Text

Further Response to FOIA Request for Five Categories of Documents Re Severe Accident Studies.Forwards App D Document Consisting of NUREG/CR-4205, TRAP-MELT2 Users Manual. Document Also Available in PDR
	ML20133C540
Person / Time
Issue date:	05/24/1985
From:	Felton J; NRC OFFICE OF ADMINISTRATION (ADM)
To:	Sholly S; UNION OF CONCERNED SCIENTISTS
References
	FOIA-84-298, RTR-NUREG-CR-4205 NUDOCS 8507200524
	Download: ML20133C540 (2)
	v • d • e

r

.,ff UNITED STATES NUCLEAR REGULATORY COMMISSION n

L

.E WASHINGTON, D. C. 20555 N4Y hy Mr. Steven C. Sholly Technical Research Associate Union of Concerned Scientists IN RESPONSE REFER 1346 Connecticut Avenue, NW, Suite 1101 TO F01A-84-928 Washington, DC 20036

Dear Mr. Sholly:

This is in further response to your letter of December 17, 1984, in which you requested, pursuant to the Freedom of Information Act (F0IA), documents in five categories relating to severe accident studies.

We previously made available documents identified in letters to you dated January 4,1985, and March 14, 1985.

The record identified on the enclosed Appendix D is now available for public inspection and copying at the NRC Public Document Room (PDR) in PDR file FOIA-84-928 under your name.

This completes NRC's action on your F0IA request.

Sinc rely,

,a2(

. M. Felton, Director Division of Rules and Records Office of Administration

Enclosure:

As stated 85072g524850524

guteyb2a

m

APPENDIX D RECORD IN PDR FILE FOIA-84-928 Category 5 1.

May, 1985 NUREG/CR-4205 (BMI-2124)

" TRAP-MELT 2 User's Manual" prepared by H. Jordan and M. R. Kuhlman, Battelle's Columbus Laboratories, Columbus, Ohio.

(70 pages).

r

]

' UNION OF CONCERNED SCIENTISTS 1346 Connerticut Asenue, N.W.. S. I101. Washington DC 20036. (202) 2%.5600 17 December 1984 Mr. J. M. Felton, Director FREEDOM OF INFORMATION Division of Rules and Records ACT REQUEST

@Qy( Q[

Office of Administration U.S. Nuclear Regulatory Commission kgI4 Jg-)$ -f Washington, D.C.

20555

Dear Mr. Felton:

Pursuant to the Freedom of Infonnation Act, I hereby request that documents in the following categories be made available at the Commission's Washington, D.C.,

Public Document Room:

1.

NUREG/CR-3025, "High Pressure Melt Streaming (HIPS) Program Plan",

Sandia National Laboratories.

2.

NUREG/CR-3440, " Identification of Severe Accident Uncertainties",

Sandia National Laboratories.

3.

All " issue papers" prepared for input to the Commission paper on severe accident issues (such papers have been prepared for NRC by NRC staff members and consultants at various national laboratories).

4.

Letter reports and other documents presenting the results of the HIPS experiments referred to in "1" above.

5.

Code manual and User's Guide for the TRAP-MELT-2 code (or whatever version of TPAP-MELT was used by Battelle Columbus Laboratories in making calculations for the BMI-2104 reports).

If there are ary questions concerning this request, please contact me at (202) 296-5600. Thank you for your attention to this matter.

Sincerely, C

Steven C. Sholly f

TechnicalResearchAssocin/

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$9$f.l-(bpfifi--

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31ain Office: 26 Church Street. Cambridge. Slassachusetts 02238. (617) 547 5552

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NUREG/CR-4205 BMI-2124 I

TRAP-MELT 2 USER'S MANUAL Prepared by H. Jordan and M. R. Kuhlman BATTELLE'S COLUMBUS LABORATORIES 505 King Avenue Columbus, Ohio 43201-2693 M

S gLed Prepared for k&O nd P

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FUEL SYSTEMS E "^"IO" BRANCH U.S. NUCLEAR REGULATORY COMMISSION Washington, D.C.

20555 NRC FIN No. B6747 A peds b/zkm2

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7;x TABLE OF CONTENTS P_ age _

a I

INTRODUCTION............................

1 DESCRIPTION OF THE MODEL......................

2 Transport Rate Equations 5

Solution Technique 7

MODEL FEATURES...........................

Intervolune Mass Transfer...................

7 8

Intravol ume Mass Transfer...................

8 Models in BETV and REMOVE 14 Models in ADH0C 18 Coa gul a ti on..........................

18 Brownian Coagul ation...................

19 Gravitational Coagulation 19 Turbulent Coagulation 21 REFERENCES.............................

FLOW CHART AND BRIEF DESCRIPTION OF SUBROUTINES 23 37 INPUT TO TRAP-MELT 2 OUTPUT FROM TRAP-MELT 2....................., e.

42 APPENDIX A A-1 EXAMPLE INDUT DATA SET FOR TRAP-MELT 2 APPENDIX B TRAP-MELT 2 SAMPLE OUTPUT...................-...

B-1

U TRAP-MELT 2 USER'S MANUAL by a

H. Jordan and M. R. Kuhlman May 9, 1985 INTRODUCTION In hypothetical severe accidents in light water reactors, radionu-clides released from the melting core will undergo chemical and physical changes and will deposit on various surfaces as they are transported through the reactor coolant system (RCS) to the containment. It is of considerable interest to know what fraction of these released materials actually reaches the containment and is potentially available for leakage to the environment.

The TRAP-MELT 2 computer code contains radionuclide transport and deposition models that are consistent with the emerging state of knowledge regarding release of radionuclides from melting cores and thermal-hydraulic behavior of the RCS during hypothetical meltdown accidents. This model is a modification and further development of the previously published TRAP-LOCA(I) code developed for analysis of fission product transport and deposition in a terminated loss-of-coolant accident and the TRAP-MELT (2) code described i previous manual.

f DESCRIPTION OF THE MODEL

[

\\

[

TRAP-MELT 2 considers a system of up to 10 control volumes that can be connected by fluid flow in an arbitrary way.

In each control volume a transported species can reside on at least two carriers either in particle or vapor form. Combining the phase with the concept of carrier, one can describe four states in which the species may reside: suspended-molecular, suspended-particle, deposited-molecular, and deposited-particle. A fifth state, surface-reacted, is used to describe the vapors which have reacted with RCS surfaces and are not considered to be subject to reevaporization.

o 2

Transport Rate Equations l}adionuclide transport can occur among the states of an individual control volume or between certain states of different control volumes if these are connected by fluid flow. The former types of transport are generally limited by molecular effects and are modeled and correlated in the code itself.

They are identified by the letter S in the following. Transport of fission products be, tween control volumes is assumed to occur in conjunction with fluid transport. This transport is imposed on the code by time-dependent thermal-hydraulic data read into the code in the subroutine INPUT and is identified in the following by the letter F.

It is important to consider the types of flow or extent of mixing expected and to specify criteria for their evaluation. Transvarse mixing is approy' by turbulent or convective flow. Longitudinal mixing generally does noi.

.;ur and is only approximated provided fractional deposition within a control volume is small. This criterion can be quantified for the si:nple situation of a single control volume in which only particle deposition with deposition velocity, vd, occurs. Then analysis of the homogeneously mixed case gives at steady state:

L=

1+Ad d V

(1)

\\ V) where n=

final particle concentration initial particle concentration n =

g v=

flow velocity Ad= deposition area cross flow area; A

=

c where the more accurate differential flow analysis gives, again for steady state:

(2)

P._.. e-(A /A )(V /v) e d c d

o The two expressions agree approximately provided

P

~

t O

3 A V /A v u 1 (3) dd c If one defjnes Tf E L/v = residence time for flow Td E V/A Vd d = residence time for deposition, where L = length of volume along flow direction V = volume, then the criterion that the completely mixed control volume approach used in TRAP-MELT 2 be adequate is

[T (4) u 1, d

and the criterion that steady state be reached is

( b + b)-1 (5) t T

'f d

Based on considerations of the above criteria, it is assumed in TRAP-MELT 2 that a given RCS can be subdivided into a sufficient number of control volumes that the transported species in each of these is expected to be well mixed.

It is further assumed that the transport rates of,,any species between states of a given control volume are proportional to the amount of the species in the state from which transport occurs. This latter assumption is equivalent to the concept of a mass transfer coefficient or deposition velocity.

Working with the mass of a given species rather than its concentration, since mass is conserved and consequently allows a more symmetrical treatment, the underlying transport equations of the code are:

k k

k dM im

bk E

s g

in in dt im + n/m I

8 M

m m

n/m

'r o

4 i

I f

M

+ jfj jm jm a

k dp M

(6)

I im im jjj where Mf, = mass of species k in volume i and state m

'k source rate of species k in volume i and state m S jm =

"B transfer coefficient for transport of species k in volume i m=

from state m to state n F.im = transfer coefficient for transport of fission product in state m from volume i to volume J.

Equation (6) may be rewritten as:

k dM mk k

i k

d n/m I" + jfi jm jm

3 I"

+Ef,Mf,,

where k

j E,= -[nfm "g'M k

I

, 7 pim

9 jfi Ifmsignifiesasurfacestate,"Bfm represents a mass release rate P; if m signifiesavolumestate,"Bfm represents a deposition velocity, v '

d multiplied by the area available for deposition, A, and divided by the j

volume, V, of the control volume. Thus, j

A m = volume state (8)

"sf,=v(m.n1,k) d

= P(m.n,1,k) m = surface state.

e

Ne 5

Bcth vd and P are, in general, strongly dependent on the thermal-hydraulic conditions existing in the given control volume. Since these in turn are time i

dependent,'vd and P are themselves functions of time. This time dependence places conditions on the technique used in solving Equation (6). These are considered in the subsequent section.

To permit flexibility in transport analyses of a variety of systems, the 8 coefficients are developed in the aerosol package and in subroutine BETV, discussed in the section entitled "Intravolume Mass Transfer". A separate subroutine, FF, is reserved for the development of the transfer coefficients, F, for transport between volumes. This subroutine is discussed in the section entitled "Intervolume Mass Transfer".

TRAP-MELT 2 does not account for chemical reaction kinetics. This implies that Equation (6) separates with respect to explicit dependence on k.

Implicitly, coupling with respect to k remains through joint radionuclide trans-port on mixed aerosol particles. This coupling can, however, be accounted for by simultaneous time translation of the set of Equation (6) for each k for each time step. For simplicity, the superscript k can therefore be dropped in the following.

The elements " Sin 'F),of Equation (6) can then be combined in a two-dimensional matrix A such that Equation (6) can formally be written h = S + AM.

(9) whereSandMhavebeenmappedintoone-dimensionalmatricesorvebtors.

The 0

elements of A are developed in the subroutine MATRIX.

Solution Technique The system of first order differential equations that results from consideration of the above listed mechanisms is conveniently split into three classes from considerattons of stiffness as well as linearity. Most of the deposition mechanisms (transfer from suspended to deposited states) are first order in the concentration of the species. They constitute the first class, whose transport scheme can be w itten in the form of Equation (9). Since all deposition terms are taken as first order, M is independent of A and depends, o

with S, on time only.

It is thus possible to solve Equation (9) as a set of first order differential equations with constant coefficients by standard

X

~

o 6

techniques. This is done in TRAP-MELT 2 for the class of linear mechanisms.

Condensation and evaporation, which have a much shorter time constant than the linear propesses, constitute the second class and are treated outside this framework but in parallel to it, as is particle agglomeration, which consti-tutes the third class of mechanisms in the TRAP-MELT 2 code.

The philosophy of this parallel treatment is as follows: Equation set (9) is taken as the master time translation operation of the overall system.

Time stepping is adjusted so that S and M change little over a time step and that the time step does not exceed one-third the smallest flow residence time for any control volume. The latter assures that the system does not translate excessively between couplings to the other two classes of mechanisms.

In addition, the characteristic agglomeration time for the aerosol in each volume is evaluated and compared to the master time step. If the former is short compared to thc latter, the master time step is appropriately reduced.

At the beginning of each time step, phase transitions of the species are effected by examining each control volume in turn and solving the molecular mass transport equations for vapor transport among the gas phase, particles, and wall surfaces. Because of the low heats of vaporization of the species in question, this is done isothermally. Redistribution of the vapor phase occurs in a time small compared to the master time step and therefore essentially decouples from the other processes considered. This justifies the time pa'al-r 1el solution treatment in most cases of interest.

Once redistribution of the vapor phase has been effected, its effect on the existing particle size distribution in each control volume is calculated 4

by assuming each size class to gain (or lose) mass in proportion to the rate of vapor transfer to (from) that size class. Conservation of number for each size class then dictates redistribution among, in general, two contiguous size classes with distribution among these determined by mass conservation.

At the end of a time step, the particle size distribution in each volume is reevaluated over that time step as a consequence of possible particle agglomeration, sources, and flow terms.

The approximations inherent in this parallel treatment are minimized by relegating mass redistribution and conservation to the master Equation (9)

(except for redistribution due to phase changes). Agglomeration and particle evaporation / condensation serve only to modify the particle size distribution and therefore affect particle deposition indirectly through mass distribution

=

7 averaged deposition velocities. Thus the aerosol portions of the problem are solved (over a master time step) completely in parallel to Equation (9), using all sources', flow terms, and particle removal terms evaluated for each size class considered. The resultant distribution is used to evaluate average particle deposition terms for use in the master equation only. Similarly, reevaluation of the particle size distribution due to phase change affects these average deposition terms only.

The sets of differential equations described above are solved using a Runge-Kutta-Verner fifth and sixth order method for the solution. TRAP-MELT 2 utilizes the subroutine DVERK(3) which is contained in the International Mathematics and Statistics Library (IMSL). This library is generally available at most computer installations, but other differential equation solver packages should work in this application where IMSL is not available.

