAS
EF'R
!J1B"
BREA
CHIN
SIDE
Of14
-TCY
L(A
SHO
LEIN
END)
******
*C(}
I)ITH
NOF
'UF'6
INCO
NTAI
NMEN
T**
****
*PA
THoIA
YIN
LET
H.H~.H
COND
lTlON
OfUf
6EX~USTED
HH
HH
HFL
(}l
••••
••••
••MA
SS(L
B)***
******
*TE
MPPR
ESRE
LEAS
EPR
ESRA
TE***
*REL
EASE
RATE
(LBI
SEC)
****
TEMP
PRES
SOLI
DLI
QUID
VAPO
RTO
TAL
(DE6
f)(P
SIA)
PHAS
E(P
SIA)
BASI
SSO
LID
LIQU
IDVA
POR
TOTA
L(D
E6f)
(PSI
A)
0.0
2585
0.6
49.4
2590
0.0
190.
000
44.1
36LI
QUID
48.6B
7CH
OKE
16.3
960.
000
17.2
7533
.671
14.7
0013
3.78
00.
023
811.
168
.623
879.
718
9.79
143
.998
LIQU
ID48
.190
CHOK
E16
.371
0.00
017
.216
33.5
8714
.700
133.
780
0.0
2177
6.BB7
.621
864.
518
9.56
543
.B48
LIQU
ID47
.705
CHOK
E16
.343
0.00
017
.153
33.4
9614
.700
133.
780
0.0
1974
8.2
106.
519
854.
718
9.31
843
.686
LIQU
ID47
.221
CHOK
E16
.313
0.00
017
.084
33.3
9714
.700
133.
780
0.0
1772
5.B
125.
117
850.
918
9.04
743
.508
LIQU
ID46
.729
CHOK
E16
.280
0.00
017
.008
33.2
8814
.700
133.
780
0.0
1571
0.1
143.
515
853.
618
8.74
543
.310
LIQU
ID46
.223
CHOK
E16
.243
0.00
016
.924
33.1
6714
.700
133.
780
0.0
1370
2.0
161.
613
863.
618
8.40
643
.089
LIQU
ID45
.694
CHOK
E16
.201
0.00
016
.830
33.0
3114
.700
133.
780
0.0
1170
2.4
179.
311
881.
818
8.01
742
.836
LIQU
ID45
.133
CHOK
E16
.153
0.00
016
.723
32.8
7614
.700
133.
780
0.0
9712
.619
6.6
9909
.218
7.56
142
.542
LIQU
ID44
.524
CHOK
E16
.097
0.00
016
.59B
32.6
9514
.700
133.7
BO0.
077
34.2
213.
379
47.5
187.
010
42.1
88LI
QUID
43.8
47CH
OKE
16.0
290.
000
16.4
4832
.476
14.7
0013
3.78
00.
057
69.8
229.
25~99.0
lB6.
314
41.7
44LI
QUID
43.0
64CH
OKE
15.9
430.
000
16.2
5932
.201
14.7
0013
3.7BO
0.0
3823
.124
3.7
4Q66
.918
5.36
241
.142
LIQU
ID42
.097
CHOK
E15
.825
0.00
016
.004
31.8
2814
.700
133.
780
0.0
1901
.425
5.8
2157
.218
3.84
940
.200
LIQU
ID40
.738
CHOK
E15
.636
0.00
015
.604
31.2
4014
.700
133.
780
.... ~
TITL
E:EX
.3,
CASE
1.14
-TON
CYL
WI
RUPT
URED
PIGT
AIL
(6IN
)
TIM
E(S
EC) O. 30.
60.
90.
120.
150.
180.
210.
240.
270.
300.
330.
360.
390.
420.
450.
480.
510.
540.
570.
600.
630.
660.
690.
720.
750.
780.
810.
840.
870.
