ML20058F896
| ML20058F896 | |
| Person / Time | |
|---|---|
| Site: | Millstone  |
| Issue date: | 08/31/1990 |
| From: | Moomau W WESTINGHOUSE ELECTRIC COMPANY, DIV OF CBS CORP. |
| To: | |
| Shared Package | |
| ML19310C840 | List: |
| References | |
| WCAP-12622, NUDOCS 9011090202 | |
| Download: ML20058F896 (53) | |
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-WESTINGHOUSE CLASS 3 WCAP 12622 WESTINGHOUSE REVISED THERMAL DESIGN PROCEDURE o
INSTRUMENT UNCERTAINTY METHODOLOGY FOR NORTHEAST UTILITIES MILLSTONE 3 NUCLEAR POWER STATION t-
' AUGUST,1990 e
W.H.Moomau 3
L
(
3
(
i -
g 41
[f.,
ij-Westinghouse Electric Corporation Energy Systems P.O. Box 355 Pittsburgh, Pennsylvania 15230 Copyright by Westinghouse Electric 1990, c All Rights Reserved
TABLE OF CONTENTS SECTION TITLE PAGE 1.
Introduction 1
II.
Methodology 2
III.
Instrumentation Uncertainties 4
IV.
Conclusions 38 References 44
' i
- 1 F
a i
i a
i "pp
']
LIST OF TABLES j
TABLE NUMBER TITLE PAGE Ia Pressurizer Pressure Control 5
System Accuracy - Veritrak transmitter 1
l 1b Pressurizer Pressure Control
)
Syste:a Accuracy - Rosemount transmitter 6
)
2 Rod Control System Accuracy 8
)
3a Flow Calorimetric Instrumentation 16 Uncertainties - Four Loop Operation, Veritrak Pressurizer Pressure Transmitter 3b Flow Calorimetric Instrumentation 20 Uncertainties - Four Loop Operation,.
Rosemount Pressurizer Pressure Transmitter 1
?
24 L
3c Flow Calorimetric Instrumentation Uncertainties Three Loop Operation, i
Veritrak Pressurizer Pressure Transmitter p
3.d Flow Calorimetric Instrumentation.
28 Uncertainties - Three Loop Operation, i
Rosemount Pressurizer Pressure Transmitter
.4a
. Flow Calorimetric Sensitivities - Four 17 l,
l Loop Operation, Veritrak Pressurizer-Pressure Transmitter-
'4 b '
Flow Calorimetric. Sensitivities - Four 21 Loop Operation, Rosemount Pressurizer Pressure Transmitter 1
4c Flow Calorimetric Sensitivities Three 25 Loop Operation, Veritrak Pressurizer Pressure Transmitter-
.4d-Flow Calorimetric Sensitivities - Three 29 i
Loop Operation, Rosemount Pressurizer Pressure Transmitter..
5a Calorimetric RCS Flow Measurement 18 Uncertainties.- Four Loop Operation, Veritrak Pressurizer Pressure Transmitter t
5b Calorimetric RCS Flow Measurement 22 Uncertainties - Four Loop Operation, Rosemount Pressurizer Pressure Transmitter 11 i
i u 1
LIST OF TABLES q
j TABLE NUMBER TITLE PAGE 5 c' Calorimetric RCS Flow Neasurement 26 i
Uncertainties - Three Loop Operation, 1
Veritrak Pressurizer Pressure Transmitter 1
1 J
5d Calorimetric RCS Flow Measurement 30 Uncertainties - Three Loop Operation; Rosemount Pressurizer Pressure Transmitter d
6a-Cold leg Elbow Tap Flow Uncertainty. -
33 Four Loop Operation, Veritrak Pressurizer.
)
Pressure Transmitter j
t 6b Cold Leg Elbow Tap Flow Uncertainty--
34 j
Four Loop Operation Rosemount Pressurizer Pressure Transmitter 4
3 jl
- 6. c Cold leg Elbow Tap Flow Uncertainty -
35 Three Loop Operation, Veritrak Pressurizer-Pressure Transmitter
)
6 d-Cold Leg Elbow Tap Flow Uncertainty -
36
'l Three Loop Operation, Rosemount Pressurizer Pressure Transmitter-1 7.a Power Calorimetric Instrumentation 40
?
Uncertainties - Four Loop Operation 7 b' Power Calorimetric Instrumentation 42 Uncertainties - Three Loop Operation-8a Secondary Side Power-Calorimetric, 41 Measurement Uncertainties - Four Loop Operation 8 b-Secondary Side Power Calorimetric 43
?
Measurement Uncertainties - Three Loop Operation-i I
t l
fi 1
4 f
iii L
' 'j s.
LIST OF ILLUSTRATIONS, i
i FIGURE NUMBER TITLE PAGE I
RCS Flow Calorimetric Schematic 46 2
Power Calorimetric Schematic 47 i
I i
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i t
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N i
WESTINGHOUSE REVISED THERMAL DESIGN PROCEDURE INSTRUMENT LNCERTAINTY METHODOLOGY (OR NORTHEAST UTILITIES MILLSTONE UNIT 3 I.
INTRODUCTIfN Four operating parameter uncertainties are used in the uncertainty I
analysis' of the Revised Thermal Design Procedure (RTDP). These parameters
]
are Pressurizer. Pressure, Primary Coolant Temperature (T,yg), Reactor Power,.and Reactor Coolant System Flow. They are frequently monitored and j
several are used for control purposes.
Reactor. power is monitored by the.
performance of a secondary side heat balance (power calorimetric) once
~
every 24 hours2.777778e-4 days <br />0.00667 hours <br />3.968254e-5 weeks <br />9.132e-6 months <br />.
RCS flow is monitored by the performance of a precision
. flow calorimetric at the beginning of each cycle. _ The' RCS Cold Leg I'
taps are. normalized against the-precision calorimetric and used C ri,y surveillance (with a small increase in uncertainty).' Pressuri*
essure is a controlled parameter and the uncertainty reflects the cor-system.. T,yg is.a controlled parameter via the temperature inp a to the rod (control' system and the uncertainty reflects this control system.
(
Westingnouse has been involved with the development of several techniques to treat instrumentation uncertainties. ~An early version (for D. C. Cook 2 and Trojan) used the methodology outlined in WCAP-8567 " Improved Thermal
)
Design Procedure",(1,2,3F which is based on the conservative assumption i
that.the uncertainties can be described with. uniform probability distributions. Another approach (for McGuire and Catawba) is based.on the more realistic assumption.that the uncertainties can be described with random, normal, two sided probability distributions.(4) This approach
.is used-to substantiate the acceptability of the protection' system
.setpoints for many Westinghouse' plants, e.g., D. C. Cook 2(5), V. C.
Summer, Wolf Creek, and others.
The second approach is now utilized for
{
}
the determination of.all instrumentation errors for both RTDP parameters
[
and. protection functions.
L i
,i IIe-METHODOLOGY i
The methodology used to combine the error components for a channel'is the square root of the sum of the squares of those groups of components, which are statistically independent. Those errors that are dependent arti i
combined arithmetica11y into independent groups, which are then systematically combined. The uncertainties used'are considered to be l
random, two sided distributions, The sum of both sides is equai to the range for that parameter, e.g., Rack Drift is typically
(-
]+a,c, the range for this parameter is [
]+a,c,
~
This te:hnique has been utilized before as noted above, and has been-
. endorsed by the NRC staff (6,7,8,9) and various industry
. standards (10,ll),
The relationships between the error components and the channel instrument error allowance are variations of the basic Westinghouse Setpoint
' Methodology (12) and are defined as follows:
I 1.
For precision parameter indication using Special Test Equipment or a DVM at the input to the racks; CSA'= ((SCA + SMTE + SD)2 + (SPE)2 + (STE)2+'(RD0VT)2)l/2 j
+ BIAS Eq. 1 2.
