ML19221A613

Task 10c:Evaluate Effect of Non-Condensible in Reflux Boiling Mode

ML19221A613
Person / Time
Site:	Crane
Issue date:	04/17/1979
From:	Ditmore D INDUSTRY ADVISORY GROUP
To:
References
OLS-790417, TASK 10C, TASK-10C, NUDOCS 7905230411
Download: ML19221A613 (14)

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Abstract

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Having addressed earlier the " Behavior of RCS with Steam Generators In Condensing Mode", C. Solbrig, et. al., April 10, 1979, the IAG was asked to further investigate the possible effect of non-condensibles under the mode of decay heat removal in which the primary system loses natural circulation and goes into a boiling (in the pressure s essel)/ condensing (in the steam generator) mode.

Snmm ry Based upon a review of the available information and the competing phenomena the following is concluded:

(a)

It is possible that a volume of evolved non-condensible gases might reach a size wherein it night te=porarily effectively seal the top of the candy cane and ibnit the flow of steam to the steam generator.

(b) This condition would nct be expected to occur unless the syst em lost natural circulation and boiled at or near atmospheric pressu e with the pressuri er relief valve (and block valve) open for a cc isiderable period; i.e., 24 - 60 hours6.944444e-4 days <br />0.0167 hours <br />9.920635e-5 weeks <br />2.283e-5 months <br /> or longer depending on the actua.1 radiolysis rate.

(c)

If thi's condition did occur it should be possible ;o break this seal by raising system pressure to the range of 10 to 20 atmospheres.

This 7,

pressurization night occur either by; (a) via pressure relief through V

the pressuri:er relief valve which under choked conditions would require *-200 psia back pressure to vent the steam generated in the core, or (b) by closing the pressurizer relief valve if that were still possible.

In either case, pressurization should occur via steaming in the core and continued evolution of non-condensibles, although this may be a very slow process.

(d) During steady state operation in a boiling mode, with or without the relief valve open, an equilibrium condition would be expected to be attained where the gases released by radiolysis during boiling should equal those which go back into solution at the condensation surface, and/or out the pressurizer relief valve if it remains open.

(e) Once the systsm has stabilized, the heat removal from the primary

~

system will either be via the pressurizer relief valve, condensation in the steam generator, or a combination of both.

Some combination which yields a system pressure somewhere between atmospheric and

• ~200 psia is =ost likely, although it is likely that steam flow to, and condensation in, the steam generator will ultimately predominate.

An

. at. premise for these conclusions is that the volume of nong 4,es w condens r atmospheris essure for a considerable period; i e., *-2000 SCF after 12 to 24 hours2.777778e-4 days <br />0.00667 hours <br />3.968254e-5 weeks <br />9.132e-6 months <br />, wculd be relatively small when the pressure increases to the range

-'200 psia.

Under these conditions the non-condensibles would either become

()

co-mingled rith the steam or in the worst case, if there was stratification they would he cocpressed Jby the steam acting as a piston) to a much smaller volume abovo the water level in the steam generator. Condensation in the

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• a

/:

/

/

steam generator should in either event oe re-established in the steaa

./

generator.

Another important factor.is that long before stable conditions g

could be achieved, percolation of-steam / oscillation of water levels should be expected.

Such percolation should also encourage good mixing of the steam and non-condensibles, if they are not already well mixed.

Discussion b

Tf natural circulatin without boiling were somehow lost and could not be re-established, the stagnant liquid in t,.e reactor vessel would eventually be brought to saturation and bulk boiling could begin.

Ostensibly the pressr-izer relief valve would be opened to allow displacement of the relatively cold pressurizer water out of the primary system for some period to be able to make vo'lume provision for the generated steam in the top of the system.

this period of initial boiling non-condensible gases would be given off by During radiolysis and would pass with the steam over to the steam generator, where the steam would condense and at least initially hydrogen could begin to buildup.

If this condition were to allow to _ontinue at low pressure it is possible that hydrogen would build up in the steam generator and ultimately over into the candy cane.

and maximum evolution of hydrogen in the core during boiling a v could build up after a considerable period of boiling at atmospheric pressure.

