ML20213G747
| ML20213G747 | |
| Person / Time | |
|---|---|
| Site: | Harris  |
| Issue date: | 10/31/1986 |
| From: | Moomau W, Tuley C WESTINGHOUSE ELECTRIC COMPANY, DIV OF CBS CORP. |
| To: | |
| Shared Package | |
| ML18004B591 | List: |
| References | |
| WCAP-11169, WCAP-11169-R01, WCAP-11169-R1, NUDOCS 8611180309 | |
| Download: ML20213G747 (25) | |
Text
_ _. _. _
E TIEHOUSE CLASS 3 WCAP-11169 Rev. 1 RCS FLOW UNCERTAINTY FOR SHEARON HARRIS UNIT 1 October, 1986 C. R. Tuley W. H. Moomau Westinghouse Electric Corporation Energy Systems P.O. Box 355 Pittsburgh, Pennsylvania 15230 Copyright by Westinghouse Electric 1984, O All Rights Reserved 8611180309 861113 PDR ADOCK 05000400 P
PDR r
iu
/
TABLE OF CDNTENTS SECTION TITLE PAGE I.
Introduction 1
II.
Methodology 1
III.
Instrument Uncertainties 4
IV.
Conclusions 17 L
References 18 t-L i
1
LIST OF TABLES TABLE NUMBER TITLE PAGE 1
Flow Calorimetric Instrtrnentation 12 Uncertainties 2
Flow Calorimetric Sensitivities 13 3
Calorimetric RCS Flow Measurement 14 Uncertainties 4
Cold Leg Elbow Tap Flow Uncertainty 16 11
LIST OF FIGURES FIGURE NUMBER TITLE PAGE 1
RCS Flow Calorimetire Schenatic 20 L
4 A
1 iii
1 l
WESTINGHOUSE RCS FIDR CAIDRIMETRIC MEASURDETI' UNCERIAINIY MEIHODOIOGY i
I.
INIRODUCI' ION RCS flow is a monitored param ter via the performance of a precision flow calorimetric at the beginning of each cycle and the normalization of the RG Cold Iag elbow taps against the calorimetric (used for monthly surveillance with a small increase in uncertainty).
Westinghouse has been involved with the developnent of several techniques to treat instrumentation uncertainties. An early version (for D. C. Cbok 2 and Trojan) used the methodology outlined in WCAP-8567 " Improved 'Ihermal Design Procedure",(1,2,3) which is based en the conservative a=9mntion that the uncertainties can be described with uniform probability distributions. Another approach (for McGuire and Catawba) is based on the more realistic aman =ntion that the uncertainties can be described with random, normal, two sided probability distributions. (4) 'Ihis 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.
Stmmar, Wolf Creek, Millstone Unit 3 an:1 others. 'Ihe second approach is now utilized for the determination of all instrumentation errors for both Improved 'Iharmal Design Procedure (ITDP) parameters, of which RCS Flow is one, and protection functions.
II.
MEIHODOIDGY
'Ihe methodology used to ocznbine the error components for a channel is the square root of the sum of the squares of those groups of ccuponents which are statistically irdependent. 'Ihose errors that are dependent are ccubined arithmetica11y into independent groups, which are then systematically combined. 'Ihe uncertainties used are considered to be _ _ - _ _ _ _ - _ _ _ -
randcza, two sided distributicms. 'Ihe sum of both sides is equal to the range for that parameter, e.g., Rack Drift is typically
[
J+a,c, the range for this parameter is [
J+a,c,
'!his technique has been utilized before as noted above, and has been endorsed by the NRC staff (6,7,8,9) and various industry standards (10,11),
'the relationships between the error -g=Ents and the channel instrument
{
error allowance are variaticos of the basic Westinghouse Setpoint Methodology (12) and are defined as follows:
1.