For parameter indication utilizing the plant process computer; i
CSA
-((SCA.+ SMTE + SD)2 + (SPE)2 +-(STE)2 + (RCA + RMTE + RD)2
+ (RTE)2 + (10)2 + (A/D)2)1/2 + BIAS Eq. 2 i
/
3.
For parameters which have control systems; I
CSA = ((PMA)2 + (PEA)2 +(SCA + SMTE + SD)2 + (SPE)2 + (STE)2
+ (RCA + RMTE + RD + CA)2 + (RTE)2)1/2 + BIAS Eq. 3
i q
where*
Channel Allowance CSA Process Measurement Accuracy j
=
Primary Element Accuracy PEA
=
-Sensor Calibration Accuracy i
SCA
=
Sensor Measurement and Test Equipment Accuracy SMTE Sensor Pressure Effects SPE
=
Sensor Temperature Effects STE
=
L SD Sensor Drift
=
Rack Calibration Accuracy RCA
=
Rack Measurement and Test Equipment Accuracy RMTE
=
Rack Tercerature Effects RTE.
Rack Drift RD
=
Readout Device Accuracy (DVM or gauge)
RDOUT
=
Computer Isolator Drift -
1 ID
=
Analog to Digital Conversion Accuracy A/D
=
Controller Accuracy CA
.The parameters above'are as defined in references 5 and 12 and are based t
I enSAMASt.andard'PMC 20.1,1973(13). However, for ease in understanding they are paraphrased below:
-PMA'-:
non-instrument related measurement errors,.e.g.,
temperature stratification of a fluid in a pipe, PEA -
errors due to a metering device,- e.g., elbow, venturi,
- orifice, SCA -.
reference (calibration) accuracy for a sensor / transmitter, y
c SPE -
changeiin input-output relationship due to a change in static pressure.for a d/p cell, STE -
change in input-output relationship due to a change.in b
ambient temperature for a sensor / transmitter, l
SD' -
change in input-output. relationship over a period of time at reference conditions for a sensor / transmitter, i
RCA.-
reference-(calibration) accuracy for all rack modules 'in
-loop or channel assuming the loop or chappel is string calibrated, or tuned, to this accuracy.
-RTE ~-
change in' input-output relationship due t) a change in ambient temperature for the rack modules,
.(
1 '.
~-- -. - -... -
. change in input-output relationship over a p2riod of time RDL at reference conditions for the rack modules,
'RDOUT -
the measurement accuracy of a special test local gauge, digital voltmeter or multimeter on it's most accurate applicable range for the parameter measured, change in input-output relationship over a period of time ID at' reference conditions for a control / protection signal isolating device, allowance for conversion accuracy of an analog signal to a A/D digital signal for process computer use, allowance for the accuracy of a controller, not including CA deadband.
BIAN-a non-random uncertainty for a sensor / transmitter or a process parameter.
- A more detailed explanation of the Westinghouse methodology noting the
. interaction of several. parameters is provided in references 5 and 12.
III.-. Instrumentation hcertainties 3
The instrumentation uncertainties will be discussed first for the two parameters.which are controlled by automatic systems, Pressurizer 4
Pressure, and Tavg (through Rod Control).
1, PRESSURIZER PRESSURE Pressurizer Pressure is controlled by comparison of the measured vapor space pressure and a reference value. Allowances are made for the transmitter and the process racks / controller. As noted on Table 1(a) for a Veritrak transmitter, the electronics-uncertainty for this. function is
[
]+a,c which corresponds to an accuracy of.[
'-]+a,c.
In addition to the controller accuracy, an allowance is made for pressure overshoot or undershoot due to the interaction and thermal inertia of the heaters and. spray.
Based on an evaluation of ' plant operatio'n, an allowance of [
-]+a,c was made for this.effect.
Therefo're, a total control system uncertainty of:[
]+a,c is calculated, which results in a standard deviation of [
]+a,c
'(assuming a normal, two sided probability distribution).
The total uncertainty for a Rosemount transmitter is (
)+a,c as shown'on Table 1(b), resulting in a' standard deviation of [
]+a,c, j
j !
I t,.
1 TABLE 1 (a)
J PRES $URIZER PRESSURE CONTROL SYSTEM ACCURACY 1
VERITRAK TRANSMITTER' l
+a,c i
SCA =
j SMTE--
STE -
=
BIAS =
]
RCA =
-i RMTE=
RTE -
RD
=
J 1
..,c ELECTRONICS UNCERTAINTY ~=
-l PLUS i
ELECTRONICS UNCERTAINTY =
PLUS l
CONTROLLER UNCERTAINTY
=
l -.
4 l
ll r
P
+
M....-.
i\\
~44;,
"'t TABLE 1 (b)
L PRESSURIZER PRESSURE CONTROL SYSTEM ACCURACY ROSEMOUNT TRANSMITTER
+a,c SCA =
SMTE=
STE =
=
BIAS.
RCA =
RMTE=
RTE =
RD
=
CA
=
+a,c ELECTRONICS UNCERTAINTY =
PLUS
. ELECTRONICS UNCERTAINTY =
PLUS CONTROLLER UNCERTAINTY
=
')
' L
2.
Tgyg F
T is controlled by a system that compares the auctioneered high ayg T
from the loops with a reference, usually derived from the First avg Stage Turbine Impulse Chamber Pressure. T is the average of the avg narrow range TH and TC values. The highest loop T is then used avg in the controller. Allowances are made (as noted on Table 2) for the RTDs, transmitter and the process racks / controller. The CSA for this function is dependent on the type of RTD, pressure transmitter, and the location of the RTDs, i.e., in the RTD bypass manifold or in the Hot and Cold Legs. Based on the assumption that 3 Ty and 1 TC cross calibrated Weed RTDs are used to calculate T and the RTDs are ayg
. located in the Hot and Cold legs, the CSA for the electronics is
(
)+a,c.
Assuming a normal, two sided probability distribution results in an electronics standard deviation (si) of
[.
)+a,c, 0
However, this does not include the controller deadband of i 1.5 F
The controller accuracy is the combination of the instrumentation accuracy and the'deadband. The probability distribution.for the deadband has been determined to be (
).+a,c The variance for the deadband uncertainty is then:
(s2) "I 3+ ' '
j
. Combining the variance for instrumentation and deadband results in a controller variance of:
(sT) " (S ) + (5 ) *I 3+
- I 2
The controller si - (
)+8' for a total uncertainty of
[-
)+a,c,,
TABLE 2 ROD CONTROL SYSTEM ACCURACY y
ROSEMOUNT TRANSMITlER j
Tavg TURB PRES 4a,c PMA.
1 SCA.
SMTE.
i STE =
=
BIAS =
RCA =
RMTE-RMTE.
RTE =
-RD
=
CA
=
BIAS =
- RTDs USED -
TH = 2 TC 1
i
+a c ELECTRONICS CSA
=
ELECTRONICS SIGMA =
CONTROLLER SIGMA
=
CONTROLLER BIAS.-
=
CONTROLLER CSA
=
'\\
r I
l' is:
, t
=
'3, RCS FLOW i
RTDP 'and some plant Technical Specifications require an RCS flow j
measurement with a high degree of accuracy.
It is assumed for this
)
error analysis that the flow measurement is performed within thirty
)
days of calibrating the measurement instrumentation.
Therefore, except where necessary due to sensor location, drift effects are not
)
I included.- It is also assumed that the calorimetric flow measurement is performed at the beginning of a cycle, i.e., no allowances have
)
been made for Feedwater venturi fouling, and above 90% RTP, The flow measurement is performed by determining the Steam Generator thermal output (corrected for the RCP heat input and the loop's share
{
- of primary system heat losses) and the enthalpy rise (Delta-h) of the primary coolant. Assuming that the primary and secondary sides are in equilibrium, the RCS total vessel flow is the sum of the individua1' primary loop flows, i.e.,
l WRCS = N(W ).
