ML20064C783

Single Tube Condensation Test Program

ML20064C783
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Issue date:	03/31/1994
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NEDC-32301, NEDC-32301-R, NEDC-32301-R00, NUDOCS 9403100218
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GE Nuclear Energy NEDC-32301 Revisioni O Class 2 March 1994

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l Single Tube Condensation

Test Program i

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1 l W. R. Usry 1,

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9403100218 940302 PDR ADOCK 05200004 A PDR

GE Nuclear Energy Genem,ewu cu ver 175 Cunw Avenue SanJaw CA 95!?5 NEDC-32301 Resision 0 Class 2 March 1994 l

l l Single Tube Condensation Test Program W. R. Usry 1

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Reviewed: N N' 'b T. ft.'McIntyre, project Manager SBWR Test Operations & Analysis Approved:_ Mhb P. W. Marriott, Manager t-Advanced Plant Technology

NEDC-32301 DISCLAIMER OF RESPONSIBILITY This document was prepared by the General Electric Company (GE). No other use, direct or indirect, of the document or the information it contains is authorized; and with respect t.o any unauthorized use, GE does not make any representation or warranty (express or implied) as to the completeness, accuracy, or usefulness of the information contained in this document or that such use of such information may not infringe privately owned rights; nor does GE assume any responsibility for liability or damage of any kind which may result from such use of such information. Furnishing this document does not convey any license, express or implied, to use any patented invention or any information of GE disclosed herein, or any rights to publish the document without prior written permission of GE.

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NEDC-32301 ABSTRACT l

l An experimental program was conducted to investigate steam condensation inside of tubes in the presence of noncondensables. The work was conducted at UC Berkeley and at MIT. The work was initiated in order to obtain a database and a correlation for heat transfer in similar conditions as would occur in the SBWR PCCS tubes during a DB A LOCA. Three researchers utilized three separate experimental configurations at UC Berkeley, while two researchers utilized one configuration at MIT. The researchers ran tests with pure steam, steam / air, and steam / helium with flowrates and noncondensable mass fractions representative and bounding of a DBA LOCA. The experimenters found the system to be well behaved for all tests with either of the noncondensables for forced flow conditions similar to the SBWR design. The results of the first test at UC Berkeley became the basis for the correlation used currently in the computer code TRACG. Recent tests at UC Berkeley have shown that the version of the correlation installed in TRACG generally overpredicts the gas-side heat transfer. A correlation based on the latest Berkeley data was used to show that the latest data do not significantly impact the containment performance. The testing at the two universities will be complete in early 1994. This document summarizes the testing programs completed previously and includes some results from the current UC Berkeley work.

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ACKNOWLEDGMENTS j

i The single tube condensation tests were conducted by students and staff at the University of California at Berkeley and at MIT. The author has learned much from his i interactions with Professors V. E. Schrock and M. W. Golay. Their efforts in assisting with the preparation of this repon, which will support SBWR design cenification in the U.S., have been invaluable. In addition, the efforts of Joseph Kuhn and Professor P.

Peterson to help meet the deadline of this report are appreciated. The reviews and subsequent comments by Jim Fitch and Jens Andersen were invaluable and are also appreciated.

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NEDC-32301 l TABLE OF CONTENTS '

Page Abstract iii Acknowledgments iv Nomenclature vi

1. INTRODUCTION 1-1 1.1 Background 1-1 1.2 Necessity of Test Program 1-2 1.3 Scope ofTesting 1-2 1.4 Status of Test Program 1-3

2. TESTS 2-1 2.1 Vierow 2-1 2.2 Siddique 2-5 2.3 Ogg 2-9 2.4 Kuhn 2-11

3. CORRELATIONS 3-1 3.1 Vierow and Schrock ("Tsukuba") 3-1 3.2 TRACG 3-2 3.3 Siddique 3-3 3.4 Ogg 3-3 3.5 Vial 3-4 3.6 Kuhn 3-6 i

4. DISCUSSION 4-1 l 4.1 Impact on TRACG Analysis 4-1 4.2 Applicability of Kuhn Correlation to IC Tubes 4-1

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SUMMARY

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6. REFERENCES 6-1 i APPENDIX - KUHN DATA USED FOR PRESSURE A-1 DROP CALCULATION l l

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NEDC-32301 i

NOMENCLATURE 1

Symbol Description b constant C constant c specific heat at constant pressure If Diameter (no subscript indicates inner diameter) f degradation factor fR friction factor i g gravity force h heat transfer coeflicient hr, latent heat of vaporization hrg' modified latent heat ofvaporization

HP horsepower i ID inside diameter  !