******
*CON
DITIO
Nor
Uf6
INCO
NTAI
NMEN
T***
****
PATH
4AY
INlE
T
AAAA
AAAA
AAMA
SS(L
B)***
******
*TE
MPPR
ESRE
LEAS
EPR
ESSO
LID
LIQU
IDVA
POR
TOTA
L(D
EGf)
(PSI
A)PH
ASE
(PSI
A)
0.0
2594
8.1
51.9
2600
0.0
200.
000
51.1
52VA
POR
51.1
520.
025
883.
852
.425
936.
219
9.36
850
.685
VAPO
R50
.685
0.0
2582
0.1
52.9
2587
3.0
198.
740
50.2
24VA
POR
50.2
240.
025
757.
053
.325
810.
319
8.11
549
.769
VAPO
R49
.769
0.0
2569
4.4
53.7
2574
8.1
197.
493
49.3
19VA
POR
49.3
190.
025
632.
354
.225
686.
519
6.87
448
.874
VAPO
R48
.874
0.0
2557
0.8
54.6
2562
5.4
196.
259
48.4
35VA
POR
48.4
350.
025
509.
854
.925
564.
819
5.64
748
.001
VAPO
R48
.001
0.0
2544
9.4
55.3
2550
4.7
195.
039
47.5
73VA
POR
47.5
730.
025
389.
655
.625
445.
219
4.43
447
.150
VAPO
R47
.150
0.0
2533
0.3
56.0
2538
6.2
193.
833
46.7
33VA
POR
46.7
330.
025
271.
456
.325
327.
719
3.23
446
.320
VAPO
R46
.320
0.0
2521
3.1
56.6
2526
9.7
192.
639
45.9
12VA
POR
45.9
120.
025
155.
256
.925
212.
119
2.04
745
.509
VAPO
R45
.509
0.0
2509
7.9
57.2
2515
5.0
191.
458
45.1
10VA
POR
45.1
100.
025
041.
057
.525
098.
419
0.87
144
.716
VAPO
R44
.716
0.0
2498
4.6
57.7
2504
2.3
190.
288
44.3
27VA
POR
44.3
270.
024
928.
658
.024
986.
618
9.70
843
.943
VAPO
R43
.943
0.0
2487
3.3
58.2
2493
1.5
189.
133
43.5
64VA
POR
43.5
640.
024
818.
458
.424
876.
818
8.56
043
.189
VAPO
R43
.189
0.0
2476
3.9
58.6
2482
2.6
187.
990
42.8
19VA
POR
42.8
190.
024
710.
058
.824
768.
818
7.42
342
.453
VAPO
R42
.453
0.0
2465
6.5
59.0
2471
5.5
186.
860
42.0
92VA
POR
42.0
920.
024
603.
559
.224
662.
718
6.30
041
.735
VAPO
R41
.735
0.0
2455
0.9
59.4
2461
0.2
185.
742
41.3
82VA
POR
41.3
820.
024
498.
659
.524
558.
218
5.18
741
.033
VAPO
R41
.033
0.0
2444
6.9
59.7
2450
6.6
184.
636
40.6
88VA
POR
40.6
880.
024
395.
759
.824
455.
518
4.08
840
.348
VAPO
R40
.348
0.0
2434
4.9
60.0
2440
4.8
183.
543
40.0
12VA
POR
40.0
120.
024
294.
560
.124
354.
518
3.00
139
.679
VAPO
R39
.679
fllJ
.lRA
TEBA
SIS
CHOK
ECH
OKE
CHOK
ECH
OKE
CHOK
ECH
OKE
CHOK
EPD
C poe
PDC poe
PDC poe
PDC
PDC
PDC
PDC
PDC
PDC
PDC
poe
poe
poe
PDC
PDC
PDC
PDC
PDC poe
PDC
******
***CO
NDITI
ONor
ur6
EXHA
USTE
D***
******
****
*REL
EASE
RATE
(LBI
SEC)
****
TEMP
PRES
SOLI
DLI
QUID
VAPO
RTO
TAL
(DEG
f)(P
SIA)
0.00
00.
000
2.12
62.
126
14.7
0019
8.78
40.
000
0.00
02.
108
2.10
814
.700
198.
