ML20154J520

Westinghouse Improved Thermal Design Procedure Instrument Uncertainty Methodology

ML20154J520
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Site:	Summer
Issue date:	12/31/1987
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References
WCAP-11657, NUDOCS 8805270030
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WCAP-11657 I

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5 WESTINGHOUSE DPROVE DIERMAL DESIGN PROCEDURE INSTRtMENT UNCERTAINTY ErHODOM VIWJIL C. SL49ER 1 NUCLEUt POWER STATION l

December, 1987 W. H. Moanau l

^

Westingh: rase Electric Corporation Energy Systens P.O. Box 355 Pittsburgh, Pennsylva.d a 15230 0

TABLE OF (XWIDrfS L

SECTION TITLE PAGE I. Introdtetion 1 -

II. Methodology 2  ;

III. Instrtanentation Uncertainties 4 IV. Conclusions 15 References 19 i i

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1 8

m - - - - - - - , . . - , -- , , ~ -- e. - .----,-,.----.vn - , , - - - , . _9

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I LIST OF TABLES l

1 i-l TAILE NUMBER TITLE PAT l l

i 1 Pressurizer Pressure Control 6 System Accuracy i

2 Rod Control Systen Accuracy 8 3 Power Calorimetric Instrtnentation 16 Uncertainties 4 Power Calorimetric Sensitivites 17 5 Secondary Side Power Calorimetric 18 Measurenent Uncertainties h

W n

11

LIST OF ILLUSTRATIONS FIGURE NUMBER TITIE PAGE 1 Power Calorimetric Schanatic 21 O

O e

iii

WESTINGHOUSE IMPROVED EERMAL DESIGN PROCEDURE

, INSTRUMENT UNCERTAINIT METHODOLOGY s FOR VIRGIL C. SUMER NUCLEAR POWER STATION I. INTRODUCTION Eis report provides the Improved '"harmal Design Procedure (ITDP) instrianent uncertainty methodology urad at South Carolina Electric ard Gas Company's Virgil C. Stener Nuclear Power Station with Westinghouse Vantage 5 nuclear fuel. Four operating parmeter uncertainties are used in the uncertainty analysis of the ITDP. These parmeters are Pressurizer Pressure, Primary Coolant Teperature (T,yg), Reactor Power, and Reactor Coolant Systm Flow. They are frequently monitored and several are used for control purposes. Reactor power is monitored by the performance of a secordary 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 perfonnance of a precision flow calorimetric at the beginning of each cycle. The RCS Cold Leg elbow taps are nonnalized against the precision calorimetric and used for monthy surveillance (with a snall increase in uncertainty). Pressurizer pressure is a controlled

\ parameter and the uncertainty reflects the control syste. T is a controlled avg pararneter via the taperature input to the rod control systs and the uncertainty reflects this control syste.

Westinghouse has been involved with the developnent of several techniques to treat instrtunentation uncertainties. An early version (for p. C. Cook 2 and Trojan) used the methodology outlined in WCAP-8567 "Improved Thermal Design Procedure",(1,2,3) which is based on the conservative asstanption that the uncertainties can be described with unifonn probability distributions. Another approach (for McGuire and Cataiba) is based on the more realistic asstanption that the uncertainties can be described with randczn, nonnal, two sided probability distributions.b) his approach is used to substantiate the acceptability of the protection syste setpoints for many Westinghouse plants,

- e.g., D. C. Cook 2(5) , V. C. Sumer, Wolf Creek, Millstone Unit 3 and others.

. Be second approach is now utilized for the Westinghouse detennination of all e instrimnentation errors for both ITDP parmeters and protection functions.

1

.. n.-

II. HE"Ih0DOLOGY he methodology used to cmbine the error cmponents for a channel is the square ,

root of the sum of the squares of those groups of components which are .

statistically independent. Rose errors that are dependent are ccrabined arithnetically into independent groups, which are then systeatically cabined.

De uncertainties used are co:1sidered to be rands , two sided distributions.