Conservative estimates for the time to do this range from 24 to 60 hours6.944444e-4 days <br />0.0167 hours <br />9.920635e-5 weeks <br />2.283e-5 months <br /> with extensive core damage (See Appendix I). The measured level of dissolved non-condensible gases remaining in the primary system as of 4/16/79 was-800 SCF*.

Therefore, boiling at atmospheric pressure for 24 to 60 hours6.944444e-4 days <br />0.0167 hours <br />9.920635e-5 weeks <br />2.283e-5 months <br /> could result in a volume of non-condensibles on the order -2000 SCF assuming no re-solution.

This volume of gas built up above the water level in the steam generator and 4-4 into the candy cane could conceivably form a seal which would block or limit steam flow to the steam generator.

Since mass diffusion of steam through hydrogen is quite low (See Appendix 2) one could argue that such a condition

~

could prevent reflux boiling. However, the volumes of non-condensible gases are still relatively low and if raised to a pressure of 10 to 20 atmospheres would represent a partial volume of 41%.of the primary system volume and 410% of the steam generator volume on the primary side.

Thus raising the system pressure to 10 to 20 atmospheres by closing the pressurizer relier valve and/or block valve, or allowing it to achieve a pressure of 17S - 20C psig naturally by steaming thru the pressurir.er relief, if it is completely ope.., would provide a means of breaking the po stulated seal of non-condensible gases.

Once the system is pressuri:.ed in this fashion the steam should begin condensing in the secondary heat exchanger, if it wasn't already doing so, on the cold tubes and/or at the water surface depending on the level of water being maintained in the heat exchanger.

in the heat exchanger on the heat transfer coeeficients for conden

• water sangles indicate 68 cc/mi $~800 SCF with a primary system vc ;ume

• 12000 ftJ.

f

}h

/

) y/ Normal condensation heat transfer coefficients on the order of 800 BTU /hr ft.2o y

/

can be expected without non-condensibles. The effect of non-condensibles is

/g expected to reduce this coefficient by approximately an order of magnitude

~

. reduction. However, even if one conser,vatively assumes a coefficient reduction of two ordsrs of magnitude there is still ample heat transfer rate to condense ab steam generated. This is true because of the large amount of heat transfer area, even if only the top 5 - 10% of the heat exchanger tube length is available for condensation.

Oncethepathforcondensatiohnhasbeenestablished,astableequilibrium condition should eventually be attained at these pressures where the steam and hydrogen would be evolved in the core, remain co-mingled, and pass to the heat exchanger and partially vent out the pressurizer if the relief valve remained open, and resolutien would occur at the same rates should be sufficient to remove available hydrogen.

With or without the relief valve open the system will stabili:e at a pressure above 1 atm and probably below

• 200 psi, an equilibrium which will be determined by the rate of resolution of H /02 which will equilibrate with the core radiolys.s.

Appendix 4 analysis 2

demonstrates that equillitrium could be established at or above-2 atm.

If the relief valve remains cpen pressures on this order are more likely, if closed they will be higher.

Id either case it is likely the secondary heat exchanger will be the predominant point of heat removal in the system, as opposed to the relief valve on the pressurizer. However, with the relief valve cpen, some makeup would be desirable over the long-term.

The higher pressures proposed to assure no problems with non-condensibles are conducive to both hi h solubility of H and low radiolysis.

It is coincidently J

2 true that the reflux boiling / condensation thermal hydraulics should also be k

more stable at these pressures since the specific volume differences of gas and liquid are much smaller than at atmospheric pressure.

Recommendations The evaluations described are of necessity somewhat qualitctive and idealized. As a consequence it is considered imperative that:

(a) A scaleti test of some sort be performed as soon as possible to confirm the conclusion that a non-condensible gas seal can be broken under varying system conditions.

o (b) Someone at BSW or in the working group should be assigned the responsibility to perform more detailed system-unique analyses for

'D!I -1I to investigate the various boiling modes, and (c) Operating procedures should be developed to assure that appropriate actions are taken to come to a stable boiling condition at a predetermined pressure, with appropriate attentior to question of non-condensibles, should natural circulation be lost.