Eq. 4 L
- The individual' primary loop volumetric flows are determined by
- correcting the thermal output of the Steam Generator for Steam
. i i
Generator blowdown (if not secured), subtracting the RCP heat addition,. adding the loop's share of the. primary side system losses,-
l dividing by the primary side enthalpy rise and multiplying by the:
L Cold. Leg specific volume. The equation for this calculation is:
1 L
L " IAIIO
- O + IO /N)){V;F i
W SG P
L L
(hy h )'
Eq. 5 C
o where; L
l00P fl0" (9P")
.W 3
0.12'47gpm/(ft/hr) j A
=
Qg
=- Steam Generator thermal output (Btu /hr) l 3
RCP heat addition-(Btu /hr)
Qp:
=
Qt Primary system net heat losses (Btu /hr)-
=.
3 VC Specific volume of the Cold Leg at TC (ft /lb)
=
[
.g.
4
_m, s
~
_.-_...g..,,
y
~. ~.-
i Number of primary side loops j
N s
hH Hot leg enthalpy (Btu /lb)
]
=
hC Cold Leg enthalpy (Btu /lb).
j i
The thermal output of the Steam Generator is determined by a precision secondary side calorimetric measurement, which is defined as:
1 Q g = (hs - hr)W7 Eq. 6 3
Steam enthalpy (Btu /lb) wheret h s
r Feedwater enthalpy (Blu/lb) h.
Feedwater flow (1b/hr).
j Wr
=
The-Steam enthalpy is based on measurement of Steam Generator outlet Steam pressure, assuming saturated conditions.
The Feedwater enthalpy is based on the measurement of Feedwater temperature and Feedwater i
pressure. The Feedwater flow is determined by multiple measurements and the following calculation:
y Wr - (K)(F )flpg)(d/p))l/2 Eq. 7 a
Feedwater venturi flow coefficient where; K
=
'Feedwater venturi correction for thermal expansion F.
a 3
Feedwater density (1b/ft )
pf
=
Feedwaterventuripressuredrop(inchesHO).
d/p
=
2 The feedwater venturi flow coefficient is the product of a number of i
constants' including as-built dimensions of the venturi and calibration l
tests performed by the vendor. The thermal expansion correction is based on the coefficient of expansion of the. venturi material and the
' difference between Feedwater temperature and calibration temperature.-
Feedwater density is based on the measurement of Feedwater temperature' and Feedwater pressure.. The venturi pressure drop is obtained from the-t output of the differential pressure cell connected to the venturi, 1
l' RCP heat addition is determined by calculation, based on the best estimate of coolant flow, pump head, and pump hydraulic efficiency.
t h
e
1 <
The primary system net heat'lesses are ~ determined by calculatiCn, 1
l considering the following system heat inputs and heat losses-Charging flow Letdown flow Seal injection flow RCP thermal barrier. cooler heat removal Pressurizer spray flow Pressurizer surge line flow Component insulation heat losses Component support heat losses l
CRDH heat losses.
A single calculated sum for 100% RTP operation is used for these losses or heat inputs.
+
The Hot Leg and Cold Leg enthalpies are based on the measurement of the Hot. Leg temperature, Cold Leg temperature and the Pressurizer pressure.
The Cold. Leg specific volume is based on measurement of the Cold Leg 4
- temparsture and Pressurizer pressure, j
The.RCS' flow measurement is thus based on the following plant measurements:
Steamline pressure (P )
[
s i
Feedwater temperature (T )
f feedwater pressure (P ).'
f L
=Feedwater venturi differential pressure (d/p) l
-Hot Leg temperature (T )
l H
Coldlegtemperature(T)'
C Pressurizerpressure-(P) p SteamGeneratorblowdown(if.notsecured)
F and on the following calculated values:
Feedwater venturi flow coefficients (K) feedwater venturi thermal expansion correction (F )
a Feedwater density (pf)
)
'11-
e, Feedwaterenthalpy(h)
'j f
Steam enthalpy (h )
s Moisturecarryover(impactsh) s
- Primary system net heat losses (Q )
L RCP heat. addition (0 )
p
' Hot leg enthalpy (hg)
Cold leg enthalpy (h )*
C These measurements and calculations are presented schematically on Figure 1.
Four calculations have been done; one set of calculations is for four loop operation and one set is for three loop operation, and each set includes calculations for Veritrak and Rosemount pressurizer pressure transmitters. The derivation of the measurement errors and flow 4
uncertainties on Table 5 are noted below.
I Secondary Side The secondary side uncertainties are in four principal areas, feedwater
. flow, Feedwater enthalpy, Steam enthalpy and RCP heat addition. These j
four areas are specifically identified on Tables Sa, b, c and d.
For the nessurement of feedwater flow, each Feedwater venturi is calibrated by.the vendor in a hydraulics laboratory under controlled conditionstoanaccuracyof_(
]?a,b,c.
The calibration i
data which substantiates this accuracy is provided to the plant by the t,
vendor.. An additional uncertainty factor of (
]+a,c is l
i included for installation effects, resulting in a conservative overall-flow coefficient (K) uncertainty of (
]+a,c, :Since RCS. loop flow is proportional _to Steam Generator thermal output which is j.
proportionalito feedwater flow, the flow coefficient uncertainty is expressed as (
)+a,c.
It.should be noted.that no allowance
' is made for venturi fouling. The venturis should be inspected, and cleaned if necessary. prior to performance of the precision measurement.
- If fouling is-present but not removed, it's effects must be treated as a flow bias..
The uncertainty applied to _the-Feedwater venturi thermal expansion correction (F )'is based on the uncertainties of the measured Feedwater a
. temperature and the coefficient of thermal expansion for the venturi
t-t material, usually 304 stainless steel for this material, a change of l
t i 1 'F ih the nominal Feedwater temperature range changes F, by t
1 0.002 % and the Steam Generator thermal' output by the same amount.
i
/
An uncertainty in F of i 5 % for 304 stainless steel is used in this a
analysis. This results in an additional uncertainty of [
)+a,c in Feedwater flow. Westinghouse uses the conservative value of [
l
)+a,c, i
Using the 1967 ASME Steam Tables it is possible to determine the sensitivities of various parameters to changes in Feedwater temperature and pressure. Tables 3a, b, e and d notes the instrument uncertainties for'the hardware used to perform the measurements. Tables 4a, b, e and d lists the various sensitivities. As can be seen on Table 4, Feedwater temperature uncertainties have an impact on venturi F, Feedvater a
density and.Feedwater.enthalpy.
Feedwater pressure uncertainties impact Feedwater density and Feedwater enthalpy.
l i
Feedwater venturi d/p uncertainties are converted to t Feedwater flow using the following conversion factor:
% flow - (d/p uncertainty)(1/2)(transmitter span /100)2 The Feedwater flow transmitter span is.[
)+ac of nominal flow.
'Using the 1967 ASME Steam Tables again, it-is possible to determine the sensitivity.of Steam enthalpy to changes in Steam pressure and Steam quality. Table 3 notes the uncertainty in Steam pressure and Table 4
=f provides the sensitivity.
For Steam quality, the Steam Tables were used to determine the sensitivity at a moisture content of [
)+a,c.This
[
value. is noted on Table 4; The net pump heat uncertainty is derived from the combination of the primary system net heat losses and pump. heat addition and are summarized 1
for a fourLloop plant as follows:
l 1
System heat losses
-2.0 MWt Component conduction and convection losses
-1.4 Pump heat adder ilLQ Net Heat input to RCS
+10.6 MWt The uncertainty on system heat losses, which is essentially all due to charging and letdown flows, has been estimated to be [
]+a,c of the calculated value. Since direct measurements are not possible, the uncertainty on component conduction and convection losses has been assumed tobe[
)+a,c of the calculated value.
Reactor coolant pump hydraulics are known to a relatively high confidence level, supported by system hydraulics tests performed at Prairie Island II and by input power menurements from several plants, therefore, the uncertainty for the pump
'heatadditionisestimatedto've(
)+a,c of the best estimate value.
y Considering these parameters as one quantity, which is designated the net pump heat uncertainty,- the combined uncertainties are less than
[
]+a,c of the total, which is [
]+a.c of core power.