The sum of both sides is equal to the range for that parameter, e.g., Rack Drift is typically [ ]+a,c, the range for this parameter is

[ ]+a,c Bis technique has been utilized before as noted above, and has been endorsed by the NRC staff (6,7,8,9) wrl various industry standards (10,11) ,

he relationships between the error caponents and the channel instrment error allo.ance are variations of the basic Westinghouse Setpoint Methodology (12) and are defined aa follows:

1. For precision parmeter indication using Special Test Equipnent or a DVM at the input to the racks; [

CSA = {(SCA + SMIE + SD)2 + (SPE)2 + (STE)2+ (RDOUT)2)1/2 Eq. 1

2. For parameter indication utilizing the plant process emputer; CSA = {(SCA + SMTE + SD)2 + (SPE)2 + (STE)2 + (RCA + RMTE + RD)2

+ (RTE)2 + (ID)2 + ( A/D)2)1/2 Eq. 2m 3 For parameters which have control systes; CSA = {(PMA)2 + (PEA)2 +(SCA + SMIE + SD)2 + (SPE)2 + (STE)2 ,

+ (RCA + RMIE + RD + CA)2 + (RTE)2}l#2 Eq. 3 .

2

where:-

> CSA = Qiannel Allowance PMA = Process Measurenent Accuracy PEA = Primary Element Accuracy SCA = Sensor Calibration Accuracy SMTE = Sensor Measurement and Test Equipoent Accuracy SPE = Sensor Pressure Effects STE = Sensor Temperature Effects SD = Sensor Drift RCA = Rack Calibration Accuracy RMTE = Rack Measurement and Test Equipnent Accuracy RTE = Rack Temperature Effects RD = Rack Drift RDOUT = Readout Device Accuracy (DVM or gauge)

ID = Camputer Isolator Drift

, A/D = Analog to Digital Conversion Accuracy y CA = Controller Accuracy The parameters above are as defined in references 5 and 12 and are based on SAMA Standard PMC 20.1. 1973(13) However, for ease in understanding they are paraphrased below: .

PMA - non-instrunent related measurement errors, e.g., tenperature stratification of a fluid in a pipe, 9 PEA - errors due to a metering device, e.g. , elbow, venturi, orifice, SCA - mference (calibration) accuracy for a sensor / transmitter, SMTS- measurement and test equipnent accuracy for calibration of sensor / transmitter, asstaned to be less than 10% of the calibration accuracy (and therefore neglected) unless otherwise stated.

SPE - change in 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 abient temperature for a sensor /transitter, j

3

( SD - change in input-output relationship over a period of time at l reference conditions for a sensor /transitter, RCA - reference (calibration) accuracy for all rack modules in loop or .

channel assming the loop or channel is string calibrated, or .

tuned, to this accuracy. ,

i RMIL measurment and test equipnent accuracy for calibration of the rack modules, assmed to be less than 10% of the calibration accuracy (and therefore negiccted) unless otherwise stated.

RTE- change in input-output relationship c w to a change in ambient taperature for the rack modules, RD - change in input-output relationship over a period of time at reference conditions for the rack modules, RDOUT- the measursent accuracy of a special test local gauge, digital voltmeter or multimeter on it's most accurate applicable range for the parameter measured, ID - change in input-output relationship over a period of time at reference conditions for a control / protection signal isolating device, A/D - allowance for conversion accuracy of an analog signal to a digital '

signal for process cmputer use, CA - allowance for the accuracy of a controller, not including deadband.

A more detailed explanation of the Westinghouse methodology noting the interaction of several paramecers is provided in references 5 and 12.

III. Instementation Uncer'tainties The instraentation uncertainties will be discusied first for the two parameters which are controlled by autmatic systes, Pressurizer Pressure, and Tavg (through Rod Control). ,

G 4

_ _ ________________ _ _ ____ . .. ___ J

1. PRESSURIZER PRESSURE d

b

, Pressurizer Pressure is controlled by ocanparison of the measured vapor space pressure and a reference value. Allowances are made for the transnitter and the process racks / controller. As noted on Table 1, the electronics uncertainty for this fbnction 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 thennal inertia of the heaters and spray. Based on an evaluation of plant operation, an allowance of [ ]+a , c was made for this effect. Therefore, a total control systen uncertainty of [ ]+a,c is calculated, which results in a standard deviation of [ ]+a,c (asstaning a nonnal, two sided probability distribution).