MODEL FEATURES Intervolume Mass Transfer Transport of species between volumes is assumed to occur solely by convection and therefore occurs only for the states suspended-molecular and suspended-particle.

Thermal-hydraulic data and the gas mass flow rates and compositions I4) are read into the code. These are at present typically taken from MERGE code calculations.

Since each control volume is assumed to be well mixed, the rate of transport of suspended species out of a volume is just the fractional rate of change of mass of the carrier gas:

j

,FXSfi.j)

(10) p o(1)VD) im s

where l

FXS(1,j) = gas mass flow rate from volume i to volume j l

3(1) = density of gas in volume i 9

V(1) = volume of control volume i.

(

p

~

8 I_n,travolume Mass Transfer Intravolume mass transfer coefficients (8's) are developed in the subroutines BETV and REMOVE.

Intravolume mass transfer that cannot readily be described by mass transfer coefficients is relegated to the subroutine ADH0C.

At present, this routine contains interphase mass transfer due to condensation and evaporation.

Models in BETV and REMOVE All deposition processes currently considered in BETV and REMOVE are modeled as rate controlled by transport across a concentration boundary layer whose thickness is very much less than the equi ~alent diameter of the RCS com-v ponent cois'idered. Such a situation exists for turbulent flow.

It then is useful to employ the concept of a mass transfer coefficient, or, equivalently, a tieposition velocity across the boundary layer.

For laminar flow the concept of a boundary layer breaks down. Trans-port through the fluid to wall surfaces bounding the flow is then continuous and the result of mass or temperature gradients. Such transport has been studied extensively and can be adequately modeled. By manipulating the corres-ponding analytical expressions, it is possible to determine a fictitious depo-sition velocity for deposition from laminar flow also. This is done in REMOVE to preserve a unified approach.

Much of the predicted flow in the primary system for the most impor-tant meltdown scenarios is of a pseudo-laminar nature. That is, the predicted Reynolds numbers indicate laminar flow, but the accompanying large Grashof numbers suggest that convective mixing occurs.

In addition, the usually small ratio of component length to diameter prevents truly laminar flow from establishing itself. Where large wall-to-fluid temeprature differences exist, the hydrodynamic boundary layer thickness may be estimated from Reynolds number correlations employing an equivalent Reynolds number:

Re,q = ( h (11) t for Grashof number 7

Gr 2 5 x 10.

ns; i

9 BETV and REMOVE consider the following mechanisms for deposition on surfaces:-

e' Vapor reaction with surfaces (BETV) e Supermicron particle deposition from fully developed turbulent flow; wall surface temperature equals fluid temperature e Submicron particle deposition from fully

' developed turbulent flow; wall surface temperature equals fluid temperature e Particle deposition from laminar flow; wall surface temperature equals fluid temperature e Particle deposition due to thermophoresis.

e Particle deposition due to gravitational sedimentation.

Generally, no significant error is incurred in assuming these mechanisms to act independently since, in fact, a particular one will usually dominate.

It sh'ould be noted in particular that thermophoretic effects can either enhance or retard deposition.

In the following, each of the mechanisms listed above is described in more detail.

Vapor Sorption. The only available data for sorption of 12 on stain-lass steel from steam is that determined s:perimentally by Genco, et al(5)

They found that for surface temperatures in the range 150-550 C, the deposition is velocity, vd' IOP I2 4 U U, M

d = 9.0 x 10 e

v where R (1.987 cal /mol K) is the gas constant T is the absolute temperature is in cm/sec. This expression is incorporated in in degrees Kelvin, and vd It indicates that surface deposition of iodine is controlled by TRAP-MELT 2.

chemical kinetics rather than bulk or boundary layer transport. Note that the temperature range for this expression does not extend to the 1000 C predictea for some meltdown scenarios. At such temperatures, other species can be expected to exist in vapor fonn and similar data for these must be developed.

Estimates of deposition velocities for the other vapor species consi-dered in the code have been incorporated in tha calculations performed in BETV also. Due to the difficulty in performing the experiments required to r.easure

o 10 surface reaction rates relevant to RCS accident cenditions, the available data are sparse and somewhat imprecise. Nevertheless they do suffice to permit order of rpagnitude estimates of deposition velocities to be made. Based upon results reported by Elrick and Sallach(6) and Sallach, et al(7), one can estimate.ieposition velocities for Cs0H on stainless steel to be on the order of 0.01 c./s and for Te, 1.0 cm/s. The deposition velocity for Csl vapor on RCS surtms appears at this time to be negligible in comparison with other potential removal mechanisms.

It is recognized that these estimated values are not precise, and that the simplification of considering the process to be irreversible may not be entirely warranted. At this time more detailed experi-mental studies are beginning to yield results and it is hoped that these will be useful for strengthening the treatment of this process in the code.

t Particle Deposition from Turbulent Flow. There are two contributions to the deposition of particles from turbulent flow: one due to diffusion from the flow, and one due to particle inertia in the flow. Deposition due to particle diffusion to the surfc.ce was investigated by Davies (0), who obtained the expression:

(Sc)-2/3 (13) y

\\

[14.5 II+*)2 + b arc tan 24-1,

w in g

g 6dj

(

l-4+4 where (V/u*) = dimensionless particle deposition V+d =locity due to diffusion ve Sc = (v/DJ = Schmidt number u* = friction velocity (f/2)1/2 y V = average fluid velocity f = Fanning friction factor D = diffusion coefficient v = kinematic viscosity

& = 1/(2.9 3 @/v).

The inertial contribution to particle deposition fror tu'rbulent flow was investigated by Friedlander and Johnstone(9) who arrived at the following expressions, valid for three different ranges of the dimensionless particle relaxation time:

11 Y+1 " ( 1

,(1525 -50.6)\\

g i

0.812, j

where V,4 = dimensionless particle deposition velocity due to inertial impaction x, = dimensionless particle relaxation time (tu*2fy) 2

= particle relaxation time (o d C/180)

T pp o = particle density p

dp = particle diameter C = slip correction factor n = gas viscosity, 1

5.04

+i

'_.L-- + 5 i n

- 0.959 - 13.73 g

0.18t, o

for 5.6 < x, < 33.3 and l

V,9 for T, > 33.3 (16)

=

Gieseke, et al(10) combined the expression for low T,with the diffusive deposition term of Davies and an additive term to correlate experi-mental data obtained in a number of laboratories and produced the expression:

V+t " Y+d

Y+1 + 2x10-8 Re (17) where Re is the Reynolds number characterizing the flow. The REMOVE subroutine utilizes the expression of V,$ appropriate for the computed value of T, in the simulation and incorporates it in the above expression for V+t*

Particle Deposition from Laminar Flow. For strictly laminar flow in simple geometries, particle deposition for whatever particle size can be calcu-lated analytically to good accuracy. This circumstance is, in fact, used in devices to measure particle size. Commonly used expressions for the fractional

g 12 number of particles deposited from flow in circular pipes are those of Gormley andKennedy(III:

= 0.8191 e-7.314h + 0.0975 e-44.6h + 0.0325 e-114h (18) for h > 0.0156, and h=1-4.07h2/3 + 2.4h + 0.446h4/3 (19) o for h < 0.0156, i

where N=

number of particles that reach the end of the pipe of length L number of particles that enter the pipe (distributed uniformly N

=

8' over the cross section) 2 h=

LD/2 va a=

pipe radius.

A fictitious deposition velocity for an equivalent, completely mixed system can be derived from these expressions as follows. Letting n be the concentra-tion of particles in the completely mixed volume and n the concentration of g

particles entering the volume, the deposition velocity, v, across a boundary d

layer is defined by the expression h=-vd V "'

where surface area A

=

i volume V

=

for y /v u 1, therefore, d

"*~V n

(21) n - n, = -vd d

e

13 or d=

(

- 1) y= (

- 1) v.

(22) v This expression is used in REMOVE.

Thermophoretic Deposition. An adequate expression for particle deposition due to thermal gradients at wall surfaces is that derived theoreti-cally by Brock (12)

His expression is known to deviate by as much as a factor of two from some experimental data, but was deemed adequate for inclusion in REMOVE since larger uncertainties may exist in requisite thermal-hydraulic data. Brock's expression for the deposition velocity is:

I d"~~N v

wh,ere t

VT = the temperature gradient at the wall surface l

T=

absolute temperature in the vicinity of the wall k /k + C Kn

)

q g t

(24) l

" l + 3C,Kn 1 + 2k n + 2C Kn g p t

I and I

= momentum and temperature accomodation coefficients C,,Ct k /k = ratio of the thermal conductivity of the gas g p to that of the particle Kn = Knudsen number of the particle C = 1 + A Kn + Q Kn e

, the empirical Knudsen-Weber correc-

-b/Kn tion to the mobility of the particle.

l l

REMOVE uses the Millikan oil drop values for these empirical parameters:

A = 1.25 Q = 0.42 b = 0.87 I

Note that for wall surfaces hotter than the fluid medium, particles will experience a repulsive force away from the surface.

Present input data on the thermal-hydraulic conditions to be expected in the reactor primary system for a given accident scenario do not include the

6 14 temperature gradient,vT, at wall surfaces.

In keeping with the present very approximate data on both wall surface and steam temperatures as well as the nature of the steam flow, VT is therefore calculated in subroutine FLUID using the Dittus-Boelter correlation of the Nusselt number with Reynolds number:

Nu = 0.021 Re.8 (25) 0 For Re, the larger of the equivalent Reynolds number as given by Equation (11),

and the actual Reynolds number is used.

Models in ADH0C Mass Transfer Involving #hase Changes. Interphase mass transfer for a given radionuclide species in a given volume can be described by the follow-ing differsiltial equations:

Ak dC (k

-C,s)-

kC P)

(26)

"~

s dt V

s dM,= A,kg(C -Cg) 5 (27) dt 3

i dM s

(28)

"#kP p (C -Cp) dt 3

i where

= concentration of the vapor suspended C

=

3 M = total mass of the vapor suspended s

M = total mass of vapor condensed on walls g

M = total mass of vapor condensed on aerosol particles p

CS = equilibrium vapor concentration of the species at the temperature of the wall surf aces (assumed independent ofpressure) f i

L 15 CS = equilibrium vapor concentration of the species at the E

temperature of the gas (assumed independent of pressure and particle surface curvature) i A, = area of wall surfaces A = surface area of aerosol particles p

k" = mass transfer coefficient for transfer between bulk gas flow and wall surfaces-gas interface k = mass transfer coefficient for transfer between P

bulk gas flow and particle surface-gas interface.

These equations have the solutions:

M,= M,, + A,k,(E - Cg )at A,k,(E - Cso)

I -,-at) gg) s M

=M

+ A k (E - C *)at - A k (E - Cso)-

(1 - e

)

(30) p pg pp p

pp (31)

-(

-Cso) e C

=

s where a=hA,k +Ak) pp 1, A,k,C,s + A,k C,s p

a Ak +Ac g

pp C

= concentration of vapor in gas phase at beginning of so time step total aass of the species on wall surfaces at beginning M,g = of time step M

= total mass of the species condensed on aerosol particles E

at beginning of time step at = length of time step.

b

_=.

i 16 I

Equations (29-31) are in the form of the general transport rate equa-tions (Equation 6) if the inhomogeneous terms are treated as a fictitious sourceterpSf,.Theyareneverthelesstreatedseparatelyfromthetransport equations because of two circumstances. First, the interface equilibrium vapor concentrations are step functions of the masses M,, M, and the Equations (29-p

31) are therefore in reality nonlinear. While the nonlinearity can be removed with sufficient accuracy, the step functior., discontinuity cannot be readily handled by the integration scheme of MATSA. Second, phase changes are, in general, much more rapid phenomena than either surface reactions or particle deposition. Inclusion of these phase changes in the general transport rate equations would therefore introduce stiffness with its consequent penalty of increased computation time.

S

,,The step function property of C, (and similarly, Cg), which is such that it equals zero when M, = 0, is treated in the following way: the Equa-tions (29-31) are evaluated over the time step, at, dictated by solution of the general transport equations.

If either M, or M become negative after p

this time step, the initial conditions are altered to reflect this result, the corresponding carrier is eliminated for the duration of that time step, and the equations are reevaluated. Thus, for example, if the solution of Equations (29-31) yields M, < 0, the mass of the given nuclide deposited on system surfaces at the beginning of the time step is distributed equally between the gas and particle carriers. This new distribution of nuclide taass is then taken as the initial condition and the following equations solved:

dC*

A ky (C, - C )

(32) 5 dt p

i i

dM "A

I p)

(33) dt pp s

These have the solutions:

s s

pp C

=C -(C -Cso)e (34) s p

p I

i s

pp M

=M

-V(C -Cso)(1.,

).

(35) p pg i

l l

a-17 To be consistent with the level of accuracy for other models within the TRAP-MELT 2 code and with the accuracy of the available input data, elemen-tary corre)ations of the mass transfer coefficients, k,and k, are sufficient p

and have been used. The aerosol particles are assumed spherical and essentially at rest with respect to the flowing gas. Furthermore, each species residing on an aerosol particle is assumed to be independent of any other (no chemical or physical reaction), and all particles in a given volume are assumed to have the same chemical composition. Then, k = D_

(36) p r

where diffusivity of the species in steam D

=

radius of aerosol particle.

r =

For k,, turbulent pipe flow is assumed and the Sherwood number, Sh, is taken to be Sc.33 (37) 0 Sh = 0.023 Re.83 0

which is analogous to the expression for the Nusselt number stated earlier (Equation 25). Sc is the Schmidt number for the system.