For precision parameter indication using Special Test Equipnent or a DVM at the input to the racks;
For parameter indication utilizing the plant s -w ocmputer; CSA = { (SCA + SMrE + SD)2 + (SPE)2 + (STE)2 + (RCA + RMrE + RD)2
+ (RTE)2 + (ID)2 + (379)2)1/2 Eq. 2 whers:
CSA Channel Allowance
=
SCA Sensor Calibratico Accuracy
=
SMTE Sensor Measurement and Test Eq11mmnt Accuracy
=
SPE Sensor Pressure Effects
=
STE Sensor b g ature Effects
=
SD Sensor Drift
=
RCA Rack Calibratico Accuracy
=
RMrE Rack Measurement and Test Egiiment Accuracy
=
RIE
=
Rack h W sture Effects Rack Drift RD
=
RDOUT Paarbit Device Accuracy (DVM or gatxJe)
=
2--
~
l ID Otznputer Isolator Drift
=
A/D Analog to Digital Corr /ersion Accuracy
=
'Ihe parameters above are as defined in references 5 and 12 and are based en SAMA Standard INC 20.1, 1973(13). However, for ease in understanding they are paraphrased below:
SCA -
reference (calibration) accuracy for a sensor / transmitter, SMIE-measurement and test equipnent accuracy for calibration of sensor / transmitter, a===ad to be less than 10 % of the calibration accuracy (and therefore neglected) unless otherwise stated.
SPE -
change in input-output relationship due to a charge in static pressure for a d/p cell, STE -
chage in input-output relationship due to a change in ambient temperature for a sensor / transmitter, change in input-output relationship over a period of time SD at reference conditions for a sensor / transmitter, RCA -
reference (calibration) accuracy for all rack modules in loop or channel a===%g the loop or channel is string calibrated, or tuned, to this acx:uracy.
PMIE-meastunnun. and test equipnent accuracy for calibration of the racks modules, aam* to be less than 10 % of the calibration accuracy (and therefore neglected) unless otherwise stated.
RTE -
change in input-output relationship due to a change in ambient temperature for the rack modules, RD change in input-output relationship over a period of time at reference canditions for the rack modules, RDOUr-the measurement accuracy of a special test local gauge, digital volt::neter or multimeter en it's most accurate applicable range for the parameter measured, ID change in input-output relationship over a period of time at reference caniitions for a control / protection signal isolating devi A/D -
allowance for conversion accuracy of an analog signal to a digital signal for process ccanputer use, - - - _ _ - _ _ _ - _ _ _ _ _ _ - _ _.
A more detailed explanation of the Westinghouse methodology notirg the interaction of several parameters is provided in references 5 and 12.
III.
INS *IRLHE2TI UNCERTAINTIES Technical Specifications, and ITDP, requires an RCS Flow meastuvuuit with a high degree of accuracy. It is a===ad for this error analysis, that this flow meastur.must is performed within the calibration (or guaranteed acx:uracy) period for the measturu=uit instrumentation, usually thirty to ninety days. 'Iherefore, except where meny due to sensor location, drift effects are not included. It is also a==M 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 70%
RTP.
'Iha flow maasta=urait is performed by determining the Steam Generator themal output (carrected 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. Assumirq that the primary and secondary sides are in equilibrium, the RCS total vessel flow is the sum of the individual primary loop flows, i.e.,
Wg = N(W ).
Eq. 3 L
'Ihe individual primary loop volumetric flows are determined by correcting the thermal output of the Steam Generator for Steam Generator blowdown (if not secured), subtracting the RCP heat addition, adding the loop's share of the primary side system losses, dividing by the primary side enthalpy rise and multiplying by the Cold Iag specific volume. 'Ibe equation for this calculation is:
WL = (A)(OSC - OP + IO /N) 1(V )-
L C
(hH-h)
Eq. 4 C
where; W3 I r flow (apc)
=
3 A
0.1247 gg:V(ft /hr)
= _ _ _ _ - _ _ _ _ _ _ _ - _.
Ogg Steam Generator thermal output (Btu /hr)
=
Qp RCP heat additicn (Btu /hr)
=
Q3 Primary system net heat losses (Btu /hr)
=
3 VC Specific volume of the Cold Iag at TC (ft /lb)
N Number of primary side loops
=
hH Hot Iag enthalpy (Btq/lb)
=
hC cold Iag enthalpy (Btu /lb).
=
'Ihe tM-1 output of the Steam Generator is determined by precision r.amndary side calorimetric meastumuent, which is defined as:
QSG " (h
- h )Wf F4 5 f
s Where; hs Steam enthalpy (Btu /lb)
=
hf Feedwater enthalpy (Btu /lb)
=
Wf Feedwater flow (lb/hr).