1

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e 5

TABLE 1 PRESSURIZER PRESSURE (DNTROL SYSTD4 ACCURACY ,

SCA = +a,c ,

M&TE=

STE =

SD =

BIAS =

RCA =

MTE=

RTE =

RD =

CA =

l .- a

_.+8 ec ELECTRONICS UNCERTAINTY = (RANDOM)

PLUS (BIAS)

ELECTRONICS UNCERTAINTY = (RANDOM)

PLUS (BIAS)

CDNTROLLER UNCERTAINTY =

[ 3+a,c V

O O

9 6

2. T AVG e

o T,yg is controlled by a systs that cmpares the auctioneered high T,yg from the loops with a reference, usually derived from the First Stage Turbine Impulse Chamber Pressure. T avg is the average of the narrow range TH dT C values. The highest loop T ,yg is then used in the controller. Allowances are made (as noted on Table 2) for the RTDs, transmit *.er and the process racks / controller. The CSA for this function is dependent on the type of RTD, pressure transmitter, and the location of the RIDS, i.e., in the RID bypass manifold or in the Hot and Cold Legs. Based on the assm ption that 1 TH and 1 TCcross-calibrated RdF RTDs are used to calculate T,yg ard the RTDs are located in the RTD bypass manifold, the CSA for the electronics is

[ ]+a,c. Asstraing a normal, two sided probability distribution results in an electronics standard deviation (s)) of

[ ]+"'U .

. However, this does not include the controller deadband of + 1.5 F. The a controller accuracy is the combination of the instrmentation accuracy and the s deadband. The probability distribution for the deadband has been determined to be [

]+a,c . The variance for the deadband uncertainty is then:

(s2 ) *b 3+ '

• Cabining the variance for instrmentation and deadband results in a controller variance of:

l (sT ) * (81 ) + (s2 ) *b 3+

• The controller sT=[ ]+ ' f r a total uncertainty of

[ ]+a,c ,

k e

7

TABLE 2 BOD CONTROL SYSIDI ACCURACY ,

Tavg TURB PRES.

PMA = n ,c SCA =

MIE=

STE =

SD =

BIAS =

RCA =

MTE=

M&TE=

RTE =

RD =

CA =

BIAS =

1. RTDs USED - TH = 1 TC = 1

+a,c ELECTRONICS CSA =

ELECTRONICS SIGMA =

CONTBOLLER SIGMA =

CDNTROLLER BIAS =

CONTROLLER CSA =

O 4

8

3 RCS FLOW s ITDP, and the Virgil Stater Technical Specifications, requires an RCS flow

~

measurement with a high degree of accuracy. It is assmed that a precision calorimetric flow measurment is perfomed at the beginning of a cycle, i.e.,

no allowances have been made for Feedwater venturi fouling, and above 70% RTP.

'Ihe reactor coolant syste flow uncertainty of 2.15 was provided by the South Carolina Electric and Gas Ca pany and is not discussed in this report.

1

4. REACTOR POWER

'Ihe plant perfoms a primary / secondary side heat balance once every 24 hours2.777778e-4 days <br />0.00667 hours <br />3.968254e-5 weeks <br />9.132e-6 months <br />  ;

when power is above 15% Rated Themal Power. This heat balance is used to l verify that the plant is operating within the limits 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.

