NUREG/IA-0068

ICSP-CO-TURFW-T

International

Agreement Report

Assessment of the "One Feedwater

Pump Trip Transient" in

Cofrentes Nuclear Power Plant

With TRAC-BF1

Prepared by

F. Castrillo, Hidroelectrica Espanola

A. G. Navarro, I. Gallego, Union Iberoamericana De Tecnologia

Hidroelectrica Espanola

Hermosilla, 3

28001-Madrid

Spain

Office of Nuclear Regulatory Research

U.S. Nuclear Regulatory Commission

Washington, DC 20555

April 1992

Prepared as part of

The Agreement on Research Participation and Technical Exchange

under the International Thermal-Hydraulic Code Assessment

and Application Program (ICAP)

Published by

U.S. Nuclear Regulatory Commission
NOTICE

This report was prepared under an international cooperative

agreement for the exchange of technical information. Neither

the United States Government nor any agency thereof, or any of

their employees, makes any warranty, expressed or implied, or

assumes any legal liability or responsibility for any third party's

use, or the results of such use, of any information, apparatus product or process disclosed in this report, or represents that its use

by such third party Would not infringe privately owned rights.

Available from

Superintendent of Documents

U.S. Government Printing Office

P.O. Box 37082

Washington, D.C. 20013-7082

and

National Technical Information Service

Springfield, VA 22161
NUREG/IA-0068

ICSP-CO-TURFW-T

International

Agreement Report

Assessment of the "One Feedwater

Pump Trip Transient" in

Cofrentes Nuclear Power Plant

With TRAC-BF1

Prepared by

F. Castrillo, Hidroelectrica Espanola

A. G. Navarro, I. Gallego, Union Iberoamericana De Tecnologia

Hidroelectrica Espanola

Hermosilla, 3

28001-Madrid

Spain

Office of Nuclear Regulatory Research

U.S. Nuclear Regulatory Commission

Washington, DC 20555

April 1992

Prepared as part of

The Agreement on Research Participation and Technical Exchange

under the International Thermal-Hydraulic Code Assessment

and Application Program (ICAP)

Published by

U.S. Nuclear Regulatory Commission
NOTICE

This report documents work performed under the sponsorship of the Consejo De

Seguridad Nuclear of Spain. The information in this report has been provided

to the USNRC under the terms of an information exchange agreement between the

United States and Spain (Technical Exchange and Cooperation Agreement Between

the United States Nuclear Regulatory Commission and the Consejo De Seguridad

Nuclear of Spain in the field of reactor safety research and development,

November 1985). Spain has consented to the publication of this report as a

USNRC document in order that it may receive the widest possible circulation

among the reactor safety community. Neither the United States Government nor

Spain or any agency thereof, or any of their employees, makes any warranty,

expressed or implied, or assumes any legal liability of responsibility for

any third party's use, or the results of such use, or any information,

apparatus, product or process disclosed in this report, or represents that

its use by such third party would not infringe privately owned rights.
FOREWORD

This report has been prepared by Hidroelectrica E spafiola in the framework of the ICAP-UNESA Project.

The report represents one of the assessment calculations submitted

in fulfilment of the bilateral agreement for cooperation in thermalhydraulic activities between the Consejo de Seguridad Nuclear of

Spain (CSN) and the United States Nuclear Regulatory Comission

(NRC), in the form of Spanish contribution to the International Code

Assessment and Applications Program (ICAP) of the US-NRC, whose main

purpose is the validation of the TRAC and RELAP system codes.

The Consejo de Seguridad Nuclear has promoted a coordinated Spanish

Nuclear Industry effort (ICAP-SPAIN) aiming to satisfy the requirements of this agreement and to improve the quality of the technical

support groups at the Spanish Utilities, Spanish Research Establishments, Regulatory Staff and Engineering Companies, for Safety

purposes.

This ICAP-SPAIN national program includes agreements between CSN and

each of the following organizations:

- Unidad Elctrica (UNESA)

- Union Iberoamericana de Tecnologia Elctrica (UITESA)

- Empresa Nacional del Uranio (ENUSA)

- TECNATOM

- LOFT-ESPANA

The program is executed by 12 working groups and a generic code

review group, and is coordinated by the "Comit6 de Coordinacion".

This comitee has aroved the distribution of this document for ICAP

purposes.

iii

TABLE OF CONTENTS

Page

Foreword iii

List of Figures/Tables vi

Executive Summary vii

1. INTRODUCTION 1-1

2. PLANT DESCRIPTION 2-1

3. TEST DESCRIPTION 3-1

4. CODE INPUT MODEL DESCRIPTION 4-1

4.1. Vessel 4-1

4.2. Recirculation system 4-2

4.3. Main Steam Lines 4-3

4.4. Fuel elements 4-4

4.5. Core power and Reactivity Feedback 4-4

4.6. Control systems and trips 4-4

5. STEADY STATE 5-1

6. TRANSIENT RESULTS AND COMPARISON WITH PLANT MEASUREMENTS 6-1

7. RUN STATISTICS 7-1

8. CONCLUSIONS 8-1

APPENDIX I: TRAC major edit for the Reference Steady State

at Nominal conditions: 100% core power/100% core flow I-I

V
FIGURES

Page

3.1.- Measured vessel level 3-2

3.2.- Measured FW flow 3-3

3.3.- Measured steam flow 3-4

3.4.- Measured Recirculation flow 3-5

3.5.- Measured Core flow 3-6

3.6.- Measured power (APRM) 3-7

3.7.- Measured Dome pressure 3-8

4.1.- C.N. Cofrentes model for TRAC-BF1 4-7

4.2.- Core channels distribution 4-8

4.3.- Pressure control system 4-9

4.4.- Feedwater control system 4-10

4.5.- Recirculation control system 4-11

6.1.- Sensed water level 6-4

6.2.- Total feedwater flow 6-5

6.3.- Steam flow 6-6

6.4.- Recirculation flow (1 loop) 6-7

6.5.- Core flow 6-8

6.6.- Core Power 6-9

6.7.- Dome pressure 6-10

7.1.- CPU time vs. transient time 7-2

7.2.- Time step size vs. transient time 7-3

TABLES

5.1.- Reference Steady State condition. 5-2

vi
EXECUTIVE SUMMARY.-

This report presents the results of the assessment of TRAC-BF1 (G1-J1) code with the model of C.N. Cofrentes for

simulation of the transient originated by the manual trip of one FW

pump

C.N. Cofrentes is a General Electric designed BWR/6 plant, with a

nominal core thermal power of 2894 Mwt, in commertial operation

since 1985, owned and operated by Hidroelectrica Espahola S.A. The

plant incorporates all the characteristics of BWR/6 reactors, with

two turbine driven FW pumps

The objective of this assessment is to generate a Cofrentes model

for TRAC-BF1 and compare code results with plant recorded data

during the start-up test transient of "one feedwater pump trip" with

the plant at nominal conditions.

The model has been developped from plant drawings and documentation,

and a documented and validated RETRAN model.

Principal characteristics of the model include a 4 rings-8 levels

vessel, two recirculation loops and one representative steam line;

control systems and trips were also modelled.

A reference/nominal steady state situation was then adjusted by

connecting submodels of portions of the system (vessel,

recirculation loops, steam lines) previously tuned to the desired

conditions. In the same way separated models for each of the

control systems (feedwater/level, recirculation, pressure) were

developped.

The point kinetic option was selected for core neutronic feedback,

as considered adequate enough for this kind of mild operational

transients. Reactivity coefficients were obtained from

perturbations on the 3D simulator, around the initial steady state

situation.

vii
The transient selected to be reproduced with TRAC-BF1 was the "ONE

FW PUMP TRIP" start-up test, performed to verify the capability of

the plant to avoid reactor trip by reducing power to a level

consistent with the capacity of the remaining operating pump.

Simulation of this operational transient with TRAC-BF1 will asses

the performance of the code/model features related to dynamic level

tracking, core neutronic feedback, recirculation and jet pumps

performance in normal operating conditions, and check models

generated for the control systems

A 150 seconds transient was run, this time including all the

important phenomena occurring in the system.

Sensed level was the most critical plant variable to reproduce.

Consideration of the water level shift between regions inside and

outside the dryer skirt, due to pressure drop across the dryer, led

to a good simulation of level behaviour as sensed in the plant.

Other variables measured: FW, steam, recirculation and core flow, as

well as power and pressure were, accurately reproduced by the code.

Some additional tuning of FW control system settings and steam lines

model would probably improve results for those variables that, in

the second portion of the transient, behave slightly different to

measurements (FW flow and dome pressure)

As a conclusion of this assessment a model of C.N. Cofrentes has

been developped for TRAC-BF1 that fairly reproduces operational

transient behaviour of the plant. A special purpose code was

generated to obtain reactivity coefficients, as required by

TRAC-BF1, from the 3D simulator. A complete validation of this

model will require additional assessment with measurements from

other transients that activates other portions and features of the

code/model.

viii
1.- INTRODUCTION

Hidroelectrica Espafiola (HE) joined ICAP as a member of the UNESA

group in order to simulate two transients of C.N.Cofrentes with

TRAC-BF1 code and compare simulation results with data recorded at

the plant.

The code information package, including tape with source program of

GIJ1 version, was received and implemented on a SIEMENS 7590-F

computer. Some adaptation was needed on the source received (CDC

version) to make it compilable; test cases were run, with results

slightly different to those provided as reference in some of them.

Later, on August 1989, the IBM version, as converted by Pennsylvania

State University, was released to HE representatives by INEL.

Implementation of this version is currently in progress.

Due to the above mentioned problems, the model and cases described

in this report were developed using the TRAC-BF1 GIJI version

implemented in a CONVEX computer owned by UITESA. This version has

been vectorized , achieving a reduction in the CPU time consumption

of about 70%. The graphics option has been implemented for this

computer and an interactive graphic system has been developped as a

user friendly tool to plot output data

1-1

2.- PLANT DESCRIPTION

Cofrentes Nuclear Power Plant, ownwed and operated by Hidroelectrica

Espahola S.A., has a BWR/6 reactor (Mark III containment), designed

by General Electric, with a rated thermal power of 2894 Mwt.

Located 50 Km from Valencia (Spain), Cofrentes comercial operation

started in 1985 and is presently running its fith cycle.

Design features of the Nuclear Supply Steam System (NSSS) include

two loop recirculation system, driven by two centrifugal pumps,

feeding a total of 20 jet pumps, with a flow control valve in each

loop. Feed-water is supplied by two turbine-driven pumps. Four

main steam lines supply the main turbine with the steam generated in

the reactor, each line equipped with isolation valves (MSIV),

safety/relief valves (SRV) and turbine stop and control valves (TSV

and TCV). Six bypass valves blowdown steam to the condenser from a

common header connected to the four steam lines, with a nominal

capacity of 35% rated steam flow.

The core consists of 624 fuel elements (Mx8) with an active length

of 150 in. and 145 control rods. Core power is monitored by 33

vertical strings, each holding 4 Local Power Range Monitors (LPRM),

arranged in a uniform pattern throughout the core. Four Average

Power Range Monitors (APRM) measure bulk power, each one averaging

24 LPRM signals.

NSSS instrumentation of interest for the transients analized in this

report and related to the Control systems and Reactor Protection

System (RPS) are briefly described: Op transducers are used to

measure flow in the recirculation, steam and feedwater lines; water

level in the vessel downcomer is also measured by a Dp transducer,

pressure signals are avaliable from sensors located in the steam

dome and in the averaging manifold in steam lines at the entrance of

TSV's

2-1
During start-up tests a special program for collecting plant signals

was carried out. Prior to each significant transient test, a set of

signals considered relevant for later analysis and simulation of the

transient was defined. The Emergency Response and Information

System (ERIS) was used as Data Adquisition System for sampling and

recording selected signals.

2-2
3.- TEST DESCRIPTION.-

This transient, identified as Start-up test PPN-23C, was carried out

on February 1985 with the plant operating at 95% thermal power and

94% core flow

The transient was initiated by manual trip of one feed-water pump,

and the objective of the test was to verify the capability of the

plant to avoid scram on low water level.

When one feed-water pump is tripped, water level starts decreasing

and feed-water controller speeds-up the other pump to restore

downcommer inventory; however, design capacity of one pump allows a

maximum flow of 85 % of rated, consequently level will keep on

dropping and eventually would reach low level (U3) setpoint, in

about 15 seconds, and reactor will be scrammed if no action is

taken. Cofrentes incorporates an automatic action that lowers power

to a level consistent with the capacity of the remaining feed-water

pump, this is acomplished by reducing core flow to a new steady

state along the original control rod line in the operating, map.

When level passes through the low water level alarm (L4), after a

single feed-water pump trip, a "Recirculation Runback" is commanded

to move both Recirculation flow control valves to a pre-stablished

position. This originates a fast core flow reduction that means an

increase of voids in the core and a subsequent power decrease. A

new steady state is reached 50 seconds after initiation of the

transient.

Figures 3.1 to 3.7 present plots of measured variables for the 150

seconds of interest, including 10 seconds previous to the initiation

of the transient.

3-1
1.05

1

0.95

0.9

0.85

LEVEL (in)

0.8

0.75

0.7

0.65

0.6

..........

..........

°

FIGURE 3.1.- MEASURED VESSEL LEVEL

...................... ............... ......................

. . . . . .. . . . . . ... . . . . . . .... . . . . . . ... . . . .

* * * * o * * K * *o * o * * *o

........ * * * p .

o * * * * o * i i

C * *IIIJ

* *ltnIF

* .111v1

..... ... ........... ................

. . . . . . ,. . . . . ; . . . . . . . ,.. . . . . .. . . . . . . . . . . .• .., -.. .i. .. . . .-'.. r V .,.. ; I ./. .

................ . ....... .........

..... .. .. .. .. ........................ . . . . . . . . . . . . .. .. . .. . . . . * * * ** * B p* *

* ' * ... . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .

* p B Bp p * *B p

0 10 20 30 40 50 60 70 80 90 100 110

TIEMPO (s)

F-ERISA -- ERISB

120 130 140 150
FIGURE 3.2.- MEASURED F.W. FILOW

1550 . . ............................................. .......

1 . 4 . 0 . . . . . . . . . . . •.. . . . . . . . .. . . . . . .... . .

1 - 3 - 5 - - - - - . . . . . . . . . . . . . o - - - . . . . . . . . . .

* * 4 4 *i .4

1300 . . . . . ................................ ..... ....... ......... .........

14500

1200 .. . . . . . . . ... . . .. . .. . . . .. .. . . .*. . . ... . . ... . ..- - - --. .. . . . . . .... . . . . . . ..--- 

1150 .. ....... .................. .. .. . .. . .. . .. . .. . .. . .. . .. . .. .

1400

1350 ......

13006 0 0 1014 6

TIEMPO (s)
(a

1600

1550

1500

1450

1400

Kg/s 1350

1300

1250

1200

1150

1100

. . . . . . . . ... . . .

. . . . . . . . . . . . .

. . . . . . . . . . . . .

°

. .. .. .. ....

FIGURE 3.3.- MEASURED STEAM FLOW

....... : ..................... ..... ....i .........i .........i .........

..... ..... ..... ......... ........ ...........

. .,.......... . o.......... ,.......... -. . . . ... I .• .......... ......... ... ... ........ .-

. a a a . a. .

. a . . . .

* a a a a a

o a a a a a a

* a a a

* a a a a

* a a a o * a a a a

. . . * . . . . . . . . . . oa . . . . . oa.. . . . . . . . . . . . .a.

*

i a

a a a a a

a a a . ai

0 20 40 60 80 100 120 140

TIME (s)

-1i

160
FIGURE 3.4.- MEASURED RECIRCUI.ATION FLOW

1500

Q 8 ̧

'.

Kg/s

iquu ------

1300 ----- ,

1200

1100 -

1000

900 ....-

o

. . . . . . . . . .

. . . . . . . . . .

a a a a a a a a a a a a a a a a a a a a a a a a

800

0 10 20 30 40 50 60 70 80 90 100 110

TIME (s)

120 130 140 150
FIGURE 3.5.- MEASURED CORE FLOW/2

t.

5200

5000

4800

4600

4400

Kg/s 4200

4000

3800

3600

3400

3200

- *,* -

. . . .

. . . . . . .

. . . . . . . . . .. . .. . .. . ... . . . . . . . . .

. . . . . . . . . .

. . . . . . . . . .

. . . . . . . . . .

. . . . . . . . . .

.. ... .. . . . . . .

. * .

. .... ........ . .. .... . . J.

. . .

a | | |

9

0 20

I I I

40 60 80 100 120

TIME (s)

1

140

1

160
FIGURE 3.6 - MEASURED POWER (APIIM)

'.3

-J

3000000000

2800000000

2600000000

2400000000

2200000000

POT 2000000000

(w)

1800000000

1600000000

1400000000

1200000000

1000000000

........... ........... ........ ......... ....

S....... ........................................

. . . .. .. .. . . . . ..- .- . . . . . . . . . . . . . . . . ... . . . . .. .. . ...- - .. .- - .. -

#A &- j L

...........

........... .............

...........

0 20 40 60 80 100 120 140

TIME (s)

160
FIGUIng 3.7 - MEASURED DOME PIESSURE

I

6880000

6860000

6840000

6820000

6800000

6780600

Pa 6760000

6740000

6720000

6700000

6680000

6660000

6640000

. . . . . . . . . . . . .

.o ... 

.4

............

............

...............

...............

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

..............

...........

...........

...........

...........

...........

...........

I

0 20 40 60 80 100

TIME (s)

120 140 160
4.- MODEL DESCRIPTION.-

Figure 4.1 shows the Cofrentes model which includes reactor vessel

and core, recirculation loops, steam lines from vessel to turbine

valves, and control systems. Input data were mainly obtained from a

documented RETRAN model.

The main components of the model are discussed in the following

sections.

4.1.- VESSEL.-

Using the VESSEL component of TRAC-BF1, 4 rings and 8 axial levels

were considered to model the reactor vessel. The three inner rings

represent the volume inside the core shroud, with the core in levels

3 and 4, and the outer ring models the downcomer. As illustrated in

Figure 4.1. levels 1 and 2 represent the core inlet plenum, with jet

pumps discharge located in bottom of level 2 (ring 4); core exit

plenum is represented by level 5 (rings 1,2,3).

For the type of transient being analized, it would be enough one

single ring to model the core region, with one average bundle (CHAN

component) to represent the fuel elements. However, three rings

were considered to allow for future accident analysis (LOCA, ATWS),

in which upper plenum 2D/3D effects, when spray is activated, are

important to simulate the distribution of coolant over the fuel

bundles.

The 624 fuel elements have been divided into three groups:

high power

average power

low power (including peripheral elements)

connected to the lower and upper plenum in each core ring, as

illustrated in Figure 4.2.

4-1
No metal structures were modeled as the time of interest in the.

transients to be analized is relatively small (150 sec. maximum),

and temperature change in the vessel is not relevant

Separators and dryer are modelled in the axial level 6 using the

perfect Separator option, after some failed attempts to use the

mechanistic model; stand pipes are also included in this level.

Vessel connections to other components include feedwater inlet,

modelled as a fill, governed by the level control system,

discharging in the downcomer via a leak path (level 5, ring 4).

Steam outlet is located in level 7, ring 4. Outlets to

Recirculation loops from lower downcomer are located in level 2

(ring 4). Recirculation flow mixes in the jet pump (component

external to vessel) with driven flow from downcomer level 4, to

discharge into lower plenum.

Channel components representing fuel bundles are connected to lower

and upper plena, with leakage flow discharging to the bypass flow

region (levels 3-4, rings 1-2-3)

ECCS injections have been also modelled, using the leak path

feature, although they are not used in the transient.

4.2.- RECIRCULATION SYSTEM.-

Both Recirculation loops have been

m.odelled, each being divided into three components:

- PUMP 11-21, representing the suction pipe, from vessel

downcomer, and centrifugal pump

- VALVE 12-22, representing the flow control valve and

discharge pipe up to jet pump inlet

- JETP 15-25, modelling the 10 jet pumps connected to each

loop.

4-2
Flow control valve area is defined by the Recirculation control

system.

Recirculation discharge piping consists of one main raiser that

divides into ten branches to feed the corresponding jet pumps; these

branches have been lumped into one single line, on the basis of

maintaining steady state pressure drop.

The JETP component of TRAC-BF1 has been used to model the 10 jet

pumps connected to each loop.

4.3.- MAIN STEAM LINES.-

One single equivalent line has been used to

model the four parallel steam pipes, with 5 main components:

- TEE 80, models pipes from vessel exit to MSIVs, relief valves

are connected to this component althoug not actuated during

the transient

- VALVE 81, represents MSIVs and associated pipe

- TEE 82 represents pipes from MSIVs to turbine control/stop

valves, and branching to bypass valves that discharge to main

condenser.

- Turbine control and stop valves, modelled by VALVE 83, with

position governed by pressure control system; they discharge

to BREAK 92, which represents pressure boundary condition at

turbine inlet.

- Bypass valves are modelled by VALVE 70 with boundary

condition represented by BREAK 73

4-3
4.4.- FUEL ELEMENTS.-

The 624 fuel elements of the core have been divided into three

groups (Figure 4.2), corresponding to the three inner rings of the

vessel model:

80 central high power

436 central average power

108 peripheral low power

The CHAN component of TRAC-BFI has been used to model the

characteristics of the fuel bundles. 11 axial nodes have been

selected, with active length between nodes 3 to 10, and one group to

represent the 8x8 fuel rods

Leakage flow to the bypass region surrounding fuel channels has been

considered by means of a leak path from the second axial node of the

channels to vessel level 3.