165
0.00
00.
000
2.09
02.
090
14.7
0019
7.54
90.
000
0.00
02.
072
2.07
214
.700
196.
936
0.00
00.
000
2.05
52.
055
14.7
0019
6.32
60.
000
0.00
02.
037
2.03
714
.700
195.
720
0.00
00.
000
2.02
02.
020
14.7
0019
5.11
70.
000
0.00
02.
002
2.00
214
.700
194.
517
0.00
00.
000
1.98
31.
983
14.7
0019
3.92
00.
000
0.00
01.
966
1.96
614
.700
193.
327
0.00
00.
000
1.95
11.
951
14.7
0019
2.73
70.
000
0.00
01.
934
1.93
414
.700
192.
150
0.00
00.
000
1.91
81.
918
14.7
0019
1.56
60.
000
0.00
01.
903
1.90
314
.700
190.
986
0.00
00.
000
1.88
71.
887
14.7
0019
0.40
80.
000
0.00
01.
872
1.87
214
.700
189.
832
0.00
00.
000
1.85
61.
856
14.7
0018
9.26
00.
000
0.00
01.
838
1.83
814
.700
188.
691
0.00
00.
000
1.82
31.
823
14.7
0018
8.12
60.
000
0.00
01.
808
1.80
814
.700
187.
564
0.00
00.
000
1.79
11.
791
14.7
0018
7.00
50.
000
0.00
01.
777
1.77
714
.700
186.
449
0.00
00.
000
1.76
21.
762
14.7
0018
5.89
60.
000
0.00
01.
748
1.74
814
.700
185.
346
0.00
00.
000
1.73
51.
735
14.7
0018
4.79
90.
000
0.00
01.
720
1.72
014
.700
184.
254
0.00
00.
000
1.70
31.
703
14.7
0018
3.71
30.
000
0.00
01.
689
1.68
914
.700
183.
175
0.00
00.
000
1.67
61.
676
14.7
0018
2.64
00.
000
0.00
01.
662
1.66
214
.700
182.
108
.... ~
TITL
E:EX
.3,
CASE
2.14-T£t~
CYL
WI
RUPT
URED
PIGT
AIL
(2FT
)
******
*C(N
)ITIlJ
IlOF
UF6
INCl
JIlTA
IfIKN
T***
****
PAT~Y
INlE
T**
****
***
C(N)
ITIlJ
IlOF
UF6
EXHA
USTE
D**
****
****
FL~
TIME
****
****
**MA
SS(L
B)**
****
****
TEMP
PRES
RELE
ASE
PRES
RATE
****
RELE
ASE
RATE
(LBI
SEC)
****
TEMP
PRES
(SEC
)SO
LID
LIQU
IDVA
POR
TOTA
L(D
EGF)
(PSI
A)PH
ASE
(PSI
A)BA
SIS
SOLI
DLI
QUID
VAPO
RTO
TAL
(DEG
F)(P
SIA)
O.0.
025
948.
151
.926
000.
020
0.00
051
.152
VAPO
R51
.152
POC
0.00
00.
000
1.91
41.
914
14.7
0019
8.78
430
.0.
025
890.
252
.425
942.
619
9.43
150
.732
VAPO
R50
.732
PDe
0.00
00.
000
1.89
91.
899
14.7
0019
8.22
760
.0.
025
832.
952
.825
885.
619
8.86
650
.317
VAPO
R50
.317
PDC
0.00
00.
000
1.88
41.
884
14.7
0019
7.67
390
.0.
025
775.
953
.225
829.
119
8.30
349
.906
VAPO
R49
.906
PDe
0.00
00.
000
1.87
01.
870
14.7
0019
7.12
112
0.0.
025
719.
553
.625
773.
019
7.74
249
.499
VAPO
R49
.499
PDC
0.00
00.
000
1.85
51.
855
14.7
0019
6.57
115
0.0.
025
663.
453
.925
717.
419
7.18
549
.097
VAPO
R49
.097
PDe
0.00
00.
000
1.84
11.