4

, Assuning that the primary and secondary sides are in equilibrita; the core power is detennined by surming the themal output of the stem generators, correcting the total secondary power for Stem Generator' blowdown (if not secured), subtracting the RCP heat addition, adding the primary side syst e losses, and dividing by the core rated Btu /hr at full power. The equation for this calculation is:

RP = {(N){Q3g - O p + (Qg/N)(100) Eq. 4 H where; RP = Core power (% RTP) N = Ntaber of primary side loops Q3g = Sten Generator themal output (B'IWhr) as defined in Eq. 5 Qp = RCP heat adder (Btu /hr) as discussed below Qg = Primary system net heat losses (Btu /hr) as discussed below H = Core rated Btu /hr at full power. 9

D For the purposes of this uncertainty analysis (and based on H noted previously) it is assumed that the plant is at 100% RTP when the measurment is taken. , Measurements perfomed at lower power levels will result in different _ uncertainty values. However, operation at low r power levels results in , increased margin to DNB far in excess of any margin losses due to increased measur ment uncertainty. We themal output of the Stem Generator is detemined by pr*; cision secondary side calorimetric measurment, which is defined as: Q3g = (h 3 - hp)Wp Eq. 5 where; h = Steam enthalpy (Btu /lb) 3 hp = Feedwater enthalpy (Btu /lb) Wp = Feedwater now (lb/hr). De Stem enthalpy is based on measurment of Stem Generator Outlet Stem pressure, asstaning saturated conditions. The Feedwater enthalpy is based on the ' measurment of Feedwater taperature and Steam pressure. The Feedwater now is detemined by multiple measurments and the following calculation: Wp = (K)(Fa ){(pp)(d/p)}1/2 Eq. 6 where; K = Feedwater venturi now coefficient F, = Feedwater venturi correction for themal expansion pp = Feedwater density (lb/ft3) d/p = Feedwater venturi pressure drop (inches H2O). The Feedwater venturi now coefficient is the product of a ntanber of constants including as-built dimensions of the venturi and calibration tests performed by the vendor. We thermal ex, sion correction is based on the coefficient of , expansion of the venturi material and the difference between Feedwater tm perature and calibration ta perature. Feedwater density is based on the , measurment of Feedwater taperature and Feedwater pressure. The venturi 10

pressure drop is obtained fra the output of the differential pressure cell connected to the venturi. A ' l e RCP heat addition is detemined by calculation, based on the best estimate of l

 ~

coolant flow, pmp head, and pmp hydraulic efficiency. The primary syste net heat losses are detemined by calculation, considering the following syst e heat inputs and heat losses: charging now Letdown flo'f Seal injection flow RCP themal barrier cooler heat reoval Pressurizer spray now Pressurizer surge line flow Ca ponent insulation heat losses Ca ponent support heat losses CRDM heat losses. 4

  , A single calculated am for 100% RTP operation is used for these losses or heat inputs.

The power calorimetric measurment is thus based on the following plant measurments: Steamline pressure (P3) Feedwater t a perature (Tp) Feedwater venturi differential pressure (d/p) Steam Generator blowdown (if not secured) and on the following calculated values: Feedwater venturi flow coefficients (K)

• Feedwater venturi them:J. upansion correction (Fa)

Feedwater density (pp) Feed ater enthalpy (hp) Ste m enthalpy (h3) 11 .

i Moisture carryover (impacts hs) Primary syste net heat losses (Qg) RCP heat addition (Qp) These measurments and calculations are presented schematically on Figure 1. The derivation of the measurement errors is noted below. _ Secondary Side The secondary side uncertainties are in four principal areas, Feedwater now, Feedwater enthalpy, Steam enthalpy and RCP heat addition. These four areas are specifically identified on Table 5 For the measurment of Feedwater flow, each Feedwater venturi is calibrated by the vendor in a hydraulics laboratory under controlled conditions to an accuracy of [ ]+a,c The calibration data which substantiates this accuracy is provided to the plant by the vendor. An additional uncertainty factor of [ ]+a,c is included for installation effects, resulting in a ' conservative overall flow coefficient (K) uncertainty of L ]+a,c , Since RCS loop flow is proportional to Stem Generator themal output which is proportional to Feedwater flow, the flow coefficient uncertainty is expressed as [ ]'*' . It should be noted that no allowance is made for venturi fouling. Venturi fouling, found to date, has resulted in indicated feedster flow higher than actual. This results in an indicated secondary side power higher than actual, which is the conservative direction. The uncertainty applied to the Feedwater venturi themal expansion correction l (F,) is based on the uncertainties of the measured Feedwater taperature and the coefficient of themal expansion for the venturi material, usually 304 stainless l steel. For this material, a change of 2 1.0 F in the nminal Feedster t aperature range changes Fa by 0.002 % and the Steam Generator thermal output , by the same amount. . 12