I Sedimentation. For particle Reynolds numbers less than one, the Stokes settling velocity is given by:

=fr pgB (38) 3 V

p g

where B is the particle mobility (C/6snr). For large particles, however, this equation no longer holds and may in fact be off by as much as a factor of two.

Therefore, empirical data (13) are used in the form of a correction factor to the above equation for particles whose Reynolds number is 1 < Re < 1260. For Reynolds numbers in excess of this value, no empirical values of V are known.

g As a compromise, the correction value for Re = 1259 is used here as well.

To account for particle nonsphericity, it is assumed that a correc-tion factor, f, exists such that F0 (39) fC

=

wr,2 p y z

2

\\

1 I

g 18 where y=

collision shape factor CF= Fanning friction factor for spheres FD= actual drag force on particle F = 6mxr D

and 2

A gr

2 p

Yg 9 nx in the Stokes regime, one can determine f to be equal to X/Y.

The collision shape factor, Y, was initially introduced (14) to account for a collision cross-section of nonspherical particles that depends on a colli.-sion radius, r, different than r.

Thus rc was taken as proportional c

The val'ue of Y has never been measured, but approximate values to r: rc = Yr.

have been inferred by backfitting computer codes. Unfortunately, Y and X have been shown to be sensitive code parameters (15},

To avoid the introduction of further parameters of comparable sensi-tivity, Y is also used as a proportionality factor between some geometric particle radius, r, of an agglomerated, nonspherical, particle and its mass equivalent radius: r = Yr. Then all data correlated on spherical particles e

is written in terms of Yr.

e Coagulation The TRAP-MELT 2 code accounts for aerosol agglomeration due to Brown-ian, gravitational, and turbulent mechanisms, each of which is described below.

The treatment of these processes is taken directly from the QUICK code (16) which has undergone significant testing against experimental results.

(1) Brownian Coagulation This coagulation mechanism is due to the random Browniap motion of the particles and the form of the coagulation kernel is the standard form originally derived by von Smoluchowski(III:

19 K(rr')=fy [h + h)h (r + r')

(M)

B N

s (ii) Gravitational Coagulation 2ngo y2[2

\\

7, - r, / (r, + r )2 D

K (r F ) = c(r,r')

G gnx g

\\

where c(r,r') = collision efficiency.

The collision efficiency can be viewed as that factor which results in correct prediction of particle number concentration as a function of time and particle size. Most recent experimental and theoretical investigations into this factor (18) have yielded data tables that have been employed in the QUICK code on large scale sodium fire simulation runs. The results of these runs are surprisingly similar to ones using the simple expression f

h2 c(r,r')=1.5 l

(4I) k r'I r

where r' refers to the larger particle. Expression (40) strictly holds for inertialess particles and r' n r only.

Its use for all values of r' and r, however, yields satisfactory agreement with simulation experiments to date.

(iii) Turbulent Coagulation i

The two most widely used theoretical treatments of turbulent coagula-tion are probably those of Saffman and Turner (19) and Levich(20). Both are based on the hypothesis that microscale turbulence is essentially isotropic and that the particles are smaller than the microscale. Both also invoke the same conceptualization of the turbulent collision process: relative particle motion due to entrainment in a variable fluid velocity field and relative particle motion due to differences in inertial response to fluid acceleration.

Therefore, it is not surprising that since quantification of isotropic micro-scale turbulence is based on dimensional analysis, the two approaches result in identical expressions except for multiplicative constants. By the same

20 token, these multiplicative constants must be considered indeterminate until experimentally determined.

The expression used for turbulent coagulation is based on Saffman and Turner's, including their multiplicative constants. Their expressions have been modified to include a collision efficiency for particle motion rela-tive to the fluid and the shape factors for non-spherical particles discussed above. While the collision efficiency for particles colliding due to their motion with a variable fluid velocity field may not be unity, no superior treatment is known. Thus 3/2 HG(r,r') = 2 M y (r,+ r')2 [cr,r')2 (t,,,)2 K

g e) ]/

(42)

+ h c(r r')2 (T,,,)2 2 +

Y (r +

e wh'ere 2r(2,D = particle relaxation time. corrected for sh t =

E = turbulent dissipation energy density.

Note that, following Saffman and Turner, the gravitational coagulation mech-anism is incorporated in K +G-T Finally, the assumption is made that K(r,r') = K (r,r') + K +G(r,r').

B T

Since Kg and K +G are of equal magnitude over a narrow particle size range T

only, this approach is not expected to result in significant error.

f

m 21 REFERENCES (1)~

Gieseke, J. A.,

P. Baybutt, H. Jordan, R. S. Denning, and R. O. Wooton (1977), " Analysis of Fission Product Transport Under Terminated LOCA Conditions", Battelle's Columbus Laboratories No. BMI-NUREG-1990.

(2)

Jordan, H., J. A. Gieseke, and P. Baybutt (1979), " TRAP-MELT User's Manual", NUREG/CR-0632, Battelle's Columbus Laboratories No. BMI-2017.

(3)

Hull, T. E., W. H. Enright, and K. R. Jackson (1976), " User's Guide for DVERK -- A Subroutine for Solving Non-Stiff ODE's", TR No. 100, Depart-ment of Computer Science, University of Toronto, October, 1976.

(4)

Freeman-Kelly, R. G. and R. G. Jung (1984), "A_ User's Guide for MERGE",

NUREG/CR-4172, Battelle's Columbus Laboratories No. BMI-2121.

(5)

Genco, J. M., W. E. Berry, H. S. Rosenberg, and D. L. Morrison, " Fission Product Deposition and Its Enhancement under Reactor Accident. Conditions:

Deposition on Primary-System Surfaces", Battelle Columbus Laboratories No.BMI-1863(March,1969).

(6)

Elrick, R. M. and R. A. Sallach (1983), " Fission Product Chemistry in the Primary System", Proceedings of the International Meeting on Light Water Reactor Severe Accident Evaluation, Vol. I, p 4.6-1, 4.6-5, ANS publication number 700085.

(7)

R. A. Sallach, C. J. Greenholt, and A. R. Taig (1983), " Chemical Inter-actions of Tellurium vapors with reactor materials", NUREG/CR-2921, Sandia National Laboratories No. SAND 82-1145.

(8)

Davies, C. N. (1966), Aerosol Science, Academic Press, London, pp 557-562.

(9)

Friedlander, S. K. and H. F. Johnstone (1957), " Deposition of Suspended Particles from Turbulent Gas Streams" Ind. Engr. Chem., 49_, 1151.

(10)

J. A. Gieseke, K. W. Lee, and M. A. Goldenberg (1980), " Measurement of Aerosol Deposition Rates in Turbulent Flows", NUREG/CR-1264, Battelle Columbus Laboratories No. BMI-2041.

(11) Gormley, P. G. and M. Kennedy (1949), " Diffusion from a Stream Flowing Through a Cylindrical Tube", Proc. Royal Irish Acad. A52, 163.

(12) Brock, J. R. (1962), "On the Theory of Thermal Forces Acting on Aerosol Particles",J.ColloidScience,J7,,768.

7 (13) Fuchs, N. A. (1964), The Mechanics of Aerosols, Pergamon Press, Oxford, England.

(14) Jordan, H., W. Schikarski, and H. Wild (1974), "Nukleare Aerosole im Geschlossenen System", KfK Report No. 1989.

rm 22 REFERENCES (Continued)

(15)

Lee,'K. W., J. A. Gieseke, and L. D. Reed (1978), " Sensitivity Analysis of the HAARM-3 Code", NUREG/CR-0527, Battelle's Columbus Laboratories No. BMI-2008.

(16) Jordan.

H., P. M. Schumacher, and J. A. Gieseke (1981), " QUICK User's Manual" NUREG/CR-2105, Battelle's Columbus Laboratories No. BMI-2082.

(17) -von Smoluchowski, M. (1917), " Mathematical Theory of the Kinetics of the Coagulation of Colloidal Solutions", Z. Phys. Chem., 92, 129.

(18) Pertmer, G. and S. K. Loyalka (1980), " Gravitational Collision Efficiency of Post-HCDA LMFBR Aerosols: Spherical Particles", Nuclear Technology, 47, 70.

(19) Saffntan, P. G. and J. S. Turner (1956), "On the Collision of Drops in Turtiulent Clouds", J. Fluid Mechanics, 1, 16.

(20) Levich, V. G. (1962), Physicochemical Hydrodynamics, Prentice Hall.

Inc., New York, New York.

t

3

^

23 FLOW CHART AND BRIEF DESCRIPTION OF SUBROUTINES In the following, a flow chart (Figure 1) indicating the main logic of TRAP-MELT 2 is given and each subroutine is described briefly.

It should be emphasized that the general dynamics of the transport and deposition in an LWR primary system during a severe accident have been divided into three categories, each with its own response time. These are:

phase transitions (treated in ADH0C), particle agglomeration (treated in the QUICK package, C0 CALL), and vapor and particle deposition and flow (treated in BETV, FF, MATRIX, and MATSA). The response times are such that it appears plausible to treat phase transitions with the remaining system at pseudo steady state and again to treat agglomeration with flow and deposition at pseudo steady state.

The solutien to the total dynamics of the system is therefore carried out sequentially rather than simultaneously by first performing phase change transitions, then flow and deposition transitions over a time step during which agglomeration causes only small changes in particle size parameters. Finally, the size distribution is changed by agglomeration, taking flow, deposition and source of particles into account.

INPUT All input to TRAP-MELT is read into the code in INPUT in engineering units and immediately written out in those units. These are then converted to the working cgs-Kelvin units of the code, except for the particle radius (pm),

particle geometric mean radius (pm), and particle geometric mean radius cubed 3

(pm ),

INPUT is subdivided by the subheadings:

o Control Data and Program Constants e Sensitivity Multipliers e Geometric Data e Thermal Hydraulic Data e Initial Conditions e Source Data.

24

( 5 TART )

e VZERO INPUT '

r set vector I

DECODE to aero Centrol Input parameters Package 8

il riew

-e-CFORM connections

$ggreg,of masses by e

species Sensitivity multipliers EMovt Access 0

storage array I

it T

1 gaggy

$ roam 5torage of scarce by I

species Nuclide 3

data

(

tti Write plot file readers h

C05tf Initialise aerosol package 4

GDF Calculate geomtric factors h

I Tais inittai t*me step f

h 75ftp Calculate timestep V

\\

Y particle 5pApf c

FtqDY "g

Determine Interpolate aerosol source N

distribution O

FIGURE la.

FLOW CHART OF TRAP-MELT 2 CODE BY SUBROUTINES

e 25 7

troge M EM0vt 3 Astrieve mass fee this species 6

170s

$we sevece este over seeties for CKM h

utg RFV tatry point to Celtviste gret e desenttien sonstr.Ct teetten volettttes steepeent fertieR ef A getria

- Fl@f NVf TN C&f A

$4PO Save spet'et Detemae DeteMae Ceafeatret10Pt bef8P9 (Re*41 Rydraulit Steen et*8f tf C8* Sale t t eal CSP 8ttioRS et et tesserefo e r

ev8Derttie4 Evffeat time 4*f Drelle tr yv!ta0 acaot Cat tel ste teaceatetten/

IUC"d pe,fere spettet ev ete rSt'e#

ggettfft tende*latte8/

e'fectl eveserstir talculatirl e

Fatyt

$ ave 50et'40 ge.teatrat'ePS SfteP teade*lat'r/

eveterSt'OR w'ta F4Cvt few stes tae C0ffF 8e.ll.tre*194Ft w

g,g g, e.tieas gq pp eg.gggt CalcuI4te ' ell e

g

,gagggn gggggy treal9ert GIettativel F4Cvf 8

l F40vt lave toestes Ce*ce*t.'St.' eP S.8't#'

l

.. i,.. et I

t.,

i,.

Co..co.t.e.. e..n.

c,e. et,e,

..w CXM V

CL*At 0.,t,s, u,t, 0.t..t..i..

e,e

.ietie.t.

.te i

l n

all G

..et i e.

t i

I O

j FIGURE la.

(Continued) 4

, +,,,.

,,, ~

26 s

lf C0 CALL Perform aerosol calculatices (see Figure la for a detailed description of C0 CALL)

UTPUT y

called on this[stea CDARt 7

Entry potat in OWNT N

Output particulate

~

informtion time 1most goe y

=

Cutorr i

"=,

syise. routine to save current i

Problem job status for g

comeisted e future restart

?

.. ~

i Y

11 c

stee

)

l l

L i

l I

i f

FIGURE la.

(Continued) l L

t 27 Call from TRAPMLT s

Initfalfze local variables if PSOURCE Calculate the aerosol particle source distribution

\\t c

r 5tfitt N5T0G Interpolate settling Calculate non 5toaestan velocities /Reynolds settling velocittes for number table aerosol particles U

REMOVE Calculate the aerosol l

removal rate for each removal mechanism 11 glRN

(

y Congulation Evaluate coagulation allowed k' '"'

N C

1l Determine aerosol flow to and from current volume c

O!FFUN U

Ovtat Evaluate aerosol Y

Advance aerosol arh equation dertvatives equation solution aerosol change N

q:

tulerian integration of aerosol equations Estt@

Add another d

site class to Y

another site efid of distribution class N

Il FLOW CHART OF AEROSOL PACKAGE IN TRAP-MELT 2 CODE FIGURE lb.

.L 28 s

G U

Isormalise aerosol mass versus MATSA mess if D100 Sun temsel reaeval by mecha91sm

'I Aecalculate deposition velocities if Let size cPennel 0A08 nsignifican

?

(11miratennoi last size en ti c Cnet.rnto T RAM 8LT s

FIGURE lb.

(Continued)

41 29 ADH0C ADHOCsolvesthemasstransferequationsforvapor-to-liquidtranst-tions of the species:

1. CsI, Cs0H, and Te over the time step determined by 2

TSTEP. The change of particle radius due to condensation and evaporation of a nuclide species is also calculated in ADH0C.