=
'Ihe Steam enthalpy is based on measurement of Steam Generator outlet Steam pressure, m eirry saturated conditions. 'Ihe Feedwater enthalpy is based on the maastuwault of Feedwater temperature and Feedwater pressure. 'Ihe Feedwater flow is determined by multiple measurements and the following calculation:
f = (K) (F )((P ) (d/p) }l/2 Eq. 6 W
a f
where;. K Feedwater venturi flow ocefficient
=
F Feedwater venturi correction for thermal expansion
=
a 3
pf Feedwater density (1b/ft )
=
d/p Feedwater venturi pressure drop (inches H O).
=
2
'Ihe Feedwater venturi flow coefficient is the product of a number of constants including as-built diwnsicos of the venturi and calibration tests performed by the vendor. 'Ihe th=1 expansion correction is based cn the coefficient of expansion of the venturi material and the difference between Feedwater temperature and calibration twture.
Feedwater density is haw on the meastu==:nt of Feedwater to:rperature and Feedwater pressure. 'Ihe venturi pressure drop is obtained from the _ _ _ _ _
output of the differential pressure cell connected to the venturi.
RCP heat addition is determined by calculation, based en the best estimate of coolant flow, pump head, and pump hydraulic efficiency.
'Ihe primary system net heat losses are determined by calculation, considering the following system haat inputs ard heat losses:
Charging f1w Istdown flow Seal injection flow RCP thermal barrier cooler heat remcval Pressurizer spray flow Pressurizer surge line flow Q:eponent insulation heat losses Otoponent support heat losses CRDi heat losses.
A single calculated sum for 100% RTP operation is used for these losses or heat inputs.
h Hot leg and Cbid leg enthalpies are based on the meastuhl of the Hot leg temperature, Cold Iag temperature and the Pressurizer pressure.
h cold leg specific clume is based on meastu==d. of the Cold leg temperature and Pressurizer pressure.
'Ihe RCS flow measurement is thus based on the following plant meastuments:
S6=1%e pressure (P )
g Feedwater temperature (T )
f Feechrater pressure (P )
f Feat.;ater venturi differential pressure (d/p)
Hot Iag temperature (T )
H cold leg temperature (T )
C Pressurizer pressure (P )
p Steam Generator blowdown (if not secured)
and on the following calculated values:
Feedwater venturi flow ocefficients (K)
Feedwater venturi thermal expansion correction (F )
a Feedwater density (p )
g Feedwater enthalpy (h )
f Steam enthalpy (h )
s Moisture carryover (impacts h )
g Primary system net heat losses (Qy)
RCP heat addition (Q )
p Hot Iag enthalpy (h )
H cold Iag enthalpy (h )
- C
'Ihese measurements and calculations are presented schematically on Figure 1.
Starting off with the Equation 6 parameters, the derivation of the meastumsal errors is noted below.
Secondary Side
'Ihe secondary side uncertainties are in four principal areas, Feedwater flow, Feedwater enthalpy, Steam enthalpy and RCP heat addition. 'Ihese four areas are specifically identified on Table 3.
It should be noted that Table 3 prwides flow uncertainties that are specifically calculated, or are bounding values, for the hardware at the plant. 'Ihis h = ant is thus specific for the Shearon Harris plant, as opposed to generic (based on generic calculations). 'Ihe plant must insure that the parameters are measured as accuractly as specified in Table 1 for this analysis to be valid.
For the meastumeit of Feedwater flow, each Feedwater venturi is calibrated by the vendor in a hydraulics laboratory under controlled conditions to an accuracy of [
]+a,b,c.
'Ihe calibration data which substantiates this accuracy is prwided to the plant by the vendor. An additional uncertainty factor of [
]+a,c is included for installation effects, resulting in a conservative overall _ - _ _ _ _ _ _ _ - _ _ _ _ _ - _ _ - _ _ -
flow ocefficient (K) uncertainty of [
]+a,c.
Since RCS loop flow is p.wLianal to Steam Generator thermal output which is
- p. w Lianal to Feedwater flow, the flow coefficient uncertainty is expressed as [
]+a,c.