4.5.- CORE POWER AND REACTIVITY FEEDBACK.-

Reactivity feedback has been modelled using the point kinetic

option, with void and Doppler coefficients and scram curve obtained

from perturbations on the 3D simulator, performed around the steady

state situation of the core

A conmon axial power distribution is defined for the three types of

fuel channel/bundles modelled.

4.6.- CONTROL SYSTEMS AND TRIPS.-

The three control systems typical of boiling water reactors are

included in the model, as well as trips associated to Reactor

Protection System and other automatic actions.

4-4
4.6.1.- Pressure control system.-

This system governs turbine and

bypass steam flow, as a function of pressure upstream turbine

control valve.

Figure 4.3 illustrates the scheme of the model developped. Special

attention was paid to the proper representation of turbine control

valve characteristic, to reproduce actual behaviour in terms of

steam flow versus position

No adjustment of the bypass portion of the system has been made for

this transient.

4.6.2.- Feedwater control system.-

Based on a level error signal and

mismatch between steam and feedwater flows, this system controls the

amount of feedwater entering the vessel.

Downcomer water level, as computed by TRAC, is corrected based on

dryer pressure drop, to obtain down~omer water level as measured in

the plant. Sensors and controllers are modelled by available

control blocks following the actual system design (Figure 4.4). A

special logic was developped to reproduce coastdown of one pump and

to obtain a smooth transition on total feedwater flow when the

remaining available pump speeds-up in response to controller demand.

4.6.3.- Recirculation flow control system.-

As the plant is operated

in manual mode, only the portion of the system representing this

function has been considered.

The output of the system determines Recirculation control valve

position, which has been translated into valve area by a separate

calculation, using a specific model of the valve to reproduce the Cv

versus position curve as given by the manufacturer.

4-5
One of the objectives of the test analyzed in this report was to

verify the behaviour of the recirculation runback. A logic has been

incorporated to the model that switches the manual valve position

demand to a fixed position (26% open) corresponding to a core flow

demand of 53.15% when low level alarm is detected, provided one

feedwater pump is tripped (Figure 4.5).

4-6
FIGURE 4.1.- C.N. COFRENTES MODEL FOR TRAC-BF1

ISTEA4 DOMtEý

+ 1- ~ -

I I I I

I ORVEP/S PARA TORS

I IPEIPEV I

-c ~ ~ IICI-c Cj

I I

LOWPER1 PLrNVhI

FEED WATER -_K-- 

r----<:K LPC!

- -- -- HPCS

"-<i•LPCS

F21

22 RECIRCULATION

PUMP

I

4-7
FIGURE 4.2.- CORE CHANNELS DISTRIBUTION

HIGH POWER

, AVERAGE POWER

B LOW POWYER (PERIPHERALS)

4-8
FIGURE 4.3. PRESSURE CONTROL SYSTEM

TLlRIZPCONTROL VALVES

17='

ta

I~1.

BYPASS CO~NTROL VALVE

-!Jislj-~ ~ '
FIGURE 4.4. LEVEL/FW. CONTROL SYSTEM

MASTER LEVEL CONIRUL

NIV.DZINC

0

(I PUMP TR4')

I..PUMP MI11011 I

r~4 fl~Qti.

Iral. ii KS-till

(I PUP TRIP)
FIGURE 4.5. RECIRCULATION CONTROL SYSTEM

VALVULA B

5.- STEADY STATE.-

A nominal steady state of the system (Table 5.1) was defined as a

reference or base line condition

Flow split to the three modelled channels and bypass were calculated

by a steady state analysis of the core with FIBWR code.

To adjust a steady state situation, with TRAC-BF1, for a model as

that described for Cofrentes, is a hard task to perform if one has

to deal with the whole system and too many variables and parameters

to control. The approach followed was to adjust separately pieces

or submodels with the proper boundary conditions, and assemble them

one by one to build up the entire model.

Partial models were adjusted for channel, Jet pumps, steam lines,

recirculation loop, vessel and each of the control system

The final steady state reached is presented in Table 5.1 for the

most significant variables, where comparison with target values is

also included.

A null transient, from the steady-state reached, was

reactivity feedback mechanism activated, to verify

steady state conditions.

run, with the

stability of

5-1
Table 5.1.- Reference Steady State condition

Variable Reference TRAC

Core flow (Kg/s) 10646 10642

Recirculation flow, I loop (Kg/s) 1550 1550

Steam flow (Kg/s) 1569 1565

Feedwater flow (Kg/s) 1569 1565

Dome pressure (Pa) 7.17E6 7.17E6

Steam collector pressure (Pa) 6.765E6 6.764E6

Water level, from downc. bottom (m) 10.71 10.71

Core support plate pres. drop (Pa) 0.17E6 0.169E6

Core bypass flow (Kg/s) 1127.5 1129

5-2
6.- TRANSIENT RESULTS AND COMPARISON WITH PLANT MEASUREMENTS.-

The initial conditions prior to initiation fo the transient, as

measured in the plant on February the 2nd, 1985, were:

Core Power 2750 Mwt. (95%)

Core flow 10080 Kg/s (94%)

Dome pressure 6.86 Mpa

Vessel level 100 cm (ref. to 0 instr.)

FW flow 1500 Kg/s

From the reference steady state, the model was conducted to a new

one corresponding to the above conditions, by adjusting the

necessary control systems setpoints, and letting it run a 100 sec.

null transient to verify stability.

Using the EXTRACT feature of TRAC, the model input file was updated

to the test initial condition.

It was necessary to run 30 sec. of null transient previously to

initiation of the event because the EXTRACT function only updates

thermal hydraulic variables, but not those corresponding to control

blocks. Availability of this feature to update control blocks, when

a EXTRACT is performed, would be a helpful improvement to the code.

Figures 6.1 to 6.7 show plots comparison of calculated and measured

values for the most relevant variables.

The most critical variable to reproduce has been the sensed level.

Several runs with different approaches to model sensed level were

considered unsatisfactory. It was found that a very accurate

simulation of sensed level evolution was achieved by taking into

account the difference in water levels inside and outside the dryer

skirt, due to the pressure drop across the dryer, as a function of

steam flow through dryer..

6-1
The initiating event: manual trip of I FW pump, was activated at t

10 sec.

FW flow quickly reduces and causes drop of downcomer water level,

reaching low water level alarm (L4 = 0.7823 m.) at t = 22.5

sec.(12.5 sec. after transient initiation), this activates the

Recirculation runback logic that commands partial closure of flow

control valves (FCVs) to 26% open position.

Partial closure of Recirculation FVCs reduces core flow to 60% in

about 3 seconds (Figure 6.5), consequently void content of the core

increases and, due to the negative void reactivity coefficient,

fission power decreases as shown in Figure 6.6, where a very good

agreement in core power response can be observed for both the

initial low power spike and further evolution to a new stable power

level.

Downcomer water level behaviuur can be seen in Figure 6.1, where the

effect of core flow reduction is well reproduced by the temporary

increase before the minimum value at t = 30 sec. is reached . As the

level control system reacts to level drop, FW flow demand increases

and the remaining operating pump accelerates to deliver its maximum

capacity. Figure 6.2 shows a good agreement in FW response during

coastdown of tripped pump arid first portion of acceleration of the

other, differences between calculated and measured responses are

observed for the second portion of the transient, where FW flow

accomodates to the new steady state; it is believed that these

differences could be reduced with further adjustment of parameters

of the level control system.

Figure 6.3 shows the evolulion of steam flow which exhibits an

initial bias that is maintained in the new steady state, and is

attributed to the poor accuracy of the instrumentation.

Sensed dome pressure is presented in Figure 6.7, both calculated and

measured traces present the same decreasing slope, consequent to

6-2
power reduction and accomodation to the new 'core conditions. A

constant shift is observed after this reduction that could be

accomoaated with a better refinement of the model for steam

lines, nevertheless the relative error is less than 1%.

6-3
FIGUR

On

.rI

1.05

1

0.95

0.9

0.85

SENSED

LEVEL ()0.8

0.75

0.7

0.65

0.6

. .. . . . . .

E 6.1.- SENSED WATER LEVE

. . . . . . . . .

..........

L

: ... .... ....

...............

........ ....... ...........

I I I I I I I I I I I I I I I

0 10 20 30 40 50 60 70 80 90 100 110 120 130 140

TIME (s)

PLANT A - PLANT B -TRAC

150 160

I
FIGURE 6.2.- TOTAL FEEDWATER FLOW

1550 ........... ..................... ............................ .......

1500 .... .... . . ...... . . . .. ..... ..........

1450 . ... . ... . ..... ... .. .. . .... . .. . . . . . . . . a a

1400 .... .............. I .... ................................... .. . . . . . . . .

1350 ----- .. ....... .... .... ........... " .. 0 . . .. o . .. " . . . . . . . . . . . ..

1400

1150 .... .............................. . .......

U'

13500 .... .. . . . . .................................................. a

1100

0 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160

TIME (s)

JPLANT -:TRýACj
FIGURE 6.3.- STEAN FLOW

1600 -.................................................................. I

1500

o)!

oi

4.

1400

Kg/s 1300

1200

1100

. .. . . . . o . .. . o . .. . ... . . .... .... .. .. .. .... . . .

... o....................... .. .. . . . .

. . . . .. . . .

* o 4 4 4 4 •

* 4 4 4 4 4 4

4'-

•L Q

* ,4 -- . .- - .. .., .-4 .4 .. . .. . 4 4. : 4 4°. .. . 4 ' . . . 4 - -4 . .,.4: . .

1000

0 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160

TIME (s)

I

- PLANT - TRAC I

|
FIGURE 6.4.- RECIRCULATION FLOW (1 LOOP)

1500 .i.......................................................................................

1400

oJ

Kg9s

1300

1200

1100 ....

1000

900

. . .... .1. . .J.

.............

......................

.... 8 ... ..... ......

i

800

0 10 20 30 40 50 60 70 .80 90 100 110 120 130 140 150 160

TIME (s)

PLANT -TRAC
FIGURE 6.5.- CORE FLOW /2

550 r0... . .. ... .... .. .

5000

0w Kg/s

4500

4000 ------

3500 .

i

-I...

.5.

J.

.S.

* S S

. . .

. .

3000

0 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160

TIME (s)

I- PLANT - TRAC I
FIGURE 6.6.- CORE POWER

3.OOE+09 -

2.80E+09

2.60E+09 -

2.40Et09 -

2.20E+09

ID W 2.OOE+09

1.8011+09

1.60E+09

1.40E+09

1.20E+09

l.00E+09

. .. . . . .... .. . . . . .. .................. .. ..... ... .....

. . . ... . . . .. . . . . . . . .. .. .. . . . . . . . . .

.. . .....................................

. . . . . . . . . . . . . .

. . . . . . .. . . . .. . .

* * . o . . . . ... . . . .

. . . . . . . . . . . . .. . .. . .

;-.... . "_ _.... _-,"... .... ...... ............................... 

.......... ...... •• :...-...:. ._ . . ..... ... ........

* * . * . . . .. a ..

94.60

04.60

74.60

64.60 %

54.60

44.60

-')A~f CA,.

0 10 20 30 40 50 60 70 80 90 100- 110 120 130 140 150 160

TIME (s)

- PLANT - TRAC
FIGURE 6.7.- DONN PRESSURE

6900000

6850000

C3!.

o

Pa

6800000 ------

6750000

6700000

-. 5

* I

--- I.

... 8..

**1 5.•t

•Qa. 

*~*1*

--. 3.

*~*1* *~~1*

a.

. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .

**~1*

6650000

0 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160

TIME (s)

PLANT -- TRAC
7.- RUN STATISTICS.-

All TRAC runs were made on a CONVEX-C120 vectorial computer owned by UITESA.

Figure 7.1 is a plot of CPU time versus transient time

Figure 7.2 plots time step size (OT) versus transient time.

(RT) and

Required calculation of "grind timeu for this transient, with a total number of 128 cells, for the 23 components of the model, is as

follows:

CPU

C

OT

RT

(total execution

(total number of

(total number of

(transient time)

time)

volumes)

time steps)

- 11401 s.

- 128

- 5008

* 150

(CPU x 103 )/(C x OT) - 17.79

7-1
FIGURE 7.1.- CPU TIME vs. TRANSIENT TIME

!

10000

9000

8000

7000

6000

CPU

TIME 5000

(S)

4000

3000

2000

1000

0

.. ..... . . . . . . . .... . . . .. . . . . . . . . . . . . . . . . . . . . .

... ........ .......... ....... .-....... ........... .8...

. . . . . . . . . . . .. . . . . .: I . . . o . . . . . . .

. . .. . . . . . . . . . o. . . .. ... . i . . ... . . . . . ... . .. . . .. . . .. . . .. .. . . . .

. . . . . . . . .~~~~~~~ . . . . . . . . . . . . . . . . . . . . . .... ...... 

*

*

.. . .. .. .. .. . .. .. .. . ......

. . .. . . . . .. ...... 

.-........... ......... ......... . .......

* a

* a

0 20 40 60 80 100 120 140

TRANSIENT TIME (s)

160
FIGURE 7.2.- TIME STEP SIZE vs. TRANSIENT TIME

0.04 ...................... ............................. ...........

0.035 -- -- -- -- .. .. .. .. . ... .... . ..

0.03 - . . .

0.0.. ...........................

0.02 .... - -................ ................. ...................

0.015 .. . . . ........ .... . . . . .. . . . . ....................... . . . ............. 

0.01 ...... ..... .......... • .......... .......... .......... ........... I.......................

0.005 ..... ................ ..................... a .......... .......... . a a . a

0

0 20 40 60 80 100 120 140 160

TRANSIENT TIME (s)

8.- CONCLUSIONS.

A model of C.N. Cofrentes for TRAC-BF1 has been

developped and proved to be adequate for operational transient

analysis.

The start-up test of "Trip of One Feedwater Pump" has been

reproduced with this model an results have been compared with plant

measured data.

A good agreement between calculated results and measured test data

has been achieved. Point kinetics option is fairly adequate for

this type of operational transients.

Control systems models closely simulate the response of plant

contollers. Further improvements/adjustments of feedwater controls

could better aproximate behaviour of feedwater flow.

Attempts to use the mechanistic model for the

to non satisfactory results.

The EXTRACT feature of TRAC should be improved

to update variable status of control blocks.

separators, have led

with the capability

8-1

APPENDIX I

TRAC Major Edit for the Reference Steady State

at Nominal conditions: 100% core power/ 100%,core flow

I. Gt . -. GGG u6Ii

;;G(.G(;GGG(,G

GGGGGGGGGG

bf~~~)r" 6,6 f-h (b~ . •-Ab b.•' 1,-6b. .b E 61 hi .o.g Ie 1•.(.61bU.Gt,b h 6E 6(66EIIb) I'|d~ .Ii.g..eL, tl,.(.666E•.l 6,bsal 666.E;66"(,( '6,::(,,e661.gl '.a.g'g,[ 33. *,~ , .. . I I 4,ihI.E66I,tlE.i,Eah~b6I,(,b6lE

666666 ICfh66666666666666 t1jUItal I-stipment L orpo. at to,, - VAXM'MS %, e ie o, V!. . I h.Cl.I.66666666666666a,666

66666666666666666666666666666666bfI.6666666666666 6666666h.6666666666666661.66.1.1.61.1 ,` 6(r66666666666616616666

GG66GGGI.661.I

I;GG(;(;GGG(.Ii

I;(;GGGG(*GiGG

DDDD

D 0

D D

D D

D D

D D

AAA

A A

A A

A A

AAAAA

A A

A A

EEEEE

E

E

EEEE

E

E

EEEEE

Cccc

C

C

C

C

C

CCCL

H N

N N

i4N N N N H N NN

N NH

N N

0 0

o O

O o

0 o

0 0

000

EEEEE

E

E

EEEE

E

E

EEEEE

N N

N N

NN N

N N N

N NN

1 N

N N

117

1

1

I

X X X X

X X X x

X x X X

X x

x x X X

x X X X

X X X X

)

X

X

X

X

X

X Xx

K X

X

X

EEEEE

E

E

EEEE

E

E

EEEEE

SSSS TTTTT

S I

S T

SSS I

S T

S T

SSSS T

cccc III

C I

C I C I

C I

C I

cccc III

AAA

A A

A A

A A

AAAAA

A A

A A

RRRR

R R

R A

RRRR

R R

A R

R R

III

III

000

0 0 I1

0 0 1

0 0 1 0 0

0 0 I

000 11 1

000

0 0

0 00

0 0 0

00 0

0 0

000

000 OO0

0 O0

0 0

0 00

00 0

0 0

000

'a

I'

II

II

TRAC-BFI/ ( I) 01/09/B7 DEVELOPED AT INEL BY THE THERMAL HYDRAULICS CODE DEVELOPMENT BRANCH

EXECUTED ON : 8-Nov-B9 TIME : 10033=tB

BWRI6 TRANSITORIO DE DISPARO DE TURBOBOMBA DE AGUA DE ALIMENTACION

* 4

• TRAC MAJOR EDIT a *

A T • AT TIME STEP ?B21 '

******.*** *********.******.*

o*GIJI PAGE 23

0 TIME : 6.49375E+00 SEC. DELT = 2.6178OE-02 SE

0 TIME STEP COURANT LIMITED BY COMPONENT 62.FA

0 TIME STEP SELECTION MODE A 4

0 TIME STEP LIMITED BY COURANT CONDITIONl

0 AVERAGE OUTER ITERATION COUNT OVER THE LAST

O TOTAL NUMBER OF TIMES THAT EACH COMPONENT WAS

TRAC COMP SEQUENCE NUMBER I - ID 0

TRAC COMP SEQUENCE NUMBER It - 20 0

1RAC COMP SEQUENCE NUMBER 21 - 23 0

0 THE LAST MINIMUM NUMBER OF OUTER ITERATIONS WA

0 THE LAST MAXIMUM NUMBER OF OUTER ITERATIONS WA

C. TIME STEPS = 281. NUMBER OF HYDRODYNAMIC

CE 0. TO 2.616E-02 SEC

IE TI ME STEPS WAS I.OCfEOr.

THE LAST TO CONVERGE SIIhCE THE LAST EDIT -

C 0 0 0 0 0 0 0 0

0 0 lB 0 0 0 0 0 0

0 0.

S 1 AT STEP 280. LIMITED BY COMPONENT B0. WITH

S I AT SIEP 280. LIMITED BY COMPONENT 80. WITH

SOLUTION ITERATIONS

DELTA-P/P = 4.59E-04

DELTA-P/P = 4.59E-04
0 JOB TIME u 7.587E402 TRAC EXECUTION 111£ z 7.58IE402

0D0*'4000*** TIME c 6.49375

TRIP INFORMATION (SET TRIPS)

DELT z 2.61780E-02 NSIEP - 281 4*0*0000#04

NO TRIP SET POINT VET REACHED

0o****'**'* TIME= 6.49375 DELT * 2.61780E-02 NSTEP * 281 ***$*04**09

POWER INFORfAATION

TOTAL REACTOR POWER = 2.894E,09

o0 0 0 0 0 EDITt 8 0 # • 0 # 1 0 0 0 • 0 • 0 1 • 0 • • 0 0 

-. 00. FILL

0 JUNI 0 0

40*÷LPCI PUMP NSTEP= 281 TIME- 6.49375 DELI= 2.617B0E-020" 0

CELL 1 LEAK FLOW RATE. O.OOOE*.0 KG/S

PRESSURE VAPOR FRAC LIQ VEL VAP VEL T SAT

CELL (PA) (M/S) (M/S) (K)

I 1.500E+06 0.000000 0. 0. 470.683

MASS FLOW RATE = O.OOO0E+0O TOTAL MASS IN =

Of 0 m 0 • EDIT= a 0 0 • 0 0 0 0 0 # 0 # • 0 1 0 0 # 0 ,

T LID

(K)

323.000

LEAK MASS FLUX. O.OOOE.OD KG/M2-S

T VAP LIG DEN VAP DEN DELIA-P lOT

(K) (KG/M3) (KG/M3) (PA)

470.683 988.7 7.441 -0.1500E*07

ICHOKE ICCF

0 0 00

rO.OOOE4O0 I- 0 0' 0 &# 1

-0e6- FILL

0 JUNI c 0

42**HPCS PUMP NSTEPa 281 TIME. 6.49375 DELI. 2.6178DE-02 0**

CELL I LEAK FLOW RATE- O.OOOE+0O KG/S

PRESSURE VAPOR FRAC LIO VEL VAP*VEL T SAT

.CELL (PA) (M/S) (M/S) (K)

I 1.500E06 0.000000 0. 0. 470.683

MASS FLOW RATE - 0.OQOOE.OO TOTAL MASS IN *

00,, 9 9 9 EDIT= 8 # # # 0 0 0 0 0 0 0 • • # # 0 0 f 0 # •

T LIQ

(K)

323.000

LEAK MASS FLUX: O.O00E400 KG/M2-S

T VAP LIO DEN VAP DEN DELIA-P 10I

(K) (KG/M3) (KG/M3) (PA)

470.683 908.7 7.441 -O.1500E,07

I CIOKE ICCF

U 0 (D0

0.00O00E#00

0f 0 0 0 #

-*#I- FILL

0 JUNI - 0

44*+ FEEDWATER FILL NSTEP= 281 TIMEx 6.49375 DELT= 2.61780E-02 *6****

CELL I LEAK FLOW RATE- 1.565E+03 KG/S

PRESSURE VAPOR FRAC LIO VEL VAP VEL T SAT

CELL (PA) (M/S) (MIS) (K)

I 7.200E406 0.000000 7.549 7.549 560.925

MASS FLOW RATE z O.OOOOE*00 TOTAL MASS IN

Do # • # o EDIT: B 0 D 0 0 1 0 # # o # # 0 0 & 0 # 0 1 • a

T LID

(K)

488.550

LEAK MASS FLUX= 6.426E*03 KG/IA2-S

T VAP LID DEN VAP DEN DELTA-P TOT

(K) (KG/133) (KG/MI3) (PA)

560.925 851.2 37.69 -0.7200E407

ICHOKE ICCF

aO 0.0

I .0176E*04

8 8 0 0f *
.- - . FILL

0 JUNI a 0

464+LPCS PUMý 46..LPCS NSTEP: PUM~~~ 281 TIME' 6.4937! VELIc )11 2.617niIE-02 .17110 00414 '' -

CELL I LEAK FLOW RATEm O.000.E00 KG/S

PRESSURE VAPOR FRAC LI VEL VAP VEL T SAT

CELL (PA) (MIS) (MIS) (K)

1 1.500DE06 0.000000 0. 0. 470.683

MASS FLOW RATE z O.OOOOE*0O( TOTAL MASS IN -

of # # • EDIT= 8 •I 0 # g r 0 1 # 0 .0 0 • p 0 , 0

7 LIQ

(K)

323.000

LEAK MASS FlUX= O.OOUE*0D0 KG/M2-S

T VAP LIQ DEN VAP DEN DELIA-P TOT

(K) (KG/M3) (KG/M3) (PA)

470.683 988.7 7.441 -0.1500E407

ICHOKE ICCF

0 0 n 0

O.0000E*00

* 01 90 00 ,

-600- PUMP 11+48OMRA DE RECI!CULACION

0 JUNI a 10 JUN2 = It

TRIP OMEGA RHO VOL. FLOW

0 1.555E+02 7.581E÷02 2.045E*00

NSTEPE 281 TIME= 6.49375 0

VAPOR FRAC SMOM HEAD

3.559E-18 2.441E103 2.441E*0.