Primary Side The primary side uncertainties are in three principal areas, Hot leg c
enthalpy; Cold leg enthalpy and Cold Leg specific volume. These are specifically noted on Table 5.
Three primary side parameters are actually measured, T, TC and Pressurizer pressure. Hot leg enthalpy is H
influenced by T, Pressurizer pressure and Hot leg temperature streaming.
H The uncertainties for the instrumentation are noted:on Table 3 and the sensitivities are provided on Table 4.
The Hot leg streaming is split into random and bias-(systematic). components.
For Fii11 stone 3 with RTDs located lin thermowells (bypass manifolds eliminated), the streaming uncertainty is,
(-
]+a,c random and [
]+a,c systematic.
4 I
The Cold Log Cnthalpy and specific volume uncertainties are impacted by TC instrument uncertainty and-and Pressurizer pressure. Table 3 notes the TC Table 4 provides the sensitivities.
Noted on Table 5 is the plant specific RTD cross-calibration systematic allowance. When necessary, an allowance is made for a systematic temperature orror due to the.RTD cross-calibration procedure. No allowance was necessary
'for this plant.
Parameter dependent effects are identified on Table 5.
Westinghouse has determined the dependent sets in the calculation and the direction of.
.i'nteraction, i.e., whether components in a dependent set are additive or subtractive with respect to a conservative calculation of RCS flow. The same work was performed for the instrument bias. values. As a result, the calculation explicitly accounts for dependent effects and biases with credit takenfor. sign (or-direction-ofimpact).
Using Table 5a (most conservative value), the 4 loop uncertainty equation (with biases) is as follows:-
+a,c Basedonfour. loops,thenumber,typeandmeasurementmethodofRTDs,ankthe vessel Delta-T, the flow uncertainty for the precision flow calorimetric.is:
- of loops' flow uncertainty-(% flow)
+a.c 4'
' Based on'three loops, the number, type and measurement method of RTDs, and the vessel Delta T, the flow uncertainty for the precision flow calorimetric is:-
- of loops flow uncertainty (% flow)
+a,c 3
r TABLE 3 (a) i-FLOW CALORIMETRIC INSTRUMENTATION UNCERTAINTIES FOUR LOOP OPERATION VERITRAK PRESSURIZER PRESSURE TRANSMITTER T
PRZ PRESS
(% SPAN)
FW TEMP FW PRES FW d/p STM PRESS TH C
+a,c SCA =
SMTE=
'l SPE =
- STE =
- SD
=
R/E =
RD00T=
BIAS =
CSA =
LOF INST USED 3
1 4
% d/p psia a
INST SPAN - 400.
2000.
120.
1300.
120.-
120.
800.
' INST:UNC.
+a,c
-(RANDOM)'-
-i c
INST.UNC.
(BIAS)-
=
NOMINAli
.436, 1057.
-957, 617.2-557.0' 2250.
- Conservative values have been used.
- All parameters are read by the process computer.,
- e,
.j k
i l
i -
j' L
TABLE 4 (a).
I FLOW CALORIMETRIC SENSITIVITIES FOUR LOOP OPERATION VERITRAK PRESSURIZER PRESSURE TRANSMITTER FEEDWATER FLOW TEMPERATURE
=
MATERIAL
=
DENSITY TEMPERATURE PRESSURE'
=
DELTA P
=
FEEDWATER ENTHALPY TEMPERATURE
=
PRESSURE
=
1194.5 BTU /LBM
-h
=
3 415.3 BTil/LBM hr 779.2 BTV/LBM Dh(SG)
STEAM ENTHALPY
+ a, c PRESSURE
=
4 M0ISTURE
=
HOT LEG ENTHALPY TEMPERATURE PRESSURE g
638.7 BTU /LBM h
=
h 555.9 BTU /LBM
=
82.7 BTU /LBM D(VESS)
=
1.540 BTU /LBM OF Cp(T )
=
H COLD LEG-ENTHALPY
+a,c TEMPERATURE =
=
PRESSURE 1.261 BTV/LBM OF Cp(T )
=
C
. COLD LEG SPECIFIC VOLUME
+ a, c TEMPERATURE
=
PRESSURE l
1 ____-___z__________
_ _ _ _ _ _ - _ _. = -. - _ _ _. _
._a
1
.i TABLE 5(a)-
CALORIMETRIC RCS FLOW P.EASUREMENT UNCERTAINTIES l
- FOUR LOOP OPERATION VERITRAK PRESSURIZER PRESSURE TRANSMITTER j
?
COMPONENT.
INSTRUMENT ERROR FLOW UNCERTAINTY FEEDWATER FLOW
+a,c o.
i VENTURI i
THERMAL EXPANSION COEFFICIENT TEMPERATURE MATERIAL-i DENSITY j
TEMPERATURE
~ PRESSURE DELTA P FEEDWATER ENTHALPY-TEMPERATURE 1
PRESSURE 1
STEAM ENTHALPY l
PRESSURE M0ISTURE m
. NET PUMP HEAT ADDITION i
HOT LEG ENTHALPY TEMPERATURE.
i
. STREAMING, RANDOM STREAMING,' SYSTEMATIC =
PRESSURE 1
COLD' LEG ENTHALPY-
-TEMPERATURE-PRESSURE t
COLD LEG SPECIFIC VOLUME t
TEMPERATURE PRESSURE RTD CROSS-CAL ~ SYSTEMATIC ALLOWANCE i
- '+, ++ INDICATE SETS OF DEPENDENT PARAMETERS t
I I
,y,.
rf
.tt j.
y k) fik e e
sh [_f.'
t,'
j s
w Af f..-
..JTABLE5(a)(CONTINUED)
.j
'N<
CALORIMETRIC RCS FLOW MEASUREMENT UNCERTAINTIES l
- n
.FOUR' LOOP OPERATION VERITRAK PRESSURIZER' PRESSURE TRANSMITTER:
j FLOW UNCERTAINTY-1'
- COMPONENT-
- f '$
- BIAS: VALUES'
+a,c.
FEEDWATER PRESSURE.
DENSITY ENTHALPY J
y; 1, ~.
LSTEAM PRESSURE ENTHALPY ll',,
PRESSURIZER 7RESSURE ENTHALPY - HOT LEG'.
J>
SPECIFIC VOLUME --COLD LEG
'ENTHALPY - COLD LEG:
1
%n<
FLOW BIAS TOTAL VALUE t
J
.I
- n
!!ita 4
+a,c f 7;,
= SINGLE' LOOP' UNCERTAINTY.(WITHOUT BIAS VALUES)-
N LOOP UNCERTAINTY
.(WITHOUT BIAS VALUES) j (WITHBIASVALUES)
't
.N JLOOP UNCERTAINTY g ).. -
DIi y '1lj '
i h
ha e...
a i
}
g
- 5. f.'
f_
,,-[t j.
kh, '
s.m 4
5
, t j
!gh I i
lO Q t
~
gi -
'i' i
-l l >;g l L / I> : p j,
5 l g,5
,p f jy
- Q.i
.cch'tilg
,{
l i
-1, 7;NUjM Q', b :
X a
- g
- ))&{ JlT. ]pl Q
l h;w[_.W[8 l
,\\,
e g
- 4
'l6 iA
.p i
w a
?h.i jt, '.
lj
~
efb(e; w,
N a:
a h
- g. h.
ww Ib =.
. i.i <
h y,
yf s
o
..t
+
t
.:(
i A. _
t.G [ '
4 y
i V,,: T
,i l'. '
, Ms p*(- f -i
.Mt h,-
.. n.
- o
li
.i >
' rf] ' $'
0%
M
(.