841
14.7
0019
6.02
418
0.0.
025
607.
854
.325
662.
119
6.63
048
.699
VAPO
R48
.699
PDC
0.00
00.
000
1.82
61.
826
14.7
0019
5.48
021
0.0.
025
552.
754
.725
607.
419
6.07
848
.307
VAPO
R48
.307
PDe
0.00
00.
000
1.81
11.
811
14.7
0019
4.93
924
0.0.
025
498.
055
.025
553.
019
5.52
947
.918
VAPO
R47
.918
PDC
0.00
00.
000
1.79
81.
798
14.7
0019
4.40
127
0.0.
025
443.
855
.325
499.
119
4.98
247
.533
VAPO
R47
.533
PDe
0.00
00.
000
1.78
41.
784
14.7
0019
3.86
530
0.0.
025
389.
955
.625
445.
619
4.43
847
.153
VAPO
R47
.153
PDt
0.00
00.
000
1.77
01.
770
14.7
0019
3.33
133
0.0.
025
336.
556
.025
392.
519
3.89
746
.777
VAPO
R46
.777
PDe
0.00
00.
000
1.75
71.
757
14.7
0019
2.80
036
0.0.
025
283.
556
.225
339.
819
3.35
846
.405
VAPO
R46
.405
PDt
0.00
00.
000
1.74
31.
743
14.7
0019
2.27
239
0.0.
025
231.
056
.525
287.
519
2.82
246
.037
VAPO
R46
.037
PDe
0.00
00.
000
1.72
91.
729
14.7
0019
1.74
642
0.0.
025
178.
856
.825
235.
619
2.28
945
.673
VAPO
R45
.673
PDt
0.00
00.
000
1.71
61.
716
14.7
0019
1.22
345
0.0.
025
127.
157
.125
184.
119
1.75
945
.313
VAPO
R45
.313
PDe
0.00
00.
000
1.70
21.
702
14.7
0019
0.70
348
0.0.
025
075.
857
.325
133.
119
1.23
144
.958
VAPO
R44
.958
POC
0.00
00.
000
1.68
91.
689
14.7
0019
0.18
5I-
"0
')
510.
0.0
2502
4.8
57.5
2508
2.4
190.
706
44.6
06VA
POR
44.6
06PD
e0.
000
0.00
01.
676
1.67
614
.700
189.
670
-:J
540.
0.0
2497
4.3
57.8
2503
2.1
190.
183
44.2
58VA
POR
44.2
58PD
C0.
000
0.00
01.
664
1.66
414
.700
189.
157
570.
0.0
2492
4.2
58.0
2498
2.2
189.
663
43.9
13VA
POR
43.9
13PD
e0.
000
0.00
01.
650
1.65
014
.700
188.
647
600.
0.0
2487
4.5
58.2
2493
2.7
189.
146
43.5
73VA
POR
43.5
73PO
C0.
000
0.00
01.
638
1.63
814
.700
188.
140
630.
0.0
2482
5.1
58.4
2488
3.5
188.
631
43.2
36VA
POR
43.2
36PD
e0.
000
0.00
01.
625
1.62
514
.700
187.
635
660.
0.0
2477
6.2
58.6
2483
4.8
188.
119
42.9
03VA
POR
42.9
03PD
t0.
000
0.00
01.
614
1.61
414
.700
187.
132
690.
0.0
2472
7.6
58.8
2478
6.4
187.
610
42.5
73VA
POR
42.5
73PD
e0.
000
0.00
01.
600
1.60
014
.700
186.
632
720.
0.0
2467
9.4
58.9
2473
8.4
187.
103
42.2
47VA
POR
42.2
47PD
t0.
000
0.00
01.
588
1.58
814
.700
186.
135
750.
0.0
2463
1.6
59.1
2469
0.7
186.
599
41.9
25VA
POR
41.9
25PD
e0.
000
0.00
01.
576
1.57
614
.700
185.
640
780.
0.0
2458
4.2
59.3
2464
3.4
186.
097
41.6
06VA
POR
41.6
06PD
e0.