Based on data introduced into the ASME Code, the uncertainty in Fa for 304 stainless steel is + 5 %. mis results in an additional uncertainty of [ 3+a,c in Feedwater flow. Westinghouse uses the conservative value of

 ~

[ j+a,c , Using the 1967 ASME Ste m Tables it is possible to determine the sensitivities of various parameters to changes in Feedwater taperature and pressure. Table 3 notes the instement uncertainties for the haMware used to perform.the measurments. Table 4 lists the various sensitivities. As can be seen on Table 4, Feedwater taperature uncertainties have an impact on venturi F ,a Feedwater density and Feedwater enthalpy. Feedwater pressure uncertainties knpact Feedwater density and Feedwater enthalpy. As noted on Figure 1, Virgil C. Smmer does not measure feedwater pressure. Instead the measured value for steamline pressure is used. For conservati n Westinghouse used a measur ment uncertainty of approximately twice the steamline pressure value for the feedwater pressure uncertainty. We SCA value on Table 3 was chosen to allow

   , internal calculation of this uncertainty.

4 Feedwater venturi d/p uncertainties are converted to % Feedwater flow using the following conversion factor: 5 flow = (d/p uncertainty)(1/2)(transitter span /100)2 Typically, the Feedwater flow transitter span is [ ]+a,c nominal flow. Using the 1967 ASME Steam Tables again, it is possible to determine the sensitivity of Steam enthalpy to changes in Steam pressure ard Steam quality. Table 3 notes the uncertainty in Stem pressure ard Table 4 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. Toe net pmp heat uncertainty is derived frm the cmbination of the primary syste net heat losses and pmp heat addition and are stmnarized as follows: 13

Syste heat losses -2.0 MWt Ca ponent conduction and convection losses -1.4 6 Pmp heat adder e.13.5 . Net Heat input to RCS +10.1 MWt - The uncertainty on syste 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 measurments are not possible, the uncertainty on caponent conduction and convection losses has been assmed to be [ ]+a,c of the calculated value. Reactor coolant pmp hydraulics are known to a relatively high confidence level, supported by syste hydraulics tests perfonned at Prairie Island II and by input power measur m ents frm several plants, therefore, the uncertainty for the pmp heat addition is estimated to be [ ]+a,c of the best estimate value. Considering these parmeters as one quantity, which is designated the net pmp heat uncertainty, the cabined uncertainties are less than [ ]+"'O of the total, which is [ ]+a,c of core power. Table 3 provides the instrument uncertainties for the measurments performed. , Since it is necessary to make this detemination daily, it has been assmed that the plant process emputer will be used for the measurments. The sensitivities calculated are noted on Table 4. As noted on Table 5, Westinghouse has detemined the depeMent 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 core power. The same was perfonned for the instrt;eaent bias values. As a result, the calculation explicitly accounts for dependent effects and biases with credit taken for sign (or direction of impact). Using the power uncertainty values noted on Table 5, the 3 loop uncertainty (with bias values) equation is as follows:

                                                             +a ,c                  -

Immmm ens 14

p g+a,c d After consideration of bias and conservatim, a value of [

• ]+"'U was used in the ITDP analysis calculations.