DELTm 2.61780E-02 004**'

DELTA - P IOROUE

I 1.8450E+06 2.874E404

MASS FLOW

1.550E103

10RUM

O.OUUE.O4I

CELL

I

2

3

4

5

0

PRESSURE

(PA)

7.177E+06

7.198E+06

7.219E406

9.063E+06

LIQ HTC*A

(W/K)

0.7543E-07

0.1614E-07

0.5769E-09

0. 1597E-10

CELL I FLOW RATE IN a 1.550E103 KG/S MAS!

CELL 4 FLOW RATE OUT a 1.550.E03 KG/S MASI

VAPOR FRAC LI0 VEL VAP VEL 7 SAT 7 LIQ

(MIS) (MIS) (K) (K)

0.000000 12.42 13.43 560.709 551.038

0.000000 12.42 13.11 560.910 551.045

0.000000 12.42 13.12 561.096 551.052

0.000000 12.42 12.42 577.024 551.666

12.39 13.14

INTERFACIAL HEAT TRANSFER (.=FLASH.-sCONDENSE)

VAPOR HTCOA WALL MASS TOTAL MASS TOT.E/(*LIO

TRANSFER RATE TRANSFER RATE OR-VAP.E)

(WIK) (KG/S) (KG/S) (JIJ)

0.3771E-07 0. -0.408OE-12 -0.7506E-16

0.0071E-06 0. -0.1066E-12 -0.2660E-17

0.2884E-09 0. -0.3884E-14 -0.2002E-10

0.7983E-11 0. -0.2941E-15 -0.1617E-19

S FLUX IN

S FLUX OUT

I VAP

(K)

560.709

560.910

561.096

577.024

= 9.413E403 KG/M2-S 2 9.413E403 KG/M2-S

LIQ DEN VAP DEN

(KG/M3) (KG/M3)

758.1 37.55

758.1 37.69

758.1 37.79

759.6 49.18

DELTA-P TOT

(PA)

0.7354E105

-0.2118E105

-0.1976E*05

-0.1845E107

2648.

FRICTION

SLIP RE•

ICHOKE

00

00

00

00

00

ICCF

0 0

0 0

0 0

0 0

0 0

CELL

1

2

3

4

5

THERMODYNAMIC

QUALITY

-0.034

-0.035

-0.036

-0.101

INTERFACIAL

SHEAR

COEFFI

(KG/M3-S)

24.9

4.93

4.23

0.

4.51

YGAS REYLIO

1.08

1.06

1.06

1.00

I .06

0. 161E-07

0.598E-09

0.402E-I0

0. ISUE- II

0.439E

0.439E

0.439E

0.440E

a TOTAL COMPONENT WATER MASS ,1 2.5702E*03 KG. TOTAL COMPONENT WATER ENERGY = 3.1249E*09 J.

PERCENT MASS CONTINUITY ERROR a 7.9339E-10 LOST MASS= 2.0392E-09 KG. PERCENT MASS FLOW 1HRU(TURNOVER) = 1.0123E-03

Of 0 0 8 0 EDIT= 8 v # 0 • v I I # 0 # I 0 I 0 # 0 0 I I a I 0 # I # # I

-*'*- VALVE

0 JUNI = 11

12*. VALVULA CONTROL RECIRCULACION

JUN2 a 12

CELL I FLOW RATE IN = 1

CELL 4 FLOW RATE OUT a I

VAPOR FRAC LI VEL VAP VEL

(MIS) (MIS)

6 0.000000 12.39 13.14

6 0.000000 28.95 29.88

6 0.000000 12.40 13.28

6 0.000000 12.40 13.27

NSTEP= 281 TIME- 6.49375 DELT= 2.6178OE-02 **0*00

CE.L

.1

2

3

4

•S SURE

(Pt.)

9.061E,0

8.700E10

8.643E.0

8.499E10

.550E*03 KG/S

.550E103 KG/S

7 SAT

(K)

577.003 5

574.106 5

573.635 5

572.443

7 L1Q

(K)

5sI.6P5

55I.545

551.526

551.477

MASS FLUX IN

MASS FLUX OUT

T VAP

(K)

577.003

574.106

573.635

572.443

= 9.413E103 KG/M2-S * 6.244E103 KG/M2-S

LIO DEN VAP DEN

(KG/M3) (KG/M3)

759.6 49.16

759.3 46.85

759.2 46.49

759.1 45.58

DELTA-P 701

(PA)

0.

0.3602E*06

0.5746E1O5

0.1441E106

I CHOKE

00

00

00

00

ICCF

0 0

0 0

0 0

0 0
5

0

CELL

1

2

3

4

5

H. ,' 8.827

INTERFACIAL HEAT TRANSFER (.=FLASH.-zCONDENSE)

LIO HTC*A VAPOR HTC*A WALL MASS TOTAL MASS TOT.EI(.LIQ

TRANSFER RATE TRANSFER RATE OR-VAP.E)

(W/K) (W/K) (KG/S) (KG/S) (J/J)

0.7443E-12 0.3722E-12 0. -0.1370E-16 -0.1314E-20

0.9942E-13 0.4971E-13 0. -0.1603E-17 -0.6723E-22

0. 0. 0. 0. 0.

0. 0. 0. 0. 0.

THERMODYNAMIC

QUALITY

-0.101

-0.008

-0.086

-0.001

INTERFACIAL

SHEAR

COEFFI

(KGIM3-S)

0.

4.60

4.72

4.10

7.68

FRI C I 1 (I1

SLIP RE

0 0 (1 (I

YGAS REYLIO

I .06

1 .03

1.07

1.07

1.07

O.867E-13

0.

0.963E-16

0. 179E-17

0.524E

0.524E

0.440E

0.254E

VALVE AREA - 7.050927E-02 PERCENT OPEN - 42.81073

VALVE HYDRAULIC DIAMETER - 1.961E-01

0 TOTAL COMPONENT WATER MASS - 4.2789E+03 KG. TOTAL COMPONENT WATER ENERGY - 5.2024E409 J.

PERCENT MA.SS CONTINUITY ERROR m 3.6571E-10 LOST MASS- 1.5649E-08 KG. PERCENT MASS FLOW 1HRU(TURNOVERI

O # , a & EDIT= - a 9 0 0 v 0 I # 0 * I # # u h 0 I A w &I& 

= 1.2016E-03

-06*- TEE 15**lOMBA DE CHORRO

O JUNI a 15 JUN2 a 16 JUl13

0 * THIS TEE IS A JET PUMP *

EFFECTIVE VALUES

M RATIO N RATIO ETA

2.4327E#00 1.1319E-O 2.7534E-01

PRIMARY TUBE

NSTEP= 281 TIME% 6.49375 DELT: 2.61780E-02 *06"

APPLICABLE VALUES

M RATIO N RATIO ETA

2.4327E200 1.2441E-01 3.02658-01

CELL

1

2

3

4

PRESSURE

(PA)

6.756E+06

7.325E*06

7.358E*06

LIQ HTC*A

(W/K)

0. 1464E-07

0.6713E-08

0.B788E-09

CELL I FLOW RATE IN - 3.771E*03 KG/S MAS

CELL 3 FLOW RATE OUT - 5.3212403 KG/S MAS!

VAPOR FRAC LIQ VEL VAP VEL T SAT T LIO (M/S) (M/S) (K) (K)

0.000000 33.07 34.28 556.616 550.903

0.000000 38.50 39.26 562.102 551.090

0.000000 7.657 8.104 562.405 551.100

7.656 8.114

INTERFACIAL HEAT TRANSFER (4=FLASH.-=CONDENSE)

VAPOR HTC*A WALL MASS TOTAL MASS TOT.El(+LIO

TRANSFER RATE TRANSFER RATE OR-VAP.E)

(WIK) (KG/S) (KG/S) (J/J)

0.7318E-08 0. -0.5495E-13 -0.7257E-17

0.3356E-08 0. -0.4977E-13 -0.1811E-17

0.4394E-09 0. -0.6699E-14 -0.2602E-18

S FLUX IN

S FLUX OUT

T VAP

(K)

556.616

562.102

562.405

= 2.507E*04 KG/M2-S

5.BOSE003 KG/M2-S

LIQ DEN VAF DEN

(KG/M3) (PG/M3)

757.7 25.10

758.2 38.42

758.2 38.62

DELIA-P IOT

(PA)

0.461 2E.06

-0.5691E*06

-0.3243E405

-0.1588E405

FRICTION

SLIP REY

I CHOKE

0 0

00a

00

00

ICCF

0-1

0 0

0 0

00

0

CELL

1

2

3

4

THERMODYNAMIC

QUALITY

-0,020

-0:040

-0.041

INTERFACIAL

SHEAR

COEFFI

(KG/M3-S)

40.4

113.

15.3

12.1

VGAS REYLIO

1.04

1.02

I .06

1.06

0.195E-08 0.401E

0.297E-09 0.440E

0.203E-10 0.202E

SIDE TUBE

CELL 2

PRESSURE VAPOR FRAC

CELL (PA)

I 8.425E806 0.000000

2 8.442E*06 0.000000

FLOW RATE OUT z -1.550E+03 KG/S MASS FLUX OUT

LIO VEL VAP VEL T SAT T LIW T VAP

(M/S) (MIS) (K) (K) (K)

-63.82 -64.87 571.830 551.453 571.830

-8.226 -8.742 571.967 551.458 571.967

-6.244E*03 KG/M2-S

LIQ DEN VAF DEN

(KG/M3) (VG/M3)

759.1 45.12

759.1 45.22

DELTA-P TOT

(PA)

-0.1669E*07

-0.1645E+05

I CHOKE

00

00

ICCF

0 0

0 0
3

0

CELL

I

2

3

LI HTCOA

(W/K)

0.

0.

-8.225 -8.827

INTERFACIAL HEAT TRANSFER (O=FLAI3.-=CONDENSE)

VAPOR HTC$A WALL MASS TOTAL MASS TO1.E)(4LIQ

TRANSFER RATE TRANSFER RATE OR-VAP.E)

(W/K) (KG/S) (KG/S) (J/J)

0. 0. 0. 0.

0. 0. 0. U.

THERMODYNAMIC

QUALITY

-0.070

-0.079

Ui.

INTERFACIAL FRICTION

SHEAR SLIP

COEFFI

(KG/M3-S)

19.2 1.02

7.64 1.06

0. 1.07

U 0 J 0

REYGAS REYLIQ

0.367E-18 0.337E

0. O.113E

0 TOTAL COMPONENT WATER MASS = 2.1016E403 KG. TOTAL COMPONENT WATER ENERGY = 2.5551E#09 J.

PERCENT MASS CONTINUITY ERROR = 2.6102E-09 LOST MASS= 5.4856E-08 KG. PERCENT MASS FLOW THRU(TURNOVER) = -2.8916E-(14

Ov # s # s EDIT= 8a 9 f 9 # 0 0 9 # • 1 • # • 0 • 0 0 & # # • 0 # 0 #

-ee0- PUMP

0 JUNI z 20

TRIP OMEGA

0 1.555E+02

21÷+BOMBA DE RECIRCULACION

JUN2 a 21

RHO VOL. FLOW

7.581E+02 2.045E+00

NSTEPc 281 TIME= 6.49375 DELl= 2.61780E-02 $*.6.0

MASS FLOW VAPOR FRAC SMOM HEAD DELTA - P TORQUE

1.550E*03 3.559E-16 2.441E+03 2.441E*03 1.8450E*06 2.874E+04 TOROM

O.OOOE+O0

CELLI

7 2 ol 3

4

5

0

PRESSURE

(PA)

7.177E*06

7.198E406

7.218E*06

9.063E,06

LIQ HTCOA

(W/K)

0.7543E-07

0. 1614E-07

0.5769E-09

0. 1597E-10

CELL I FLOW RATE IN x 1.550E*03 KG/S MASS

CELL 4 FLOW RATE OUT a 1.550E.03 KG/S MASS

VAPOR FRAC LI VEL VAP VEL T SAT T LIQ

(MIS) (M/S) (K) (K)

0.000000 12.42 13.43 560.709 551.038

0.000000 12.42 13.11 560.910 551.045

0.000000 12.42 13.12 561.096 551.052

0.000000 12.42 12.42 577.024 551.666

12.39 13.14

INTERFACIAL HEAT TRANSFER (*=FLASH.-=CONDENSE)

VAPOR HTCOA WALL MASS TOTAL MASS TOT.EI(*LIQ

TRANSFER RATE TRANSFER RATE OR-VAP.E)

(W/K) (KG/S) (KG/S) (J/J)

0.3771E-07 0. -O.4880E-12 -O.7506E-16

0.8071E-08 0. -0.1066E-12 -O.2860E-17

0.2884E-09 0. -0.3884E-14 -0.2002E-18

0.7984E-11 0. -0.2941E-15 -0.1617E-19

FLUX IN

FLUX OUT

T VAP

(K)

560.709

560.910

561.096

577.024

9.413E*03 KG/M2-S

9.413E403 KG/M2-S

LIO DEN VAP DEN

(KG/M3) (KG/M3)

758.1 37.55

758.1 37.68

758.1 37.79

759.6 49.18

DELTA-P 101

(PA)

0.7354E+05

-0.2118E405

-0.1976E-05

-0. 1845E407

2640.

FRICTION

SLIP RE

ICHOKE

00

00

00

00

00

ICCF

a 0

a 0

0 0

0 0

o n

CELL

1

2

3

4

5

THERMODYNAMIC

QUALITY

-0.034

-0.035

-0.036

-0. 101

INIERFACIAL

SHEAR

CUEFFI

(KG/M3-SI

24.9

4.93

4.23

0.

4.51

VGAS REYLIO

I . 0 A

I .06

I .06

1 .00

I .06

0. 161E-07

0..598E-U9

0.402E-10

0. ISOE- 11

0. 439E

0.439E

0.439E

0.440E

0 TOTAL COMPONENT WATER MASS a 2.5702E403 KG. TOTAL COMPONENT WATER ENERGY = 3.1249E409 J.

PERCENT MASS CONTINUITY ERROR : 7.9548E-10 LOST MASS= 2.0446E-08 KG. PERCENT MASS FLOW THRU(TURNOVERI = 1.0123E-03

O# s a # # EDIT= 8 1 0 # 0 # I # • 0 N 0 # # # A A A m 0 0 a A # & m # 

-0**- VALVE 22++ VALVULA CONTROL RECIRCULACION

0 JUNI a 21 JUN2 = 22

CELL I FLOW RATE IN = I

CELL 4 FLOW RATE OUT = I

PRESSURE VAPOR FRAC LIQ VEL VAP VEL

CELL (PA) (M/S) (M/S)

NSIEP= 281 T71lJE 6.49375 DELI= 2.617BUE-02

.550E.03 KG/S

.550E*03 KG/S

T SAT

(K)

MASS FLUX IN = 9.413E*03 KG/M2-S

MASS FLUX OUT : 6.244E+03 KG/M2-S

T VAP LIQ DEN YAP DEN DELTA-P TOT

(K) (KG/M3) (KG/M3) (PA)

T LIO

(K)

ICIlOKE ICCF
1

2

3

4

5

0

9.061E*06 0.000000 12.39 13.14 577.003 551.665

8.700E*06 0.000000 28.95 29.88 574.106 551.545

8.643E+06 0.000000 12.40 13.28 573.635 551.526

8.499E#1)6 0.00O000 12.40 13.27 572.443 551.477

8.225 8.827

INTERFACIAL HEAT TRANSFER (.=FLASH.,-=CONDENSE)

LI HTCOA VAPOR HTCOA WALL MASS TOTAL MASS TOT.E/(*LIQ

TRANSFER RATE 7RA14SFER RATE OR-VAP.E)

(W/K) (w/K) (KG/S) (KG/S) (J/J)

0.7453E--12 0.3726E-12 0. -0.1371E-16 -0.1315E-20

0.9841E-13 0.4920E-13 0. -0.1587E-17 -0.6655E-22

0. 0. 0. 0. 0.

0. 0. 0. 0. 0.

577.003

574.106

573.635

572.443

- s5!l. t.

759.3

759.2

759. 1

-1!. 11

46.49

45.58

U.

0.3602E406

0.5746E405

0.1441E*06

0.5704E405

FRICTION

SLIP RE

(I0

0

0

0

a

0

0

0

0

0 0

O 0

O 0

O 0

0 0

CELL

1

2

3

4

5

THERMODYNAMIC

QUALITV

-0. 101

-0.088

-0.0e

-0.081

.INTERFACIAL

SHE AR

COEFFI

(KG/M3-S)

0.

4.60

4.72

4. 10

7.68

YGAS REYLIO

I .OG

1.03

1.07

1 .07 1 .07

U. RGGE- 13

(I.

0. 252E- 15

0.327E- 17

0.524E

0.524E

0.440E

0. 254E

VALVE AREA a 7.050927E-02 PERCENT OPEN a 42.81073

VALVE HYDRAULIC DIAMETER - 1.961E-01

O TOTAL COMPONENT WATER MASS w 4.2789E503 KG. TOTAL COMPONENT WATER ENERGY - 5.2024E+09 J.

PERCENT MASS CONTINUITY ERROR a 3.6559E-10 LOST MASS= 1.5643E-08 KG. PERCENT MASS FLOW THRU(TURNOVER) - 1.2010E-03

0 0 a S N EDIT- 8 I# 0 0 0 m 0 # I s I 9 0 I 0 I I 0 S f I I I I 9 I I I

-000- TEE 25**BOMBA DE CHORRO

0 JUNI - 25 JUN2 = 26 JUN3 = 22

0 * THIS TEE IS A JET PUMP *

EFFECTIVE VALUES

M RATIO N RATIO ETA

2.4327E500 1.1319E-01 2.7534E-01 2.

PRIMARY TUBE

NSTEPv 281 TIMEa 6.49375 DELTz 2.61780E-02 404

APPLICABLE VALUES

M RATIO N RATIO ETA

4327E*00 1.2441E-01 3.0265E-O0

PRESSURE

CELL (PA)

I 6.756E*06

2 7.325E#06

3 7.358E*06

4

LID HTC&A

CELL

(W/K)

1 0.1464E-07

2 0.6713E-08

3 0.878BE--O9

4

SIDE TUBE

CELL I FLOW RATE IN = :1.771E*03 KG/S MAS:

CELL 3 FLOW RATE OUT 5 !.321E*03 KG/S MAS:

VAPOR FRAC LIQ VEL VAP VEL T SAT T LI1

(M/S) (M/S) (K) (K)

0.000000 33.07 34.28 556.616 550.903

0.000000 38.50 39.26 562.102 551.090

0.000000 7.657 8.104 562.405 551.100

7.656 8.114

INTERFACIAL HEAT TRANSFER (-:FLASH.-:CONOENSE)

VAPOR HTCOA WALL MASS TOTAL MASS TOT.E/(*LIQ

TRANSFER RATE TRANSFER RATE OR-VAP.E)

(W/K) (KG/S) (RG/S) (J/J)

0.7318E-08 0. -0.5495E-13 -0.7257E-17

0.3356E-08 0. -0.4977E-13 -0.1811E-17

0.4394E-09 0. -0.6699E-14 -0.2602E-18

S FLUX IN =

S FLUX OUT -

T VAP

(K)

556.616

562.102

562.405

2.507E*04 KG/M2-S

5.805E.03 KG/M2-S

LID DEN YAP DEN

(KG/M3) (KG/M3)

757.7 35.10

758.2 38.42

758.2 38.62

DELTA-P TO.T

(PA)

0.4612E406

-0.5691E*06

-0.3248E.05

-0. 18BE#O5

FRIC1IOt1

SLIP REV

ICHOKE

00

00

00

00

ICCF

0-1

0 0

B 0

O 0

THERIdO'DNAMI C

OUAL I TV

-0.02C

-0. 04C

-0.041

INTERFACIAL

SHEAR

COEFF I

(KG/M3-S)

40.4

113.

15.3

12.1

YGAS REVLIO

1 .04

I .G1"

0.195E-08 0.401E

0.297E-09 0.440E

0:203E-10 0.202E

CELL 2 FLOW RATE OUT a -1.550E+03 KG/S MASS FLUX OUT = -6.244E403 KG/M2-S
PES1S lRE

CELL (PA)

I 8.425E*06

2 8.442E406

3

VAPOR FRAC LIO VEI.