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APPENDIX I J

g Non-Condensibles Currently in Prim. cy Water

~

~

Water sample measure:nent as of 4/16/79 indicates 68 cc cf water.

This' represents a volume fraction of 68 cc (1 gm/cc) '.. at STP per Kg

.068 (1000 gm)

Total Print-v Syste:a Volume-12000 Ft k

3

..r-.-

Total Volume of Non-Condensibles at STP in primary system::12000 x 816 SCF -800 SCF

.068 =

Non-Condensibles Evolution During Boiling At Atmotpheric Pre sure in the evolution of both HUnder boiling conditions in the core,. with decay heat 2 and 0 '

, radiolysis will result 2

indicates an upper bound on HThe attached letter, P. W. Marriott to D. Rockwe

, 1979, assu=ptions and a core thermaI power of S mw.2 evolution would be 73 SCF/hr using ",. G 3M level yields 43.8 SCF/hr at atmospheric pressure. Adjusting this to t..o current 43.8 SCF x 24 hrs = 1051 SCF H With 0 2

2 this would become 1576 SCF.

Total if all currently dissolved gases come out of solution = 1576 2392 2400 SCF.

, h of 300 to 600 SCF/ day are more likely, particularly as the steam / hyd This is very conservative.

+ 816 =

More realistic rates on the order above the core increases.

to achieve levels as high as *2400' SCF with no resolutiAt more realistic rates r days of all currently dissolved gases.

on and complete release e

a lr i

j t

6 nd he ehe-m mM*s'==**

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>>wwm-'~tsnwCu ~&D*MtMMYYth I97. 01 -

.us.a.rq - (b~...- -. =

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a 4 'E v = i~~ Y ~

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This ceso soszaartzes our mts on several hydsvsco-related subjects rcqcested by GFU ever the past t2o drys.

c.,-

1.

Redceticet of Cdlant Teuveratere to Mexf afre Net DGrssf aq.

MIT catsultsats.crw tinrt 4) for 515 psia of Ha prtssure at 200 F the 0

mmt of B diss,cived to tha teter is G.63 ii!!1/gs (ma get 0.f,4 d1/gn).

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b) for 503 psia of 5 pressure at 14d'F the nznat of 5 dissolved fa the asater 1

2 is G.63 a l / g n (ir get 0.57 el/gs).

c) a:=mmat of Mr dissoired f a uster at 20 psta of Hz and a te.ature of F is 0.02 (we get 0.GZ5 al/gs),

d) Uthe amnesst of B: dissolved ta water at 20 psia of W and a fwrature of

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140 F is 0.01 (we get 0.022).,

3 s

The practical czz:clusions are:

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1) He agree as high a pressure as practical trill get the maximum arcant hi of B dissolved in tfur ::ater. ::ad therefore, the maricuas Fisase o,1 2

the let d:mn.

2) Me be11ere, based on GE experfe:1ce in de supersItaration of M 3

fa

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u;:ter that the fe,p'rature is not facurtant in the range of' 150 to 200 F.

3) i cer!d fet rh1-There is a pastbility that flashing frew 2BU"F '(but. smt from 200 F)

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.tutter than 230*wtth fica ia the lat auss lina. Thartrfare. ZadDF u.:uld be F for net deJassing.

II._ M drew. Generation Eate Lomy-Tens

• $t. :.Icpat:

Thesisal Pomarr 5 R~ir 165 3hc r

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[N N.' Cata 1..rtLtca'; any tctifsg fa the care, and with an overvmsuro er Ha la o:s a.

g.q; g ;[ths let 4:=w Tact at T-12G F of 1 ata of Na the radfolysis sbauld b 8

g'."[{lh5 Cast 2. Emnt zey to1Riss is the care, and with an fatact ' core, tha s4 k

$, ssed ce X2Lfd/52 pg. 8 2:9d ccqwisco with UR data should be.