ARRAY ARRAY is used by INPUT to read the thermal hydraulic input data.

BETV The deposition velocity elements are developed in BETV which is organized so that new expressions can readily be inserted as they become avail-able.

CDIF The mass transport derivatives for each volume are calculated by CDIF. The derivatives are used by the DVERK differential equation solver package to calculate mass transport for MATSA.

CFORM The nuclide mass of each state of the system is stored in the vectors C and CO. C is a temporary storage employed in MATSA. To conserve computer core storage space, C and C0 are overwritten as each new species is considered.

CFORM is used to transfer each species dependent image of C0 to external core storage and to retrieve these images as needed.

C0 CALL C0 CALL serves as the interface to the aerosol coagulation package which was derived from the QUICK code. C0 CALL performs the aerosol calculations

30 for each control volume in turn for every time step. The DVERK differential equation solver package in the IHSL Math Library is used to take the actual time step., C0 CALL transfers the atmosphere conditions (pressure, temperature, etc.) from the TRAP-MELT storage locations into the variables used by the aerosol package. The flows into and out of each control volume are calculated so that the effects of interconnected flow can be considered.

C0 CALL examines the derivatives of the aerosol number concentration to find the most rapidly changing size channel.

If the time step is small for this channel, then C0 CALL uses an Eulerian method for the time step; otherwise, the DVERK routine is used.

C0 CALL monitors the last channels in the aerosol distribution to determine when additional channels should be added to the distribution or when the large,, size channels are no longer needed. The aerosol distribution is normalized to the total aerosol mass developed in MATSA so that both sections of the code are working with the same aerosol mass. The deposition velocities for the aerosol removal mechanisms are also calculated in C0 CALL.

COSET COSET is partsof the aerosol package.

It calls the routines needed to initialize che aerosol calculations.

DEPO DEP0 is part of the aerosol package. It calculates the removal rate for aerosol for all the removal mechanisms during each time step.

DIFFUN DIFFUN is part of the aerosol package. The rate of change of the number of particles in each size interval, required by the DVERK routine, is computed by subroutine DIFFUN. The first portion of the routine includes the effects of the source and removal terms. The second portion of the routine handles coagulation by two particle collisions.

FV

~

s, 31 DIFFUN uses the next to last and the last channel to accumulate the number and pass, respectively, of particles which grow beyond the range of particle size being considered. The number of channels considered is NS-1.

(SeesPSOURCE for a discussion of the development of NS.) As the particle size distribution widens, NS is increased to include larger particles in the system of equations.

(See EXTEND for a description of the channel extension proce-dure.)

DROP DROP is part of the aerosol package. DROP eliminates the largest aerosol size class from the distribution when the concentration in that channel becomes insignificant.

EM'0VE EMOVE is called by CFORM and SFORM to access the mass and source data for each species.

EXTEND EXTEND is part of the aerosol package. When coagulation necessitates the inclusion of an additional channel in the distribution, subroutine EXTEND performs the required operations. NS is incremented by 1.

i ff.

IF of Equation (6). These are simply FF calculates the flow terms j

the mass flow rate of steam through junction i, j divided by the mass of steam in volume 1.

FINDY FINDY is a general linear interpolation routine for arbitrary spacing of arguments.

It is used for interpolating input tables of data.

a 32 FLUID F,luid properties, dimensionless groups, and particle-fluid properties are calculated in FLUID for all volumes for a given time. These are as follows:

e Gas velocity e Gas viscosity s

e Gas Reynolds number e The turbulent energy dissipation rate for the gas e The temperature gradient at the wall surfaces using the Dittus-Boelter correlation for the heat transfer coefficient for pipe flow together with input data on temperature differences between bulk flow and wall sur-faces

'e The friction velocity of the gas e The mean free path of the gas e The Knudsen number of an average particle s The slip correction factor for an average particle e The diffusion coefficient of an average particle.

FMOVE FMOVE transfers the contents of one vector into another..-

FRPATH FRPATH is called by FLUID to calculate the mean free path of the gas.

GDF This subroutine determines the geometry dependent factors of the is matrix elements "6 ofEquation(6). These are in the form A /V where Ad d

the deposition surface area and V is the volume of the control volume consi-dered.

e I

33 i

MESH RESH is part of the aerosol package.

It calculates the boundaries of the particle size channels and the effective particle radius for each size range used by the aerosol package to determine the aerosol behavior.

l NST0KE NST0KE is part of the aerosol package. It applies a correction for non-Stokesian behavior of large particles. SETTLE is used to determine the non-Stokesian settling velocity.

PSOURCE PSOURCE is part of the aerosol package. It calculates the aerosol particle source size distribution assuming a log normal distribution. The particle source distribution parameters are allowed to change witii time, as dictated by the user.

REMOVE REMOVE is part of the aerosol package. The particle removal rates for the various removal mechanisms are calculated here.

SETTLE SETTLE is part of the aerosol package.

It determines the non--

Stokesian settling velocity of the aerosol particles.

INIT INIT is part of the aerosol package.

It sets the control parameters of the aerosol package and zeros the aerosol storage arrays.

A 34 IUPACK

,IUPACK is used to unpack binary coded words.

KERN KERN is part of the aerosol package.

It calculates the aerosol col-lision kernel for Brownian, gravitational, and turbulent coagulation.

MATRIX MATRIX sets up the matrix elements of the Matrix A in Equation (9).

MATSA MATSA calls the DVERK package to advance the solution of the mass transport equation by the time step developed in TSTEP.

RET RET writes the headers for the species retention plot files.

SFORM The table of mass source rate data as a function of time for each volume is stored in the fields SE and SET. To conserve computer core space, these fields are overwritten for each new species considered. SFORM is used to transfer each species-dependent image of SE and SET to external core storage and to retrieve these as needed.

SOURCE SOURCE is used to calculate the source rate, S, for theemass trans-port in a given volume at a given time using the interpolation routine FINDY on the source data tables SE and SET.

nn 35 SPART I

hPARTutilizestheinputsourceparticledistributionparameters PSE(I,J) and corresponding times PSET(I,J) for each volume and determines the distribution parameters PS(L) for each volume source at time t.

SPSCALC SPSCALC supplies ADHOC with the species specific vapor pressure l

information needed for the condensation / evaporation calculations.

RHOMU RHOMU calculates the density and viscosity of the gas mixture.

STOR l

STOR is a general vector sunmation routine.

It sums the source rate S, over all species and stores this sum in SSTOR for use by C0 CALL.

It also sums the masses in the steam-particle state for each volume after operation l

with MATSA. This sum is stored in CSTOR.

THDATA THDATA develops the following thermal hydraulic data for a given time:

Gas mass flow rate through each junction e

e Gas temperature e Gas pressure e Gas density e Wall surface temperature.

I

7 36 TSTEP

.TSTEP develops the appropriate time step for each iteration. At present, because of the sequential solution technique employed, the time step is read in as estimated from trial runs on the criterion that transport of species per time step not proceed through more than three or four volumes.

TSTEP reevaluates the coefficient matrix and the source terms as frequently as required to limit the maximum relative change of each element to less than ETA 2, specified in the input. ETA 2 is generally chosen to be 0.1.

XDP

')(DP Is the last part of the aerosol package.

It determines the num-ber fraction of particles entering a size class as the result of a collision of particles from two smaller size classes.

VZERO VZERO sets the argument field equal to zero.

OUTPUT OUTPUT is called at DIV subdivisions of the meltdown tinie interval to be calculated. DIV is read into the code in the main program.

It prints out all parameters of interest and is discussed in detail in a separate section below.

I The subroutines DECODE, INPA. INPI, INPF, INPB, INPI8, IADD, ERROR, and OUTREC are part of an input package that permits input for TRAP-MELT to be unformatted.

The subroutine DVERX is a general purpose differential equation solver available in the IMSL library. DVERK is used to solve both the mass transport and aerosol equations.

t

,. ~.

3 37 l

INPUT TO TRAP-MELT 2 A list of input cards for TRAP-MELT 2 is schematically given In the following, the listed parameters will be described in below.

detail. Note that input to TRAP-MELT 2 is unformatted.

f DATA cards with an asterisk (*) in the first O.

KOMENT column are interpreted as coment cards used for organizing large data decks. If K0 MENT = 1, these are printed along with the rest of the input data from INPUT. A (*) card at the head of the data deck is printed back in any case. This can be used to title a run.

l If K0 MAD =1, comments are printed from ADHOC that 1.

K0 MAD give information on total evaporation of a nuclide species from either particles or walls.

i I

If NRES=1, TRAP-MELT restarts from a previously l

2.

NRES interrupted run using initial values previously stored on the NTAP files; only this and the previous card are read in.

l Central processor time (seconds) allowed the 3.

CPMAX This will problem before dumping for restart.

not halt program execution.

Divides the time interval over which the code is 4.

DIV to run into DIV equal subintervals. DUTPUT is called at the end of each subinterval.

Are read in on one card, separated by blank 5.

T,TMAX, DELTM T is the time at which to start the

, spaces.

TMAX is the time in seconds up to which problem.

DELTM is the maximum the calculation is to run.

time step to be taken per iteration. Its value

,i is discussed in the description of TSTEP.

Are read in on one card. REL is the convergence 6.

REL, ETA 1, ETA 2 criterionfortheDVERKtimejntegrationofthe 10-is recomended in master equation (MATSA).

ETA 1 is the relative change allowed most cases.

in the source rate over a source time step. ETA 2 is the relative change allowed in the matrix over a matrix time step.

7.

NK NV, NS, NDP Are read in on one card. NK is the number of species to be considered. NV is the number of control volumes considered. NS is the number of

38 states. This number must be 5 unless minor modifications in BETV are undertaken. NDP is the number of particle parameters considered. This value must be 2 at present.

8.

SN(1),....SN(NK) Are read in on one card. Each SN is the two-character name of a species (A format). Source information must appear in same order as SN values.

9.

NCC Contains the flow connections of the control volumes in binary form. Each word is placed on a new card. The first word contains all flow con-nections to the first volume.

If flow occurs to the first volume from the second volume, a 1 must appear as the second digit of the first wor'd, and so on.

10. NB,ET.

Gives the number of program control flags in BETV.

There are three of these.

11. NB Contains the control flags of BETV for each volume in binary form. Each word appears on a new card and represents the control for the volume whose number corresponds to the sequence number of the word. The first digit of a word must be 1 if vapordeposition(otherthancondensationTisto be permitted in that volume. The second digit of a word must be 1 if particle deposition is to be permitted in that volume. The third digit must be 1 if gravitational settling occurs across the fluTd flow or a 0 if settling is counter flow.

The use of 1 is ordinarily recommended.

GivesthenumberofcontrolflagsinA'Dh0C.

There

12. NH0C is only one of these at present.

13. ND Binary coded control words for ADH0C. If ND=1, condensation is permitted for the corresponding volume.

14. NOC0G Binary coded control word. The nth digit corres-ponds to the nth volume.

If coagulation is to be considered in this volume, this digit is set equaltoJ_.

15. VPM Arbitrary multiplier of all vapor pressure terms.

Can be used to measure code sensitivity to uncer-tainties in vapor pressure correlationst

16. FRM Arbitrary multiplier of the steam mass flow rates in all volumes. Can be used to measure code sen-sitivity to changes in flow rate.

v 39 l

l l

17. STM Arbitrary multiplier of surface temperatures in all volumes. Can be used to measure code sensi-l tivity to uncertainties in surface temperatures.

l

18. SRM Arbitrary multiplier of the I2 adsorption velo-city. Can be used to gauge code sensitivity to uncertainty in this parameter.

l

19. THDM Arbitrary multiplier of the thermophoretic depo-sition velocity. Can be used to measure code sensitivity to uncertainty in this expression, 1

f

20. TOM Arbitrary multiplier of the deposition velocity due to particle deposition from turbulent flow.

Can be used to gauge code sensitivity to uncer-tainty in this velocity.

21. VTM Arbitrary multiplier of the vapor mass transfer coefficients used in ADH0C. Can be used to gauge code sensitivity to uncertainty in these.

(

22. NTC0AG If equal to 1, turbulent coagulation is computed for all volumes.

23. VOLNAM(I)

A 20 character (or less) description of the control volume.

24. LENGTH (I),

The five geometric parameters are read in on one DIAME (I) card in English units, one card per control AREA (I) volume. LENGTH is the length, DIAME the equiva-(

ASED(I) lent diameter, AREA the cross-flow area, ASED the l

HEIGHT (I) surface area available for sedimentatio.n of aero-sol particles, HEIGHT the vertical length of the control volume. Values used for the last volume are arbitrary in this problem.

25. NTST Number of entries in the time-flow data table for l

the fluid flow at a given junction.

TFLOW Time data (in seconds) corresponding to the flow

[>

data. These are listed chronologically with up ll' to 20 entries. Any number of cards may be used.

FLOW Steam mass flow rate data (lb/sec) corresponding to the time data above. Again, up to 20 entries may be used. These can be entered on any number of cards.

26. NTST Number of entries in the time-pressure data table.

TPRESS Time data (in seconds) corresponding to the pres-sure data.

40 PRESS Gas pressure (psia) data.

27. NTSI Number of entries in the time-gas temperature data table.

TTEMP Time data (in seconds) corresponding to the tem-perature data.

TEMP Gas temperature (*F) data.

28. NTST Number of entries in the time surface temperature data table.

TDTEMP Time data (seconds) corresponding to the tempera-ture data.

DTEMP Surface temperature (*F) data.

29. NTST Number of entries in the time-H2 fraction data.

TH2FRAK Times corresponding to the H2 fraction values.