(M/S)

0.000000 -63.82

0.000000 -8.226

-8.225

YAP vEL

(MIS)

-64.87

-8.742

-8.827

T SAT

(K)

571.830

571.967

I I 10

(K)

551.453

551.450

T VAP

(K)

571.830

571.967

LIO iOEI

(KG/M33

759. 1

759.1

VAP DENl

IKG/M3)

45.12

45.22

DELIA-P 101 (PA)

-0. 1G69E1 l17

-(.1645E4O5

0.

I I()IV ~ Itt. I

U 11 0I 0

U ( 0 U

a 0 0 0

0 INTERFACIAL HEAT TRANSFER (.:FLASH.-=CONDENSE) INTERFACIAL FRICTION

CELL

1

2

3

LIO HTCOA VAPOR HICOA WALL MASS

TRANSFER RATE

(W/K) (W/K) (KG/S)

0. 0. 0.

0. 0. 0.

TOTAL MASS

TRANSFER RATE

(KG/S)

0.

0.

7OT.E/(.LIQ

OR-VAP.E)

(JJ)

0.

0.

THERMODYNAMIC

OUALITY

-0.078

-0.079

SH EAR

COEFFI

(KGIM3-S)

19.2

7.64

0.

SLIP

1.02

1.06

1.07

REYGAS REVLIQ

0.287E-16 0.337E

0. 0.113E

0 TOTAL COMPONENT WATER MASS a 2.1016E+03 KG. TOTAL COMPONENT WATER ENERGY = 2.5551E*09 J.

PERCENT MASS CONTINUITY ERROR = 2.6157E-09 LOST MASSn 5.4971E-08 KG. PERCENT MASS FLOW THRU(TURNOVER) a -2.0932E-04

Os a * s # EDIT= 8 0 # 0 0 0 f 1 # 0 0 0 0 0 0

-6e0- CHAN 60.+ 108 CANALES PEIRIFERICOS NSTEP= 283 TIME= 6.49375

0 MAXIMUM SURFACE TEMPERATURE a 5.673183E402. WHICH IS IN ROD GROUP 1. CELL 6

0 JUNI a 60 JUN2 a 63

DELTz 2.617G0E-02 040000

CELL I FLOW RATE IN - 1.158E+03 KG/S

CELL I1 FLOW RATE OUT a 1.099E*03 KG/S

CELL 2 LEAK FLOW RATE: 5.935E+01 KG/S

MASS FLUX IN : 6.400E.03 KG/M2-S

MASS FLUX OUT x 1.286E403 KG/M2-S

LEAK MASS FLUX- 2.748E+03 KG/M2-S

CELL

1

2

3

4

5

6

7

8

9

10

I1

12

0

CELL

1

2

3

4

5

c

7

8

9

30

II

12

PRESSURE

(PA)

7.253E+06

7.251E#06

7.247E*06

7.242E#06

7.237E,06

7.232E#06

7. 227E#06

7.222E.06

7.218E#06

7.213E#06

7. 2IOE.06

VAPOR FRAC

0.000000

0.000000

0.000000

0.000000

0.037132

0.129163

0.239952

0.330522

0.397737

0.429324

0.440340

LIO VELI

(M/S)

8.440

1.447

1.373

1.379

1.389

1.452

1.601

1.817

2.039

2.242

2.357

2.970

YAP VEL

(M/S)

8.883

1.604

1.490

1.498

1.900

1.198

1.917

2.371

2.728

3.033

3.054

3.690

T SAT

(K)

561.428

561.409

561.372

561.323

561.274

561.227

561.181

561.136

561.092

561.052

561.020

T LIQ

(K)

551.066

551.083

552.803

555.449

558.323

559.883

560.681

561.000

561.098

561.100

561.029

T VAP LIO DEN VAP DEN

(K) (KG/M3) (KG/M3)

561.428 758.1 38.00

561.409 758.1 37.99

561.372 754.6 37.96

561.323 749.1 37.93

561.274 743.0 37.90

561.226 739.6 37.87

561.179 737.8 37.85

561.134 737.1 37.82

561.089 736.9 37.79

561.048 736.9 37.77

561.018 737.0 37.75

DELTA-P TOT

(PA)

0.9907E*05

2095.

3933.

5189.

5186.

4963.

4870.

4773.

4691.

4188.

3426.

4982.

I CHOKE

00

0 II

O0

O00

00

00

00

O01

00

0 0

0 0 00

ICCF

0-2

0 0

0 0

0 0

0 0

0 0

0 0

0 a

0 U

0 0

a 0

0-1

INTERFACIAL HEAT TRANSFER (+:FLASH.-=CONDENSE) INTERFACIAL FRICTION

LIO HTCOA VAPOR HTCOA WALL MASS

TRANSFER RATE

(W/K) (W/K) (KG/S)

0.1664E-07 0.8321E-08 0.

0.3052E-08 0.1526E-08 0.

0.9302E-09 0.4651E-09 0.

0.1126E-09 0.5631E-10 0.

C.0365E*06 0.1927E*06 3.437

C.1608E-07 0.2880E*06 9.572

([.4526E°07 0.8365E*06 14.36

2.e976E.07 o.1766E+07 3,3.09

0.1399E*08 0.2852E+07 12.09

0.9695E+07 0.1916E+07 3.840

0.1604E+08 0.3380E.07 0.

TOTAL MASS

TRANSFER RATE

(KG/S)

-0.1158E-12

-0.211SE-13

-0.5349E-14

-0.4438E-15

1.781

8.122

12.84

13.27

12.14

4.144

0.8966E-01

TOT.E/(*LIQ

OR-VAP.E)

(JJ)

-0.2519E-16

-0.5920E-17

-0.4444E-18

-9.3453E-19

0.3540E-01

0.4r46E-01

0.3802E-01

0.3099E-01

0. 2261E-0I

0. 1426E-01

0.1891E-03

THERMODYNAMIC

DUAL I T.Y

-0.037

-0.037.

-0.031

-0.021

-0.009

0.003

0.018

0.032

0.044

0.049

0.049

SHEAR

COEFFI

(KG/M3-S)

9.67

26.5

79.6

79.5

317.

0. 124E*04

0.256E*04

0.337E*04

0.352E404

0.329E*04

0.573E#04

0.407E04

SLIP

3.05

3.31

1.09

1.09

1.37

0.825

1.20

1.31

1 .34

1.35

1.30

1.24

REVGAS REYLIO

0.133E-09 0.111E

0.418E-11 0.143E

0.371E-12 0.140E

(0.485E-13 0.141E

0.149E-04 0.140E

0.S21E*04 0.136E

0.133Eo05 0.133E

0.218E*05 0.132E

0.296E#05 0.132E

0.338E405 0.134E

0.383E+05 0.153E
6. COIIvU*YIVE CELL AVERAGE (t AItII IIS FOR INNER CIIAN WALL USED FOR WALL CIIERGV IRAIISFER 10 CHA14 FLUID (A HFG. fIll IS OP•; SEE MAIJIJ

TSUHF H-LIO(COIJV) H-VAP(CONV) QTOI(CONV) Il-LIQ(RAC-) H-VAP(RAD) OIOI(CONV4RAD) OIOT/FI.tI.II [IJrRGY

CELL (K) (W/M*02-K) (W/Mt#2-K) (w) (W/M'*2-K) (W/M$02-K) (W) (J/J)

1 551.278 0.2095E405 0. O.3934E*05 0. 0. 0.3934E+05 0.5747E-05

2 551.904 0.1292E#05 0. O.1058E*06 0. 0. D.1058E*06 0.1987E-04

3 553.178 0.1287E+05 0. 0.1286E+06 0. 0. O.1286E#06 0.7171E-05

4 555.033 0.1274E+05 0. -0.1504E406 0. 0. -0.1504E*06 -0.7847E-05

5 557.031 0.1251E*05 0. -0.4588E406 0. 0. -0.4588E#06 -0.2466E-04

6 558.403 O.1219E#05 0. -O.5121E*n6 0. 0. -0.5121E#16f -O.3OU2E-O4

7 559.294 0.1200E*05 0. -0.4919E*06 0. 0. -0.4919E#06 -0.3117E-04

8 559.951 0.1393E405 0. -O.3978E*06 0. 0. -0.3978E#D6 -0.3050E-04

9 560.246 0.1559E405 0. -0.3771E406 0. 0. .- 0.3771E#(16 -0.3032E-04

10 560.288 O.1652E*05 0. -0.1912E#06 0. 0. -O.1917E#06 -O.3204E-04

It 560.319 0.1818E.05 0. -0.2573E406 0. 0. -O.2573E*06 -O.2754E-014

0 WALL COARSE MESH CONDUCTION INFORMATION (MODES USE ABOVE CELL FLUID PROPERTIES EXCEPT LAST ONE: Hl-COEFF. ARE AVERAGE

( ........ INSIDE WALL CONDUCTION DATA ...... ..... OUTSIDE WALL CONDUCTION DATA .....

MESH MESH H-LIO H-VAP MESH H-LIC H-VAP WALL RADIAL NODE TEMPERATURES (K)

0 HT-MODE (W/M2-K) (W/M2-K) HT-MODE (W/M2-K) (W/M2-K) 'INSIDE

I 1.20 0.429E+05 0. 1.20 0.598E*04 0. 551.175 552.060

2 1.20 0.134E*05 0. 1.20 0.598E*04 0. 551.381 552.164

3 1.20 0.128E+05 0. 1.20 0.598E404 0. 552.426 552.651

4 1.20 0.128E405 0. 1.20 O.598Ef04 0. 553.930 553.353

5 1.20 0.127E*05 0. 1.20 O.598E.04 0. 556.137 554.383

6 l.20 0.124E+05 0. 1.20 0.598E*04 0. 557.925 555.220

7 1.20 0.121E*05 0. 1.20 O.598E*04 0. 558.881 555.667

a 1.20 0.132E+05 0. 1.20 0.731E+04 0. 559.707 556.973

9 1.20 0.149E*05 0. 1.20 O.876E#04 0. 560.196 557.769

10 1.20 0.163E*05 0. 1.20 0.876E*04 0. 560.295 557.607

11 1.20 0.167E405 0. 1.20 0.876E*04 0. 560.280 557.801

12 1.20 O.198E.05 0. 1.20 O.876Ef04 0. 560.358 557.830

ROD HEAT TRANSFER FOR GROUP NUMa I

CONVECTIVE CELL AVERAGE QUANTITIES USED FOR ROD ENERGY TRANSFER 70 CHAN FLUID

0-

CELL1

2

3

4

5

6

7

8

0

MESH

2

3

4

5

6

7

TSUR-LIQ TSUR-VAP H-LIQ(CONV)

(K) (K) (wMe.2-K)

558.754 558.750 O.128EO05

563.092 562.904 O.149EO05

565.684 565.654 O.199E*05

566.634 566.629 0.238E*05

567.114 567.113 0.267E*05

567.198 567.198 0.273E405

566.509 566.500 0.258E405

565.124 565.100 0.232E+05

ROD COARSE MESH CONDUCTION

MESH CHF H-LIQ H-VAP

HT-MODE TRIP (W/M2-K) (W/M2-K)

1.20 0 0.128E*05 0.

2.02 0 0.132E405 0.

2.42 0 0.177E405 0.

2.42 0 0.221E+05 0.

2.42 0 0.254Eo05 0.

2.42 0 0.271E-05 0.

2.42 0 0.267E405 0.

H-VAP(CONV) OTOT(CONV) H-LIOIRAO) H-'

(WIM*02-K) (W) (W/M'*2-K) (W,

0.OOE-09 0.763E*OS 0.

O.IOOE-09 0.114E*UE. 0.

O.IO E-09 0.147E#0E. 0.

0.IOE-09 O.161E.OE. 0.

O.1OOE-09 O.172E#OE. 0.

O.100E-09 0.169E*OE. 0.

O.IODE-09 .0.140E40t. 0.

O.IOOE-09 0.935E*OE 0.

NFORMATION (MODE, TRIP AND TCHF USED ABOVE MESH

TCHFsTMIN RADIAL NODE TEMPERATURES (K)

(K) <CENTER

0.000 597.646 592.0(8 586.497 580.917

556.649

595.375 635.565 625.178 614.861 604.583

560.851

600.070 688.213 670.5e8 653.212 636.033

564.957

599.932 707.432 687.0(0 667.029 647.277

566.352

599.297 716.125 694.4e4 673.231 652.299

566.907

601.315 724.335 701.470 679.040 656.975

567.318

602.839 709.678 689.065 668.802 648.825

567.077

VAP(RAD) Q7IOT(CONV.RAD) IM'*2-K) (W)

0. 0.763E*05

0. O. 114E*D0

0. 0.147E#06

0. 0.161E*06

0. 0.172E#06

0. 0.169E.06

0. 0.140E*06

0. 0.935E*05

FLUID PROPERTIES FOR ALL

OTOT/FLUID ENER

(J/J)

0. 425E-05

0.594E-05

0.789E-05

0.943E-05

0. 109E-04

0. 130E-04

0. 112E-04

0. 157E-04

BUT TOP MESH)

557.942

563.147

568.625

570.502

571.275

571 .894

571.265

575.324

594.340

619.042

627.795

631.678

635.262

629. 125

569.664

584.069

602. 136

608..464

611.241

613.769

609.502

559.332

565.615

572.561

574.955

575.961

576.801

575.757
a 2.42 0 0.249E405

9 2.42 0 0.226E*05

0. 604.064 (.ill.34(1 0 oC,. 4 (413.'933 626.435 612.056 597.70f, 572.421 569.0U57

S.65.922

0. 604.566 625.053 616.659 600.303 599.960 591.625 583.2410 560.163 566.150

564.277

a IOTAL COMPONENT WATER MASS = 2.9242E*03 KG. TOAL COMPONENT WATER ENERGY = 3.7043E409 J.

PERCENT MASS CONTINUITY ERROR = 6.1873E-06 LOST MASS= 1.8093E-04 KG. PERCENT MASS FLOW TIHRU(TURNOVER)

00 s # EDITz a 0 9 9 s I s 9 • s • # s 1 0 s 0 s 0 # 

0-00- CHAN 614+ 436 CANALES INTERMEDIOS NSTEP= 281 TIME= 6.49375 DELI= 2.6178OE-012

O MAXIMUM SURFACE TEMPERATURE z 5.772382E+02. WHICH IS IN ROD GROUP 1. CELL 5

0 JUNI = 61 JUN2 - 64

= -2.0391E-03

. 0 04 44

CELL I FLOW RATE IN z 7.712E+03 KG/S

CELL It FLOW RATE OUT a 7.118E+03 KG/S

CELL 2 LEAK FLOW RATE2 5.940E+02 KG/S

MASS FLUX IN a 5.912E#03 KGIM2-S

MASS FLUX OUT - 2.064E403 KG/M2-S

LEAK MASS FLUX= 6.812E*03 KG/M2-S

CELL

I

2

3

4

5

6

7

8

t' 9o

12

PRESSURE

(PA)

7.319E+06

7.316E+06

7.310E+06

7.303E+06

7. 296E*06

7.288E#06

7.278E406

7.267E406

7.254E*06

1.240E+06

7.228E+06

VAPOR FRAC

0.000000

0.000000

0.000000

0.153812

0.358398

0.525501

0.632190

0.692971

0.731772

0.763037

0.769752

LIQ VEL

(M/S)

7.797

2.306

2.202

2.226

2.629

3.407

4.458

5.523

6.367

7.034

7.858

9.972

VAP VEL

(M/S)

8.272

2.613

2.345

3.166

3.102

4.214

5.605

7.275

8.803

10. 15

10.36

12.81

T SAT

(K)

562.047

562.014

561 .958

561.895

561.830

561.755

561.664

561.554

561.432

561.307

561. 186

7 LIQ

(K)

551.085

551.111

555.102

558.735

561.016

561.595

561.791

561.931

561.892

561.764

561.331

T VAP

(K)

562.047

562.034

561.958

561.895

561.828

561.753

561.660

561.547

561.421

561.281

561. 164

LIQ DEN

(KG/M3)

758.2

758.1

749.9

742.2

737.2

735.9

735.5

735.1

735.2

735.5

736.4

yAP DEN DELTA-P TOT

(KG/M3) (PA)

38.39 0.3411E405

38.37 3476.

38.33 6014.

38.29 6693.

38. 25 7012.

38.21 7961.

38.15 9710.

38.08 0.1170E05

38.01 0.1292E-05

37.93 0.1328E*05

37.85 O.1289E.05

0.2292E#05

I CHOKE

0 0

0 0

0 0

00a

0 0

0 0

0 0

0 0

0 0

a00

0 0

00

ICCF

0-2

0 0

O 0

0 0

0 0

0 0

a 0

O 0

00

0 0

0 0

U-I

0 INTERFACIAL HEAT TRANSFER (-=FLASH.-=CONDENSE) INTERFACIAL FRICTION

CELL

I

2

3

4

5

6

7

8

9

101

12

0

CELL

1

2

3

4

5

6

7

LIQ HTCOA VAPOR HTCOA WALL MASS

TRANSFER RATE

(W/K) (W/K) (KG/S)

0.2343E-06 0.1172E-06 0.

0.5949E-07 0.2974E-07 0.

0.3200E-07 0.1600E-07 0.

0.9147E*07 0.1634E*07 97.36

0.7041E+08 O.1476E*08 707.0

0.1089E409 0.4192E*08 745.3

0.1478E*09 0.5287E+08 755.7

0.3448E*09 0.4461E#08 155.1

0.4249E#09 0.4299E#08 E2.24

0.1947E409 0.2017E+08 15.36

TOTAL MASS

TRANSFER RATE

(KG/S)

-0.,1729E-11

-0.4365E-12

-0.1476E-12

77.92

168.4

233.5

268.2

242.1

213.0

74.62

TOT.E/(*LIQ

OR-VAP.E) (J/J)

-0.9295E-16

-0.3017E-16

-0.3020E-17

0.9144E-01

0.8495E-01

0.8044E-01

0.7389E-01

0.6621E-01

0.5305E-01

0.3559E-01

0.2585E-02

USED FOR WALL

THERMODYNAMIC SHEAR

QUALITY COEFFI

(KG/M3-S)

-0.039 9.14

-0.039 22.3

-0.025 80.4

0.001 641.

0.031 0.377E604

0.066 0.362E*04

0.104 0.228E#04

0.138 0.167E*04

0.168 0.136E.04

O.1DB 0. 114E604

0.183 0.178E.07

0.504E.07

ENERGY TRANISFER TO CHAN FLUID

SLIP

1.06

1.10

1.07

3.42

3.18

1.24

1.26

3.32

1.38

1.44

1.32

1.28

(A NEG.

REYGAS REYLIO

0.605E-09 0.147E

O.'315E-3O 0.232E

0.558E-33 0.225E

0.126E*05 0.210E

0.342E605 0.198E

0.673E#05 0.191E

0.106E406 0.188E

0.145E6 06 0.187E

O.IOE*06 0.104E

0.203E406 0.181E

0.231E4(16 0. 20E

HIC IS OK; SEE MANU

0.9361E08 0.3130E608 0.1889E-01 8.678

CONVECTIVE CELL AVERAGE QUANTITIES FOR

TSURF H-LIQ(CONV) H-VAP(CONV) (K) (WIM*02-K) (WIM*02-K)

551.203 0.2594E.05 0.

552.567 0.1877E*05 0.

555.169 0.2025E*05 0.

557.794 0.1584E405 0.

559.880 0.1789E+05 0.

560.864 0.2384E405 0.

561.340 0.2885E*05 0.

INNER CHAN WALL

QTOT(CONV)

(W)

0. 1097E+06

0. II0E+607

0. 1468E606

-0.1708E+07

-0.2329E+07

-0.1996E+07

-0.1553E607

H-LIQ(RAD) H-VAP(RAD)

(W/M*'2-K) (w/l"62-K)

0. 0.

0. 0.

0. 0.

0. 0.

0. 0.

0. 0.

0. 0.

QTOT(CONV.RAD)

(W)

0.10976E06

O.IIOIE0 07

0.1468E606

-0.1708E+07

-0.2329E*07

-0.11996E+07

-0.1553E.07

OTOT/FLUID ENERGY

(J/J)

0.3968E-05

0.5123E-04

0.2021E-05

-0.2547E-04

-0.4395E-04

-0.4827E-04

-0.4399E-04
8 561.667 O.3448E405 0.

9 561.744 O.3983E*0J 0.

10 563.567 0.4260E40S 0.

11 561.334 -0.6106E8O5 0.

0 WALL COARSE MESH CONDUCTION

( ........ INSIDE WALL CONDUCTION DATA...

MESH MESH H-LIO H-VAP

0 HT-MODE (W/M2-K) (W/M2-K)

3 1.20 O.377E*05 0.

2 1.20 0.200E+05 0.

3 1.20 0.187E*05 0.

4 1.20 0.175E+05 0.

5 1.20 0.179E+05 0.

6 0.20 0.217E*05 0.

7 0.20 0.274E*05 0.

8 1.20 0.331E405 0.

9 1.20 O.377E405 0.

10 1.20 0.414E*05 0.

II 2.42 0.4256E05 0.

12 1.20 0.507E*05 0.

-(0.9975E406 0. ().

-0.6738E406 0. 0.

-0.4825E406 U. 0.

-0.1500E405 0. 0.

INFORMATION (MODES USE ABOVE CELL FLUID

..... OUTSIDE WALL CONDUCTION DATA...

MESH H-LIQ H-VAP

HT-MODE (W/M2-K) (W/M2-K)

1.20 0.3006E04 0.