Ww TABLE 3 (b)-
FLOW CALORIMETRIC INSTRUMENTATION UNCERTAINTIES 4
FOUR LO')P OPERATION ROSEMOUh' PRESSURIZER PRESSURE TRANSMITTER 4
TC_
PRZ PRESS
(% SPAN)L FW TEMP. FW PRES FW d/p STM PRESS TH
+a,c
- SCA =
SMTE=:
SPE =
STE ='
w,
- q.-
SD- -
?[
R/E =
l[,
- RDOUT=
i-BIAS =
.-CSA =
- OF' INST USEDi
'3 1
4
, g k
F 0F' ps'ia
-% d/p psia F.
0 OF psia
.j
- INST SPAN i gn0
- 2000, 120.-
- 1300, 120,
- 120, 800,-
4
! NST UNC,.
+a,c-(RANDOM) =
. INST:UNC,
.J
- (BIAS)?
=
Nt NOMINAL: =l436,
- 1057,
- 957.
617,2 SS7,0 -
- 2250.
4
- 1+
- *c Conservative values have been used.
+
i All. parameters are read lby the process computer.
'i.
i 1
E t
W'
-y o
TABLE 4:(b) l FLOW CALORIMETRIC SENSITIVITIES 4
FOUR~ LOOP OPERATION l
^
ROSEMOUNT! PRESSURIZER-PRESSURE TRANSMITTER.
FEE 9 WATER FLOW.
i F'
+a,c.
a
,t
- TEMPERATURE
=
MATERIAL-
=
DENSITY-S TEMPERATURE-J:&
PRESSURE
=
DELTA.P 6
=
FEEDWATER ENTHALPY TEMPERATURE
=
=
PRESSURE' 1194.5 BTV/LBM
. l h
3 hr
~
415.3-BTU /LBM~
=
779.2 BTU /LBM Dh(SG)
=
STEAM ENTHALPY
+a,c PRESSURE
~
=
MOISTURE
=
1 HOT: LEG:ENTHALPY:
+
TEMPERATURE'
=
PRESSURE
=
a t
hH 638.7 BTU /LBM 4
=
555.9 BTV/LBM-
.hc(VESS)
=
82.7iBTU/LBM Dh
==
o 1.540 BTU /LBM OF
- Cp(T ):
=
H COLD LEG ENTHALPY
--+a,c-
.TEMPERATUREL i=
l h
PRESSURE
=
1.261 BTU /LBM O ?-
F
+
LCp(T )
=
C
['
[COLDLEGSPECIFICVOLUME-
+a,c
" TEMPERATURE
=
4,, '
PRESSURE-s l' ('
3 t
.s e '
1
,1 v
6,
~
1 o,
v f
4 TABLE S (b)'-
U 4
CALORIMETRIC RCS FLOW MEASUREMENT UNCERTAINTIES-
.FOUR LOOP OPERATION-h-
ROSEMOUNT' PRESSURIZER PRESSURE TRANSMITTER COMPONENT-INSTRUMENT ERROR FLOW UNCERTAINTY
)
FEEDWATER FLOW
+a,c VENTURI
.' THERMAL EXPANSION COEFFICIENT
' TEMPERATURE.
MATERIAL
' DENSITY' TEMPERATURE.
PRESSURE Dell A P FEEDWATER ENTHALPY-TEMPERATURE PRESSURE STEAM ENTHALPY PRESCURE MOISTURE NET. PUMP HEAT ADDITION HOT LEG.ENTHALPY-
-TEMPERATURE:.
t 3
STREAMING,; RANDOM:
STREAMING, SYSTEMATIC
.. PRESSURE 4
bM_
' COLD LEG ENTHALPY iTEMPERATURE
.a
' PRESSURE-COLD LEG SPECIFIC' VOLUME-1 TEMPERATURE LPRESSURE-
-RTD CROSS-CAL SYSTEMATIC ALLOWANCE'
~
'.'I
_ $ "i
,.+, ++ INDICATE SETS OF DEPENDENT PARAMETERS lr K
q 4
)
] :
-l
- g;
.l
+
(!t,
.}
q.-
TABLE.5 (b)(CONTINUED)1 J
CALORIMETRIC RCS FLOW MEASUREMENT UNCERTAINTIES FOUR LOOP OPERATION
-t.
t ROSEMOUNT.' PRESSURIZER PRESSURE TRANSMITTER COMPONENT-FLOW UNCERTAINTYT l
BIAS VALUES-
+a,c FEEDWATER PRESSURE DENSITY ENTHALPY
- in
-STEAM PRESSURE-ENTHALPY PRESSURIZER PRESSURE--
ENTHALPY - HOT LEG ENTHALPY.--COLD LEG 1
SPECIFIC VOLUME - COLD LEG
' FLOW BIAS TOTAL VALUE
+a,c SINGLE LOOP UNCERTAINTY-(WITHOUT~ BIAS VALUES) l 2
N LOOP UNCERTAINTY..
.(WITHOUT BIAS VALUES) i N zLOOP UNCERTAINTY.
(WITHBIASVALUES)
?
'2
'I
)
.i
- {
a
. il 3
1 4
l ;.-
{
it.,
p' 1 n
ka!l.
c.
~
\\
i
~
i l
. w.
.t,'
y s J\\
t
.I j
e TABLE 3(c)
FLOW CALORIMETRIC INSTRUMENTATION UNCERTAINTIES THREE LOOP OPERATION VERITRAK PRESSURIZER PRESSURE TRANSMITTER-PRZ PRESS
(% SPAN)
FW TEMP FW PRES fwd /p STM PRESS TH TC
-+a,c-
-l
'SCA~-
n SMTE=.
'SPE:=
JSTE -
-SD
=
R/E -
RDOUT=
BIAS =
-CSA -
j f 0F' INST ~USED 3
1 4
l 0F OF psia l
0F;
' psia
% d/p psia
- INST SPAN.-
- 400.'
~2000.
120..
1300.
-120.
- 120, 800.
-l e
INST UNC;
+a,c-
-(RANDOM).-
i INST UNC.
(BIAS)-
NOMINAL
'-l 404'.
1000; 900.-
609.0-550.2-
-2250.
m
- c 1
fs
-* Conservative values have been used.
1 q
LAll parameters 'are-read b'y the process computer, l
o o
i -
-t l
1 s
.i.
'i ):
1 TABLE 4 :(c)-
T-FLOW CALORIMETRIC SENSITIVITIES:
-THREE LOOP OPERATION
'V'ERITRAK PRESSURIZER PRESSURE TRANSMITTER FEEDWATER FLOW
. TEMPERATURE
=
MATERIAL
=
g-DENSITY:
-TEMPERATURE-PRESSURE DELTA P
=
FEEDWATER ENTHALPY:
' TEMPERATURE-PRESSURE..
=
a' 1196.4 BTU /LBM h
=
y 380.5 BTU /LBM hr
=
815.9 BTU /LBM-q Dh(SG)
=
STEAM ENTHALPY
+a,c
. PRESSURE M0ISTURE HOT LEG ENTHALPY L
TEMPERATURE
=
PRESSURE!
H 626.3 BTU /LBM i
'h
=
- Dh(VESS)_
547.4 BTU /LBM d
he:
78.9 BTU /LBM-
=
_l.479_ BTU /LBMOF Cp(Tg);
- =
- COLD LEG ENTHALPY
+a,c-TEMPERATURE;
=
-m PRESSURE'
=
1.243 BTU /LBM OF
(
Cp(T ).
C.
a COLD LEG SPECIFIC VOLUME.
+a,c :
b p'
TEMPERATURE
=
L
' PRESSURE i=
g s
- i;\\
i :.
d
. ~, -
k
[
(s I,
t s'-
3
'Ng
- -TABLE 5 (c) s
.CALO'RIMETRIC RCS FLOW MEASUREMENT UNCERTAINTIES
--THREE LOOP OPERATION-J
~{
VERITRAK PRESSURIZER PRESSURE TRANSMITTER'
. COMPONENT INSTRUMENT ERROR FLOW UNCERTAINTY-j 3-FEEDWATER FLOW
+a,c 1
3;8,
1 VENTURI' r
A THERMAL EXPANSION COEFFICIENT-A TEMPERATURE
("
-MATERIAL t
DENSITY o
M.