H2FRAK H2 mass fraction of the gas.

NOTE:

If one wishes to use a constant value for any parameter set NTST = 1 and the time value = 0 l

or T (see Card 5).

30. NOC0 Binary coded control words.

If the nth bit from the left in the mth word is 1 species m has ini-tial masses present in the nd volume.

31. C0 Is filled by the initial masses in all states, in the sequence: volume 1, steam-molecule; steam-particle; wall-molecule; wall-particle; volume 2, etc.

If N0C0 indicates that the given nuclide species has no masses present in the system ini-tially, these cards are skipped. C0 can be entered on any number of cards.

NOTE: This set of cards is repeated for each species that has masses in the system initially.

32. N050V Binary coded control word of NV bits.

If the nth bit is 1., source data exist for volume n.

33. N050S Binary coded control word of NS bits.

If the nth bit is 1, source data exist for the state n.

34. NTST Number of entries in the source rate-time data table.

. 2..

a 41 SET Timedata(seconds)correspondingtothesource rate data.

i SE Source rate (g/sec) data.

NOTE:

NTST, SET, SE are repeated for each state in each volume that has a source. The sequence in which they are read in is: states of the first volume first, starting with the first state. Then the second volume, and so on. Volumes and states that have no source are skipped. All cards under Item 30 are repeated for each species considered.

35. NOSPV Binary coded control word of NV bits. If the nth

)

bit is 1, the source rate of state suspended particle of volume n has the lognormal size f

distribution parameters og and rg read in.

NTST Number of entries in the o (rg)-time data table.

g PSET Time data (seconds) corresponding to the og(rg) data.

PSE og(rg in pm) data.

NOTE: NTST, PSET, PSE are read in first for og, then for r$. These two sets are repeated forsuspended particl each volum with a sequence.

i

36. PDEN Gives the particle density in each volume. By permitting change in density as a function of control volume, it is possible that gross changes in particle constitution can be approximated.

t 9

42 OUTPUT FROM TRAP-MELT 2 The OUTPUT routine for TRAP-MELT is called the number of times requested by the DIV input parameter. Thus DIV equally spaced printouts are generated during a run. The output is divided into three sections:

e Header information e Species information e Aerosol information.

Each section will be described below.

Header Information

~'The header gives general information regarding the progress of the calculations. The printout number, problem time, and time step used to reach the current time are shown on the first line. The second line shows the total number of time step iterations taken and the average time step used since the previous printout. The third line shows the time step constraints imposed by the variation of coefficients in the A matrix and the sources. Values above the average time step indicate that difficult problem conditions are not slowing the code. The CP time shows the central processor time used for the run.

+

Species Information TRAP-MELT shows the distribution of each chemical species by control volume and physical state and the total mass in each state. The mass flow rate into the last volume, which is assumed to be the contain-ment, is displayed next.

The fractional distribution of each species is given. The VAP entry represents the fraction of the species in the wall, molecular and sorbed states. The AERO entry is for the wall, particle state and the SUSP entry represents the two steam states. The sum of VPA, ABRO, and SUSP is 1.0.

The retention efficiency is determined by dividing the mass of each species in each of the three wall states by the total mass of that species currently in that volume plus all of the mass of that

I1

~

.s 43 The flow is assumed to species which passed into subsequent volumes.

follow p single path from the first to the last volume in numerical order.

Multipath flows will produce erroneous results in the volumes which are parts of t.he split flow paths.

Aerosol Information The number of aerosol particle size intervals used by C0 CALL is given followed by a table of steam flow velocities, flow and Grashof Reynolds numbers, and deposition velocities for each of the removal mechanisms considered in the code. The velocities are all in cm/sec units.

The removal mechanisms and their headings are:

e Inertial deposition from VTU turbulent flow e Diffusional deposition from VDT turbulent flow e Diffusional deposition from VDL laminar flow Thermophoretic deposition VTH e

VDI e 12 vapor sorption on stainless steel e Gravitational settling VSE Several parameters of the aerosol distribution are then shown for each The final output shows the aerosol mass distribution by control volume.

particle size for each control volume before and after C0 CALL executes.

j This gives an indication of the rate of change of the aerosol distribu-tion at the current time.

4

,[

~

t s

e s

3 i

APPENDIX A EXAMPLE INPUT DATA SET FOR TRAP-MELT 2

,4 4

'.. a.

~~

TRAPNELT 2 TEST DATA SET DATE: MARCH.1985 O

O O

CPMAX = 100 CPSEC

100.

l

NUMBER PRINT STEP DESIRED = 3

l 3,

START AT T=0 ; E M AT T=300 SEC ; DELTA T MAX =2.8 SEC

1 j

0. 300.

2.7777

.0001.1.1

9 SPECIES, 7 VOLUMES, 5 STATES, 2 PARTICLE PARAMETERS i

1 9752 i

e SPECIES NAMES

l 12 CI CH PS TE SR RU LA NG

GAS FLOW PATH THROUGH RCS i

0000000 1000000 i

Of00000 0010000 i

000f000 0000100 0000010

EETV CONTROL FLAGS FOR VAPOR DEPOSITION. PARTICLE DEPO-4

SITION, AND DIRECTION OF SETTLING OF PARTICLES.

i 3

3 010 y

111 111 111 111 111 000

ADHOC CONTROL FLAGS FOR CONDENSATION OF VAPORS 1

1 1

1 a

1 1

1 O

COAG.iLATION CONTROL FLAG FOR EACH VOLUME

,j 111110

SENSITIVITY WLTIPLIERS FOR VAPOR PRESSURES, GAS FLOW RATE *

SURFACE TEMPS, VAPOR DEPOSTION VELOCITIES THERMOPHORETIC *

DEPOSITION, TUR8ULENT DEPOSITION, AND VAPOR MASS TRANSFER

i 1

1.

TUR90 LENT COAGULATION FLAG 1

CORE 12.0 0.05

50. 50. 12.

UPPER GRID PLATE

50. 50. 2.5 2.5 0.05.ee

~..

UPPE2 CORE SARREL 1.0 2.5 98.0 0.001 1.0 HDT LEG 11.0 2.5 25.0 25.0 11.0.

PRES $URIZER 48.0 7.0 38.5 38.5 48.0 CONTAIDSEENT 1000. 1. 1000. 1000. 1000.

MASS FLOW RATES OF GAS THROUG1 EACH JUNCTION 4

0. 87. 203. 300.

.8886E+01.5711E+01.3392E+01.2248E+01 4

O. 87. 203. 300.

.8888E+01.5711E+01.3392E+01.2248E+01 4

0. 87. 203. 300.

.8888E+01.5711E+01.3392E+01.2248E+01 4

0. 87. 203. 300.

.8666E+01.5711E+01.3392E+01.2248E+01 4

0. 87. 203. 300.

.8866E+01.5711E+01.3392E+01.2248E+01 4

0. 67. 203. 300.

.8868E+01.5711E+01.3392E+01.2248E+01

VOLUDIE #1 T-H DATA

4

0. 87. 203. 300.

33

.2545E+04.2545E+04.2545E+04.2544E+04 4

0, 87. 203. 300.

.1424E+04.1471E+04.1564E+04.1641E+04 4

0. 87. 203. 300.

.1978E+04.2122E+04.2369E+04.2578E+04 2

0. 300.

0.0 0.25

VOLUME #2 T-H DATA

4

0. 87. 203. 300.

.2545E+04.2545E+04.2545E+04.2544E+04 4

0. 87. 203. 300.

.8553E+03.8557E+03.8551E+03.8522E+03 4

O. 87. 203. 360.

2025. 2145. 2285. 2325.

2

0. 300.

0.0 0.25

VOLUME #3 T-H DATA

4

0. 87. 203. 300.

.2545E+04.2545E+04.2545E+04.2544E+04

^ 40. 87. 203. 300.

.2553E+03.8557E+03.8551E+C3.8522E+03 4

O. 87. 203. 300.

~

s e

.8559E+03.8557E+03.8554E+03.8526E+03 2

6. 300.

0.0 0.25

VOLUME #4 T-H DATA

4 i

G. 67. 203. 300.

.2545E+04.2545E+04.2545E+04.2544E+04 4C. 87. 203. 300.

.8553E+03.8557E+03.8551E+03.8522E+03

40. 87. 203. 300.

.7271E+03.7305E+03.7372E+03.7434E+03 2

C. 300.

O.0 0.25 j

VOLUME #5 T-H DATA

40. 87. 203. 300.

.2545E+04.2545E+04.2545E+04.2544E+04 4

0. 87. 203. 300.

.8553E+03.8557E+03.8551E+03.8522E+03 4

0. 87. 203. 300.

.7864E+03.7918E+03.8015E+03.8094E+03 2

b

0. 300.

0.0 0.25 l

VOLUME #8 T-H DATA *

40. 87. 203. 300.

.2545E+04.2545E+04.2545E+04.2544E+04

40. 87. 203. 300.

.7457E+03.7451E+03.7417E+03.7372E+03

40. 87. 203. 300.

.6727E+03.8740E+03.6763E+03.8783E+03 2

C. 300.

0.0 0.25 f

VOLUME #7 T-H DATA 1

0.

13.

1 0.

100.

1 0.

80.

2 C. 300.

0.0 0.25

INITIAL NASSES PRESENT OF EACH SPECIES IN EACH VOLUME 0000000 0000000 ennnonn

,e:

0000000 0000000 0000000 0000000 ees SPECIES RELEASE RATES ***

ese 12 ***

1000000 10000 I

4 0.0000 28.5500 j

60.0000 15.0400 i

180.0000 18.7900 300.0000 14.3700 ese CI ***

1000000 10000 4

0.0000 58.4500 80.0000 30.8000 180.0000 34.3800 300.0000 29.4100 se* CH *es 1000000 10000 4

0.0000 571.5200 80.0000 180.5600 180.0000 201.5600 3=

s 300.0000 172.4500 A

see PS ***

1000000 01000 4

0.0000 5485.3700 80.0000 990.8300 180.0000 842.0000 300.0000 764.8200 es* TE ***

1000000 10000 3

0.0000 1.1000 270.0000 1.4100 300.0000 2.3400 see SR ***

1000000 01000 3

0.0000 2.3100 180.0000 4.9100 300.0000 8.7300 ese RU ***

1000000 01000 3

0.0000 3.5200 180.0000 4.7000 300.0000 7.5300 ese LA ***

1000000 01000

ul-A-5 1

lii!

saa agas inRR i

>=

111 liti!

i" dad sgg;"

sg2RcE d

on E

El

'g g"

e-

..s :.6 4

(

l

y-A.

s l

J s

APPENDIX B TRAP-MELT 2 SAMPLE OUTPUT Echo of Input Data Set e

Output at Time Step #3 e

NAUA Igrut Data Set s

e Retention Tables 9

~!

i e

m.. -. ----.*,, -

y,.__--._m

,y_

-,-,._y-

.-e.

.--,,. -..---%y,ye-..

7

- - ~.

,,t--

DATE: MARCH.1985

TRAPNELT 2 TEST DATA SET T*APMELT2 CODE, MARCH, 1985 CP TIME LIMIT =

100. SEC KOMAD =

0, KONENT =

0 DIV =

3.0 START TIME = 0.

SEC FINAL TIME = 300.0 SEC MAXIMUM TIME STEP = 2.778 SEC t

CONVERGENCE PARAMETERS:

REL ETA 1 ETA 2

.1000E-03.1000E+00.1000E+00 MJMEER OF CHEMICAL SPECIES 9

7 PRAMBER OF CONTROL VOLUMES l

5 MJMBER OF STATES 2

MJMBER OF PART. DIST. PARAMETERS SPECIES = 12 CI CH PS TE SR RU LA NG FLOW COMdECTIONS (FROM COLuted INDEX TO R0W INDEX):

1 2

3 4

5 6

7 1

0 0

0 1

2 1

0 0

2 3

0 1

0 0

0 3

4 0

0 1

0 0

4 cu 0

0 0

0 1

0 0

0 5

L 0

0 0

1 0

0 6

7 0

0 0

1 0

7 1

2 3

4 5

6 7

6 THE teJMBER OF FLOW ColedECTIONS =205 THE A MATRIX DIMENSION =

FISSION PRODUCT TRANSPORT SWITCHES:

A=1 PERMITS VAPOR DEPOSITION IN VOLUME B=1 PERMITS PARTICLE DEPOSITION IN VOLUME C=0 DENDTES COUNTER-FLOW GRAVITATIONAL SETTLING j

C=1 DENOTES CROSS-FLOW GRAVITATIONAL SETTLING VOL ABC 1

010 2

11 1 3

11 1 4

1 1 1 5

111 6

1 1 1 7

000 ADHDC TRANSPORT SWITCHES:

I 1 PERMITS VAPOR CONDENSATION IN VOLUME j

VOL SWITCH 1

1 4

2 1

3 1

- 4 1

6 1

i 7

0

d VOL-SWITCH 1

0 2

1 3

1-4 1

5 1

8 1

7 0

SENSITIVITY BRJLTIPLIERS:

VPN 1.000 FRM 1.000 STM 1.000 SRM 1.000 THDM 1.000 TDM 1.000 VTM 1.000 TUR8ULENT COAGULATION SWITCH =

1 A =1= PERMITS TUR8ULENT COAGULATION IN ALL VOLUMES WHICH ALLOW COAGULATION GEOMETRIC DATA:

FOR COMPARTMENT 1: CORE LENGTH (FT)

=

12.00 EQUIVALENT DIA (FT)

=

.5000E-01 FLOW AREA (FT2)

= 50.00 SEDIMENTATION AREA (FT2) = 50.00 HEIGHT (FT)

=

12.00 FOR COWARTMENT 2: UPPER GRID PLATE LENGTH (FT)

= 2.500 EQUIVALENT DIA (FT)

=

.5000E-01 FLOW AREA (FT2)

= 50.00 SEDIMENTATION AREA (FT2) = 50.00 m

HEIGHT (FT) 2.500 g

=

FOR COMPARTMENT 3: GUIDE TU8ES LENGTH (FT)

=

10.50 EQUIVALENT DIA (FT)

=

.7500 FLOW AREA (FT2)

=

1.500 SEDIMENTATION AREA (FT2)

=

.1000E-02 1

HEIGHT (FT)

=

10.50 I

l FOR COMPARTMENT 4: UPPER CORE BARREL LENGTH (FT)

=

1.000 1

EQUIVALENT DIA (FT)

= 2.500 j

FLOW AREA (FT2)

98.00 SEDIMENTATION AREA (FT2)

.1000E-02 HEIGHT (FT)

=

1.000 FOR COMPARTMENT 5: HDT LEG LENGTH (FT)

=

11.00 EQUIVALENT DIA (FT)

= 2.500 FLOW AREA (772)

= 25.00 SEDIMENTATION AREA (FT2) = 25.00 HEIGHT (FT)

=

11.00 FOR COMPARTMENT 8: PRESSURIZER

= 48.00 LENGTH (FT)

EQUIVALENT DIA (FT)

= 7.000 FLOW AREA (FT2)

= 38.50 SEDIMENTATION AREA (FT2) = 38.50

= 48.00 HEIGHT (FT)

FOR COMPARTMENT 7: CONTAlle0ENT LENGTH (FT)

=

1000.