1.20 0.300E#04 0.

1.20 0.300E404 0.

1.20 0.300E+04 0.

3.20 0.300E404 0.

3.20 0.300E404 0.

3.20 0.3006E04 0.

1.20 01.553E404 0.

1.20 0.628E+04 0.

3.20 0.0206404 0.

1.20 0.82BE404 0.

1.20 0.8286E04 0.

- 11. 9 7!;Ei IIl. iI. :i.hllllf -04

-0.67313E .06 -II. 2503E3-04

-0.482.E.406 -0.3089E-04

-0.150DE,05 -0.7749E-06

PROPERTIES EXCEPT LAST ONE; H1-COEFF. ARE AVERAGE

WALL RADIAL NODE TEMPERATURES (K)

<INSIDE

551.164 551.730

551.241 551.787

553.893 553.471

556.445 555.094

559.143 556.011

560.617 557.750

561.112 558.065

561.560 559.741

561.767 560.735

561.722 560.717

561.412 560.597

561.256 560.536

ROD HEAT TRANSFER FOR GROUP HUM- I

CONVECTIVE CELL AVERAGE QUANTITIES USED FOR ROD ENERGY TRANSFER TO CHAN FLUID

T'-

0

TSUR-LIQ TSUR-VAP H-LIO(CONV)

CELL (K) (K) (W/M*02-K)

1 567.200 567.000 O.2398*05

2 572.414 572.251 0.341E305

3 575.780 575.780 0.419E605

4 577.006 577.002 0.4386*05

5 577.217 577.218 0.461E605

6 576.381 576.402 0.481E#05

7 573.793 573.824 0.484E405

8 570.032 570.030 0.474E+05

0 ROD COARSE MESH CONDUCTION

MESH MESH CHF H-LIQ H-VAP

I HN-MODE TRIP (W/M2-K) (W/M2-K)

1 2.02 0 0.221E405 0.

2 2.42 0 0.2896.05 0.

3 2.42 0 0.3913605 0.

4 2.42 0 0.4256.05 0.

5 2.42 0 0.445E*05 0.

6 2.42 0 0.473E*05 0.

7 2.42 0 O.484E.05 0.

a 2.42 0 0.487E+05 .0.

9 2.42 0 0.473E.05 0.

"H-VAP(CONV) QTOT(CONV)

(W/M*62-K) (W)

O.O00E-09 0.289E#06

O. IOOE-09 0.467E*06

0. 300E-09

0. 100E-09

0. 300E-09

0. 300E-09

0. 0OE-09

0. 006E-09

INFORMATION (MODE.

TCHFiTMIN

(K) <CENTI

600.490 747.61

0.619E#06 0.

0.675E*06 0.

0.712E606 0.

0.695E.06 0.

0.576E.06 0.

0.3926*06 0.

TRIP AND ICHF USED ABOVE ME

RADIAL NODE TEMPERATURES (

H-LIO(RAD)

(W/M *2-K)

0.

0.

H-VAP(RAD) OTOT(CONV.RAD) (W/M* e2-K) (W)

0. 0.289E+06

0.. 0.4676*06

0. 0.619E#06

0. 0.6756.06

0. 0. 712E406

0. 0.695E#06

0. 0.576E406

0. 0.392E406

'SH FLUID PROPERTIES FOR AL!

QTOT/FLUID ENER

(J/J)

0.397E-05

O.696E-05

0.117E-04

0. 163E-04

0. 202E-04

0.244E-04

0.214E-04

0.316E-04

L BUT lOP MESH)

ER80

601.713

602.332

605.048

605.923

605.165

603.728

601.909

602.892

564.292

924.438

569.708

1209.050

574.793

1323.297

576.766

1376.454

577.238

1427.599

577.198

1330.773

575.606

1091.643

572.042

848.425

568.017

720.653

868.061

1098.562

1189.468

1231.451

1271.633

1195.135

1004.148

805.195

694.241

814 153

995.730

1065.902

1097.989

1128.470

1069.977

921.912

763.489

668.359

762.485

899.956

951 .878

975.321

997.362

•. 1

954.571

844.496

723.3148

642.991

712.976

810.093

846.911

862.898

877.707

848.420

771.682

684.130

617.979

665.275

727.706

749.916

759.510

768. 165

750.417

702.860

646.176

575.266

589.134

605.682

611.663

613.945

615.637

60i.858

598.543

5s3.936

569.500

579.099

589.756

593.683

595.039

595.844

592.696

584.870

575.707

TOTAL COMPONENT WATER MASS =

PERCENT MASS CONTINUITY ERROR

8.1061E+03 KG. TOTAL COMPONENT WATER ENERGY = 1.0618E+10 J.

* 2.52546-05 LOST MASS= 2.04716-03 KG. PERCENT MASS FLOW THRU(TURIIOVERI x -7.6417E-04

00# 1 1 0 EDIT= as 1 0 # u 1DT 0 Sf 0 09 u #& 0 0u # u 9 00 0 0# I
-00- CHAIN 62,.. 80 CANALES CALIENTES NSTEP• 281 TIME: 6.49375

0 MAXIMUM SURFACE TEMPERATURE - 5.775008E*02. WHICH IS IN ROD GROUP 1. CELL 5

0 JUNI = 62 JUN2 a 65

DELT= 2.617eoE-02 60406*

CELL I FLOW RATE IN =

CELL II FLOW RATE OUT -

1.404E*03 KG/S

1.294E403 KG/S

MASS FLUX IN - 5.064E,03 KGIM2-S

MASS FLUX OUT - 2.045E*03 KG/M2-S

CELL 2 LEAK FLOW RATE- 1.097E*02 KG/S LEAK MASS FLUX= 6.856E*03 KG/M2-S

CELL1

2

3

4

5

6

7

8

9

10

11

12

0

CELL

2

3

4

5

6

7

a

9

10

11

12

PRESSURE VAPOR.FRAC LIQ VEL

(PA) (M/S)

7.3206.06 0.000000 7.734

7.317E*06 0.000000 2.366

7.311E*06 0.000000 2.181

7.304E406 0.162546 2.206

7.297E*06 0.371106 2.630

7.289E406 0.537287 3.437

7.280E406 0.641313 4.513

7.268E406 0.701210 5.582

7.256E+06 0.758117 6.438

7.241E*06 0.770736 7.667

7.228E+06 0.777566 7.976

10.14

VAP VEIL

(M/S)

8 .206

2.592

2.324

3.165

3. 139

4.268

5.708

7.413

8.980

10(.09

1(0.57

13.06

T SAT

(K)

562.057

562.025

561 .969

561 .907

561.842

561.768

561.676

561 .567

561.450

561.308

561 191

T LIQ

(K)

551.086

551.114

555.222

558.847

561.100

561.621

561.851

561.973

561.973

561.787

561.339

T VAP

(K)

562. 057

562,025

561.969

561.907

561.841

561 766

561.673

561.559

561.439

561 277

561. 168

LID DEN

(KG/M3)

758.2

758.1

749.7

741.9

737.0

735.9

735.3

735.0

735.0

735.4

736.4

VAP DEN

(KG/M3)

38.40

38.38

38.34

38.30

38.26

38.21

38.16

38.09

38.02

37.93

37.86

DELlA-P TOT

(PA)

0.3364E405

3441.

5941.

6591.

6943.

7936.

9736.

0.1170E605

0.1238E*05

0.1511E605

0.1238E405

0.2348E*05

ICHOKE

00

00

00

00

00

00

00

00

00

00

00

00

ICCF

0-2

a 0

0 0

0 0

0 0

0 0

0 0

0 0

0 0

0 0

0 0

0-1

INTERFACIAL HEAT TRANSFER (4-FLASH.-:CONDENSE) *INTERFACIAL FRICTION

-4

LIQ HTCOA VAPOR HTC*A WALL MASS

TRANSFER RATE

(W/K) (WlK) (KG/S)

0.4657E-07 0.2329E-07 0.

0.1175E-07 0.5875E-0O8 0.

0.6373E-08 0.3186E-08 0.

0.1863E*07 0 33468*06 19.12 0.1470E.08 0 3122E+07 39.46

0.1992E*08 0.8717E*07 46.26

0.3306E.08 0.9596E607 46.36

0.6849E608 0.8062E407 27.00

0.8535E+08 0.7372E+07 9.821

0.3708E*08 0.3640DE07 2.415

0.1698E+08 0.5611E607 0.1672E-02

TOTAL MASS

TRANSFER RATE

(KG/S)

-0.3439E-12

-0.8629E-13

-0.2893E-13

IS: 29

32.12

44.28

50.20

45.67

39.73

14.26

1.603

TOT.E/(*LIQ

OR-VAP.E)

(J/J)

-O.IOOBE-15

-0.32518- 16

-0.3224E-17

0.925;E-01

0.8524E-0I

0.8128E-0I

0.7430E-01

0.6725E-01

0.5203E-01

0.3671E-01

0.2576E-02

THERMODYNAMIC

QUALITY

-0.039

-0.039

-0.024

0.002

0.033

0.070

0.108

0.144

0.181

0.188

0.190

SHEAR

COEFF!

(KG/M3-S)

9.18

22.4

80.4

656.

0.3896.04

0.359E.04

0.223E404

0.163E404

0.130E404

0.112E*07

0.301E407

SLIP

I.06

I.10

1.07

1 43

1. 19

1.24

1.26

1.33

1.39

1.32

1.33

1.29

(A NEG.

REYGAS REYLIQ

0.649E-09 0. 146E

0.335E-10 0.230E

0.601E-I1 0.223E

0 134E405 0.207E

0.3596*05 0.195E

0.699E*05 0.189E

0.110.E06 0.186E

0.150E+06 0.184E

0.188E*06 0.175E

0.206E+06 0.184E

0.238E606 0.206E

0 CONVECTIVE CELL AVERAGE QUANTITIES F HTC IS OK; SEE MANU

TSURF H-LIO(CONV) H-VAP(CON%

CELL (K) (W/MO$2-K) (W/M*62-KJ

1 551.259 0.2591E+05 0.

2 552.646 0.18668*05 0.

3 555.230 0.3128E+05 0.

4 557.799 0.1578E+05 0.

5 559.829 0.1824E*05 0.

6 560.792 0.2417E#05 0.

7 561.288 0.2937E*05 0.

8 561.657 0.3491E*05 0.

9 561.760 0.4008E405 0.

10 561.563 0.4312E+05 0.

11 5E1.309 0.5799E405 0.

0 WALL COARSE MESH CONDUCTION

( ........ !NSIDE WALL CONDUCTION DATA ....

MESH VESH H-LIQ H-VAP

0 HI-MODE (W/M2-K) (W/M2-K)

1 1.20 0.3758*05 0.

2 1.20 0.198E+05 0.

:OR INNER CHAN WALL USED FOR WALL ENERGY TRA

QTOT(CONV) H-L1i (RAD) H-VAP(RAD)

) (W) (W/M0e2-K) (W/M*02-K)

0.2941E605 0. 0.

0.2113E+06 0. 0.

5069. Er. 0.

-0.3477E806 0. 0.

-0.4876E*06 0. 0.

-0.4214E406 0. 0.

-0.3618E406 0. 0.

-0.2227E406 0. 0.

-0.17926.06 0. 0.

-0.1018E*06 0. 0.

-0.2600E605 0. 0.

INFORMATION (MODES USE ABOVE CELL FLUID PR

..... OUTSIDE WALL CONDUCTION DATA .....

MESH H-LIQ H-VAP

HT-MOOE (W/M2-K) (W/M2-K)

1.20 0.447E404 0.

1.20 0.447E404 0.

0.737E+07

NSFER TO CHAN FLUID

QTOT(CONV+RAD) Q

(w)

0.2941 E+05

0.2113E+06

5069.

-0.3477E*O6

-0.4876E*06

-0.4214E406

-0.3618E#06

-0.22276*06

-0.1792E+06

-0.1018.E06

-0.2600E605

OPERTIES EXCEPT LAS• )

WALL RADIAL

<INSIDE

551.205 552.05)

551.313 552.11

TOT/FLUID ENERGY

(J/J)

0.5799E-05

0.5357E-04

0.3801E-06

-0. 2851-04

-0.51OIE-(14

-0.566)E-04

-0. 5694E-04

-0.4353E-04

-0.3893E-04.

-0.45718-04

-0.7488E-05

T ONE: HT-COEFF. ARE AVERAGE

NODE TEMPERATURES (K)

7
3

4

5

6

7

a

9

10

11

12

I. 20

1.20

1.2U

0.20

0.20

0.20

I .20

1 .20

2.42

1.20

0. 165E*0(l

0.173E405

0.179E,05

0. 219E405

0.277E405

0.336E*05

0.360E405

0.419E*05

0.430E405

0.513E405

II.

U.

0.

0.

0.

0.

0.

0.

0.

1.20

1.20

1.20

.20

1.20

1.20

1.20

,.20

1.20

1.20

0.447E404

0.447E*04

0.447E404

0.447E*04

0.447E*04

0.628E*04

0.B25E04

0.825E404

0.825E*04

0.825E404

0.

0.

0.

0.

0.

0.

0.

0.

0.

0.

553.979

556.481

559.117

560.541

561.043

561.533

561.781

561.740

561.387

561.231

553.554

554.904

556.328

557.098

557.370

559. 128

560.391

560.375

560.238

560.177

ROD HEAT TRANSFER FOR GROUP HUMa

CONVECTIVE CELL AVERAGE QUANTITIES USED FOIR ROD ENERGY TRANSFER TO CHAN FLUID

CELL

2

3

4

5

6

7

0

0

TSUR-LIQ

(K)

567.448

572.654

576.046

577.277

577.482

576.648

574.018

570. 182

RO

-4

N,

MESH MESH

& HT-MODE

I 2.02

2 2.42

3 2.42

4 2.42

5 2.42

6 2.42

7 2.42

a 2.42

9 2.42

TSUR-VAP H-LIO(CONV)

(K) (W/MO$2-K)

567.247 0.241E#05

572.494 0.347E*05

576.046 0.424E*05

577.274 0.442E+05

577.482 0.466E*05

576.669 0.486E4O5

574.053 0.489E+05

570.177 0.480E*O5

0D COARSE MESH CONDUCTION

CHF H-LIQ H-VAP

TRIP (W/M2-K) (W/M2-K)

0 0.223E*05 0.

0 0.293E*05 0.

O 0.396E*05 0.

0 0.429E*05 0.

0 0.450E*05 0.

0 0.476E#05 0.

0 0.469E+05 0.

0 0.492E+05 0.

0 0.478E405 0.

H-VAP(CONy)

(WIMO$2-K)

0. 100E-09

0. 100E-09

0. IOOE-09

0. IOOE-09

0. IOOE-09

0. IODE-09

0. 100E-09

0. 100E-09

INFORMATION (MODE.

TCHF TMIN

(K) <CENTI

600.778 752.9

QTOTICONV) H-LIO(RAD)

(w) (W/M*#2-K)

O.295E106 0.

0.479E406 0.

0.633E406 0.

0.692E406 0.

0.729E106 0.

0.713E#06 0.

0.589E406 0.

0.403E*06 0.

TRIP AND TCHF USED ABOVE MI

RADIAL NODE TEMPERATURES I

ER

II

601.566

602.468

605. 128

605.899

605.004

602.614

602.466

602.536

564.550

934.972

569.943

1229.338

575.046

1347.767

577.046

1402.865

577.501

1455.940

577.464

1355.555

575.874

1107.729

572.231

856.418

568. 123

725.082

876.726

1114.740

1208.823

1252.272

1293.919

1214.721

1017.107

811.823

697.906 671.293

821 .097

1008.249

1080.724

1113.860

1145.391

1084.963

932.059

768.842

767.843

909.242

962.737

986.880

1009. 625

965.538

852.121

727.310

645.227

716.878

817.345

854.346

870.754

885.989

855.918

777.059

687.181

619.546

667.837

731.680

754.408

764.206

773.075

754.937

706.234

648.187

575.791

589.031

606.675

612.771

615. O8

616. 822

611.969

599.370

584.42

H-VAP(RAD) QTOT(CONV*RAD)

(W/M**2-K) (W)

0. 0.295E*06

0. 0.479E*06

0. 0.633E*06

0. 0.692E406

0. 0.729E406

0. 0.713E.06

0. 0.569E*06

0. 0.403E406

ESH FLUID PROPERTIES FOR ALL

QTOT/FLUID ENER

(J/J)

0.221E-04

0.393E-04

0.663E-04

0.930E-04

0.115E-03

0. 139E-03

0.128E-03

0.181E-03

BUT TOP MESH)

0 569.975

6 579.560

5 590.370

1 594.371

5 595.730

2 596.559

9 593.376

0 585.369

7 576.000

0 TOTAL COMPONENT WATER MASS =

PERCENT MASS CONTINUITY ERROR

O0 0 0 & I EDIT- a 0 & 0 * g g

1.4627E+03 KG. TOTAL COMPONENT WATER ENERGY 1.9192E*09 J.

a 2.7036E-05 LOST MASSz 3.9549E-04 KG. PERCENT MASS FLOW THRU(IURNOVER) = 4.3996E-03

m m m m m mm mm mm m m m m

-**6- TEE

0 JUNI = 8

PRIMARY TUBE

80- RAMA DE DESCARGA

JUN2 - 80 JUN3 - 90

NSTEP= 281 TIME= 6.49375 DELT= 2.61780E-02 o00000

CELL I FLOW RATE IN = 1.565E*03 KG/S MASS FLUX IN - 1.565E*02 KG/M2-S

CELL 6 FLOW RATE OUT = 1.565E*03 KG/S MASS FLUX OUT a 1.660E403 KG/M2-S
PRESSURE

CELL (PA)

1 7.132E406

2 7.010.E06

3 6.998E+06

4 6.993E*06

5 6.991E*06

6 6.326E*06

7

0

LIO HTC*A

CELL

(W/K)

1 0.2459E*05

2 0.1936E*06

3 0.4453E605

4 0.5702E+05

5 0.5049E+05

6 0.1230E*06

7

VAPOR FRAC LIQ VEL VAP VEL T SAT 1 LIO

(M/S) (MIS) (K) (K)

0.999998 5.044 4.166 560.283 560.283

0.999971 43.67 44.38 559.108 559.100

0.999965 44.79 45.01 558.987 559.988

0.999956 44.88 45.08 558.942 558.943

0.999949 44.93 45.11 558.926 558.926

0.999924 178.9 180.2 552.232 552.484

49.93 48.85

INTERFACIAL HEAT TRANSFER (*zFLASH.-:CONDENSE)

VAPOR HTC'A WALL MASS TOTAL MASS TOT.E/(*LIQ

TRANSFER RATE TRANSFER RATE OR-vAP.E)

(W/K) (KG/S) (KG/S) (J/J)

0.7023E+05 0. -0.2418E-01 -0.2409

0.9681E*06 0. -0.8491 -0.1608

0.2226E#06 0. -0.2041 -0.1510

0.2851E*06 0. -0.2591 -0.1203

0.2525E*06 0. -0.2245 -0.9868E-01

0.2532E+06 0. -1.077 -1.648

7 VAP

(K)

559.767

557.788

557.606

557.573

557.586

545.521

LI DElI

(KG/M3

738.5

740.9

741.1

741.2

741.3

753.8

VAP DEH

) (KG/M3)

37.41

36.87

36.81

36.78

36.76

33.93

INTERFACIAL

SHEAR

COEFFI

(KG/M3-S)

1.32

33.1

0.941

0.710

0.462

759.

107.

(OELIA-P 101

(PA)

0.3688E405

0. 1224E*06

0.1246E405

4650.

1695.

0.6649E406

-0.5697E#06

FRICTION

SL|IP RE)

I CHOKE

0 0

00

00

00

0 0 00

00

ICCF

a 0

0 0

0 0

a 0

0 0

0 0

0 0

THERMODYNAMIC

QUALITY

0.998

0.995

0.995

0.995

0.995

0.978

YGAS I#EYLI1

0.826

1.02

I.00

1.00

1.00

1.01

0.978

0. 261E408

0. 476E408

0.479E408

0.479E408

0.890E608

0.874E*08

184.

0.548E

0.680E

0.839E

0. 183E

0.276E

SIDE TUBE

CELL I FLOW RATE OUT a -9.920E-07 KG/S MASS FLUX OUT a -3.481E-06 KG/M2-S

PRESSURE VAPOR FRAC LID VEL YAP VEL T SAT T LIQ T YAP LIQ DEN YAP DEN DELIA-P lOT

CELL (PA) (MIS) (M/S) (K) (K) (K) (KG/M3) (KG/M3) (PA)

I 6.993E*06 1.000000 -1.305 -0.1564E-05 558.930 558.938 556.562 741.2 36.56 431.2

2 -1.991 -0.7009E-07 414.6

0 INTERFACIAL HEAT TRANSFER (I.FLASH.-=CONDENSE) INTERFACIAL FRICTION

LIQ HTCOA VAPOR HTCOA WALL MASS TOTAL MASS TOT.E/(.LIQ THERMODYNAMIC SHEAR SLIP

CELL TRANSFER RATE TRANSFER RATE OR-VAP.E) QUALITY COEFFI

(W/K) (W/K) (KG/S) (KG/S) (J/J) (KG/M3-S)

1 4738. 23.18 0. -0.5785E-05 -0.1770E-01 0.526 0.144 0.120E-05 0

2 0.219 0.352E-07

0 TOTAL COMPONENT WATER MASS a 6.0102E*02 KG. TOTAL COMPONENT WATER ENERGY z 1.5483E*09 J.

PERCENT MASS CONTINUITY ERROR x -6.7263E-03 LOST MASS= -4.0425E-02 KG. PERCENT MASS FLOW THRU(TURNOVER)

Do # p a # EDIT= 8 9 0 & & 0 0 0 0 0 0 g # # p # 0 & 0 0 0 0 9 0 0 9 0 # A

I CHOKE

00

00

ICCF

0 0

0 0

REVGAS REYLIQ

.237 0.426E

5.17B1E-03

0 1

CELL

2

3

4

VALVE 61.+ VALV. AISLAMIENTO VAPOR PRINCIPAL

JUNI - 80 JUN2 = 81

CELL I FLOW RATE IN : 1.565

CELL 3 FLOW RATE OUT x 1.565

PRESSURE VAPOR FRAC LIQ VEL YAP VEL T

(PA) (M/S) (M/S)

6.896E*06 0.999891 49.93 48.85 55

6.856E+06 0.999861 46.13 45.73 55

6.810E*06 0.999827 46.10 45.96 55

NSTEPS 281 TIME= 6.49375 DELT= 2.61780E-02 *****.