000
0.00
01.
565
1.56
514
.700
185.
147
810.
0.0
2453
7.1
59.4
2459
6.5
185.
597
41.2
90VA
POR
41.2
90PD
e0.
000
0.00
01.
553
1.55
314
.700
184.
657
840.
0.0
2449
0.3
59.6
2454
9.9
185.
100
40.9
78VA
POR
40.9
78PD
t0.
000
0.00
01.
540
1.54
014
.700
184.
169
870.
0.0
2444
4.0
59.7
2450
3.7
184.
606
40.6
70VA
POR
40.6
70PD
e0.
000
0.00
01.
529
1.52
914
.700
183.
684
TITL
E:EX
.3,
CASE
3.14-Ttt~
CYL
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180.
210.
240.
270.
300.
330.
360.
390.
420.
450.
480.
510.
540.
570.
600.
630.
660.
690.
720.
750.
780.
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****
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****
****
TEMP
PRES
RELE
ASE
PRES
SOLI
DLI
QUID
VAPO
RTO
TAL
(DEG
F)(P
SIA)
PHAS
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0.0
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025
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152
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0.0
2584
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52.7
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790.
253
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843.
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686.
953
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740.
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288.
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345.
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420.
025
098.
457
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357
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881.
418
8.61
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858
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792.
518
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542
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VAPO
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9.7
58.9
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8.6
187.
211
42.3
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POR
42.3
170.
024
645.
959
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704.
918
6.75
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VAPO
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0.0
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59.2
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291
41.7
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359
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618.
618
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SOLI
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1.70
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1.67
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RATE
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TITL
E:EX
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CASE
1.RE
LEAS
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X.2.
2),
FORC
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ORNE
SOLI
DS
DATA
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RATE
DBY
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TEMP
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tOO
TIME
(SEC
)
0.0
120.
024
0.0
360.
048
0.0
600.
072
0.0
840.
096
0.0
1080
.012
00.0
1320
.014
40.0
1560
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80.0
1800
.019
20.0
2040
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60.0
2280
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00.0
2520
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40.0
2760
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80.0
3000
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20.0
3240
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60.0
3480
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00.0
TITL
E:EX
.5.
REPE
ATOF
EX.
4.1
WI
RELE
ASE
(EX.
2)SE
IJ1EN
TED
DATA
GENE
RATE
DBY
FODR
F1--
AFO
RCED
DRAF
lVE
NTIL
ATle
NSY
STEM
Tm.lS
IEN
TCC
tlPAR
THEN
THO
DEL.
CeNO
ENSA
TEAC
CLtlU
LATE
OeN
FLOO
R
TIME
(SEC
)
0.0
120.
024
0.0
360.
048
0.0
6/10.0
720.
084
0.0
%0.
010
80.0
1200
.013
20.0
1440
.015
60.0
1680
.018
00.0
1920
.020
40.0
2160
.022
80.0
2400
.025
20.0
2640
.027
60.0
2880
.030
00.0
3120
.032
40.0
3360
.034
80.0
3600
.0
AIR
V
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CCtlP
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TMA
SS(L
B)HF
LHF
VUF
6S
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U02F
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1.46
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24.
629£
+02
7.74
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21.0
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031.
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1.66
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32.5
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2.96
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33.
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3.116
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3.12
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33.
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3.14
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33.
143£
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3.14
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33.
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033.
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~ t>:l
TITL
E:EX
.5.
REPE
ATOF
EX.
4.1
WI
RELE
ASE
(EX.
2)SE
9'lEN
TED
DATA
GENE
RATE
DBY
FODR
FT--
AFO
RCED
DRAF
TVOOILATI~
SYST
EMT~SIENT
C(IoI
PART
MENT
MOD
El.
U~lltI
AND
HFRE
LEAS
ES~RY
AND
C(tIfl
ARTM
ENTC~CENTRATI~S
TIM
E(S
EC)
0.0
120.
024
0.0
360.
048
0.0
600.
072
0.0
840.