S,kT.13 50%) x o.c3 q x co ghr) x o.ca,g:a cotienc,

, cs o.3 ss&

e.. -

g.

t n

' %.:t'.-We.4

+

-2 p;'..s. / ". * *.? y.

hs Hing

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7....,.,.

A..

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% A.Otte 1._t 8512g AG 1.3 and 18 as m

wi."ans en fission y ui. rulusa, tof1fo Det?

cpm -+ -. Ihe pecarstic:a rata of a mature 27CO mftere w.. ' rodfolysfs is m. rir.g. (or a cesra s).

y:

T care at 10 days is 73 scfh of Ng s

3 Q <.. &,3 7

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W

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,e w

e m-m;, 4. ~,..n -- ;F.. -,_ w- - - : ~-- %.

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p

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,.m _.

3p

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...... cc. r-y - -

pe.*~.

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April 9,1979 F

' L::d k."'~'*;

.. -. m u y.-

.--. O.4 M.

- ~ ~ A 2 @y.,

.::[ 2 i G ;f p.- f' -

~ 19.-2 Expeffesce dd.a fms GE Buts eo sbat d:m:r at 5 IQt. (as in 2 ahore)_.__

s_.,,,. __ ; Q ;M 3 d

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wip.:. : q 4

z.

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_ 9 sefhW 'O M.2 Case 5 The most likely volta is case,1 with the. W con hs11fnD correctfazz' 3

c'%

faecr of o.0.1:

n (sefh) x o.c3 (nes i

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==).

.p g i Ha rmwa1 rate by solubility tased os 515 psia and 200 F, 8

we cza remove 100 scfb.

Conclusion:

even at 10 sps with a factor of safety greater that 10 (base As per 1bCO PST this date d lure data from plant I

III.. Pe tas:1tzs Pemanganate as a *bb,Es Eetter Me hare considered what problems night be enfgantered 113 Assu=esu thtcrated loop st 500 psi ZEU'F:

In using K PinOg to rexxrve m

of 1.6 x 10' kg of saturated 2%sD unter solution - about 6% of the total p ithis 1 cap 1>olun or ahcut 1403 a1 cutes at 3 gpa.

r mary Thf s socid 1.d.3 abcat 1000 K 9 of K Fri0 and yield sh it 600 kg Macs the 11: were reacted.

g KGH is en end product of the reaction, so tie coolut could ImThis auch sicxig (pft % 12) tn $0e h-r m the reaction pred::ct is !! 0.Rzterials prcperties are still being studie guite bas 16 of d Os to funz'Or (free) s.-hich could lead to !!z402The major gr:stion is the dm- =;-2sttien reaction.

the U 0 could freediately react erfth aspie HeThe h-asition toald be less troc and the possib111ty of rapid 2

ps trrt..

fr the victatty of the tsjection c

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3 APPENDIX 2 r

FO giffusi n f Steam Thr ugh H Gas 7

J=

- AD Ax %

E3 V

A=

36 in.2 *1 bi2 D f 1 cm2

/230f -10m sec J=

- 104 2

m,"1 a2 0 - 1.0 = + 10 cm3 x 1 ft3

= 10~

ft3 (30.24 cm)3 2 77 x 103 sec 1000 cm sec J,= 0.36 x 10-2 3

ft /sec Need for steam generation rate

$ = (3 mw) 6 (3.413 x 10 ) BW/Hr mw x 26.8 ft3 =.0723 x 103 3

ft 970.3 BTW/lb (3600 sec) lb see hr )

E2at1atm=72.3ft/see 3

This says straight diffusion through a hydrogen slug is not practical at

~

1 atm.

Hydrogen will tend to pile up more and more if the mechanism relied totally on mass diffusion through a slug of gas in the pipe.

If gas is compressed into secondary Hx due tg increased pressure to a depth of -/hr, and Acrossection = 25.2 ft2 -2.3 m k

104 x 2.3 x 1 cm2 0 -1.0 1

_ = 2.3 x 10

.8310- 1 J

2 3

ft / ec see 100 (30.24)J 2.77 x lua Still 12 to low for diffusion through the H. However, by the time the 2

steam reached the top of the Hx it would begin to condense on the tubes and run down through the hydrogen plug.