IV. CONCLUSIONS Be preceding sections provide the methodology for what Westinghouse believes is a reasonable means of accounting for instrumentation tmcertainties for pressure, taperature and power. De plant-specific instrtmentat.'on has been reviewed for Virgil C. Stamer and the uncertainty calculations are completed for use in the ITDP analysis. 4 e a

TABLE 3 POWER CALORIETRIC INSTRUMENTATION UN2RTAIhTIES $ (5 SPAN) W TEMP FW PRES W d/p S1H PRESS [ SCA = +a.c METE = SPE = STE = E = BIAS = RCA = M&TE= , RTE :- RD = 4 b = A/D = CSA = F psia  % d/p psia INST SPAN = 500. 1500. 120. 1300. - INST UNC - _ (RANDOM) = +a,c INST UNC (BIAS) =_ , NOMINAL = 435, 968. 868. 9 O e I a 16

TABLE 4 o POWER CALORI)ETRIC SDISITIVITIES o FEEDWATER PLOW F. _ _ TDFERATURE = +a,c MATERIAL = DENSITY TDFERAIURE = , PRESSURE = DELTA P = FEEDWATER ENTHALPY TDPERATURE = PRESSURE = . h = 1197.4 BWLBM 3 hp = 413 9 BWLBM Dh(SG) = 783 5 BIU/LBM STEAM ENTHALPY

   ,         PRESSURE       =                         +a,c POIS1URE       =

P I 9 4 17

TAILE 5 SEENDARY SIDE POWER CALORIMETRIC MEASURDIENT UNTRTAINTIES COMPONENT INSTRUMENT ERROR POWER UNCERTALNTY FEEDWATER PLOW _

                                                                                 +ag VDmlRI
      'DIERMAL EXPANSION Cf' EFFICIENT                                                     ,

TDIPERATURE MATERIAL DENSITY TENPERATURE PRESSURE DELTA P FEEDWATER ENTHALPY TENPERATURE PRESSURE STEAM DmiALPY PRESSURE POISIURE NET PUMP HEAT ADDITION BIAS VALUES FEEDWATER DELTA P FEEDWATER PRESSURE DENSITY ENTHALPY STEAM PRESSURE ENDIAIPY POWER BIAS TOTAL VALUE I 8, " INDICATE SETS OF DEPENDENT PARAET. ERS_ SINGLE LOOP UNCERTAINIT (WITHOUT BIAS VALUES) 3 LOOP UNCERTAIN 1T (WITHOUT BIAS VALUES) , , 3 LOOP UNCERTAINTY (WITH BIAS VALUES) , k 18 l -

REFERENCES Q c 1. Westinghouse letter NS.-CE-1583, C. Eicheldinger to J. F. Stolz, NRC, dated

 -          10/25/77.

i l

2. Westinghouse letter NS-PLC-5111, T. M. Anderson to E. Case, NRC, dated i 5/30/78.

3 Westinghouse letter NS 'INA-1837, T. M. Anderson to S. Varga, NRC, dated 6/23/78. l l

4. Westinghouse letter NS-EPR-2577, E. P. Rahe Jr. to C. H. Berlinger, NRC, dated 3/31/82.

5. Westinghouse Letter NS 'INA-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 Canpany, dated 2/12/81.

7. NUREG-0717 Supplement No. 4, Safety Evaluation Report 'related to the operation of Virgil C. Staner Nuclear Station Unit No.1, Docket 50-395, August, 1982.

8. Regulatory Guide 1.105 Rev. 2, "Instrunent Setpoints for Safety-Related Systems". Qted 2/86.

9 NURED/CR-3659 (PNL-4973), "A Mathenatical M: del for Assessing the Uncertainties of Instrunentation Measurenents for Power and Flow of PWR Reactors", 2/85.

   . 10. ANSI /ANS Standard 58.4-1979, "Criteria for Technical Specifications for
  .         Nuclear Power Stations".

19

11. ISA StandaM S67.04,1982, "Setpoints for Nuclear Safety-Related Instrtanentation Used in Nuclear Power Plants" '

I

                                                                                       \

12. Tuley, C. R. , Miller, R. B. , "Westinghouse Setpoint Methodology for Control ,,

and Protection Systes", 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 Measurenent and Control Teminology".

l W 4 4 e 4 20

FIGURE 1 - POWER CALORIMETRIC SCHEMATIC l I l I J o o U h 3 h f P f r, K 1 l if W  ; f 9 D - calculated O-measured 0g 3

                                                                                   \t
                                                                                      +

j U l a t

                                                                            =      E     =         Eo, lf Core Power 21

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