TEMPERATURE Jii 1 PRESSURE
.Y DELTA P'
- FEEDWATER~ENTHALPY.
m TEMPERATURE-Aq PRESSURE W'
STEAM'ENTHALPY-
- PRESSURE.
- e MOISTURE' i
NET PUMP' HEAT-ADDITION f,
' HOT LEG ENTHALPY
- )
TEMPERATURE-STREAMING,1 RANDON.
y ', 1 STREAMING, SYSTEMATIC
'W n
-PRESSURE COLD ~ LEG ENTHALPY N,
TEMPERATURE-L
' PRESSURE LCOLD' LEG SPECIFIC VOLUME?
l J
TEMPERATURE o
~ PRESSURE j
n
~ '
^
RTD' CROSS-CAL' SYSTEMATIC ALLOWANCE M
y.
1 a1
- l. q p
- +,-++ INDICATE SETS'0F DEPENDENT PARAMETERS.
' ' ~ ' '
7 i
+
l., b. h 'i i
M 5t n.
s t.
\\
=t-ji
- q' 26-
-l 4
m
_1_'_________________m___,___m_.
.v
L
-o.
. TABLE 5.(c)(CONTINUED) 3 CALORIMETRIC RCS FLOW MEASUREMENT UNCERTAINTIES THREE LOOP OPERATION VERITRAK PRESSURIZER PRESSURE. TRANSMITTER'
^
COMPONENT FLOW UNCERTAINTY
' BIAS VALUES- '
+a,c
-FEEDWATER PRESSURE-DENSITY ENTHALPY l
STEAM PRESSURE ENTHALPY PRESSURIZER PRESSURE ENTHALPY - HOT LEG
,f ENTHALPY - CdLD LEG FLOW BIAS TOTAL VALUE
+a c
.y
. SINGLE LOOP UNCERTAINTY (WITHOUT BIAS VALUES
^
N. LOOP UNCERTAINTY (WITHOUT BIAS VALUES N-LOOP. UNCERTAINTY (WITH BIAS VALUES)
]
n t
t l
i w
l
".(
I f:
i i
k a
a i
f -,
I-('
i l
y l'
j.. -
y
+
i TABLE,3 (d)
-FLOW CALORIMETRIC INSTRUMENTATION UNCERTAINTIES j
THREE LOOP OPERATION ROSEMOUNT-PRESSURIZER PRESSURE TRANSMITTER L,
._(% SPAN)
FW TEMP-' FW PRES-FW d/p STM PRESS TH TC PRZ PRESS t
-+a,c SCA =
.SMTE=
SPE --
STE =
1,
SD ='-
R/E =
RD0UT=
- BIAS =
CSA =
,; 1i '
't I
- OF-INST-USED 3
1 4
0F 0F psia 0F-
' psia
%d/p psia _
e 4
. INST SPAN400.
2000.
120.
1300.
120.-
120.
800.-
INST UNC.
+a,c-
. (RANDOM) -
LINST UNC.
(BIAS)-
=
1 NOMINAL -- 404.-
'1000.
900,-
609.0 550.2
-2250.-
- Conservative values have been used.
y m
m'
/All parameters :are read by the process computer.
s v2.
j ll m
pi \\}[
i, 1
l.
l ;-
P,
D j
'f, i
, TABLE 4 (d).
FLOW CALORIMETRIC SENSITIVITIES l) 1 c
THREE LOOP OPERATION' 1
ROSEMOUNT PRESSURIZER PRESSURE TRANSMITTER-FEEDWATER FLOW
'F*
+a,c oC TEMPERATURE l
. MATERIAL
=
'l DENSITY >
. TEMPERATURE
.=
4
' PRESSURE DELTA P-.
FEEDWATER ENTHALPY l
TEMPERATURE-PRESSURE:
1196.4 BTV/LBM-h h
shr:
380.5 BTU /LBM, j
Dh(SG) 815.9 BTU /LBM l
o s
- STEAM ENTHALPY
+a,c:
PRESSURE M0ISTURE 7
HOT; LEG ENTHALPY-,
i
-TEMPERATURE-1 m
=
PRESSURE-
=
H 626~.3 BTU /LBM h.
W ~q
'Dh(VESS) 547.4 BTU /LBM he 1
. 78.9' BTU /LBM.
1.479 BTU /LBM OF.
M v
Cp(T)
=-
H Y
COLD'L'EG ENTHALPY.-
^
l-
+a,c H
TEMPERATURE:
4 PRESSURE-
.1.243. BTU /LBMN:
E
-Cp(T)
F C
COLD LEG SPECIFIC VOLUME
+a,c'
' TEMPERATURE.
PRESSURE "
- =
n l j t. i t
..d..
1.
i i
3 5
6 1
1G
[
., ' ;[ +e
- ,,1)
TABLE 5 (d)
C4LORIMETRICRCSFLOWMEASUREMENTUNCERTAINTIES
-THREELLOOP OPERATION s
ROSEMOUNT PRESSURIZER PRESSURE-TRANSMITTER COMPONENT INSTRUMENT ERROR FLOW UNCf.RTAINTY' FEEDWATER FLOW
+a,c VENTURI THERMAL EXPANSION COEFFICIENT
' TEMPERATURE MATERIAL DENSITY.
TEMPERATURE PRESSURE DELTA P FEEDWATER ENTHALPY-TEMPERATURE PRESSURE-STEAM ENTHALPY PRESSURE 4--
MOISTURE
-NET PUMP HEAT ADDITION
- HOT LEG ENTHALPY -
TEMPERATURE-
- STREAMING, RAND 0M STREAMING,. SYSTEMATIC PRESSURE COLD-LEG ENTHALPY'
-TEMPERATURE PRESSURE 1
-COLD ~LEGiSPECIFIC VOLUME iTEMPERATURE-PRESSURE'
.RTD CROSS-CAL SYSTEMATIC l ALLOWANCE
, +, ++ INDICATE SETS OF DEPENDENT PARAMETERS F
m i-
'c i,
t4 u
TABLE 5 (d)(CONTINUED) t y.
1 CALORIMETRIC RCS FLOW MEASUREMENT UNCERTAINTIES h
THREE LOOP OPERATION i
}
ROSEMOUNT PRESSURIZER PRESSURE TRANSM3TTER l
COMPONENT FLOW UNCERTAINTY BIAS VALUES
+a,c FEEDWATER PRESSURE DENSITY ENTHALPY L
STEAM PRESSURE ENTHALPY-PRESSURIZER PRESSURE ENTHALPY - HOT LEG E
ENTHALPY - COLD LEG E
SPECIFIC VOLUME - COLD LEG i
-FLOW BIAS TOTAL VALUE
+ a, C I
SINGLE LOOP UNCERTAINTY-(WITHOUT BIAS VALUES)
N LOOP UNCERTAINTY.
'(WITHOUT BIAS VALUES)
N LOOP UNCERTAINTY.
(WITH BIAS VALUES) j b'
- 1 h
t L
I 1*
f i
1 i,
A
As noted earlier,:the precision flow calorimetric is used as the reference'for the normalization of the Cold Leg elbow taps.
Assuming that the elbow tap d/p
-transmitters are used to feed the plant process computer, it is a simple matter j
to perform Technical Specification required su,,eillance.
Tables 6a, b,- c and d note the instrument uncertainties for normalization of the elbow taps, assuming one elbow tap per-loop. The d/p transmitter uncertainties are converted to % flow on the same basis as the Feedwater venturi d/p, The ' elbow tap-uncertainty'is then combined with the precision flow calorimetric uncertainty.