O

1

~

APPENDIX 3 C7 Flowrate Through Pressurizer Relief Valve

$0 Valve throat area 51.05 in Critical Isentr-ic F1 w through a No zie

~

2 G"53 lb/hr in psi at 1 atm

= 1150 BTU /lb G"52 lb/hr in2 psi at 15 atm ng = 1200 B7U/lb b

= (3mw) (3.413 x 106 IrIV/mv hr) = 12.28 x 10 lb/hr at 15 atn steam 833.6 BTU /lb

12.28 (833.6) x 103,'10.55 x 10 lb/hr at I atm Steam 970.3 P,

10.55 x 103 lb/hr 1

pst

193.2 psi 1.05 ind 52 lb/hr in psi psi

12.28 x 103 P

1

= 220.6 psi

~

1.05 53

.This say; :. hat to vent through the relief valve on the pressurizer will require about 200 psi back-pressure.

In other words the system will tend to pressurize k

it self when venting through the pressurizer relief valve.

k.

e 165 348 6

1 APPENDIX To.

D. C. Ditmore - Industry From:

P. W. Marriott 4/17/79 Advisory-g L. Nesbitt Group M. Siegler subject: Hydrogen Solubility Evaluations

'INI - Gas Removal / Mass. Transfer (3 x lb kw) x 3413 Power = 3mw =

BTU

= 10.2 x 100 B'IU kG hr Assume: 212 F 1 atmosphere pressure hf 970.3 BTU

=

g 3g-Steam Generation Rate of Saturation Conditions = 10.2 x 10 6

= 1.05 x 104 lb

~

970.3 E

Solubility of H2 at I atm, 2120F = 1.69 x 10-6 lb H2 (1) lb water (atm)

(Note that the solubility is proportional to the number of atmospheres of pressure.

Higher pressure improve the solubility).

Solubility in the available in condensing steam is:

. (1.05 x 104 lb g ) (1.69 x 10-6.atm) (359 ft H2 at STP) 3

= 319 x 10-2 3

3 ft /hr at SIP w 3 ft /hr H2 solubility in the condensing steam.

This limits the amount of H2 which can be transferred.

(If the rate of evolution of H.,

by radiolysis in the core during boiling exceeds this rate th H

2 will build ik in the system in the secondary steam generator.)

en As an alternate case, if you assume 1200F instead of 212 F0, the result is approximately the same.

Solubility of H2 at 12005 = 1.48 x 10-6 13 IF ata

,', Solubility Rate in Available Condensing Steam is,

= 3.19 (1.48 x 10-6) = 2.8 ft /hr k

3 1.69 x 10-b

Now, if you look at the case of 15 atmospheres total pressure t=3920F H2 Solubility = 3.36 x 10-6 g Ib atm

i

~

APPENDIX 4 (Cont.)

J' If you then take into account the 15 atm pressure, the H transport into

~

V' #

the condensing steam would be 2

f (2.05 x 104 lb steam) (970.3) (3.36 x 10-6 Ib

) (mole) (339 ft3 at STP) (15 atm)

, hr 833.6 lb atm 2 lb mole 11087.6 x 10-2 = 110.9 ft /hr 3

=

As an alternate case if you look at 120 F the result is:

0 3

(110.9) (1.48) = 48.8 ft /hr (STP) 3.36

,', The actua' solubility during condensation probably falls in the ranges 3

2.8 -3 ft /hr at I atm, and 3

48.8 -110.9 f2 /hr at 15 atm But, what really helps at the higher pressure is that the radiolysis should be sup;.ressed because of the dissolved H.

15 atm would probably work, (since very conservative estimates indicate H y fufi n due to radiolysis when boiling 2

at 1 atm in the postulated core condition for 'DfI - II is no greater then 43.8 SCF/hr*.

