ML19221A158

Submits Task Close Out Document Re Evaluate Effect of non-condensibles in Reflux Boiling Mode

ML19221A158
Person / Time
Site:	Crane
Issue date:	04/17/1979
From:	Ditmore D, Paddleford D, Selbrig C INDUSTRY ADVISORY GROUP
To:
References
NUDOCS 7905190218
Download: ML19221A158 (14)

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Abstract 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 vessel)/ condensing (in the steam generator) mode.

Summary 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 might temporarily effectively seal the top of, the candy cane and limit the flow of steam to the stean generator.

(b)

This condition would not be expected to occur unless the system lost natural circulation and boiled at or near atmospheric pressure with the pressurizer relief valve (and block valve) open for a considerable 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 actual radiolysis rate.

(c)

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

This pressurization might occur either by; (a) via pressure relief through the pressurizer 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 system 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 most likely, although it is likely that steam flow to, and condensation in, the stean generator will ultimately predorinate.

An important, premise for these conclusions-is that the volute of non-condensibic gases which might be expected to be present even aftcr boiling at atmospheric pressure 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 />,'would be relatively small when the pressure increases to tne

'Re

-'200 psia.

Under these conditions the non-condensibics would either bect _

co-mingled with the steam or in the worst case, if there was stratification they would be compressed (by the steam acting as a pisten) to a much smaller volume above the water level in the steam generator. Condensation in the

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• 3

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steam generator should in either event be re-established in the steam

entrator.

Another important factor is that long before stable conditions could h-achieved, percolation of steam / oscillation of water levels should be

. x

t. ed.

Such percolation should also encourage good mixing of the steam a.., ron-crndensibles, if they are not already well mixed.

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

Ostensibly the pressurizer 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 volume provision for the generated steam in the top of the system.

During this period of initial boiling non-condensible gases would be given off by 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 continue at low pressure it is possible that hydrogen would build up in the steam generator and ultimately over into the candy cane. Assuming no re-solution in the generator, which is very conservative, and maximum evolution of hydrogen in the core during boiling a volume ef 1050 SCF, 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-~S00 SCF*.

Therefore, boiling at a"nospheric 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-condensit 'es on the order -2000 SCF assuming no re-solution.

This volume of gas built up above the water level in the steam generator and 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 415 of the primary system volume and 110'. of the steam generator volume on the primary side. Thus raising the system pressure to 10 to 20 atmospheres by closing the pressuri:cr relief valve and/or block valve, or allowing it to achieve a pressure of 175 - 200 psig naturally by steaming thru the pressurizer relief, if it is completely open, would provide a means of breaking the postulated seal of non-condensible gases.

Cnce the system is pressurized in this fashion the steam should begin condepsing in the secondary heat exchanger, if i+ wasn't aircady doing so, on the cold tubes and/or at the water surface depending on the level of water being maintained in the heat exchanger.

One potentially important censideration is the effect of non-condensibles in the heat exchanger on the heat transfer coceficients for condensation.

• water san,les indicate -,63 cc/ml "-S00 SCF with a pri..ary syste,m volume of

~12000 ftb.

17r nc0 IJJ UJU e

4

-3 Normal condensation heat transfer coefficients on the order of S00 BTU /hr ft.2 F can be expected without non-condensibles.

The effect of non-condensibles is expected to reduce this coefficient by approximately an order of magnitude reduction. However, even if one conservatively assumes a coefficient reduction of two orders of magnitude there is still ample heat transfer rate to condense all 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.

Once the path for condensation has been established, a stable equilibrium 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 resolution would occur at the same rates should be sufficient to remove available hydrogen.

With or without the relief valve open the system will stabilize 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 radiolysis. Appendix 4 analysis 2

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

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

I6 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 pressuri:er. However, with the relief valve open, some makeup would be desirable over the long-term.

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

It is coincidentIV true that the reflux boiling /condensatien thermal hydraulics should also be 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 qualitative and idealized. As a consequence it is considered imperative that:

(a) A scaled 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.