E603 KG/S

E.03 KG/S

SAT T LI

(K) (K

7.999 557.5

7.605 557.6

7.152 557.1

SH.-=CONDENSE)

0

74

96

MASS FLUX IN =

MASS FLUX OUT -

7 VAP

(v)

556.519

555.981

555.372

1.660E403 KG/M2-S

1.660E403 KGIM2-S

10 DEN VAP DEN DELTA-P TOT

(KG/M3) (KG/M3) (PA)

744.0 36.23 0.

743.9 36.03 0.4012E*05

744.7 35.79 0.4594E+05

8970.

INTERFACIAL FRIC7ION

I CHOKE

0 0

00

00

0 0

ICCF

0 0

0 0

0 0

46. 15 46.23 0 0

0 INTERFACIAL HEAT TRANSFER (-:FLA
LIO HICOA VAPOR HTC*A WALL MASS

CELL TRANSFER RATE

(w/K) (W/K) (KG/S)

I 0.1608E#06 0.8042E+06 0.

2 0.1765E+06 O.8Q23E*06 0.

3 0.2035E*06 0.9671E*06 0. 4

1OTAL MASS

TRANSFER RATE

(KG/S)

-0.8317

-0.9458

-I. 128

TOT.E/(4LIQ

OR-YAP.E)

J•. W)

-0.5963E-01

-0.5348E-01

-0.5112E-01

THERMODYNAMIC

QUALITY

0.993

0.992

0.991

S1tEAR

COEFF I

IKG/M3-SJ

0.

5.94

0.331

0.733E-01

SL I P

0.978

0.991

0.997

1. 00

REYGAS REYLIQ

0.497E408 0.224E

O.48OE4O8 0.273E

O.480E408 0.341E

VALVE AREA - 9.425000E-01 PERCENT OPEN = 100.00000

0 TOTAL COMPONENT WATER MASS a 5.8900E*02 KG. TOTAL COMPONENT WATER ENERGY = 1.5157E*09 J.

PERCENT MASS CONTINUITY ERROR = 1.5947E-05 LOST MASSm 9.3926E-05 KG. PERCENT MASS FLOW rIIRU(TIIRNoVERI z -2.5441E-04

0# # # s # EDIT: a 1 0 0 0 9 & # 0 # * # 0 0 0

-**a- TEE

0 JUNI , 81

PRIMARY TUBE

82+- MSIV-TURBINA/BYPASS

JUN2 a 82 JUN3 u 70

CELL I FLOW RATE IN -

CELL 9 FLOW RATE OUT a

NSTEPx 281 TIMEs 6.49375 DELTs 2.617B0E-02 00*

1.565E+03 KG/S

1.565E+03 KG/S

MASS FLUX IN - MASS FLUX OUT a 1.660E*03 KG/M2-S

1.235E*03 KG/M2-S

T'

CELL

2

3

4

5

6

7

8

9

10

PRESSURE

(PA)

6.801E406

6.795E+06

6.794E406

6.788E*06

6.776E*06

6.763E÷06

6.759E.06

6.764E406

6.763E406

VAPOR FRAC

0.999764

0.999739

0.999695

0.999680

0.999628

0.999614

0.999598

0.999589

0.999582

.LIQ VEL

(MIS)

46.15

46.20

41.30

41.17

41.12

40.94

40.69

35.45

35.08

35.04

VAP VEL

(MIS)

46.23

46.33

40.79

40.83

40.86

40.96

41.03

34.75

34.73

34.74

T SAT

(K)

557.063

557.004

556.989

556.931

556.813

556.687

556.641

556.695

556.685

T LIQ

(K)

557.071

557.014

556.991

556.947

556.822

556.723

556.649

556.678

556.683

T VAP

(K)

555.609

555.687

555.947

555.936

556.047

.555.890

555.991

556.119

556.146

LIT DEN

(KG/M3)

744.9

745.1

745.1

745.2

745.4

745.6

745.8

745.7

745.7

VAP DEN

(KG/M3)

35.67

35.61

35.54

35.50

35.38

35.31

35.25

35.27

35.26

DELTA-P TOT

(PA)

0.

6011.

1485.

5784.

0. 1195E605

0.1273E.05

4561.

-5427.

995.3

665.3

0

0

0

0

0

0

0

0

0

o

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

ICHOKE ICCF

0 INTERFACIAL HEAT TRANSFER (*=FLASH.-=CONDENSE) INIERFACIAL FRICTION

LID HTCOA VAPOR HTCSA

CELL

I

2

3

4

5

6

7

8

9

10

(W/K)

0.4231E*06

0.2195E406

0.4219E*06

0.1450E*06

0.7520E+06

0. 1636E+06

0.SBIOE*06

0. 1 165E*06

0.2118E*06

(W/K)

0.2111 E.07

0. 1094E.07

0. 2109E607

0. 7205E606

O .3283E407

0.7135E+06

0. 2164E*07

0. 3798E+06

0. 6384E+06

WALL MASS

TRANSFER RATE

(KG/S)

0.

0.

0.

0.

0.

0.

0.

0.

0.

TOTAL MASS

TRANSFER RATE

(KG/S)

-2.019

-0.9468

-1.445

-0.4707

-1.649

-0.3697

-0.9214

-0.1451

-0.2265

TOT.E/(#LIQ

OR-VAP.E)

(J/J)

-0.4088E-01

-0.3699E-01

-0.2931E-01

-0.2795E-01

-0.1882E-01

-0.2006E-01

-0.1362E-01

-0.1067E-01

-0.9165E-02

THERMODYNAMIC

QUALITY

0.990

0.990

0.990

0.990

0.990

0.989

0.989

0.999

0.989

SHEAR

COEFFI

(KG/M3-S)

0.

0.412

14.5

5.20

2.28

0.985E-03

6.08

15.2

2.03

1.23

SLIP

1 .00

1.00(

U .988

0.992

0.994

t.00

I .fll

0.911O

0.990

0.992

REYGAS REYLIO

0 .400E#08

0. 451E.90

0.421E#08

0.421E*00

0.420E*08

0. 42(6E.08

0.41BE408

0.412E*08

0 .411 E08

0.464E

0.406E

0.537E

0.561E

0. 650E

0.671E

0. 704E

0.7 15E

0. 724E

SIDE TUBE

CELL 2. FLOW RATE OUT - -3.649E-05 KG/S MASS FLUX OUT = -7.297E-05 KG/142-S

PRESSURE VAPOR FRAC LI VEL

CELL (PA) (M/S)

I 6.762E*06 1.000000 -1.906

VAP VEL T SAT

(M/S) (K)

-0.1107E-04 556.680

T LI T VAP LI0 DEN VAP DEN DELIA-P 10T

(K) (K) (KG/M3) (KG/M3) (PA)

556.680 555.960 745.7 35.29 694.3

IClIOKE ICCF

60 00
6.;GIE406 1.000000 -2.265 -0.1225E-O4 556.668 !E6.668 555.971 745.7 35.20 1143. o i U (Ii

3 -0.5695E-02 -0.1423E-05 0.1171E-03 0 0 II 0

0 INTERFACIAL HEAT TRANSFER (4=FLASH.-=CONDENSE) INTERFACIAL FRICTION

LID HTC*A VAPOR HTCOA WALL MASS TOTAL MASS TOT.E/(4LIQ THERMODYNAMIC SHEAR SLIP REYGAS REVLIO

CELL TRANSFER RATE TRANSFER RATE OR-VAP.E) DUALITY COEFFI

(WIK).. . (W/K)- .- -----. (KG/S)- (KG/S) (J/J) (KG/M3-S)

I 0.6403E+O5 508.9 0. -O.2407E-03 -0.7061E-02 0.445 0.140 O.581E-U5 1U.3 2.52

2 495.4 0.6208E¥05.. 0. -0.2272E-03 -0.7386E-02 0.489 0.945E-01 0.541E-05 5.08 1.04 3 0.417E-02 0.250E-03

0 TOTAL COMPONENT WATER MASS 1 1.9423E+03 KG. TOTAL COMPONENT WATER ENERGY = 4.9970E*09 J.

PERCENT MASS CONTINUITY ERROR : -7.9458E-07 LOST MASS= -I.5433E-05 KG. PERCENT MASS FLOW 1HRtI(TURNOVER) z -2.4951E-03

o0s # 0# EDITx 8aI I0 # DD# 0 I0 0 , 0 0 1 I I # 0 DD, 0 # 0 # # i 0 # #

-0e0- VALVE

0 JUNI - 82

83.. VALV. CONTROL DE TURBINA

JUN2 a 83

NSTEP= 281 TIME: 6.49375 DELT- 2.61780E-02 00**00

CELL

I

2

3

0

CELL

2

3

PRESSURE

(PA)

6.762E06

6.762E406

LIO HTCOA

(W/K)

0.1072E*06

0.1072E06

CELL I FLOW RATE IN a 1.565E.03 KG/S MASS

CELL 2 FLOW RATE OUT a 1.565E#03 KG/S MASS

VAPOR FRAC LIQ VEL VAP VEL T SAT T LIQ

(MIS) (MIS) (K) (K)

0.999577' 35.04 34.74 556.679 556.680

0.999577 35.04 34.89 556.679 556.679

35.11 34.75

INTERFACIAL HEAT TRANSFER (+:FLASH.--CONDENSE)

VAPOR HTCOA WALL MASS TOTAL MASS TOT.E/(+LIQ

TRANSFER RATE TRANSFER RATE OR-VAP.E)

(W/K) (KG/S) (KG/S) (J/J)

0.3115E*06 0. -0.1070 -0.8559E-02

o.2976E.06 0. -0.9847E-01 -0.786AE-02

FLUX IN •

FLUX OUT a

T VAP

(K)

556.155

556.175

1.235E403 KG/M2-S

1.235E.03 KGIM2-S

LIQ DEN VAP DEN

(KG/M3) (KG/M3)

745.7 35.25

745.7 35.24

DELTA-P TOT

(PA)

0.

6.222

7304.

FRICTION

SLIP

I CHOKE

00

00

0 a

ICCF

0 0

0 0

00

L'

0.T

THERMODYNAMIC

QUALITY

0.989

0.989

INTERFACIAL

SHEAR

COEFFI

(KG/M3-S)

0.

0.160

2.30

REYGAS REYLIO

).992

0.996

0.990

0.411E.08 0.730E

0.411E+08 O.731E

VALVE AREA z 1.261706E+00 PERCENT OPEN : 99.58214

VALVE HYDRAULIC DIAMETER a 6.324E-O1

0 TOTAL COMPONENT WATER MASS - 9.0077E+01 KG. TOTAL COMPONENT WATER ENERGY : 2.3153E*08 J.

PERCENT MASS CONTINUITY ERROR x -1.9686E-07 LOST MASS- -I.7732E-07 KG. PERCENT MASS FLOW THRU(TURNOVER) • 7. 1146E-04

0 9 a 9 0 EDIT= 8 • 0 0 0 # 0 0 & 1 v # I # 5 # # a I # 0 # # I p 5 # # I

-0.0- VALVE

0 JUNI : 90

PRESSURE

CELL (PA)

I 6.992E.0

2 1.853E+0

3 1.853E40

90+. VALV. AL

JUN2 - 91

CELL 1

CELL 5

VAPOR FRAC

6 1.000000

5 1.000000

)5 1.000000

IVIO-SEGURIDAD NSTEP= 281 TIME: 6.49375 DELT: 2.61780E-02 *00004

FLOW RATE IN 2 -9.920E-07 KG/S

FLOW RATE OUT x 7.758E-08 KG/S

LIQ VEL VAP VEL T SAT T LIQ

(M/S) (M/S) (K) (K)

-1.991 -0.7009E-07 558.934 558.934

0.1000E-O9 0.100OE-09 390.369 390.369

1.935 0.2343E-06 390.371 390.371

MASS FLUX IN

MASS FLUX OUT

T VAP

(K)

558.580

390.198

390.223

* -3.481E-06 KG/M2-S * 2.722E-07 KG/M2-S

LIQ DEN VAP DEN

(KG/M3) (KG/M3)

741.2 36.55

941.5 1.029

941.5 1.029

DELTA-P TOT

(PA)

0.

0.6807E*07

-10.55

ICHOKE

00

0-2

0.-1

ICCF

0 0

0 0

0 0
4 I.153E+05 1.0(loi0t0O .UII 0.5985E-06 390.377 390.377

5 1.1154E*05 1.000000 3.031 0.3510E-06 390.389 390.389

6 3.030 -0.1200E-09

0 INTERFACIAL HEAT TRANSFER (43FLASH.-=CONDENSE)

LIQ HTC$A VAPOR HTCOA WALL MASS TOTAL MASS TOT.E/(#LIQ

CELL TRANSFER RATE TRANSFER RATE OR-VAP.E) (W/K) (W/K) (KG/S) (KG/S) (J/J)

1 212.7 1.113 0. -0.2619E-06 -0.5096

2 974.7 0.4844 0. -0.3738E-07 -0.2261

3 1684. 0.8729 0. -0.5819E-07 -0.1041

4 0.2267E-01 0.1134E-01 0. 0.3866E-07 0.6148E-09

5 0.4375E-01 0.2187E-01 0. 0.4953E-07 0.4896E-09

6

397.934

395.407

941 .5

941 .5

THERMODYNAMIC

QUALITY

0.735

0.647

0.605

0.688

0.398

1.00B -37.77

1.015 -70.51

.87.6U1

INTERFACIAL FRICTION

SHEAR SLIP

COEFF!

(KG/M3-S)

0. 0.352E-07

0. 1.00

0.193 0.121E-06

0.290 0.206E-06

0.302 0.116E-06

0.303 -0.395E-1U

0-I 0 0 0-I Oil

09 a U

REYGAS REYLIO

O.508E-02

0.71BE-03

0.5 (IE-O2

0.556E-02

0.209E-02

0. 365E

0.201E

0. 171E

0. 136E

0. I 6E

VALVE AREA = 0.O00000E+00 PERCENT OPEN = 0.00000

VALVE HYDRAULIC DIAMETER - 1.OOOE-05

0 TOTAL COMPONENT WATER MASS - 5.7281E600 KG. TOTAL COMPONENT WATER ENERGY = 1.457OE407 J.

PERCENT MASS CONTINUITY ERROR z 2.7311E-07 LOST MASS- 1.5644E-08 KG. PERCENT MASS FLOW THRU(TURNOVER) z 2.2093E-05

0#IID EDIT= 8a 9 • • 0 • IDDI0 8 1 1 D•••

-***- VALVE

0 JUNI a 70

C• CELL

1

2

3

PRESSURE

(PA)

6.761E*0

6.600E+0

LIO HTCOA

(W/K)

6936.

0.1886E.

70++ VALVULA BYPASS TURBINA NSTEPz 281

JUN2 a 71

CELL I FLOW RATE IN - -3.649E-05 KG/S MAS

CELL 2 FLOW RATE OUT a 2.586E-04 KG/S MAS

VAPOR FRAC LIQ VEL VAP VEL T SAT T LID

(M/S) (M/S) (K) (K)

6 0.999995 -0.5695E-02 -0.1423E-05 556.668 556.668

6 0.999991 0.10OOE-09 O.OOOE-09 555.050 555.050

0.8557E-02 0.1325E-04

INTERFACIAL HEAT TRANSFER (+=FLASH.-=CONDENSE)

VAPOR HTCOA WALL MASS TOTAL MASS TOT.E/(*LIQ

TRANSFER RATE TRANSFER RATE OR-VAP.E)

(W/K) (KG/S) (KG/S) (J/J)

63.26 0. -0.2884E-04 -O.4608E-03

05 209.7 0. -0.2581E-03 -0.2431E-02

S FLUX IN

S FLUX OUT

T VAP

(K)

555.975

553.164

TIME- 6.49375 DELTz 2.617S0E-02 00#060

LIO DEN

(KG/M3

745.7

748.9

VAP DEN DELTA-P TOT

) (KG/M3) (PA)

35.28 0.

34.59 0.1613E 06

-0.3476E-04

INTERFACIAL FRICTION

SHEAR SLIP RE)

COEFFI

(KG/M3-S)

0. 0.250E-03 0.21

0. 1.00 2.

0.417E-02 0.155E-02

ICHOKE

00

00

0a

ICCF

0 0

0 0

0 0

- -7.297E-05 KG/M2-S

2 5.172E-04 KG/M2-S

CELL

1

2

3

THERMODYNAMIC

QUALITY

0.686

0.881

rGAS REYLIO

6444 0. 236E

0. 607E

VALVE AREA = 0.000000E*00 PERCENT OPEN = 0.OCOOO

VALVE HYDRAULIC DIAMETER z 1.O0OE-05

0 TOTAL COMPONENT WATER MASS x 3.4937E+01 KG. TOTAL COMPONCNT WATER ENERGY = 9.0134E+07 J.

PERCENT MASS CONTINUITY ERROR = -4.6750E-05 LOST MASS= -1.6334E-05 KG. PERCENT MASS FLOW THRU(TURNOVER) = 5.5065E-03

O 0 0 0 0 EDIT= a 0 • • N • • 0 s # • 0 a 6 0 • #I • • 0 0 0 # a 0 'r •

-000- BREAK 92++ TURBINA NSTEP= 281 TIME- 6.49375 DELT= 2.61780E-02 000*00

0 JUNI c 83
PRESSURE

CELL IPA)

i 6.755E*06

0 MASS FLOW RATE

O I # s I EDITVAPOR FRAC LIO VEL VAP VEL

(MIS) (MIS)

1.000000 35.11 34.75

" l.5649E*03 TOTAL

8 0 # a • I # D# I I

1 •Al

(K)

556.606

MASS OUT -

1I # # 1 0

1 tI(. I VAP LIO DElI yAP DrEi DELIA-P 101

flli 1K) (KG/M3) I(KGIM3) (PA)

55C..L5G 556.556 746.0 35.11 0.

1.0162E*04

# 9 * 0 # 0 • 9 0

ICII(IKF ICCF

0 0 00

.***- BREAK

0 JUNI a 91

914+ ESCAPE VALVULAS ALIVIO NSTEP- 281 TIME- 6.49375 DELIs 2.61780E-02 $00000

.PRESSURE VAPOR FRAC LIB VEL

CELL (PA) (MIS)

I I.8556E 05 1.000000 3.039

0 MASS FLOW RATE a 7.7579E-08

0D # # # # EDIT- 8 # f I# # I 9 I

VAP VEL T SAT

(MIS) MK)

-D.1200E-09 390.403

TOTAL MASS OUT a

T LIO T VAP LIQ DEN VAP DEN DELTA-P TOT

(K) |9) (KGIM3) (KG/M3) (PA)

390.403 390.403 941.5 1.030 0.

-8.3338E-07

# f # 0 D& # II

ICHOKE ICCF

0 0 0 0

-.00- BREAK

0 JUNI - 71

73++ BYPASS TURBINA NSTEP- 281 TIMEz 6.49375 DELI" 2.617806-02 006006

PRESSURE VAPOR FRAC7 LIQ VEL

CELL (PA) (MIS)

I 6.600E.06 1.000000 0.6557E-02

O MASS FLOW RATE -= 2.58586-04

Of • I I # EDIT= . a r #I I I I I

VAP VEL T SAT

(MIS) (K)

0.1325E-04 555.050

TOTAL MASS OUT -

IIDI &I 0 S

T LIO T YAP LIO DEN MAP DEN DELTA-P lOT

(K) (K) (KG/M3) (KG/M3) (PA)

555.050 555.050 748.9 34.21 0.