This combination of uncertainties results in the following total flow uncertainty for four loop operation:
- of loops -flow uncertainty (% flow) 4-
--i 2.3 The corresponding RTDP value.for four loop operation is:
i 4
,y
- of. loops -
standard deviation (% flow)-
+a,c
~4-l 1
IThe total' flow uncertainty for three loop operation is:
i
- 'of loops flow uncertainty-(% flow)
H-3:
2.6 The corresponding RTDP-value for three-loop operation is:
- .of loops-standard deviation (% flow) o
- +a,c'
~3 i
TABLE 6 (a)
COLD LEG El. BOW TAP FLOW UNCERTAINTY FOUR LOOP OPERATION VERITRAK PRESSURIZER PRESSURE TRANSMITTER INSTRUMENT UNCERTAINTIES
% d/p SPAN-
% FLOW
+ a, c
. PMA -
PEA -
SCA =
SPE =
STE -
SD -
RCA -
RMTE-RTE -
RD ---
ID -
- A/D -
. RDOUT=
BIAS -
FLOW CALORIM. BIAS FLOW CALORIMETRIC JINSTRUMENT SPAN 1
+ a, c SINGLE LOOP ELBOW TAP FLOW UNC -
N LOOP ELB0W TAP FLOW UNC'
~ H. LOOP RCS FLOW UNCERTAINTY 2.3 (WITH BIAS VALUES)-
r=
w
{
l e
l'(
> 1
TABLE 6 (b).
COLD-LEG ELBOW TAP FLOW UNCERTAINTY FOUR LOOP OPERATION ROSEMOUNT PRESSURIZER PRESSURE TRANSMITTER INSTRUMENT UNCERTAINTIES t
% d/p SPAN
% FLOW
+ a, c
.PMA =
PEA =
SCA =
'SPE =
STE =
SD L =
RCA =
RMTE=
RTE =
RD
=
ID --
LA/D =
.RDOUT=
' BIAS =
FLOW CALORIN. BIAS
=-
FLOW CALORIMETRIC.
=
INSTRUMENT SPAN'
=
+a,c
-SINGLE LOOP ELB0W TAP FLOW UNC =
N' LOOP.ELB0W TAP FLOW UNC
?
.(WITHOUT BIAS VALUES)
-=
'(WITH BIAS VALUES) 2.2-
=
I i !
TABLE 6.(c)
COLD' LEG ELBOW TAP FLOW UNCERTAINTY THREE LOOP OPERATION VERITRAK PRESSURIZER PRESSURE TRANSMITTER INSTRUMENT UNCERTAINTIES
% d/p SPAN
% FLOW
+a,c PMA =
PEA =
SCA =
SPE -
STE -
=
RCA =
RMTE--
. RTE =
RD
=
10
=
- A/D =
RDOUT=-
BIAS =-
FLOW CALORIM. BIAS =
FLOW CALORIMETRIC.
=
INSTRUMENT SPAN
=
+ a, c
-SINGLE LOOP ELB0W-TAP FLOW UNC =
N LOOP ELBOW TAP FLOW UNC
=
H LLOOP RCS' FLOW UNCERTAINTY
_(WITHOUT BIAS VALUES)
N LOOP RCS' FLOW UNCERTAINTY 2.6
-(WITH BIAS VALUES)
=
l c _-_-- _ ____- -______ ___-_
~
k g
TABLE 6 (d)-
tCOLD. LEG ELBOW TAP FLOW UNCERTAINTY THREE LOOP OPERATION ROSEMOUNT. PRESSURIZER PRESSURE TRANSMITTER a-INSTRUMENT UNCERTAINTIES
,+
% d/p SPAN
% FLOW
+ a c PMA =
'l
" PEA =
SCA =
SPE =
STE =
SD =
RCA' -
RMTE=
RTE RD =
- ID -
A/D =
- RD00T=
BIAS =
1 FLOW CALORIM. BIAS' =
7 FLOW CALORIMETRIC
=
INSTRUMENT SPAN
=
6' SINGLE' LOOP ELB0W TAP' FLOW UNC =
Ni LOOP ELBOW TAP' FLOW-UNC'
=
N iLOOP RCS; FLOW UNCERTAINTY
- (WITHOUT BIAS VALUES)-
N LOOP RCS FLOW UNCERTAINTY-2.5'
- (WITH BIAS VALUES)
i i Y
b l
.id 6 t
4.1 = Reactor Power 1 Generally a plant performs a primary / secondary side heat balance once
- every 24 h'ours when power is above 15% Rated Thermal Power. This heat-balance is-_used to verify that the plant is operating within the limits L
of the Operating License and to adjust the Power Range Neutron Flux channels when the difference between the NIS and the heat balance is
. greater. than that required by the plant Technical Specifications, n
Assuming that the primary and secondary sides are in equilibrium; the i
core power is determined by summing the thermal output of the steam generators, correcting ~ the total secondary power for Steam Generator blowdown (if not secured), subtracting-the RCP heat addition, adding the, primary side-system losses, and dividing by the core rated Btu /hr i
T.
at fullipower. The equation for this calculation is:
3 p + (0 /N)))(100)
RP = H N)(03g - O t
H Eq. 8 i
- where;
- Core power (% RTP)
.=>
N Number of primary side 1 oops-
=
Steam Generator thermal output-(BTV/hr) as defined in
~Q g
_3 L Eq' : 6.
'Q
-- ' RCP heat: adder;(Btu /hr) as-defined in Eq.- 5 p
=t Primary system net heat losses (Btu /hr) as defined in:
y Qt Eqh 5 Core' rated Btu /hr at_ full power.
-H' For the purposes of this uncertainty: analysis (and ba~ sed on H noted.
X $
.above) it fisf assumed that the' plant is at 100% RTP when the measurement -
is-taken. Measurements performed at lower power -levels will. result.in
-1
'different uncertainty values.
However, operation at-lower power levels..
-results in increased margin to DNB far in excess ofLany margin losses
.due.to: increased. measurement uncertainty.
The secondary. side power calorimetric equations and effects are the
- same as those noted for the precision flow calorimetric :(secondary side
portion)', equations 6 and 7.
The measurements and calculations are r
presented schematically on Figure 2.
Tables ~ 7a and b provides the
= instrument uncertainties for those measurements performed.
Since it is necessary to make this-determination daily, the plant process computer is used for the measurements. The sensitivities calculated are the-
- same as those noted for the secondary side on Table 4.
As noted on Table 8a and b, Westinghouse has determined the dependent sets in the calculation and the direction of interaction.
This is the same as that performed for the RCS flow calorimetric, but applicable only to power.-
The'same was performed. for the bias values noted.
It should be noted that Westinghous'e does not include any allowance for Feedwater venturi fouling. The effect of fouling is to result in an indicated power
~
~
- higher than-actual, which is conservative.
Using the power uncertainty values noted on Table 8a, the 4 loop
. uncertainty.(with bias values) equation is as follows:
+a,c l
y Based en.-four loops'and the instrument uncertainties for the four
. parameters, the power measurement uncertainty.for the' secondary side
~
power calorimetric is:
- #: of. loops power uncertainty (% RTP)
'+a,c q
l
-Based on three loops and'the instrument uncertainties for the four (parameters,- the power. measurement uncertainty for the. secondary side
' power calorimetric is:-
.# of ~ loops-power uncertainty (% RTP) l
+a,c.
IV. CONCLUSIONS.
.The preceding sections. provide the methodology to account for -
,n
~
y
., [ e
'l m..
o
,L 1
' pressure,--temperature, power and RCS flow uncertainties for the RTDP
~
~
analysis ~. t The plant-specific instrumentation and procedures have been reviewed for Millstone 3 and the uncertainty. calculations are-More conservative values are used in'the RTDP analysis and l
f completed.1 are-specified for Veritrak and Rosemount transmittters as indicated
'.below :.
Both types of transmitters are used at Millstone 3.