EQUIVALENT DIA (FT) 1.000

=

_m

-.. ~..........

.e+

9

~

i

=

1000.

FLOW AREA (FT2) 1000.

SEDIMENTATION AREA (FT2)==

1000.

HEIGHT (FT) 0 JUNCTION 1*

2 FROM VOLUME 1=

4 THE 98JMBER OF TIME STEPS FOR THE FLOW TO VOLUME tit 0ES (SEC)

O.

87.00 203.0 300.0 FLOW (L8S/SEC) 8.888 5.711 3.392 2.248 JUNCTION 2*

3 FROM VOLUME 2=

4 THE NUMBER OF TIME STEPS FOR THE FLOW TO VOLUME 8

TIMES (SEC)

O.

87.00 203.0 300.0 FLOW (L85/SEC) 8.888 5.711 3.392 2.248 JUNCTION 3*

4 FROM VOLUME 3=

4 THE peUMBER OF TIME STEPS FOR THE FLOW TO VOLUME TIMES (SEC)

O.

87.00 203.0 300.0 I

FLOW (L85/SEC) 8.888 5.711 3.392 2.248 JUNCTION 4*

5 FROM VOLUME 4=

4 THE NUMBER OF TIME STEPS FOR THE FLOW TO VOLUME TIMES (SEC)

O.

87.00 203.0 300.0 I

FLOW (LBS/SEC) 8.888 5.711 3.392 2.248 4

JUNCTION 5*

8 FROM VOLUME 5=

4 THE NUMBER OF TIME STEPS FOR THE FLOW TO VOLUME TIMES (SEC)

O.

87.00 203.0 300.0 a

FLOW (LBS/SEC) 8.888 5.711 3.392 2.248 at b

I JUNCTION 8*

7 FROM VOLUME 8=

4 THE DAMBER OF TIME STEPS FOR THE FLOW TO VOLUME j

l TIMES (SEC) 0, 87.00 203.0 300.0 i

FLOW (LBS/SEC) 8.888 5.711 3.392 2.248 4

d

VOLUME 1*

1=

4 THE NUMBER OF TIMES FOR THE PRESSURE IN VOLUME j

TIMES (SEC)

O.

87.00 203.0 300.0 l

i PRESSURE (PSIA) 2545.

2545.

2544.

1=

4 THE DRIMBER OF TIME STFPS FOR THE GAS TEMPERATURE IN VOLUME TIMES (SEC)

O.

87.00 203.0 300.0 GAS TEMPERATURES (F) 1424, 1471.

1584.

1841.

j 1=

4 THE DRIMBER OF TIME STEPS FOR THE SURFACE TEMPERATURE IN VOLUME 4

TIMES (SEC)

O.

87.00 203.0 300.0

{

ORY SURFACE TEMP (F) 1978.

2122.

2389.

2578.

1=

2 THE DRneER OF TIME STEPS FOR THE H2 MASS FRACTION IN VOLUME TIMES (SEC)

O.

300.0 H2 MASS FRACTION 0,

.2500 1

VOLUME 2*

2=

4 l

THE 98JMBER OF TIMES FOR THE PRESSURE IN VOLUME i

TIMES (SEC)

O.

87.00 203.0 300.0 PRESSURE (PSIA) 2545.

2545.

2545, 2544.

2=

4 THE 98JMBER OF TIME STEPS FOR THE GAS TEMPERATURE IN VOLUME TIMES (SEC)

O.

87.00 203.0 300.0 855.7 855.1 852.2 CAS TEMPERATURES (F) 855.3 2=

4 i

vtwr MTEPS FOR THE SURFACE TEMPERATURE IN VOLUME e n 7no.n

- - - -*v a ar

~

I. +

DRY SURFACE TE9F (F) 2025.

2145.

2285.

2325.

TIE ftNSER OF TIME STEPS FOR THE H2 MASS FRACTION IN VOLUME 2=

2 TIMES (SEC)

O.

300.0 H2 MASS FRACTION 0.

.2500

VOLUME 3*

THE NUMBER OF TIMES FOR THE PRESSURE IN VOLUME 3=

4 TIMES (SEC)

O.

67.00 203.0 300.0 PRESSURE (PSIA) 2545.

2545.

2544.

s THE D8JMBER OF TIME STEPS FOR THE GAS TEIFERATURE IN VOLUME 3=

4 TIMES (SEC)

O.

67.00 203.0 300.0 GAS TEMPERATURES (F) 855.*.s 855.7 855.1 852.2 THE NUISER OF TIME STEPS FOR THE SURFACE TEMPERATURE IN VOLUME 3=

4 TIMES (SEC)

O.

87.00 203.0 300.0 DRY SURFACE TEIF (F) 855.9 855.7 855.4 852.8 THE DRIMBER OF TIME STEPS FOR THE H2 MASS FRACTION IN VOLUME 3=

2 TIMES (SEC)

O.

300.0 H2 MASS FRACTION 0.

.2500

VOLUME 4*

THE Elh8ER OF TIMES FOR THE PRESSURE IN VOLUME 4=

4 TIteES (SEC)

O.

87.00 203.0 300.0 PRESSURE (PSIA) 2545.

2545.

2545, 2544.

THE 98JeseER OF TIME STEPS FOR THE GAS TEMPERATURE IN VOLuteE 4=

4 m

e TIMES (SEC)

O.

57.00 203.0 300.0 GAS TEMPERATURES (F) 855.3 855.7 855.1 852.2 THE 98JIIBER OF TIME STEPS FOR THE SURFACE TEMPERATURE IN VOLUME 4=

4 TIMES (SEC)

O.

67.00 203.0 300.0 DRY SURFACE TEMP (F) 727.1 730.5 737.2 743.4 THE DANIBER OF TIteE STEPS FOR THE H2 SEASS FRACTION IN VOLUME 4=

2 TIMES (SEC)

O.

300.0 H2 98 ASS FRACTION 0.

.2500

VOLUISE 5*

THE D&lI4BER OF TIMES FOR'THE PRESSURE IN VOLUseE 5=

4 TI88ES (SEC)

O.

87.00 203.0 300.0 PRESSURE (PSIA) 2545.

2545.

2544.

THE DANIBER OF TIIeE STEPS FOR THE GAS TE9EPERATURE IN VOLUISE 5=

4 TIMES (SEC)

O.

87.00 203.0 300.0 GAS TEIIPJRATURES (F) 855.3 855.7 855.1 852.2 Tete D8JIIBER OF TIteE STEPS FOR THE SURFACE TEOFERATURE IN VOLUISE 5=

4 TIteES (SEC)

O.

87.00 203.0 300.0 DRV SURFACE TEMP (F) 788.4 791.8 801.5 809.4 THE NUMBER OF TIIEE STEPS FOR THE H2 ISASS FRACTION IN VOLUDIE 5=

2 TIIIES (SEC)

O.

300.0 H2 94 ASS FRACTION 0.

.2500

VOLUIIE 8*

THE NUMBER OF TIMES FOR THE PRESSURE IN VOLUME 8=

4 TIIeES (SEC)

O.

87.00 203.0 300.0 PRESSURE (PSIA)

2545, 2545.

2545.

2544.

_,m--

...j

.t 4

8=

4 THE MJMBER OF TIME STEPS FOR THE GAS TEWERATURE IN VOLUME TIMES (SEC)

O.

87.00 203.0 300.0 745.1 741.7 737.2 GAS TEMPERATURES (F) 745.7 8=

4

THE MJMBER OF TIME STEPS FOR THE SURFACE TEMPERATURE IN VOLUME TIMES (SEC)

O.

87.00 203.0 300.0 c

874.0 878.3 878.3 DRY SURFACE TEMP (F) 872.7 8=

2 THE NUMBER OF TIME STEPS FOR THE H2 MASS FRACTION IN VOLUME TIMES (SEC)

O.

300.0 H2 MASS FRACTION 0.

.2500

VOLUME 7*

7=

1 THE NUMBER OF TIMES FOR THE PRESSURE IN VOLUME TIMES (SEC)

O.

PRESSURE (PSIA) 15.00 7=

1 THE NUMBER OF TIME STEPS FOR THE GAS TEMPERATURE IN VOLUME TIMES (SEC)

O.

GAS TEMPERATURES (F) 100.0 7=

1 THE MJMBER OF TIME STEPS FOR THE SURFACE TEMPERATURE IN VOLUME TIMES (SEC)

O.

DRY SURFACE TEMP (F) 80.00 7=

2 THE NUMBER OF TIME STEPS FOR THE H2 MASS FRACTION IN VOLUME TIMES (SEC)

O.

300.0 cp H2 MASS FRACTION 0.

.2500 b

- INITIAL CONDITIONS **

FOR CHEMICAL SPECIES 12 SUSPENDED,M SUSPENDED.P WALL.M WALL.P REACTED THE INITIAL MASSES (GRAMS) ARE:

1

.0000000E+00

.0000000E+00 2

.0000000E+00 0000000E+00

.0000000E+00

.0000000E+00 3

.0000000E+00

.0000000E+00 4

.0000000E+00

.0000000E+00 5

.0000000E+00

.0000000E+00 8

.0000000E+00

.0000000E+00 7

.0000000E+00

.0000000E+00 FOR CHEMICAL SPECIES CI SUSPENDED.M SUSPENDED.P WALL.M WALL,P REACTED THE INITIAL MASSES (GRAMS) ARE:

1

.0000000E+00

.0000000E+00 2

.0000000E+00

.0000000E+00 3

.0000000E+00

.0000000E+00 4

.0000000E+00

.0000000E+00 5

.0000000E+00

.0000000E+00 8

.0000000E+00

.0000000E+00 7

.0000000E+00

.0000000E+00 0000000E+00

.0000000E+00 FOR CHEMICAL SPECIES CH SUSPENDED,M SUSPENDED.P WALL,M WALL.P REACTED THE INITIAL MASSES (GRAMS) ARE:

1

.0000000E+00

.0000000E+00 0000000E+00 0000000E+00 2

.0000000E+00

.OO00000E+00

.0000000E+00

.0000000E+00 annnannr.66 onoo000E+00

.0000000E+00

-ear,na onnonnor+oo

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- SOURCE DATA **

SOURCE MASS RATES:

CHEMICAL SPECIES 12 VOLUME 1 STATE 1

TIMES MASS RATE (SECS)

(G/SEC) 28.55 0.

80.00 15.04 180.0 16.79 300.0 14.37 CHEMICAL SPECIES CI VOLUME 1 STATE 1

TIMES MASS RATE (SECS)

(G/SEC) 58.45 O.

80.00 30.80 180.0 34.38 en 300.0 29.41 k

CHEMICAL SPECIES CH VOLUME 1 STATE f

TIMES MASS RATE (SECS)

(G/SEC) 571.5 O.

80.00 180.8 180.0 201.6 300.0 172.5 CHEMICAL SPECIES PS VOLUME 1 STATE 2

TIMES MASS RATE (SECS)

(G/SEC) 5485.

O.

80.00 990.8 180.0 842.0 300.0 784.8 OtEMICAL SPECIES TE VOLUME 1 STATE 1

TIMES MASS RATE (SECS)

(G/SEC) 1.100 O.

270.0 1.410 300.0 2.340 CHEMICAL SPECIES SR VOLUME 1 STATE 2

TIMES MASS RATE (SECS)

(G/SEC) 2.310 O.

1#0.0 4.910

.w CHEMICAL SPECIES RU VOLUME 1 STATE 2

TIMES MASS RATE (SECS)

(G/SEC)

O.

3.520 180.0 4.700 300.0 7.530 CHEMICAL SPECIES LA VOLUME 1 STATE 2

TIMES MASS RATE (SECS)

(G/SEC)

O.

.2200E-01 240.0

.8200E-01 300.0

.1670 CHEMICAL SPECIES NG VOLUME 1 STATE 1

TIMES MASS RATE (SECS)

(G/SEC)

O.

787.1 60.00 336.0 180.0 375.1 300.0 320.9 o* PARTICLE DATA **

SOURCE PARTICLE SIZE DISTRIBUTION PARAMETERS:

VOLUME 1

e TIME SIGG CD 0.

1.700 VOLUME 1

TIME RG (MICRONS)

O.