1.6930E-03

0 ID 0I • D & f 9

ICHOKE ICCF

00 00

'-4 -*00- VESSEL 1*. VASIJA COFRENTES NSTEP= 281 TIME: 6.49375 DEL7= 2.6I7a0E-02 *4*

LEVEL I NSTEP- 281 . TIME _-= 6.49375 DELT = 2.61780E-02

CELL(RING.THETA) 1.( I. I) 2.( 2, I) 3.( 3. 1) 4.( 4. I)

PRESS(PA)

VOID FRAC

VV-Z(M/S)

VL-Z(M/S)

VV-R(M/S)

VL-R(MIS)

MV-Z(KG/S)

ML-Z(KG/S)

MV-R(KGIS)

ML-R(KG/S)

ILE%6

DZLEV

VLEV

ALPP

ALPM

ICCFLN

ICCFL

TV(K)

TL(K)

TSAT

7.373194E406

6.604957E-15

3.0488316*00

2.715953E*00

-3.587647E-01

-2.689042E-01

4.936537E-13

1.304176E#03

-3.770601E-13

-1.304176E*03

0

3.390000.E00

0.0000006E*00

O.000006E*00

0.OOOODE÷00

0

0

5.625495E+02

5.510995E+02

5.625495E+02

7.373171E+06

4.2448156-15

3.039150E#00

2.705297E600

-8.6580216-01

-6.965974E-01

1.711981E-12

7.032315E403

-4.816343E-13

-e.336474E+03

0

3.390000E+00

0.000000E+00

0. 00000E+00

0. 0000OE +00

0

0

5.625493E+02

5.510996E602

7.373180E*06

9.105277E-16

1.503711E*00

1.194237E600

-5.040148E-01

-3.757366E-01

1.349732E-13

2.306086E.03

-4.143485E-13

-1.064252E*04

0

3.390000E+00

0.0000006E.00

0.000000(E+00

0.000000E*00

0

0

5.625494E-02

5.511003E602

7. 373528E*06

5. 68502DE-16

0.0000006*00

0. 0000006*00

0.0000006.00

O .0ODOODOE400

0. 000000E*00

0 000000E400

0 00OO0OE*DO 0 .000000E400

0

3.3900OOE400

O.000000E*00

0.000000.E00

5.685020E-16

0

0

5.625526E*02

5.511049E*02

5.625493E.02- 5.625494E+02 5.625526E402
LEVEL 2 HSTEP= 281 TIME a 6.49375 DELT - 2.617B0E-02

CELL(R!NG.IHETA) 1.( 1. 1) 2.( 2. 1) 3.( 3. 1) 4.( 4. 1)

PRESS(PA)

VOID FRAC

VV-Z(M/S)

VL-Z(M/S)

VV-R(M/S)

VL-R(M/S)

MV-Z(KG/S)

ML-Z(KG/S)

MV-R(KG/S)

ML-R(KGIS)

ILEV

DZLEV

VLEV

ALPP

ALPM

ICCFLN

ICCFL

TV(K)

TL(K)

TSAT

7.353975E106

6.335712E-15

9.975813E*00

9.349055E100

-6.86810r.E-02

-5. 24033()E-02

1.563014E-14

4.542445E.01

-5.47158HE-14

-I.448653E+02

0

1.5700004E00

0.00000(IEC00

O.00000(1E00

0.OOOOE+0

0

0

5.623707E+02

5.510931E+02

5.623707E*02

7.353359E+06

5.662089E-15

9.946397E100

9.321171E100

-2.727141E-01

-2.066057E-01

8.020707E-14

2.608235E.02

-1.753776E-13

-1.085859E*03

0

1.570000DE00

O.OOOOOE*00

O.OOOOOOEOO

O.OOODOE00

0

0

5.623649E+02

5.510932E.02

5.623649ED02

7.352436E+06

2.406706E-15

1.031026E#01

9.452999E400

0.000000E*00

0.00O001.E00

8.26340)E-15

6.185907E*01

0.000000E.00 O.DQOOOOE4OO

1.5700000E*0

O.OOOOOOE00

O.O00OOOE400

0.000000E.00

0

0

5.623563E#02

5.510926E*02

5.623563E+02

7.250770E*06

7.051088E-16

-8.425197E-01

-6.837287E-01

O.O000OOE*00

0.00000OE.00

-9.749249E-13

-3.100543E403

O.O000000.00

O.O00000.E00

0

1.570000E*00

O.OOO000E*00

O.OOO00OE00

O.OOOOOOE*00

0

0

5.614041E+02

5.510617E102

5.614041E*02

LEVEL 3 NSTEP. 281 TIME = 6.49375 DELT - 2.617S0E-02

CELL(RING.TIIETA) 1.( 1. 1) 2.( 2. I) 3.( 3. 1) 4.( 4. I)

0I

PRESS(PA)

VOID FRAC

VV-Z(M/S)

VL-Z(M/S)

VV-R(M/S)

VL-R(M/S)

MV-ZIKGI/)

ML-Z(KG/S)

MV-R(KG/IS)

ML-R(KG/S)

ILEV

DZLEV

VLEV

ALPP

ALPM

ICCFLN

ICCFL

IV(K)

1L(K)

ISAT

7.230559E+06

5.61105(1E-15

4.608144E-01

3.815353E-01

8.348061E-02

6.234895E-02

2.3708I1E-14

6.966242E101

3.223981E-14

8.545357E*01

0

2.890000E400

0.000000E+00

O.O00000(1E+O

O.O00000(IE*OO

0

0

5.612135E+02

5.5305601.E02

5.612135E+02

7.230414E*06

4.291324E-15

2.935048E-01

2.290BOOE-Ol

3.05052?E-0D

2.277721E-01

5.770724E-14

2.099187E102

2.106209E-13

7.3040181E020

2.890000E100

0.OOOOOEOO

0.000000E*00

0.000000E+00

0

0

5.612122E.02

5.527368E*02

5.612122E102

7.229981E.06

4.856424E-15

1.216493E100

8.162597E-01

0.000000E00

0.000000E*00

.3.085696E-13

8.516107E*02

0.000000E00

0.000000E*00

0

2.890000E100

0.000000.E00

0.0000001E00

0.0000001E.00

0

0

5.612081E+02

5.528483E.02

5.612081E.02

7.234221E106.

5.105938E-15

-1.136267E#00

-9.686332E-01

O.O00000E*00

O.OOOOOE*00

-8.687977E-14

-3.100501E*03

0.0000OOE00

0.0000000EOD

0

2.890000E*00

D.0OOO0E+00

0.000000E400

0.000000E00

0

0

5.612481E102

5.510560E102

5.612481E402

LEVEL 4 NSTEP: 281 TIME a 6.49375 DELT - 2.61780E-02

CELL(IRNG.THETA) 1.( 1. 1) 2.( 2. 1) 3.( 3. 1) 4,( 4. 1)

PRESS(PA)

VOID FRAC

7.213795E*06 7.213823E*06 7.213328E+06 7.217235E*06

1.298211E-01 1.425195E-01 4.766574E-02 4.792230E-16
vI. 1114/S)

VV- R II/S I

vI-RIM/S)

MV-Z(KGIS)

ML-Z(2(G/S)

U V-ft I G/SI

MI-RE KG/S)

21EV

OZLEV

VLEV

AIPP

ALPM

ICCFLN

ICCFL

TV(I()

TL(K)

TSAI

-2.410259E-01

-9.5266991-01

1.128802E-01

1.646087E-01

-I.719173E400

-3.723373E401

5.639017E-01

I.080521.*02I

1.3507271400

-4.246391E-06

7.810300E-01

5.611056E-15

0

-1

5.6105791402

5.5950521.02

5.610552E402

-3.219684E-01

-9.64611-02E6.127336E-01

3.3964801-01

-1.143799E101

-1.905905E402

7.855403E400

5.127117E402I

1.386887E100

-4.338587E-06

9.9900OOE-01

4.291324E-15

0

-1

5.6105871.02

5.6007951402

5.6105546402

2.0533431400

1.392686E400

0. 00000OE400

0.0000001E00

5.098819E400

1.367092E403

0.000000E+o0

0.000000E100

U

1.620000.E00

0.000000.E00

0.0000OOE400

0.9000000E*00

0

-1

5.610507E+02

5.5631501E02

5.610507E402

-2. (1b7lI7E400O

-1.7931776100

O. OOOOOO00

-1 939185E-13

-I .064227E+04

0. OOOOOOE00

0.no0DoOE00

U2

I. 620000E+00

0. 0000E0100

0. 000000E'400

0. 0000001EOO

0

0

5.610877E.02

5.510554E402

5.610877E102

LEVEL 5 NSTEPs 281 TIME a 6.49375 DELT = 2.61780E-02

CELLIRIHC..THETA) 1.( 1. 1) 2.1 2. 1) 3.( 3. 1) 4.( 4. 1)

IT0

PRESS(PA)

VOID FRAC

VV-Z(M/S)

VL-Z(M/S)

VV-R(MIS)

VL-R(M/S)

MV-Z(KG/S)

ML-Z(KG/S)

MV-RtKG/S)

ML-R(KG/S)

ILEV

DZLEV

VLEV

ALPP

ALPM

ICCFLN

ICCFL

iV(K)

TL(K)

TSAI

7.204698E+06

7.810300E-01

1.1083261401

1.053276E#01

3.4394651-01

1.731032E-01

1.3986461.02

7.203184E402

1.0293471402

2.938670E+02

-2

5.314844E-01

1.285019E+00

0.000000E.00

0.000000E00

0

0

5.6096531*02

5.609841E*02

5.609691E*02

7.204680E106

7.784695E-01

1.227507E#01

1.1626901E40

5.3486112-02

1.782998E-01

9.811667E402

5.1688696+03

4.040444E102

7.491206E402

-I

6.766908E-01

4.848796E-01

0.0000D0E*00

0. 0000001. 00

0

0

5.6096501.02

5.609855E.02

S. 6096891. 02

7.2050691406

6.926191E-01

1.359314E*01

1.1351231*01

0.000000E*OO

0.0000DOE400

4.396027E102

3.184778E#03

0.00OOOOE400

0. 00000014 00

-2

7.561484E-01

5.791157E-01

O.OOOOOOE00

0.0000OOE400

0

0

5.6097251402

5.609022E102

5.609726E102

7.203609E106

3.118068E-16

-2.722293E400

-2.412613E+00

0.000000E*00

0.00000OE400

0.0000001E.O

-9.077346E403

O.OOOOOOE00

0.0000001E00

0

2.1000001E00

O.OOOOOE00

O.OOOOOEOO

0.000000E00

0

0

5.609588*102

5.5105441*02

5.609589E*02

LEVEL 6 NSTEP2 281 TIME = 6.49375 DELIT 2.61780E-02

CELL(RIIN6.THl1TA) 1.(1. 1.) 2.( 2. 1) 3.( 3. 1) 4.( 4. 2)

PRESS(PA]

VOID FRAC

VV-Z(M/S)

VL-Z(MIS)

VV-R(V:/S)

VL-R(V/! I

MV-Z(VG/S)

ML-Z(KG/S)

MV-R(KG/S)

ML-R(KG/SI

7.202306E.06

8.3564931-01

1.2390666*01

4.9298451-17

-6.3026806-02

4.421229E-01

2.672321E*02

2.558848E-15

-2.728295E+01

7.282359E*02

7.202284E106

8.445914E-01

1.208336E#01

4.917519E-17

-7.495805E-02

1.494919E*00

1.047465E#03

1.533790E-14

-9.295743E+01

5.896491E#03

7.201286E106

9.5558401-02

7.769949E.00

4.2926886-17

1.811221E-14

7.0758791.00

3.464822E#02

1.7360786-15

2.557133E-11

9.081435E+03

7.1836121406

9.902340E-02

6.797820E-03

-7.6972941.00

0.0000001E00

0.000000E400

3.821206E100

-7.911312E-02

0.0000001EOO

0.000000E00
]LE!V

021. Ev

VLEV

ALPP

ALPM

ICCFLN

JCCFL

TV(K)

TL(K)

TSAT

-I

0.00000!E400

0.000UOOE00

O.OOOOOOE*00

0.O000000!E00

a

0

5.609462E.02

5.609475E!02

5.609465E*02

-I

0I. (0. 41100(iflof 11OOfOOE 4On00

0.11110000!.400

0.000000E400

0

0

5.609450E*02

5.609477E*02

5.609463E,02

-I

0.00000OE400

0.000000E400

0. 000000E# 00 0. 000000E400

0

0

5.609353E**02

5.609347E!02

5.609368E402

I

2.462640!E00

3.207523E-05

o.5000OOE-0I

0.00000OE400

0

0

5.607693E402

5.608133E402

5.607693E*02

LEVEL 7 NSTEP- 281 TIME - 6.49375 DELT - 2.61780E-02

CELL(RXNG.THETA) 1.( 1. 1) 2.( 2. 1) 3.( 3. 1) 4.( 4. 1)

PR! SS(CPA ) VOID FRAC

vV-Z(M/S)

VL-Z(U/S)

VV-R(M/S)

VL-ACUIS)

MV-Z(KG/S)

UL-Z(KG/S)

MV-R(XG/S)

ML-AC KG/S 3 ILEV

DZLE!V

VLEV

ALPP

ALPU

I CCFLN

I CCFL

TV(K)

71(K)

ISA7

7.169987E406

9.999982E-01

5.471788E400

5.036825E+00

-3.343605E-02

7.337599E-03

1.914724E402

6.217365E-03

-2.424633E*'0

1.876976E-04

-I

O.OOOOOOE+00

O.O000 !OE*00

o.O000000!E00

0.000000E#00

0

0

5.604008E*02

5.606400E*02

5.606400E402

7.169985E*06

9.999979E-01

5.344667E*00

4.909244E#00

5.852537E-03

2.902054E-02

1.012432E403

3.902056E-02

1.074779E+01

2.236218E-03

-1

0.000000E!00

O.OOOOOOE00

O.OOOO00E!00

0.000000E+D0

0

0

5.604011E*02

5.606400'E02

5.606400E+02

7.16998IE406

9.999973E-01

S.375985E!00

4.937579E!00

0.00000!E400

O.OOOOOOE*00

3.572151E*02

1.762800E-02

0.000000E!00

0.000000E*00

-1

0.000000!E00

0.O000000E400

0.000000E!00

0.,000000E!00

0

0

5.604092E+02

5.6C6399E+02

5.606399E402

7.1693)3E-06

9.999992E-01

-2.362656E*00

-2.61590BE*00

0.000000E!00

0.000000E400

-1.561086E*03

-9.789857E-02

0.000000E00

0.O000000E!00

0

0,O00000!'O00 O.O0000E#O00

O.OOOOOOE*OO

0.0000OOE!00

0. 000000!'00

0

0

5.604013E#02

5.606341E!02

5.606341E*02

rN)

0

LEVEL 8 NSTEP- 281 TIME a 6.49375 DELT - 2.61780E-02

CELLCRING.THETA) 1.C 1. 1) 2.( 2. 1) 3.( 3. 1) 4.( 4. 1)

PRESS(PA)

VOID FRAC

VV-Z(M/S)

VL-Z(M/S)

VV-nCM/S)

VL-R(MIS)

MV-Z(KG/S)

ML-Z(KG/S)

MV-R(KG/S)

ML-R(KGIS)

ILEV

DZLEV

VLEV

ALPP

ALPM

ICCFLN

ICCFL

TV(K)

7.168631E*06

9.999860E-01

O.O000000E*0

0.000000E*00

3.991362E-01

8.203761E-02

0.O00000E+00

O.O00000DE00

1.914690!E02

!.081827E-02

-1

O.O000000E*0

O. 00000E00

0.O000000!E00

O.OOOOOOE*00

0

0

5.603844E*02

7.168625E-06

9.999958E-01

O.00000'E*00

0. 000000E!OO

1.285578E!00

9.230453E-01

0. OOOOOE'00

O.O000004E00

1.203879E!03

7.166847E-02

-1

0.000000E*00

0.00000E!00

0.O000000E400

0.000000E*00

0

0

5.603839E*02

7.168547E*06

9.999959E-01

0.000000E+00

0.000000E!O0

1.719981E#00

1.305231E*00

0.000000E*OO

0.000000E!'0

1.561089E+03

9.540109E-02

-1

0.000000E*O0

0.O000000E!00

0.000000E*00

0.000000E00

0

0

5.603842E*02

7.168367E+06

9.999971E-01

0.00000'E400

0.00009E0O0

0.00000 0E00

0.000000E0OO

0.000000!E00

0.000000E+00

O.OOOOOE00

0. 000000!E#00

-1

0.000000E00

0.000000E00

0.00000'E400

O.OOOOOOE00

0

0

5.60381SE'02
TLIK) 5.606271E402 5.606270E*n2 5.606263E*O2 !,. hfb24,E tV..

TSAT 5.606271E402 5.606270E*02 5.606263E+02 5.60r24(E[40:'

0 TOTAL COMPONENT WATER MASS - 1.694064E.05 KG. TOTAL COMPONENT WAILR ENERGY z 2.211676E411 J.

PERCENT MASS CONTINUITY ERROR 1 I.300510E-Oa LOST KILOGRAMS. 2.20296BE-05 PERCENT MASS FLOW THRU(TURNOVER)= -8.189923E

LOWER PLENUM LIQUID VOLUME= 8.481867E+O0 LOWER PLENUM LIQUID MASS= 6.431200E*04

DOWNCOMER LIQUID LEVELS (BY THETA ZONE) 1.07118E+0I

O TOTAL COMPONENT WATER MASS u 1.6941E*05 KG. TOTAL COMPONENT WATER ENERGY = 2.2117E411 J.

PERCENT MASS-CONTINUITY ERROR 1 l.3005E-0B LOST MASS- 2.2030E-05 KG. PERCENT MASS FLOW T7IRU(TURNOVER) = -8.1899E-03

TOTAL SYSTEM WATER MASS = 2.030640E*05 TOTAL SYSTEM WATER ENERGY= 2.675709E*ll

TOTAL MASS DISCHARGED AT BREAKS - 1.016236E.04

TOTAL MASS INJECTED AT FILLS a 1.017619E#04

COMPUTED SYSTEM INITIAL MASS x 2.030501E+O5 O SYSTEM PERCENT MASS CONTINUITY ERROR a -1.857522E-05 LOST MASS. -3.771700E-02 KG PERCENT MASS FLOW THRU(TURNOVER)= -6.8289

O MAXIMUM CORE SURFACE TEMPERATURE w S.775008E.02. WHICH IS IN CHAN 62. ROD GROUP 1. CELL 5

OSTEADY STATE - TOTAL SYSTEM NET RATE OF MASS CHANGE a -1.564934E+03 KG/SEC

OSTEADY STATE - TOTAL SYSTEM NET RATE OF ENERGY CHANGE a 1.966636E+07 JISEC

OSTEADY STATE TIME STEP NO. 281 CONVERGED IN 1 ITERATIONS. TIME a 6.493749E*00

N)

VARIABLE

PRESSURE

VOID FRACTION

LIQUID VELOCITY

VAPOR VELOCITY

LIQUID TEMP

VAPOR TEMP

SYSTEM METAL TEMP

ROD TEMP

ICONTROL SYSTEM EDIT

MAX. CHANGE RATE

1.IOO500EOI

-1.40368OE-D5

-1.080196E-04

8.713309E-03

4.1055OOE-03

4.708060E-03

2.694699E-07

-1.853502E-O7

MAX. CHANGE RATE (%)

1.753757E-04

-5.849840E-03

1.692486E-04

2.497451E-02

7.450250E-04

8.511152E-04

4.881098E-OB

-3.304806E-08

COMPONENT

TEE 80

CHAN 60

TEE 15

VALVE 83

VESSEL I

VALVE 70

CHAN 60

CHAN 60

DELT = 2.617799E-02

LEVEL/GROUP/CELL

6

7

5

2

4000004

2

1 1002

TIME - 6.49375E÷00 CONTROL SYSTEM TIME STEP SIZE - 2.61760E-02 CONTROL SYSTEM TIME. STEP NUMBER z 280

CONTROL SYSTEM TIMESTEP SIZE LIMITED BY CONTROL BLOCK NUMBER a

SEQ

NO.

20

21

1

2

3

4

22

23

24

25

26

S

BLK

NO.

2

4

6

8

10

14

102

104

106

108

110

112

LK

TYPE

CONS

SUBT

LAG

LAG

LAG

LAG

DEAD

DEAD

SUBT

SUBT

SUBT

LLAG

BLOCK

INPUT I

O.0000E+OD

1.0712E*01

8.8175E-01

1.5649E*03

1.5648E*03

6.7631E*06

8.8174E-01

9.9639E.o0

9.9639E*01

8.8174E-01

8.8258E-01

8.825BE-0I

BLOCK

INPUT 2

O.OOOOE*O0

9.8300E+O0

0.OO0E*00

O.O00DE+O0

O.0DODE+OO

O.O000E.00

O.O00E.00

0.O000E+0O

9.9639E01

-8.3335E-04

-2.0774E-07

8.8213E-01

BLOCK

INPUT 3

O .0UE.00

0 DODE+00

O 0 ODE00

0 O0E. 00

0 O0DE-00

0 O00E*O0

O.OOOE*00

O.OOODEOD

O.ODDE.00

O.000E+00

O.DOOE+00

8.BODE-Oi

BLOCK

CONST I

9.83E+00

O.OOE.O0

2.50E-01

I. DOE-O I

2.50E-01

I .OOE-O0

O.OOE+0O

1.ODE*02

O.OOE+00

O.OOE+O0

O.OOE+00

I.50E400

BLOCK

CONST 2

O.0DE*00

0.ODE.00

O.O0E.00

O.ODE*00

O.OOE 00

0. ODE*O0

O.DOE*00

2.O0E#02

O.OOE.O0

D.OOE+00

0.ODE.00

7.50E+00

GAIN

FACTOR

1.00

1.00

1.00

0.06

0.06

1.00

1.00

0.00

0.01

1.00

1.00

1.00

UPPER

LIMIT

I .0OE+50

I .OOE50

1 .5 2E * O

.. OCE-0O

I .OOE+50

I .OOE*50

I .OOE#50

I .DOE#50

LOWER INITIAL

LIMIT OUTPUT VALUE

-I.OOE.50 9.B3OE400

-I.ODE.50 8.8DOE-Oi

-I.OOE450 B.BOOE-01

-I.OOE+50 9.999EO01

-I.00E450 9.999E*0I

-I.00E+50 6.765E*06

0.OEDO0 8.OOE-OI

-1.27E-01 -2.550E-05

-I.OOE.50 0.OO0E*O0

-I.O0E+50 8.8O0E-01

-I.O0E*50 8.800E-01

-I.OE.50 8.800E-01

BLOCK

OUTPUT

9.B300EtOD

8.8175E-01

8.8 74E-O0

9. 9639E *01

9. 9639E dI

6. 763 1E.06

8.81 74E-OI

-8 3335E-04

-2. 0774E-07

8.8258E-01

8.8258E-01

8 .8222E-01

BLOCK

FLAG NAME

NA HIVEL 0

UL NIV.REL

GO NIV.MED

GO STM.FLOW

GO FW. FLOW.