It should be noted that no allowan::e is made for venturi fouling. 'Ihe venturis should be inspected, and cleaned if r-ry, prior to performance of the precision measurement.
If fouling is present but not removed, it's effects must be treated as a flow bias.
'Ihe 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 material, usually 304 stainless steel. For this material, a charge of 1 F in the ncuninal Feedwater temperature range charges F DY a
! 0.002 % and the Steam Generator thermal output by the same amount.
hai on data intMM into the ASME Cbde, the uncertainty in F for a
304 stainless steel is 5 %.
'Ihis results in an additional uncertainty of [
]+a,c in Feedwater flow. Westinghouse uses the conservative value of [
]+a,c, Using the 1967 ASME Steam Tables it is possible to determine the sensitivities of various parameters to changes in Feedwater temperature and pressure. Table 1 notes the instrument uncertainties for the hardware used to perform the measturwds. Table 2 lists the various sensitivities. As can be seen on Table 2, Feedwater temperature uncertainties have an impact on venturi F, Feedwater density and a
Feedwater enthalpy. Feedwater pressure uncertainties impact Feedwater density and Feedwater enthalpy.
Feedwater venturi d/p uncertainties are converted to % Feedwater flow using the following conversion factor:
% flow = (d/p uncertainty)(1/2)(transmitter sparV100)2 Typically, the Feedwater flow trans: titter span is [
Ja,c nominal flow. ___
Usirq 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 1 notes the ura efusinty in Steam pressure and Table 2 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 2.
'Ihe net pump heat uncertainty is derived frm the cmbination of the primary system net heat losses and pu::p heat addition and are summarized g
for a four locp plant as follows:
Systen heat losses
-2.0 HRt Otmponent conduction and convection losses
-1.4 PLmp heat adder
+18,0 Net Heat input to RCS
+14.6 HWt
'Ihe uncertainty m 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 meastuw=ds are not possible, the uncertainty on cmponent conduction and convection losses has been assumed to be [
]+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 irput power measurements frm several plants, therefore, the uncertainty for the pu=p heat addition is estimated to be [
]+a,c of the best estimate value. Considering these parameters as one quantity, which is designated the net pump heat uncertainty, the cmbined uncertainties are less than
[
]+a,c of the total, which is [
]+a,c of core power.
Primary Side
'Ihe primary side uncertainties are in three principal areas, Hot Ieg enthalpy, Cold Iag enthalpy and cold Leg specific volume, these are specifically noted on Table 3.
'Ihree primary side parameters are actually measured, T, TC and Pressurizer pressure. Hot Iag enthalpy H
is influenced by T, Pressurizer pressure and Hot Iag temperature H
streaming. 'Ihe uncertainties for the instrumentation are noted on Table 1, the sensitivities are provided cn Table 2.
Based on Westirghouse evaluation of Hot Leg circumferential temperature data frun several plants, the Hot leg streamirx; uncertainty is split into randam (loop independent) and systematic (loop dependent) ocuponents.
For plants with direct immersion RIDS located in RID bypass manifolds fed by scoops in the legs, the streaming uncertainty is [
]+a,e i
for both random and systematic cxmponents. Ibr plants with RIDS located in thermowells placed in the scoops (bypass manifolds eliminated), the streaming uncertainty is, (
)+a,c randca and
(
)+a,c systematic.
~
(
'Ihe Cold Ieg enthalpy and specific volume uncertainties are impacted by TC and Pressurizer presuure. Table 1 notes the T instrument e
uncertainty and Table 2 provides the sensitivities.
Noted on Table 3 is the plant specific RID cross-calibration systematic allowance. When rw=n=n, an allowance is made for a systematic temperature error due to the RID cross-calibration prrvwhmt. No allowance was determined to be zw===n for this plant.
Parameter dependent effects are identified on Table 3.
Westinghouse has determined the dependent sets in the calculation and the direction of interaction, i.e., whether components in a dependent set are additive or subtractive with respect to a conservative calculation of RCS flow. 'Ihe same work was performd for the instrument bias values. As a result, the calculation explicitly acocunts for dependent effects and biases with credit taken for sign (or directicn of impact).