(b)

Someone at BSW or in the working group should be assigned the responsibility to perform more detailed system-unique analyses for TMI -II te investigate the various boiling codes, and (c) Operating procedures should be developed to assure that appropriate actions are taken to come to a stabic boiling condition at a

predetermined pressure, with appropriate attention to question of non-condensibles, should natural circulaticn be lost.

i35 059 e

e APPENDIX 1 Non-Condensibles Currently in Primary Water Water sample measurement as of 4/16/79 indicates 6S cc. at STP per Kg of water. This represents a volume fraction of 6S cc (1 gm/cc) =

.068 (1000 gm) 3 Total Primary System Volume--12000 Ft Total Volume of Non-Condensibics at STP in primary system::12000 x.068 =

816 SCF -800 SCF Non-Condensibles Evolution During Boiling At Atmospheric Pressure Under boiling conditions in the core, with decay heat, radiolysis will result in the evolution of both H2 and 0

• 2 The attached letter, P. W. Marriott to D. Rockwell, of April 9, 1979, indicates an upper bound on H 3 evolution would be 73 SCF/hr using Reg. Guide 1.7 assumptions and a core thermal power of 5 mw.

Adjusting this to the current 3M level yields 43.8 SCF/hr at atmospheric pressure.

43.8 SCF x 24 hrs = 1051 SCF H, With 0, this would become 1576'SCF.

Total if all currently dissolved gases come out of solution = 1576 + 816 =

2392 2400 SCF. This is very conservative. More realistic rates on the order of 300 to 600 SCF/ day are more likely, particularly as the steam / hydrogen pressure above the core increases.

At more realistic rates it could take 2 to 5 days to achieve levels as high as -2400 SCF with no resolution and complete release of all currently dissolved gases.

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e APPENDIX 2

~

Diffusion of Steam Through H, Gas J=

- AD @jc J:

A=

36 in.2 si m2 D f I cm2 2 2T'F -10m see 4

2 2

0 - 1.0 = + 10 cm3 x 1 ft3

10 ft3 J

- 10 cm,1 cm (30.24 cm)3 2777 x 103 sec 1000 cm see see J=

0.36 x 10-2 3

ft /sec

.Need for steam generation rate b = (3 mw) 6 3

(3.413 x 10 ) BTU /Hr tw x 26.8 ft3 =.0723 x 103 ft 970.3 BTW/lb (3600 sec) lb see hr )

3 a at 1 ata = 72.3 ft /sec 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 2 -2.3 m depth of'-/hr, and Acrossection = 25.2 ft 6

J=

- 104 x 2.3 x 1 cm2 0_-7 0 1

,= 2.3 x 102 I

3 ft /sec

.8310-

=

see 10 (30.24)J 2.77 x 105 Still is to low for diffusion through the H,.

However, by the time the steam reached the top of the Rx it would begin t5 condense on the tubes and run down through the hydrogen plug.

9 O

i35 063 O

e APPENDIX 3 Flowrate Through Pressuri:er Relief Valve Valve throat area wl.05 in Critical Isentropic Flow through a No::le 2

G 53 lb/hr in psi at I atm hg = 1150 BTU /lb G'52 lb/hr in2 psi at 15 atm hg = 1200 BTU /lb b

= (3mw) (3.413 x 10 BTU /aw hr)

= 12.28 x 10 lb/hr at 15 atm 6

3 steam 833.6 BTU /lb b

= 12.28 (833.6) x 10 = 10.55 x 10 lb/hr at I ats 3

steam 979,3 P

,=

10.55 x 103 lb/hr 1

= 193.2 psi Ps1 1.05 in" 52 lb/hr in' psi 12.28 x 103 P

1

220.6 psi psi

1.05 53 This says that to vent through the relief valve on the pressurizer will require about 200 psi back-pressure.

In other words the syrtes will tend to pressuri e it self when venting through the pressuri:er relief valve.

O 7 I h [

M e.

e APPENDIX 4 To:

D. C. Ditmore - Industry From:

P. W. !!arriott 4/17/79 Advisory L. Nesbitt Group M. Siegler

Subject:

Hydrogen Solubility Evaluations THI - Gas Removal / Mass Transfer 6

Power = 3mw = (3 x 10 kw) x 3413 BTU

= 10.2 x 10 BTU kw.hr hr Assume:

212 F I atmosphere pressure h'E 970.3 BTU

=

lb Steam Generation Rate of Saturation Conditions = 10.2 x 106

= 1.05 x 104 lb 970.3

• hr

-6 Solubility of H., at I atm, 2120F = 1.69 x 10 lb H2

{l) 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:

4 3

,', (1.05 x 10 lb_ ) (1.69 x 10-6.ata) (359 ft H2 at STP) hr 3

3

= 319 x 10-2 ft /hr at STP u 3 ft /hr H2 solubility in the condensing steam.