.5000E-01 PARTICLE DENSITIES (G/CN**3):.300E+01.300E+01.300E+01.300E+01.300E+01.300E+01.300E+01 DISCRETE PARTICLE RADII PERMITTED (CM):

.985E-06

.177E-05

.318E-05

.571E-05

.103E-04

.184E-04

.331E-04

.594E-04

.107E-03

.192E-03

.344E-03

.619E-03

.111E-02

.2OOE-02

.358E-02

.644E-02

.116E-01

.208E-01

.373E-Of

.670E-01 ENTER EXTEND NS=

8 ENTER EXTEND NS=

9 ENTER EXTEND NS= 10 ENTER EXTEND" NS= 11 ENTER EXTEle NS= 12 ENTER EXTEND NS= 13 ENTER EXTEND NS= 14 ENTER EXTEND NS= 15 ENTER EXTEND NS= 16 ENTER EXTEND NS= 17

m

'.. ~........,

, _ := ? %

P TIME STEP 3 TIME.3000E+03 SEC DELT 1.1903 SEC MAT 32X T. STEP.1190E+01 SEC SOURCE T. STEP.1190E+01 SEC CP TIME 97.58 SEC ITERATION 150 AVE. T. STEP

.2245E+01 SEC a

---I2 ---

REACTED SPECIES MASS (G) BY LOCATION SUSPENDED.N SUSPENDED.P WALL.M WALL.P 1

2219155E+04

.0000000E+00 0000000E+00

.0000000E+00

.0000000E+00 2

.6687864E+03 0000000E+00

.0000000E+00

.4020127E+00 0000000F+00

.0000000E+00

.5765163E-01 4

4590892E+03

.0000000E+00

.Or% 000E+00

.0000000E+00

.1431219E+00 3

. 830857'tE+02

.0000000E+00 S

.8595199E+03

.0000000E+00 0000000E+00

.0000000E+00

.1468130E+00 6

.7414048E+03

.0000000E+00

.0'sv0000E+00

.6182820E-01 7

.6638644E+02

.0000000E+00

.0000000E+00 TDTALS:

.0000000E+00

.8114274E+00 5097428E+04 MASS INJECTION RATE (G/S) INTO CONTAIPSIENT e

.5310410E+00 eeeeeeeeeeeeeeeeeeeeeeeeeeeeee FRACTIONAL DISTRIBUTION OF 12:

eo VAP AER0 SUSP 4

.00

.99 se**eesesessesseessessessesses RETENTION EFFICIENCIES:

VOL TOT M

P SOR8ED 0

.00

.00 5

.00

.00 00

.00 4

.00

.00 3

.00

.00 l

2

.00

.00 1

.00

---CI REACTED SUSPENDED.M SUSPENDED,P WALL.M WALL,P SPECIES NASS(G) BY LOCATION 1

1261571E+04 3281666E+04

.0000000E+00

.5273941E+00 0000000E+00 2

8101241E+01

.1337143E+04

.0000000E+00

.1173199E+03

.0000000E+00 3

.7665982E-01

.1644950E+03 4691530E-03

.8040619E+02

.0000000E+00 4

.t163411E-01

.8988890E+03 4298918E-02

.2805504E+02

.0000000E+00 5

.2207039E-01 4260695E+03 1473832E-01 2272155E+04

.0000000E+00 6

.9452118E-02

.3363437E+03 9540345E-03

.1821529E+03

.0000000E+00 7

.3574916E-02 4353871E+02

.0000000E+00

.0000000E+00 TOTALS:

.6488145E+04

.2046043E-01

.2680617E+04

.0000000E+00

.1269795E+04

.3067641E+00 MAS % INJECTION RATE (G/S) INTO CONTA!!d8ENT =

esseeeeeeeeeeeeeeeeeeeeeeeeees FRACTIONAL DISTRIBUTION OF CI:

f 1

VAP AERO SUSP

.00

.26

.74

........e

....e.e....e eeeeeee l

r i

6

.32

.00 32

.00 5

.70

.00

.70

.00 4

.01

.00

.01

.00 3

.02

.00

.02

.00 2

.02

.00

.02

.00 1

.00

.00 i

j

...CH ---

1 j

SPECIES NASS(G) BY LOCATION SUSPENDED.N SUSPENDE0.P WALL.N WALL.P REACTED i

1

.4460194E+04

.2346821E+05

.0000000E+00

.3771559E+01

.0000000E+00 d

2 2841470E+02

.8433475E+04

.0000000E+00

.7391566E+03

.1237366E+03 3

3271045E+00

.1038544E+04

.7508281E-03

.5653871E+03

.1360629E+00 4

4223923E+00

.5824295E+04

.2291424E+00

.2004375E+03

.6790395E-01 5

.1171120E+01

.2805318E+04

.5119548E+00

.1650565E+05

.1806963E+00 6

.1152398E+01

.2413415E+04

.2045350E+00

.1387450E+04

.6287362E-01 i

7 4084591E+00

.3368634E+03

.0000000E+00

.0000000E+00 t 9, TOTALS:

j

.4492000E+04

.4431992E+05

.1246383E+01

.1940185E+05

.1241842E+03 l

NASS INJECTION RATE (G/S) INTO CONTAll60ENT =

.2299167E+01 esseeeeeeeeeeeeeeeeeeeeeeeeeee FRACTIONAL DISTRIBUTION OF CH:

VAP AERO SUSP

.00

.28 71 esseeeeeeeeeeeeeeeeeeeeeeeeese "e

RETENTION EFFICIENCIES:

o i

VOL TOT N

P SORSED 6

.34

.00

.34

.00 1

i 5

.70

.00

.70

.00 1

4

.01

.00

.01

.00 l

3

.02

.00

.02

.00 2

.02

.00

.02

.00 1

.00

.00 t

---PS ---

SPECIES NASS(G) BY LOCATION SUSPENDED.N SUSPEleED.P WALL.N WALL.P REACTED 1

1

.0000000E+00

.1397097E+06

.0000000E+00

.5620035E+04

.0000000E+00 2

.0000000E+00

.8940348E+04

.0000000E+00

.1873736E+06

.0000000E+00 l

3

.0000000E+00

.1114832E+04

.0000000E+00

.1216030E+04

.0000000E+00 4

4

.0000000E+00

.7555210E+04

.0000000E+00 4631691E+03

.0000000E+00 1

5

.0000000E+00 4001630E+04

.0000000E+00

.4056397E+05

.00C0000E+00 1

6

.00000@E+00

.5597180E+04

.0000000E+00

.4310101E+04

.0000000E+00 7

.0000000E+00

.1132383E+04

.0000000E+00

.0000000E+00 TOTALS:

.0000000E+00

.1680513E+06

.0000000E+00

.2395469E+06

.0000000E+00

.6432030E+01 NASS INJECTION RATE (G/.S) INTO CONMW =

.......e FRACTIONAL DISTRIBUTION OF PS:

VAP AERO SUSP

.00

.59 41 sessessessesesesessesessessess CETENTION EFFICIENCIES:

um tnt se P

%OR9ED

+

l4 iy o

= "

00000000 0

0300010 3

D+000000 0

0

+

D+000000 0

EE++++++

++

+

T0EEEEEE E

EE+++EEE E

C0000000 0

T0EEE A0000000 0

C0551870 9

A0830180 7

E0000000 0

E0189890 0

R0000000 0

R0456460 8

0000000 0

0763860 8

0000000 0

963600 9

000000 0

0.174120 1

20310210 3

0000000 0

+000000 0

0

++

+

+000000 0

P.E++++EE E

++

+

6EEEE P,E++++EE 0EEEE E

L4145130 8

L0000000 0

L6882020 4

L0000000 0

A1 315480 1

A0000000 0

W0841560 3

W0000000 0

4535390 9

0000000 0

1557060 4

000000 0

428750 5

2 0.000000 0

0 5

0 E

1 2

0 0

9 3

0000000 0000000 0

9

+000000 0 0 0

++

+

8 M.E++++EE

+000000 0

2 0EEEE E

4

++

+

8 0EEEE E

8 L0000000 0

9 M.E++++EE L0000000 0

L0000000 0

7 A0000000 0

L0000000 0

A0000000 0

W0000000 0

0000000 0

000000 0

000000 0 =

0.000000 0

=

TN T

E N

t E

e M

P.30212221 3

I p

N D+000000 0 A P. 00000000 0

I

++++

+

T D+000000 0 A EC++EEEE E

N

++

+

T D2EE D0EEEE E

N N4685364 7

O EE++++EE N0000000 0 O E6760912 3 C E0000000 0 C P6278459 7

e s

P0000000 0

e e

S1248123 7

Oe:

e S0000000 0

Oe:

s D

U8882647 8

TsR e

U0000000 0

TsE e

E S7659303 8

NsS e

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R204290 N

452111 8

sF e

000000 0 NsT e

B S0.000000 0

eF e

O786590 O

Ie e

sO e

)

000000 N

I Se e

000000 O

)eO e

S T

/ sN e-I Ss e

A GsO eM _

T

/ eN e:

C eS (eIP e

A GsO eEP000000 OM0 931211 O M.30011122 3

eTS9eI 000000 L 0000000 0

sTS2eT C

(SIP E s U U 6.e 'M er D+000000 0

TeBS i

+++

+

D+000000 0

EsUU4.eC YEE+++EEE L

370070 AsI e

E TsBS eN BD0EEE YEE+ - - - - -

+

BD2EEFEEE E

AeI eE N0000000 0 RsR eT 1

RsR eI

)E0000000 0

eTO e =c 000000 GP7907892 3 NeSR0eI 000000 GP0000000 0

NsSR8e.

)E5296601 8

sTO eCM000000 N8921846 S0000000 0 O s I E 3.e r ec IeDA

(

000000 (S2371320 2

OsIE0.eF SU0000000 0

000000 0 Ts ee SU9015912 3 IsDA sF SS0.000000 A

0 CsL e,

016363 9 Te sE EeAP e.

SS1.423161 1

CsL e

T A

EsAP sNO204290

- M JsNA0e<

N s O V 0.e+

931211

- M JeNA1 SOT 785590 e.

S IeI S

NsOV5.eI 370070 E

IsI sT L

sT e -

S R

I S

A SeC e+

L eT sNL E

A SsC eEO S C 1

E 234567 T sea e-E I

654321 E

234567 T SsA sTV654321 O

AsR e

T C 1

P T

M F

P O

AeR eE S

S T

M F

R

, A V

os$

g 0

0 0000000 0

0000000 0

D+000000 0

EE++++++

+

EE++++++

+

T0EEEEEE E

C0000000 0

0 A0000000 0

A0000000 E0000000 0

E0000000 0

R0000000 0

R0000003 0

000000 0

0.00000.C.

0000000 0

00000 0

000000 0

0.000000 0

0 0

2 0111010 1

031121 0 3

+000000 0

E+

- - +- +

+

P.2EEEEEE P.6EEEEEE E++++++

+

E E

L4610930 5

L079471 0 9

L5588000 2

L764561 0 7

A2251 180 0

A01 99440 1

W2445820 0

W6890060 6

770641 0 0

-5940420 8

980200 0

1610460 8

1.421870 6

531860 6

3 1

0 0

E E

8 9

0 0

0 7

0000000 0

4 0000000 0

1

+000000 0

0

+000000 0

4

+

1

+

5 M.E+++t++

M,E++++++

0EEEEEE E

1 0EEEEEE E

1 L0000000 0

L0000000 0

A0000000 0

W0000000 0

0000000 0

000000 0

0000000 0

0.000000 0

=

000000 0

=

T T

N N

E E

I I

S S

P. 20010001 2

I D

P,0212221 3

D 3

I D+000000 0 A D+00000O 0 A EE++++++

+

T EE+

+++-

+

T 6EEEEEE E

N e4EEEEEE E

N e4867788 8732504 0 O 2

O t

E4473557 6 C E2576697 4

C t

P8647080 9

s e

P2198171 0

s e

m S9317759 6

Oe:

s D

S2177008 4

Oe:

s U3896101 7

TsU e

E U1977367 6 tea s

439427 4 NsR s

S S1457725 2

NeL e

000000 NS7.452111 8

Ie s

R000000 N

673111 1

Ie s

eF s

sF e

O000000 O

000000 O

eO e

)

sO s

S I

)

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T Se s

A

/ eN s:

A

/sN e :

C GsO sS C

GeO eS (eIP sE-( eIP sEP401211 O N,00000000 0

eTS5sI ON.0000000 0

391211 L

0 sTS8eI 370070 L

360070 eC sC D+000000 0

EeUU6.sN D+000000 0

EsUU5.sN YEE++++++

+

TeBS YEE++++++

+

Te8S BD0EEEEEE E

AsI eE BD0EEEEEE E

AeI sE N0000000 0 RsR sI N0000000 0 ReR eI 000000

)E0000000 0

eTO sCM000000

)E0000Q00 0

eTO sC 000000 GP0000000 0

NeSR2eI 000000 GP0000000 0 NeSR5eI sF (S0000000 0

OeIE3.sF sF S0000000 0

IsDAO s I E 4.s F SU0000000 0

IeDA (SU0000000 0

000000 0 Te

.eE SS0.000000 000000 0 Te eE SS0.000000 A

0 CeL s

A 0 CsL s

T EeAP sN EsAP sNO401211

. M 391211

. M 360070 JeNA0eOT370070 JeNA0eO NeOV0.sT sI sI S

NsOV0.sT S

E S

IeI E

S IsI u

I L

eT eNL A

I L

eT eN g C 1

A SsC sEO L.

C 1

A SeC sE E

234567 T sea sT 654321 E

234567 T SsA sTV654321 P

O AeR eE P

O AeR eE S

T M

F R

S T

M F

R

6

..s G

B-13 8

I

. I 8 8. I s. s.