L
'Veritrak Transmitters
+a,c j
l,,
. Pressurizer pressure-(control)
Temper.ature (control)
.j Power-4 loop operation 3 loop operation RCS Flow:
i 2.3% flow 4 loop operation-
+ 0.1% flow bias 2.7% flow '
3 loop. operation
+ 0.1% flow bias Rosemount Transmitters
+a,c
. Pressurizer pressure (control).
i LTemperature.(control)
Power 4 loop w eration' i
3' loop' operation o
RCS Flow <
1.2.4% flow:
4 loop operation
- 1
? 2.8% flowi 3 loop. operation i
,i 4
0 k
- 5. (-[
if
' ~f,j j-x 4
t i?
--.L-- l.
TABLE. 7.- (e)
POWER CALORIMETRIC INSTRUMENTATION UNCERTAINTIES FOUR LOOP OPERATION
(% SPAN).
FW TEMP FW PRES 'FW d/p STM PRESS
)
+a,c SCA -
SMTE-
' SPE -
BIAS-RCA -:
. RMTE-RTE -
e
.RD a
. I0 -
- A/D =
CSA-'-
0F
-psia
% d/p psia J
INST SPAN - 400.
2000.
120.
1300.
7 INST UNC-
+a,c (RAND 0M)-
1
- INST-UNC.
(BIAS)
=
NOMINAL
- 436.-
1057.
957.
4
?
4 i
b
\\
f J
'I,
= TABLE 8 (a)
SECONDARY SIDE POWER CALORIMETRIC MEASUREMENT UNCERTAINTIES FOUR LOOP OPERATION COMPONENT-INSTRUMENT ERROR POWER UNCERTAINTY
+a,c FEEDWATER FLOW-VENTURI
-THERMAL EXPANSION COEFFICIENT TEMPERATURE MATERIAL DENSITY' TEMPERATURE PRESSURE DELTA P-FEEDWATER ENTHALPY TEMPERATURE PRESSURE STEAM ENTHALPY PRESSURE M0ISTURE
- NET' PUMP HEAT ADDITION BIAS VALUES FEEDWATER DELTA-P
'FEEDWATER PRESSURE-DENSITY ENTHALPY STEAM PRESSURE ENTHALPY POWER BIAS TOTAL VALUE-INDICATE _ SETS-0F' DEPENDENT PARAMETERS SINGLE LOOP UNCERTAINTY (WITHOUT BIAS' VALUES)_
N. LOOP UNCERTAINTY.
(WITHOUT BIAS VALUES)
N-LOOP UNCERTAINTY =_
(WITH. BI AS:. VALUES) s i
4
/
\\
\\.
-_-,---_....,u..,
)
,.(.-
1 TABLE-7 (b)
POWER CALORIMETRIC INSTRUMENTATION UNCERTAINTIES THREE LOOP OPERATION
(% SPAN)
FW TEMP FW PRES FW d/p STM PRESS
+a,c SCA =
SMTE '
SPE =
STE =
=
BIAS =
RCA--
RMTE='
RTE =
RD -
- ID --
A/D.=
CSA =
0F psia
% d/p psia INST SPAN = 400.-
2000.
120.
1300.
INST.UNC
+a,c (RANDOM)=
- INST UNC-(BIAS)-
=
N0'ilNAL
- 404.
1000.
900.
Y n
5 I
i 5
a I
i i
.__._____._____m
_m_
______.____._.____m_.___
L
. TABLE 8-(b)'
SECONDARY SIDE POWER CALORIMETRIC MEASUREMENT UNCERTAINTIES
_THREE_ LOOP OPERATION COMPONENT
-INSTRUMENT ERROR POWER UNCERTAINTY
+a,c FEEDWATER FLOW
~ VENTURI THERMAL EXPANSION COEFFICIENT TEMPERATURE
-MATERIAL DENSITY
! TEMPERATURE PRESSURE _
DELTA P
-FEEDWATER ENTHALPY.
o
, TEMPERATURE' PRESSURE STEAM ENTHALPY PRESSURE
'M0ISTURE?
NETEPUMP HEAT ADDITION
. BIAS VALUES-FEEDWATER DELTA ~P-FEEDWATER-PRESSURE-DENSITY-ENTHALPY-STEAM-PRESSURE ENTHALPY POWER-BIAS TOTAL VALUE
. INDICATE-SETS OF DEPENDENT PARAMETFRS J*
SINGLE LOOP UNCERTAINTYL(WITHOUT BIAS VALUES)
LN LOOP: UNCERTAINTY
-(WITHOUT BIAS VALUES)J N LOOP UNCERTAINTY?
- (WITH'BIASVALUES)
-i 4
I t
f.... _
1 REFERENCES
~
1.: Westinghouse letter NS-CE-1583, C. Eicheldinger to J. F. Stolz, NRC, dated 10/25/77, t.
o 2.
Westinghouse letter NS-PIC-5111, T M. Anderson to.E. Case, NRC, dated 5/30/78.
l 3.
Westinghouse letter'NS-TMA-1837, T. M. Anderson to S. Varga, NRC, dated 6/23/78.
4.
Westinghouse letter NS-EPR-2577. E. P. Rahe Jr. to C. H. Berlinger, NRC, 1
~ dated 3/31/82.
1 5.
Westinghouse Letter NS-TMA-1835, T. M. Anderson to E. Case, NRC, dated 6/22/78, 6.
NRC. letter, S. A. Varga to J. Dolan, Indiana and Michigan Electric Company,.
-i dated 2/12/81'.
ti 7.'. NUREG-0717 Supplement No. 4, Safety Evaluation Report related to the operation of_ Virgil C. Summer Nuclear Station; Unit No.1, Docket 50-395,
' August, 1982.
- 8.. Regulatory Guide 1.105-Rev. 2, " Instrument Setpoints for Safety-Related
- Systems", dated 2/86.
. 9.
NUREG/CR-3659 (PNL-4973), "A Mathematical'Model for. Assessing the-Uncertainties of Instrumentation Measurements'for Power and Flow of PWR
~
- Reactors",2/85._
- 10. ~ ANSI /ANS: Standard l58.4-1979, " Criteria for Technical Specifications for i -
Nuclear Power Stations".
11'. ;ISA Standard S'67.04,1982, "Setpoints for Nuclear Safety-Related Instrumentation 'Used in Nuclear Power Plants" 44 M
u-w-
4
I
- 12. Tuley, C. - R.,- Miller, R. B., " Westinghouse SetpointL Methodology for Control Land Protection Systems",:IEEE Transactions on Nuclear Science, February, 1986, Vol. NS-33 No. 1, pp. 684-687..
- 13. Scientific Apparatus Manufacturers Association, Standard PMC 20.1, 1973,
" Process Measurement.and Control Terminology".
r.
s 1
N......._ _ _ _ _
1'
,1 M.
,+
I :
W h
FIGURE 1 RCS FLOW CALORIMETRIC SCHEMATIC l
c:
i p.ij l
p lp l
TC I
I Pp 1
TH Ps I
Pf I
l Tf op 1
1
.l 1.x A
I
+
z i
.hC hHc hs hf of Fa K-i
- h-.
-Ah Wf
. tl 4
7,'(
1 1
-QSG c
f Measured O Q'L.
[-
07 w
lT.
L Calculated -
o U
l-1 Mell'
.)
WL.
Q
.,T n :,n g
y L /f N
- ,,o 7
Wg h_
- !Three' hot leg temoeratures-.per
]
3 Other Loops:
- 1oop are averaaed 4
- p RCS Volumetric Flow 46-
(
o FIGURE 2
+
POWER CALOR! METRIC SCHEMATIC
\\
I P
j l
P i
l T
I L AP s
f f
t
\\.
6 3
I l
A i
L h
h pf F
K s
f a
i i
=
b i t g
W
~
f t
J 1 P O-===ure
' 58 0 - caiculated b
Other Loops Og hp Com Power j _
l' b
47-4 e-.
w
-+e-~
ne,-e,,.e-,,
.--~~
e-s,ee-,
ww.m.,.~
,--,--s,ge
-