This limits the amount of H.,which can be transferred.

(If the rate of evolution of H., by radiolysis in the core during boiling exceeds this rate then H will build Up in the system in the secondary steam generator.)

2 As an alternate case, if you' assume 1200F instead of 212 F, the result is 0

approximately the same.

Solubility of H2 as 12005 = 1.48 x 10-6 lb lb atm

• Solubility Rate in Available Condensing Steam is,

= 3.19 (1.48 x 10-6) = 2.8 ft /hr 3

1.69 x 10-6 Now, if you look at the case of 15 atmospheres total pressure t h392 F, H2 S lubility = 3.36 x 10-6 13 Ib atm nr

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APPENDIX 4 (Cont.)

If you then take into account the 15 atm pressure, the H, transport into the condensing steam would be lb steam) (970.3) (3.36 x 10-6 lb

) (mole) (359 ft at STP) (15 ata)

(1.05 x 104 3

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

=

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

3 (110.9) (1.48) = 48.8 ft /hr (STP) 3.36

,', The actual solubility during condensation probably falls in the ranges of:

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

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

15 atm would probably work, (since very conservative estimates indicate 11, avofulion due to radiolysis when boiling 1 atm in the postulated core condition for TMI - II is no greater than at 43.8 SCF/hr*.

In fact some pressure below 15 atm but above 1 atm would probably have sufficient solubility rates compared to radiolysis evolution rates for H.)

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

lb.atm 6

4 0 Transport (To Condensing Steam) = (25.2 x 10 )(1.05 x 10 )(1 mol

)(359 ft3 STP) 2 32 lb mole 3

= 296.8 x 10~

~ 3 ft /hr at STP and 1 atm at 392 F 0 Solubility = 45.1 x 10-6 lb lb.atm O., Transport = (45.1 x 10-6)(1.05 x 10 )(970.3)( 1 )(359) 4

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

0., numbers are '. quite similar to H., numbers on a volumetric basis.

Note: All transports are based on either 1 atm or 15 atm availabic gas pressure.

O., generation rate should be -1/2 H, ande 1/2 (43.8 f t /hr) " 21.9 f t /hr at 3

3 tile rost at I ata.

So again at 1 atm you'can't remove all generated gas, but 15 atn considering the decrease expected in radiolysi. you should be abic at to recove all evolved 11, and 0, bared on full equilibrite, being reached in 2

!! 0 for each gas.

(In fact su t ficient solubility rates esgared to radiolysis 2cvolution rates for 0,)

1 W. 0. 6 S

. s,_ m

s APPENDIX 4 (Cont.)

Try 2 Atm Pressure Let's assume that 2 opm by weight of H = suffici it to suppress radiolysis 2

2 x 10-6 gg,

{Hj0 Assume v-2 qtm total pressure tsat = 2520F hfg = 944.2 4

4 Steam Rate at 3 mw = (1.05 x 10 lb) (970.3) = 1.08 x 10 lb hr 944.2 hr 2 x 10-6 lb H, x 10.S x 10 lb x 359 ft'3 lb H O hr 2 lb H2 2

3

= 3877 x 10-3 ft /hr H required to be transported to maintain 2 ppm is condensed steam.

solubility at 252 F and 2 atm total pressure = 1.91 x 10-6 lb 0

H2 lb.atm Mass cansport into Condensing =(10.8 x 10 lb)(1.91 x 10-6 lb

)(2 atm)(359 SCF )=7405 x 10-3=7.4 ft3 Steam hr lb.ata 2 lb hr at 2 ppm H, and 2 atm the rate of resolution possible during condensation is > than the rate of evolution due to radiolysis.

Conclusions 3

Mass transfer calculations yielded-255 ft /hr capabic of being transferred if H,0 film reaches equilibrium saturation valve.

But at 2 ppa concentration you only need about 4 ft /hr.

System will probably seek a higher liquid level than the Icvel assumed in mass transfer calculation of -25'.

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