'lllllll g.

sg...

..IgggI g

'lllllllg E

sgggggg gg E

v W

Y sIss@sg)

E 5

h I!I i 0

s'

als.s.s.s.s.a.

":g s.a.s.s.s..

E g

a:

g"g?ft191 1 e::in.:s ssssa

's i

n35s;5 s =.

>I. vi=e=s! =g :a s

=

- 8 s...

. _ :,a, s. e.s.s.s s.a.

g:m

e=s s

g8.1:

s.s.s.s.s.a.

8

c:

I

.e 3:.p,s,:.ses.s.s.s.s.s.

a.s.s.a.r.s. :,g gig ign......

7 S.. e.,

4 7

h I

j BASSER OF PARTICLE SIZE CLASSES USEO:

20 WOL STEAM.V STEAM.RE GRAS..RE VTU VOT WOL VTH VDI VSE H2 FRAC l

1

.201E+01

.125E+03

.192E+03

.000E+00

.513E-04

.000E+00

-I

.000E+00

.249E+00 l

2

.128E+01

.178E403

.88SE+03

.000E+00

.111E-04'

.000E+00

.125E-05

.518E+01 249E+00 3

419E+02

.SS2E+05 858E+03

.136E-01

.535E-04

.000E+00

.241E-04

.258E+03

.249E+00 4

.854E+00 459E+04

.881E+05

.133E-02

.SSSE-OS

.000E+00

.340E-04 401E-04 457E+03 249E+00 5

.251E+01

.176E+05 414E+04

.847E-03

.315E-05

.000E+00

.939E-05

.292E-04

.121E+02

.249E+00 8

.149E+01

.347E+05

.282E+08

.565E-02

.172E-05

.000E+00

.195E-04

.568E-04

.845E+01

.249E+00 7

454E+01 402E+03

.345E+03

.000E+00

.0,00E+00

-I

.000E+00

.249E+00 NASS I

l 9&NESER GEOMETRIC GEOMETRIC

. MEDIAN DIAMETER l

CONCENTRATION MEAN RADIUS STANDARD DEVIATION (MICRONS)

(PARTS /CN**3)

(MICRONS) i 1

.149E+13 549E-01

.185E+01

.190E+00 2

.801E+10

.935E-01

.218E+01

.34SE+01 3

.865E+09

.217E+00

.22SE+01 577E+01 j

)

O

.182E+09 456E+00

.232E+01

.743E+01 5

.287E+0S

.566E+00

.217E+01

.604E+01 8

.477E+07

.830E+00

.199E+01

.588E+01 7

.225E+04

.499E+00

.220E+01

.549E+01 l

l j

PARTICLE MASS IN EACH SIZE CLASS BY VOLUME (G/Op*3) BEFORE COCALL:

d i

.0000E+00

.3512E-05.1591E-03

.1814E-02

.4256E-02 314SE-02 8752E-03 4226E-04

.7757E-06

.0000E+00 VOLUME 1

.0000E+00.0000E+00.0000E+00.0000E+00

.0000E+00.0000E+00 0000E+00

.0000E+00.0000E+00 7

)

a

.0000E+00.0000E+00.0000E+00.0000E+00.2871E-04

.2392E-03 2645E-03

.4992E-03

.1034E-02

.1217E-02 VOLUME 2

.783SE-03

.5424E-03.4037E-03.3032E-03

.1822E-03

.5853E-04 7531E-05.2792E-OS

.0000E+00 1

.0000E+00

.0000E+00.0000E+00.1425E-08.2647E-05.2480E-04 7335E-04 2638E-03

.7846E-03

.10SSE-02 l

VOLUME 3

1

.7743E-03

.5761E-03

.4429E-03

.3412E-03

.2549E-03

.1850E-03 1178E-03 5811E-04

.2387E-03

.0000E+00.0000E+00.0000E+00.0000E+00.1798E-08.2878E-05 1718E-04 1209E-03

.5445E-03

.1144E-02 VOLUME 4

i

.7775E-03

.8347E-03.4993E-03

.3SSOE-03

.3021E-03.2225E-03.1178E-03

.3953E-04 4867E-03 l

l 0000E+00 0000E+00

.0000E+00.0000E+00.1257E-07

.2984E-08.2527E-05.2204E-04

.1077E-03

.2374E-03 VOLUME 5

i 1599E-03

.1319E-03.1046E-03

.8253E-04

.5678E-04

.2331E-04 4306E-05

.2SS4E-06 2479E-06 i

)

.0000E+00

.0000E+00.0000E+00.0000E+00.3829E-07 4341E-08 4029E-05.1962E-04

.4082E-04 l

j VOLUME 8

l

.2779E-04

.2287E-04

.1834E-04 14452-04

.385SE-05.2649E D5.3187E-OS 1076E-07 0000E+00 l

.0000E+00.0000E+00 0000E+00 9786E-14.1723E-11

.2487E-10.2271E-09

.1897E-08

.7297E-08

.1355E-07 VOLUME 7

i j

.9392E-08

.7541E-OS 592SE-OS 4393E-08

.2390E-08

.8509E-09

.882SE-10.2029E-11

.7247E-12 1

PARTICLE MASS.IN EACH SIZE CLASS SY VOLUME (G/CM**3) AFTER COCALL:

J

.0000E+00.3534E-05.1593E-03 1813E-02 4251E-02.3144E-02

.8741E-03 4220E-04 7745E-08.0000E+00 VOLUME 1

j

.0000E+00

.0000E+00.0000E+00

.0000E+00.0000E+00.0000E+00

.0000E+00 0000E+00.0000E+00

.0000E+00

.3781E-OS

.2770E-06 458SE-05.2457E-04

.8414E-04

.1821E-03

.5080E-03

.1036E-02 1210E-02 VOLUME 2

.7822E-03

.5435E-03 4045E-03

.3034E-03.1822E-03

.5847E-04

.7515E-05.2783E-06

.2245E-08 4

I

.0000E+00.0000E+00.5045E-08 1342E-OS.2405E-05.2300E-04

.7286E-04

.2880E-03.78645-03 1090E-02 1

VOLUME 3

.7759E-03.5773E-03 4438E-03

.3418E-03

.2559E-03

.1864E-03

.1190E-03

.58SOE-04

.2420E-03 I

.0000E+00

.0000E+00.0000E+00

.2614E-08 1842E-08.2779E-05

.1896E-04

.1203E-03

.5432E-03 1143E-02 1

VOLUME 4

7769E-03

.8346E-03

.4992E-03

.3879E-03 3020E-03.2225E-03.1177E-03

.3945E-04

.4874E-03

i b 9

-A e

.0000E+00.0000E+00.0000E+00.0000E+00 1249E-07.2919E-06.2522E-05.2199E-04

.1074E-03.2371E-03

.1597E-03

.1317E-03

.1045E-03.8242E-04

.5668E-04

.2325E-04 4288E-05

.2861E-06

.2434E-06

.0000E+00

.0000E+00.0000E+00

.1663E-10

.3812E-07

.4327E-06 4022E-05.1960E-04 4081E-04 VOL M 6

.2777E-04

.2286E-04

.1833E-04 1444E-04

.8657E-05

.2648E-05

.3165E-06

.1061E-07 6424E-09

.0000E+00.0000E+00.0000E+0?.5786E-14.1723E-11

.2475E-10.2281E-09.1706E-08

.7341E-08

.1365E-07 VOLUME 7

.9455E-08

.7592E-08

.5969E-08 4425E-08

.2410E-08 6568E-09

.6899E-10.2053E-11

.7254E-12 ese TOTAL NASS INJECTION RATE (G/S) INTO CONTAIM4ENT:

.9059063E+01 e** FRACTION OF TOTAL NASS INJECTED:

CI CH PS TE SR RU LA

.3386E-01

.2538E+00

.7100E+00 8702E-06 1047E-02

.1270E-02

.1230E-04 as u,

+

TRAPIIELT 2 TEST DATA SET DATE: MARCH,1983

- - NAUA 199U7 OATA ***

0.0

.T..5E-5.5.3 0.0

.T.

.5E-5.5.3

.000

'C1" 0.

O.

1 "CH" 0.

O.

P5" 0.

O.

TE" 0.

O.

'SA" O.. O.

'stu" 0.

O.

~

'LA" 0.

O.

4402E+00

.T.

.3833E-04

.7824E+00

.3000E+01 O.

.T.

.3833E-04

.7824E+00 3000E+01.101635E+03 "CI".124875E-01 0.

'CH".113867E+00 0.

'PS".872413E+00 0.

'TE".116576E-05 O.

'SR".503983E-03 0.

'Itu" 722061E-03 0.

'LA" 513386E-05 O.

5662E+01

.T.

.5289E-04

.7729E+00 3000E+01 0.

.T.

.5289E-04

.7729E+00

.3000E+01.201218E+03 "CI".217531E-01 0.

'CH".180406E+00 0.

'PS".796170E+00 0.

'TE".848854E-06 0.

"SR".712930E-03 0.

8 Ellu".948785E-03 0.

'LA".779073E-05 O.

.9059E+01

.T.

.6303E-04

.6902E+00

.3000E+01 C.

.T.

.6303E-04

.6902E+00

.3000E+01.300000E+03 "CI".338627E-01 0.

'CH".253797E+00 0.

'PS".710011E+00 0.

"TE".870171E-06 0.

'SR".104657E-02 0.

'RU".126957E-02 0.

'LA".123024E-04 0.

.1875E+04

.T.

.5513E-05

.5029E+00

.3000E+01 C.

.T.

.5513E-05

.5029E+00

.3000E+01.420000E+03 "CI".342790E-01 0.

'CH".215399E+00 0.

"PS".741705E+00 0.

eTE".858649E-03 0.

SR".394317E-02 0.

RU".375910E-01 0.

'LA".560976E-04 0.

6 0

4 O

iM t

DATE: MARCH.1985

TRAPMELT 2 TEST DATA SETAND TRAPMELT2 DETERMINED RETAINED MASS (KG) 0F THE FOLLO TE COR$0R PREDICTED RELEASED MASS (KG)

CH PS TIME RET TDT DET TOT RET TDT RET

' TOT RET TOT CI I2

.1010C+03

.6763E-04.1958E+01

.1265E+00.4010E+01 1099E+01.3065E+02 4809E+02.2402E+03

.2863E-01.1173E+00

.2012E+03 34040-OJ.3573E+01

.1072E+01.7316E+01 8372E+01.5003E+02

.1477E+03.3287E+03

.1033E+0D.2432E+00

.3000E+03 8114C-03.5098E+0f

.2681E+01 1044E+02

.1953E+02.6834E+02

.2395E+03 4076E+03

.1988E+00.3920E+00 DATE: MARCH,1985

TRAPMELT 2 TEST DATA SETAND TRAPMELT2 DETERMINED RETAINED MASS (KG) 0F THE FOLL 1

NG CORSOR PREDICTED RELEASED MASS (KG)

LA RU SR TIME RET TOT RET TOT RET TOT

.1018E+03 4097E-01.3041E+00

.5535E-01.3892E+00 4418E-03.3435E-02

.2012E+03

.2240E+00.7426E+00

.2728E+00.8355E+00

.2632E-02.9197E-02 3000E+03

.5493E+00.1438E+01

.6080E+00.1456E+01

.6806E-02.1945E-01

?.

M

s o*

NRC PORM 335 U.s. NUCLEAR REGULATORY COMMISSION

" 8 NUREG/CR-4205 BIBLIOGRAPHIC DATA SHEET BMI-2124

3. TlTLE AND SUBTITLE (AWW Vakame No., sf esprepriser)

2. (Leere alan 41 8

l TRAP-MELT 2 User's Manual

3. RECIPIENT S ACCESSION NO.

7. AUTHORLS)

5. DATE REPORT COMPLETED M ON TH lYE.R H. Jordan and M. R. Kuhlman March 1985

9. PERFORMING ORGANIZATION NAME AND M AILING ADDRESS (Inctum Z,a coolel DATE REPORT ISSUED MONTH l vE R Battelle's Columbus Laboratories May 1985 505 King Avenue 6.(tes e alaani Columbus OH 43201-2693

8. (Leare stank)

12. SPONSORING ORGANIZATION NAME AND MAILING ADDRESS (inclue Inp Cocle;

10. PROJECT / TASK / WORK UNIT NO.

Fuel Behavior Branch

u. CONTRACT NO.

U.S. Nuclear Regulatory Comission Washington, D.C.

20555 NRC-04-80-177

13. TYPE OF REPORT PE RIOD COVE RED (inclusive daers/

Code user's guide

15. SUPPLEMENTARY NOTES

14. (Leave alai &)

16. ADSTR ACT G00 words or leu)

The TRAP-MELT 2 code is a development of the previously issued TRAP-MELT code which simulates the transport and deposition of aerosol particles and certain vapors in the reactor coolant system under hypothetical accident conditions in a light water reactor. This manual contains a brief description of the models of the processes treated in the code and of the code organization.

The input to the code for a sample run are presented and output from a run

{

are presented as well.

l

17. KEY WORDS AND DOCUMENT ANALYSIS 17a. DESCRIPTORS Fission product transport Light water reactor accident analyses Reactor coolant system models 17b. IDENTIFIE RS/OPEN EN DE D TERMS tf: AVAILABILITY STATEMENT

19. SECURITY CLASS (This report)

21. NO. OF P AGES IIncl acti fie d Unlimited

20. SECURITY CLASS (This papel

22. P RICE Unclassified s

NRC PORM 335 (7 771

___

ML20133C540

Contents

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Enclosure:

Dear Mr. Felton:

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ML20133C540

Text

Dear Mr. Sholly:

Enclosure:

Dear Mr. Felton:

98.00 SEDIMENTATION AREA (FT2)

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