In fact some pressure below 15 atm but above 1 atm would probably

{

12ve sufficient solubility rates compared to radiolysis evolution rates for H 3 2

O i

Quick Look At Oxygen Solubility at 212 F 0 S lubility = 25.2 x 10-6 lb 2

lb.atm 0 Transport (To Condensing Steam) = (25.2 x 10b(1.05 x 10 )(1 mol )(359 ft3 STP; 2

4 32 lb mole

-2 3

= 2S6.8 x 10

- 3 ft /hr at STP and 1 atm at 392 F 0 Solubility = 45.1 x 10-6'lb lb.atm 0 Transport = (45.1 x 10-6) (1.05 x 10) (970.3) ( 1 ) (359) 2 833.6 32

= 9242 x 10-2 ~92 ft /hr 3

165 550 0 numbers are

• quite similar to'H numbers on a volumetric basis.

2 Note:

All transports are based on either 1 atm or 15 atm availatie gas pressure.

O., gene. Ttion rate should be"1/2 H, and e 1/2 (43.8 ft / hr) ^ 21.9 ft /hr at 3

3 gg tiie most at 1 atm.

So again at I atm you*can't remove all generated gas, but at 15 atm considering the decrease expected in radiolysis you should be able to remove all evolved H., and 0,, based on full equilibrium being z eached in H,0 for each gas.

e'olution rates for 0 )(In fact sufficient solubility rates compared to radiolysis 2

• Appendix I

,- - t.z n - M.!%1 R & a* M5Y S

APPENDIX 4 (Cont.)

8 py 2 Atm Press,tre

,/

Fe -

Let's assume that 2 ppm by weight of 117 = sufficient to suppress radiolysis

(

2 x 10-6 g

]

4g.

Assume e 2 qta total pressure tsat = 2520F h

= 944.2 f

H Steam Rate at 3 av = (1.05 x 10 4 jlb (970.3) = 1.08 x 104 lb nr 944.2 lir 2 x 10-6 lb H, x 10.8 x 103 lb x 359 ft Ib lijo E

2 lb 112 3

= 3877 x 10-3 fg /hr 11 condensed steam.

required to be transported to maintain 2 ppa is

!!2 solubility at 2520 F and 2 atm total pressure = 1.91 y 10-6 lb lb.atm Mass Transport into Condensing =(10.8 x 103 jlb (1.91 y 10-6 lb i

Steam lir

)(2 atm)(359 JSCF=7405 x 10-3=7.4 ft3 0

ib.atm 2 lb F

at 2 ppm 11 is y than the rate of evolution due to radiolysisand 2 Atm the 2

ondensation Conclusions ifHOfilmreachesequijibriumsaturationvalve.. Mass transfer calcu 3

2 you only need about 4 ft /hr.

But at 2 ppm concentration

.. in mass transfer calculation of -25'. System will probably seek a ssumed

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s+eam 2 S'o*F P

a a+m-j Adsoch q &

200 'Fif j 7,

f 0s1btM Wbon khdh o4 eypcarb Tuhes 2

'7-)2M W=

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' luz+fedpcAmh)I hkhINS4 ra [Ner' fi!m 4ttdate Vdoch3r/0M,-

O T m

tofed

\\ 100%14,docodeuodion S-lea ***hkdert?dt A vew;e +tt wTe~p. =acc*F y o,cooJ/g s a

1 M

l 120'F Cooling wocter Temp. l g4ch <j ert-crA4er

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From Bin:1 - s+ea4 -LiqL%d:

p. sso O

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v n,-,n, - W t.. p TT L

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'l -1.'!t to o 0 h u, @ =l.7 % t o U,,

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( where. -/ = s p a,

towlsh seooov=laxio%mik :

1 p uto-a l = ls74tO 1]rancNx y 9 A4% QOllsven Q lLlm & Hn,

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h m wo-Ms Tf 21"Y >

t p.,, e z ab.

I,oz y to'yikdia WA 165 352 O hT' =

Q. s x 1,0 2.

x 4.bCx to'3

,ol2 % =250 &

x LS kluGn w M An,

^

A

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un fp ad L 4w

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