0%
0.0
1080
.012
00.0
1320
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40.0
1560
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80.0
1800
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20.0
2040
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60.0
2280
.024
00.0
2520
.026
40.0
2760
.028
80.0
3000
.031
20.0
3240
.033
60.0
3480
.036
00.0
CltIU
LATI
VEHA
TERI
ALRE
LEAS
EDOR
FORM
EDFR
(IoI
RELE
ASED
HATE
RIAL
(LB)
UF6
U02F
2TO
TAL
UHF
HFFR
(IoI
UF6
TOTA
LHF
O.OOO
E+OO
O.OOO
E+OO
O.OOO
E+OO
O.OOO
E+OO
O.OOO
E+OO
O.OOO
E+OO
O.OOO
E+OO
6.384
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4.933
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1.70
9E+0
2O.O
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OO1.
709E
+02
1.913
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1.832
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1.545
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5.04
1E+0
24.
350E
+Ol
5.47
6E+0
21.0
39E+
032.9
31E+
032.9
68E+
038.2
96E+
022.3
63E+
021.
066E
+03
2.379
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3.999
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4.699
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1.15
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35.4
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021.
700E
+03
4.053
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5.045
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6.639
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1.49
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39.2
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022.4
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035.9
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038.7
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031.
822E
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1.35
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33.
181E
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7.887
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7.115
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1.083
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2.161
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1.79
3E+0
33.9
54E+
038.8
92E+
038.1
53E+
031.2
31E+
042.5
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032.0
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034.5
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039.1
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69E+
031.3
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042.8
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2.078
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5.16
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39.1
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63E+
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78E+
035.
342E
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9.142
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1.065
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1.441
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3.394
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2.07
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35.
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9.142
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1.086
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1.457
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3.490
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2.078
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5.56
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39.1
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559E
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035.
687E
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9.142
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1.113
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1.479
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3.645
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5.72
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39.1
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9.142
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1.120
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1.483
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3.690
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2.078
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5.769
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9.142
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1.121
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1.485
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3.704
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2.078
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5.78
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39.1
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031.1
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041.4
86E+
043.7
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032.0
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035.7
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799£
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9.142
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1.123
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1.486
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3.726
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9.142
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1.124
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1.487
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3.73O
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2.078
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5.80
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39.1
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043.7
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032.0
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035.
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9.142
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1.124
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1.48
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43.7
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2.078
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1.124
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1.487
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3.738
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2.078
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5.817
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9.142
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1.124
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1.487
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3.73
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32.0
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817E
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CCtlP
ARTM
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CH
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RAT
I~S
(LB
lFT*
*3)
~lltI
HF
O.OOO
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O.OOO
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4.23
1E-0
31.
489E
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7.06
3E-0
31.
854E
-03
9.12
3E-0
31.
871E
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1.05
3E-0
21.
881E
-03
1.15
0E-0
21.
887E
-03
1.23
3E-0
21.
891E
-03
9.93
6E-0
31.
881E
-03
6.53
6E-0
31.
868E
-03
4.19
5E-0
31.
807E
-03
2.76
2E-0
31.
314E
-03
1.81
4E-0
39.
529E
-04
1.19
0E-0
36.
903E
-04
7.79
7E-0
44.
995E
-04
5.10
6E-0
43.
612E
-04
3.34
2E-0
42.
611E
-04
2.18
7E-0
41.
887E
-04
1.43
1E-0
41.
364E
-04
9.36
0E-0
59.
852E
-05
6.12
2E-0
57.
118E
-05
4.00
5E-0
55.
142E
-05
2.61
9E-0
53.
714E
-05
1.71
3E-0
52.
683E
-05
1.12
1E-0
51.
938E
-05
7.32
9E-0
61.
400E
-05
4.79
4E-0
61.
011E
-05
3.13
5E-0
67.
305E
-06
2.05
1E-0
65.
276E
-06
1.34
1E-0
63.
811E
-06
8.77
2E-0
72.
753E
-06
5.73
7E-0
71.
989E
-06
~ C.:l