GO PRES.COL

NL LIMITADR

NL PROG.LVL

NL VAP.AA

EQ NIV.IEL

0 NIV-ERRQ

GO eJDMP
27

6

28

29

30

31

81

32

7

33

34

35

36

9

a

10

37

38

39

40

41

42

11

43

44

45

46

47

48

82

83

84

.5

13

12

49

50

51

52

is

14

53

54

16

55

56

57

58

59

114

116

Ie

120

122

124

126

128

130

132

134

136

138

140

142

144

146

148

ISO

152

154

156

158

160

162

164.

166

302

304

306

308

310

312

314

316

310

320

402

404

406

408

410

412

414

416

418

420

422

424

1115w

|NT

FNGI

FNlGI

ADD

SUBT

FNGI

CONS

I NTM

wSUM

FNGI

INSW

FNGI

LAG

SOTF

INT

FNGI

FNGI

GATE

MULT

FNGI

MAXS

INT

FNGI

MULT

FNGI

MOLT

FNGI

CONS

INSW

FNGI

DLAY

SUBT

LAG

INT

FNGI

ABSV

FNGI

SUBT

LLAG

SOTF

DER

SUBT

LAG

CONS

MINS

DLAY

F 14G I

SUBT

B.825aE-01

O.00OO,0E0

0.OOOOE400

6. 4676E400

0 OO0E*00

8 .8000E-01

8 5994E#01

0. OO0E.00

-8.7312E-02

-8.7307E-02

6.4676ED00

8.6200E.01

8.5994E.01

7.282BE01

7.2849E*01

0.00000E+0

O.00OOE*00

7.2079E601

7.2879E401

1.0000E400

O.O00DOE00

9.7870E.01

0.000OE00

O.OODE.00

1.0000E400

7.1694E606

9.7670E601

6.4676E400

O.0000.E00

5.1710E601

9.4810E01

7.4996E*01

7.4996E+01

-7.6881E-12

-I.0293E-II

7.4996E+01

4.2811E-01

6.4676ED00

6.7631E#06

1.8721E*05

9.0571E01

9.0579E*01

9.0570E*01

9.0577E*0i

0.O0000E00

9.0589E#01

9.0589E*01

9.0592E601

3.7389E+01

-1.0396E-01

-3.9790E-03

0.0000E+00

O.0000.E00

3.7493E401

3.7493E401

0.00006E00

9.0589E+O4

O.0OO0DE00

9.0589E*01

O.000DE400

1.1500E+02

8.7589E*01

6.4676E*00

-3.0000.E00

8.6222E-01

O.0000.E00

O.O0000E00 O.O000E*00

8.B0O0E-Ot

8.8222E-01 0.0000E.00

0.OO00E+00

I.00004E00

8.6168E601

0.0000ED00

8.5994E601

0.0000E+00

0.0000.E00

-3.1403E-02

0.0000.E00 0. 00006.00

0.O0000E00

O.O0000E00

9.7870E+01

0.O000E.00

0.OOOE+00 0.00006400 O.ODOEO00

9.78170E01

0..000064O00

1.0190E+00

0.OO0EO0 0.0000E400

9.4810E601 0.00006400

0.0000E+00

7.4996E401

0.0000E.00

0.0000.E00

0.O000E.00

O.OOOE*00

0.0000E400

6.5759E.06

9.0664E401

-3.0834E-02

0.O0000E00

-5.9345E-03

0.00004E00

O.0000E600

1.0000E402

0.0000E*00

D.00006.00

3.7493E.01

0.00006E00

0.0000.E00

0.0000E#00

0. O0O0E00

I.00004E02

0. 000E*00

0.OOOED00

3.0000E+00

0.0000E400

I.OOOE600

0.0000.E00

9.0589E601

9.0589E+01

O.000E0E00

O.000E+O00

0.000E400

0.000E.00 0.000E.00 0.000E*00

O.O0OE4OO

0.000E+00

0.00DE.00

0.000DE.00 I 0.000.E00 .OODE*OO

0.000.E00

0.000.E00

0.000E.00 0.000E+00

0.000E+00

0.000E*00

0.000E+00

O.000E+00

0.000.E00

0.O00E+00

0.000.E00 O.O00E*00

0.000E*0O

0.000E600

O.000E*O0

0.000.E00

0.000E.00

0.0OOE*00

O.OOOE00

0.000E.00 0.0004E00

0.O0E*00

0.000 E00

0.00E6O00

0.006E+00

0.000E*00

0.0006400

0O00OE*00

0.000E+00

0.000E*00

9.123.E+0

0.000.E00

0.0DODE00

0,000E+00

0.OO0E+00

0.12OE*01

0.0006.00 O.0O0E*00

D.ODOEDOO

O.DODE*00

O.000E+00

0.000.E00

O.000E+00

O.000E*00

0.O00E00

O.OO0E*00

0.0006.00

O.00QE+OO

0.000E.00

O.O00E+O0

0.O00E0OO

0.OD0ED00

0.000E+00

0.000E*00

O.000E+00

0.000E.00

0.0O0E.00

0.00ED00 O.00E+00

0.00DE.00

O.OOE*00 0.ODE.00

O.00E+00

0.00E*00

1.00E+00

0.OOED00

I . ODE+DO

1.DOE*OD

0.00.E00

2.00E.00

0.18E+00

.4OE*.00

0.00 E00

0.00E*00

1.406400

O.QOE+O0

0.ODE*00

0.ODE*00

0.O0E.00

0.DOE.00

O.DOE+OO

O.00E*OO

O.00E+00

0.ODE+00

O.00E*00

O.006E00

5.17E+01

0.0DE+O0

O.00E+00

1 40E-02

0. OE+0O

1 3BE-0I

0 00E*O0

9 .00E00

O ODE.00 0. OE*00

2. 40E-01

O . OE.00

O.00E+00 3.60E-01

1 .00E.02

0.OOEO0D 9. 2OE-02

0. DOE*00

0.O0E.00

-I.OOE-OI

0.00-E00

0. DOE*00

O.OOE.00

0.00E. 00

0. 006.00

0.OOE+O0

0.0OE+O0

0.006E00

0..0OE 400

1. 15E+02

0.00DEO00

0.00E. 00

0. DOE. D0

0.00DE. 00

0. DOE. 00

000OE400

O. 00E400 0. 006O00

0. DOE. DO

O.ODE400 O,00E*00

0.00E400

I.O0E400

0.ODE.00

0.O0E00 00.DE.00

O.O0E+00

0.OOEE00

O.OOE+O0

O.00E*O0

0.00E+00

0.00E*00

0,0DE*00

0.00E4OO

O.OOE*00

O.OOE*00

0,00E*O0 0.OOEDO0

O,00E400

O.00E+O0

0,00E4OO

O.00E*OO

O.OOE*00

O.00E*00

0,00E*00 0.ODED00

O.ODE*00

0.DOE 00

0.DOE400

0.DOE*00

0.00DE .00

5.40E*00

1. 441E-02

0.DOE.00

0.ODE.00

0 00E400

00.OE+00

0.0OE. 00

000OE*OO

0. 00E*00

O OOE.00

I.00E-01

000OE*00 0 .00E*00

0 0 .DED00 00E*00

0.0OE.00

S.40E.00

0.O0E*00

0.00E+00

0.DOE+00

0,00E.00

0.00E+00

0.DOE+00

0. 00E+*00

1.00

I .00

1.00

1.00

1.00

39.37

1.00

!.00

0.07

1.00

1.00

1.00

1.00

1.00

1.00

1.00

1.00

1.00

1.00

1.00

1.00

1.00

1.00

1.00

1.00

1.00

15.69

1.00

1.00

1.00

1.00

1.00

1.00

4.24

I.O0

2.06

1.00

1.00

1.00

0.00

1.00

0.19

1.00

1.00

1.00

1.00

I.00

I.00

1.00

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10.00

1.00

1.00

1.00

0.01

1.00

1.00

1.00

1.00

1.00

1.00

1.00

1.00

1.00

I.00E450 1 .00E,50 I .00E.50

I.OOE+50

I.OOE+50 i.00E+50

1.00E+00

1.00E#50

I.OBE*02

I.00E450 1.0DE*50

I .0E+02

I .0E.50

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I .OOE*50

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- . IO E 0 511

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I .00E+50

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0.11-1111, 111( 0. WIDEl I II(

0. OUIIE # 00

0.BOOE-01

8.800E-01

O.ODOE*OO

I. 000E*00

I . 00OE#00

8. 620E*01

8.620E+01

8.620E01

8.620E#01

7.323E601

7.323E#01

7.323E401

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1 .00DEDO0

9.814E#01

9.814E*01

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9.48 IE401

7.S0OE*O1

7.500E+01

0.OO0E+00

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4.550E-0I

4.550E-0I

6.576E.06

I .889E*05

9. 123E601

9. 123E#01

O.00OEU00

9. 123E601

9. 123E601

I .O0OED02

9. 122E*01

9. 123E.01

3.813E*01

0.000E*00

O.000.E00

3.813E#D01

O.000.E00

I.000E*O2

3.813El01

I .O0OE*00

3.000E400

I.O000E00

I.O000E00

I .O00E*00

I. 150E+02

0.000EO00

O.0006E00

I.000E600

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ii.0272E-0I

(. 006E.0 O.OOOOE*OO

8.B0OOE-OI

8.B006E-01

-8.7307E-02

1.OOOE+OD I.O000E*00

8.6160E 0I1

8.5994E#0I

8.620OD+01

8.5994E#01

7.2820E*OI

7.2848E*Oi

7.2879E401

O.O000E+00

I.O000E000

9.7870E.01

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9.7870E*01

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9. 787DE4OI

0 ODOOE*OO

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9. 787[E 401

I .0190E00

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9.48 5. liIOEsOI 10E.01 5.1710EoOl

9.4810E*01

7.4996E601

7.4996E.01

-7.4891E-12

-1 4772E-II

7. 4996E*01

4.2811E-01

4.2811E-01

6.5759E#06

1 .8721E*05

9.0570E*01

9.0579E.01)

-5.9345E-03

9.0576E401

9. 0589E401 1.O0000E.02

9.05896E01

9. 0592ED01

3. 7389E*01

-1.0396E-01

-3.9597E-03

3.7493E601

O.O00006DO

I.O000DE02

3.7493E#01

9.9582E-01

3.DOD0EDO0

B. 7!.B896 D1I I.0001E600

9.0589E.01

1. 150[E402

2.4411E.01

-3.OOOOE*00

0.Ou00(E 00

0.O0000EO0

0

HL

0

0

0

0

UL

0

NL

0

0

0

0

HL

HL

NL

0

0

0

0

0

0

HL

0

0

0

0

0

0

0

0

0

0

HL

HL

0

0

0

0

ML

NL

0

0

"L

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

PASO 1/3

TRPTSCRM

SCRM NIV

SETP.NIV

SP.NIVCO

ERR.NIV

LIM.ANT

CONST I

INT.LIM

SAL.PI

DEM.MAN

MAN/AUTO

LIN TB0

ENT.1B8

SAL 0BB

TRPT ITO

CDWN. 11B

RESP.218

DISP.118

CORCOAST

RESPIT1B

CDOMI1BB

TRPT2188

CDWN21BB

a PREV

COR.PRES

Fw(L/S)

DEM.POS.

ENC.RBK.

RBK.TR-9

LIN.DPOS

RETDO P

ENT.PV

POS! VAL

SAL PV

CV/POS I

CV/POS 2

TAR.PRES

ERR.PRES

/IDO.DEM

RE SON. I

RE50N.2

COMP.1

COMP.2

LIM.CARG

RESTA

RIAR.TCV

LIN 1CV

ENT TCv

DEAD TCv

SALI 7CV

TRPT3

CIER.TCV

POS TCy

0.TCV

BIAS BPV

DEM BPv

PERM BPV

PA.AP.BP

L.MAX.CO

DEF. 0

AP. OP.

APMA" OP

S1L MAX

60 426 DEAD

17 428 1NT

to

61

62

63

64

65

86

87

66

as

09

67

430

432

434

436

438

440

442

444

446

448

450

452

INT

FNGI

M1NS

FNGI

CONS

SUBT

NOT

GATE

CONS

SUBT

SUBT

FNGI

90 454 MAXS
*.,1 .0,4 M I1W11 k

i.' 4511 MLAY n

93 460 511SOT

94 462 DEAD 0

19 464 INT a

68 466 flIGI a

96 468 GATE 0

97 470 MAXS 0

98 472 FNGI 0

69 474 FNGI 6

70 476 FHGI 6

71 478 INSW 9

99 480 MULT 0

72 482 CONS 0

73 484 LSTH 0

95 486 AND 0

74 500 CONS 0

75 502 GREQ a

76 504 ZOH 0

77 506 CONS 0

78 508 LSEO 8

79 510 ZOH 0

80 520 MINS 0

TIMING EDI

SUBROUTINE

.44 i IE.I

. IIOUOE 4 U

'.0000E80

.000G8*0

I.O81000E.O

).Q000E#O

.76408.0

.7640E*0

'.9320E-0

*.0000E*O

i.0000E*0 ).OOOOE*O

.0000E4O ).OOOOE#O

.8174E-0

).O00OE8. ).0000E.0

.8174E-0

p.000088+

I.O000.EO

7

I1 0.00O.E0DO 0O 9.OO~nE*O0 0 0.0000E.00

0 0.OOOOE*00 0 0.0000.E00

0 0.0000E+00

10 0.0000.E00

0 0.0000.E00

10 0.0000.E00 30 0.0000E.00

16 0.OOOOE.00

16 0.0000E.00

I1 7.6955E-01

0 7.6955E-01

0 0.0000E*00

10 9.9000E801

10 1.0000E*00

0 0.0000.E00

1 1.3208E800

10 O.O000E*OO

0 0.00000E*0

1 6.33008-01

0 O.0000E+00

10 0.0000EO00

TOTAL TIME s

U -UOIIE.0010) .OE+00

.u110a8 o00 9.208-02

0.000.tOO 0.0OE400

0OOOE*O0) -I.OOE-Ol

0.0OOE0.0 0.OOE.00

0.OOOE+00 0.00E*00

0.000E,013 O.00E+00

0.000.E00 O.OOE00

0.0008E00 O.00E+00

0.000Es00 0.OOE.00

0.000E+00 0.00E.00

0.OOOE.01) O.00E+OD

0.000E.00 0.00E400

0.O00E01)0 9.90E801

0.000.E00 0.008400

0.000.E00) O.00E+00

0.0008400 1.32E*00

0.OOOE#00 O.OCE*00

0.000E.00 O.OOE400

.OOOE00 8.33E-01

0.000E*00 0.00E.00

O.000.E00 O.004E00

0.0008.00 O.00E*00

760.759 SEC

0. (l1Et 00 O6. titlE # 00

0.OOE.00

1.00E-01

0.00E400

0.OOE00

0.OOE*00

0.OOE*00

O.OOE*00 O.004E00

0.008+00

0.OOE800

O.008400

O.OOE00

0.OOE+00 0.008+ 00

0.OOE*O0

O.OOE+OO 0.008400

O.OOE+00

0.OOE*00

O.OOE00

O.OOE+00

2.86

1.00

1.00

1.00

10.00

1.00

1.00

1.00

15.70

1.00

1.00

1.00

1.00

1.00

1.00

1.00

1.00

1.00

1.00

1.00

1.00

1.00

1.00

I.00.E02 I.OOE*50 1.00E450

4.20E801

I.00E450

1.00E*50

I .008+50

I.00E+50

I .00E50

I .008+50

I.00.E50

I .00E*50

I .OOE*50

I.008450

I .0OE50

l.OOE50

I.O08.50

I.0OE+50

I .00E50

1.008450 I .00E.50

I .00E.50 I.0OE*50 I.0OE*50

SI. OOE-01

-I.OOE#50

-I. 008.50

-4. 208E01

-I.008E50

- I.00E+50

-1.00E*50

-I.OOE50

-. OOE+50

- 1.00IE50

-I.00E+50

-I.OOE50

-1.008450

-1.00IE50

-1.OOE+50

-1.00E+50

-1.008+50

-1.OOE+50

- 1.00E+50

-1.00E50

-1.00E*50

-I.008E50

-I.OOE+50

O.O00E+00

O.O000E00

0.000E400

0.0004E00

0.OOE800 O.O00E400

0. 0.0008.00 00084 00

0.00DE.00

O.0008+00

1.0008.00

1.00O0800

1.0008E00

0.000E400

9.900E801

1.000E+OO

0.0008+00

1.321E800

0.000E+00

0.000E+O0

B.33DE-01

0.000E.00

0.000E+00

O.0008E00

0.(0008E+00

0.0(100.E00

0.0000E800

0.00008.00

0.0000E+00

0.0000E+00

0. 00008E*00

O.O0000E00

0.0000E+00

7.6955E-01

9.9320E-01

7.6955E-01

0.0000E800

9.90008E01

I .00008.00

0.0000E800

1.3208E*00

0.0000.E00

0.00008O00

8.3300E-01

0.0000.E00

0.0000E+80

0.0000.E00

0

0

0

0

HI

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

0

POS/MInu

RET OP

ETR SP

BMTA.BPV

SAL.BPV

AP.R.BPV

PA.AP.BP

SEL POS

@ BPV

CORR.NOR

CORR.CRI

SEL CORR

CODRQBPV

99/100oP

DEM--99

AP RAP

NIVEL 8

COMP.NI

SUJETDR

NIVEL 4

COMP.NI

SUJETOR

SELECTR

CPU TIME (SEC) PERCENT NO. OF CALLS

T'-

P,3

INPUT

INIT

TRANS

.DUPIT

EDIT

PREP

PAPID

VSL I

MFROD

HTCOR

OUTER

INNER TFIDS

TFIE

IFI1

FFI0

HEA7TI

FRICI

FRCw

CHOKE

VSL2

TF3E

IF31

PSIlID

VSL3

FF30

FROn

El ROP

U•RC.•

TmERMZ

CONTROL

OTHE DUMP FILE

151.803

0.667

0.031

1.248

16.883

5.037

0.841

17.212

22.705

47.821

1.244

3.237

61.502

30.688

3.475

32.594

32.822

36.146

14.811

0.978

11.744

18.007

20.987

31.825

30.185

15.776

10.879

40.594

10.964

14.529

2.105

40.775

23.859

6.785

HAS BEEN CLOSED IN S.

19.95

0.09

0.00

0.16

2.22

0.66

0.11

2.26

2.98

6.29

0.16

0.43

8.08

4.03

0.46

4.28

4.31

4.75

1.95

0.13

1.54

2.37

2.76

4.18

3.97

2.07

1.43

5.34

1.44

1.91

0.28

5.36

3.14

0.89

R. CLEAN

9

2

a

281

5339

281

843

42993

303

11514

17271

5339

5757

5757

34001

37935

39621

726

606

2248

2248

281

5339

843

2248

843

7617

65175

843

54097

14779

281

NRC FORM 335 U.S. NUCLEAR REGULATORY COMMISSION 1. REPORT NUMBER

12-89) (A" wgned by NRC. Add Vol., Supp., Rev.. NRCM 1102, and Addendum Numbers, If any.) 3201.3202 BIBLIOGRAPHIC DATA SHEET NUREG/IA-0068

MSee instructions on the reverse) I CSP -CO-TU RFW- T

2. TITLE AND SUBTITLE

Assessment of the "One Feedwater Pump Trip Transient" in

Cofrentes Nuclear Power Plant With TRAC-BF1 MONTHEYEA MONTH I YEAR

April. 1992

4. FIN OR GRANT NUMBER

A4682

5. AUTHOR(S) 6. TYPE OF REPORT

F. Castrillo, Hidroelectrica Espanola

A. G. Navarro, I. Gallego, Union Iberoamericana De Tecnologia Technical

7. PERIOD COVERED (Inclusive Dates)

8. PERFORMING ORGANIZATION - NAME AND ADDRESS (If NRC. provide Division, Office or Region, U.S. Nuclear Regulatory Commission, end mailing address,'if contractor, provide

name and mailing addresL)

Hiidroelectrica Espanola

Hermosilla, 3

28001 -Madrid

Spain

9. SPONSOR ING ORGANIZATION - NAME AND ADDRESS (If NRC, type 'Tjm as above' if contractor. provide NRC Division, Office or Region, U.S. Nucear Regularory Commison,

and mailing address.)

Office of Nuclear Regulatory Research

U.S. Nuclear Regulatory Commission

Washington, DC 20555

10. SUPPLEMENTARY NOTES

11. ABSTRACT (200 words or less)

This report presents the results of the assessment of TRAC-BF1 (GIJi) code with the

model of the C. N. Cofrentes for simulation of the transient originated by the manual

trip of one pump.

12. KEY WORDS/DESCR!PTORS (List words or phrases that will assist researchers in locating the report.) 13. AVAILABILITY STATEMENT

LUnl imited

Cofrentes, TRAC-BF1, Plant Transient 14.SECURITY CLASSIFICATION

(This Pagel

Unclassified

(This Report)

Unclassified

15. NUMBER OF PAGES

16. PRICE

NRC FORM 335 (2-89)


THIS DOCUMENT WAS PRINTED USING RECYCLED PAPER

NUREG/IA-W08 ASSESSMENT OF THE"ONE FEEDWATER PUMP TRIP TRANSIENT" IN COFRENTES

NUCLEAR POWER PLANT WITH TRAC-BF1

APRIL 1992

UNITED STATES

NUCLEAR REGULATORY COMMISSION

WASHINGTON, D.C. 20555

SPECIAL FOURTH-CLASS RATE

POSTAGE AND FEES PAID

USNRC

PERMIT NO. G-67

OFFICIAL BUSINESS

PENALTY FOR PRIVATE USE, $300