Using Table 3, the N loop uncertainty equation (with biases) is as follows: _
+a,c Dependirg on the rumber of loops, rumber, type and mastu.aumd. mthod of RIDS, and the vessel Delta-T, the flow uncertainty can vary by a significant amount. 'Ibe equation noted above and Tables 1, 2 and 3 are for Shearon Harris only and result in an uncertainty of
[
]+a,c.
Using an expected set of measurement uncertainties, a three loop plant would be expected to have a precision flow calorimetric measurement uncertainty of [
]+a,c.
'Ihus Shearon Harris has a more accurate measurement than a generic Westirghouse calculation.
As noted earlier, the precision flow calorimtric is used as the reference for the normalization of the Cold Iag elbow taps. Assumire that the elbow tap d/p transmitters are used to feed the plant process otzputer, it is a simple matter to perform 'Nchnical Specification required surveillance. Table 4 notes the instrument uncertainties for norralization of the elbow taps, ace =4rq one elbow tap per loop.
Included as cne of the uncertainties is the impact of [
]+a,c.
h d/p transmitter uncertainties are converted to % flow cm the sam basis as the Feedwater venturi d/p. 'Iha elbow tap uncertainty is then ocabined with the precision flow calorimetric unce @. 'Ihis ocabination of uncertainties results in a total flow uncertainty of i 2.0 % flow. 'Ihe typical total uncertainty expected for a three loop plant is
[
)+a,c, trus the Shearon Harris total uncertainty is better than the typical value. _ _ _ _ - _
l
'IABI.E 1 FICW CAIORDEIRIC INS'IRUMENIATICH UNCERIAINI'IES
(% SPAN)
W TEMP N PRES W d/p S'IM PRESS T
T PRZ PRESS H
C SCA =
+a,c M&TE=
SPE =
STE =
SD =
P/E =
RIX D=
BIAS =
CSA =
- OF INST USED 1
1 3 **
OF psia
% d/p psia F
O C
F psia INST SPAN = 568.
1200.
120.
2000.
100.
100.
800.
INST UNC.
(RANDCH) =
+a,c INST UNC.
(BIAS)
=_
NCHINAL
= 435.
1064.
964.
620.2 557.4 2250.
[
3+a,e Number of Hot Iag and Cold Iag RrDs used for reasurement in each loop and the rumber of Pressurizer Pressure transmitters used overall, i.e., one per loop.. _ _ _ _ _ _. -
'IABIE 2 FIJ0W CAIfRDElIRIC SDEITIVITIES FEEDWATER FI.0W Fa
+a,c TDTERAIURE
=
HATERIAL
=
DENSITI TDEERAIURE
=
PRESSURE
=
DELTA P
=
FEEDWATER DTIHAIPI TDEIL"URE
=
PRESSURE
=_
hs 1194.2 BIU/IHi
=
hg 414.0 BIU/ IBM
=
Di(SG) 780.2 BIU/IHf
=
STEAM DOIAIFl
+a,c PRESSURE
=
POISIURE
=
H0r IEG DTIHAIFl TDTERAIURE
=
PRESSURE
=
hH 643.3 BIU/IHf
=
hC 556.4 BIU/Inf
=
Dh(VESS) 86.9 BIU/IIM
=
H 1.565 BIU/IH{ OF Cp(T )
=
CDID IEG DTIHAIPI
+a,c HESSL"E
=
C 1.262 BIU/IRi OF Cp(T )
=
CDID IEG SPECIFIC VOIIEE
- +a,c PRESSURE
=
TABIE 3 CAIDRIMEIRIC RCS FIN MEASURDEU UNCERIAINI'IES CDGMDE INSTRUMDC ERROR FIN UNCERIADTIY
- +a,c VENIURI THERMAL EXPANSICH COEFFICIDE 3
TDGERATURE NATERIAL DDGITY TDEERATURE PRESSURE DELTA P FEEIMATER DTIHAIPI TDEERATURE PRESSURE SIEAM DTIHALPY PRESSURE
}OISIURE NET RIMP HEAT ADDITION HCTI IEG DTIHAIFl TDEERATURE STREAMING, RANDCH STREAMING, SYSTDETIC PRESSURE CDID IEG DTIHAIPl TDEERATURE PRESSURE COID IEG SPECIFIC VOLUME TDTERAIURE PRESSURE RID CROSS-CAL SYSTDRTIC AINICE
- , **, +, 4+ INDICATE SEIS OF DEFENDDE PARAMEIERS
TABLE 3 02frINUED CAIIRIMEIRIC RCS FICW MEASURDENT UNCERIAINTIES CC25WENT FICW UNCERIAINIY BIAS VAIDES
+a,c FEEDWATER PRESSURE IENSITY DfIHALPY STEAM PRESSURE BfIHAIPY PRESSURIZER PRESSURE BfIHALPY - IDI IR3 DTIHALPY - CDID IEG SPECIFIC VOIDME - COID IB3 FIDW BIAS 'ICIAL VAIDE
~
SINGIE IDOP UNCEREADirY (WITOUT BIAS VAIDES)
+a,c
~
N IDOP UNCERIAINIY (WII1OUT BIAS VAIDES)
N IDOP UNCERIAINIY (WIIH BIAS VAIDES) m e
TABIE 4 00ID IEG EIBOW TAP FIN WCERIADTIY INSTRUME2E WCERIADEIES
% d/p SPAN
% FIN INA =
+a,c PEA =
SCA =
SPE =
STE =
=
RCA =
M&TE=
RTE =
RD
=
ID
=
h/D =
m BIAS =
FIN CAIDRIM. BIAS
=
FIN CAIORDEIRIC
=
INSTRUME2E SPAN
=
~
~
SDGII ICOP EIBOW TAP FIN WC =
+a,c N IOOP ELBOW TAP FIN WC
=
N IDOP RCS FIDW WCERIAINIY (WITinE BIAS VAIDES)
=
N IDOP Rci FIOR WCERIAINIY (WIIH BIAS VAIDES)
=
2.0 _--
IV.
CONCIUSIONS
'Ihe g -Ming sections provide the methodology for dat Westirx#ouse believes is a reasonable means of accountirxJ for instrument uncertainties for the measurement of RCS Flow. As noted in this dm= ant, the calculations presented are specific for the Shearon Harris plant. Also noted are the expected results for a typical three loop plant. 'Ihe results indicate that the Shearon Harris plant meastuuuent uncertainty for RCS Flow is better than the typical expected value. 'Ihis is due to the lower instrument uncertainties for the hardware used by the plant staff.
REFERENCES 1.
Westinghouse letter NS-CE-1583, C. Eic:heldinger to J. F. Stolz, NRC, dated 10/25/77.
2.
Westinghouse letter NS-PIC-Sill, T. M. Anderson to E. Case, NRC, dated 5/30/78.
3.
Westinghouse letter NS-7MA-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, dated 3/31/82.
5.
Westinghouse Istter NS-GMA-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 Campany, dated 2/12/81.
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-Relattd Systems", dated 2/86.
9.
NURIU/CR-3659 (PNIr-4973), "A Mathematical Model for Assessing the Uncertainties of Instrumentation Measurements for Power and Flow of IMR Reactors", 2/85.
- 10. ANSI /ANS Standard 58.4-1979, " Criteria for Tbchnical Specifications for Nuclear Power Stations".
- 11. ISA.etandard S67.04, 1982, "Setpoints for Nuclear Safety-Related Instrumentation Used in Nuclear Power Plants" ____
- 12. 'Ibley, C.
R., Miller, R. B., "14@ Setpoint Methodology for Control and Protection Systems", IEEE Transactions an Nuclear Science, February, 1986, Vol. NS-33 No. 1, pp. 684-687.
- 13. Scientific Apparatus Manufacturers Association, Standard PMC 20.1, 1973, "Preca Maastu.cauent and Control 'hmninology".
FIGURE 1 RCS FLOW CALORIMETRIC SCHEMATIC TC Pp TH Ps Pf Tf ap hC hH hs hf of Fa K
\\/
\\/-
N Ah f
u QSG O
g Measured
- ~~
OP T
Calculated C U
Mass WL If vC Ol' WL
~
y
{
Other Loops u
RCS Volumetric Flow 20