Ja Jakob number = Cpm /(Tb -Tw)/hrg

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, k thermal conductivity i

, L length Ma noncondensable gas mass fraction 4 MIT Massachusetts Institute of Technology i N number of data points .

Nu Nusselt number = hD/k m OD outside diameter P pressure q"(x) local heat fiux as a function of x R thermal resistance Re Reynolds number (defined in text) l s standard deviation l T temperature UCB University of California at Berkeley i V,v Bulk velocity, local velocity i W mass flow rate x axial coordinate along condensing surface referenced to the top X mole fraction z axial coordinate in the coolant annulus Greek Letters Si condensate film thickness assuming no interfacial shear 62 condensate film thickness assuming interfacial shear F condensate mass flow rate per unit width I shear p mass density p viscosity v kinematic viscosity = /p 4 function vi

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j NOMENCLATURE i

(Continued) l Subscripts a air or other noncondensable a adiabatic wall b bulk c coolant Cw Cooling water e est eff effective exp from experiment ,

f film l l g gas )

i inner or interface

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1 liquid m mixture l 0 outer I ref reference at saturation t turbulent v vapor w or W wall Win inner wall Wo outer wall z axial direction l

Acronyms hte heat transfer coeflicient DBA Design Basis Accident LOCA Loss of Coolant Accident SBWR Simplified Boiling Water Reactor SSAR Standard Safety Analysis Report Vil

NEDC-32301 LIST OF TABLES Page 2.1-1 Test Matrix for Vierow 2-15 2.2-l a Test Matrix for Air / Steam Runs of Siddique 2-16 2.2-lb Test Matrix for Helium / Steam Runs of Siddique 2-17' 2.3-la Test Matrix for Air / Steam Runs of Ogg 2-18 2.3-lb Test Matrix for Helium / Steam Runs of Ogg 2-19 2.4-la Test Matrix for Pure Steam Runs ofKuhn 2-20 2.4-lb Test Matrix for Air / Steam Runs ofKuhn 2-21 2.4-Ic Test Matrix for Helium / Steam Runs of Kuhn 2-22 s

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i i NEDC-32301 l LIST OF FIGURES i

Page 2.1-1 a Schematic of Vierow [1990] Experiment (Used with 2-23 permission) j 2.1-lb Key to System Schematic of Vierow [1990] Experiment 2-24 (Used with permission) 2.1-2a Experimental Instrumentation of Vierow [1990] Experiment 2-25 (Used with permission) 2.1-2b Key to Experimental Instmmentation of Vierow [1990] 2-26 experiment (Used with permission) 2.1-3 Typical Steady-State Condenser Tube Wall Temperatures for 2-27 l

Vierow [1990] Experiment (Used with permission)  !

2.1-4 Sample Thermocouple Time Records for an Oscillatory Run 2-28 of Vierow [1990] (Used with permission) 2.2-1 Schematic of Siddique [1992] Experiment (Used with 2 29 permission) l 2.2-2 Test Section and Thermocouple Configuration for Siddique 2-30

[1992) Experiment (Used with permission) i 2.2-3 Detail of Test Section Instrumentation for Siddique [1992) 2-31 Experiment (Used with permission) l 2.2-4 Plot of Heat Transfer Coeflicient as Predicted by the Siddique 2-32 l Correlation and the Vierow [1990] Correlation (not Vierow and Schrock) Versus Mixture Bulk Air Mass Fraction (Taken from Siddique [1992] and used with permission) l 2.2-5 Ratio of Nusselt Numbers When Helium is Present Versus When 2-33 Air is Present Plotted Versus the Mole Fraction of Noncondensable Gas (Taken from Siddique [1992] and used with permission) 2.2-6 Ratio of Nusselt Numbers When Helium is Present Versus When 2-34 Air is Present Plotted Versus the Mass Fraction of Noncon-densable gas (Taken from Siddique [1992) and used with permission) 2.2-7 Detailed Sketch of the Upper Part of Siddique's [1992] Test 2-35 Section (Used with permission) ix

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NEDC-32301 Page 2.3-1 System Schematic of Ogg [1991] Experiment (Used with 2-36 permission) j 2.3-2 Typical Temperature Profiles from Ogg [1991) (Used with 2-37 permission) 2.4-1 General Schematic Drawing of Kuhn et al. [1994] Experimental 2-38 Apparatus 2.4-2 Sketch Showing the Condensing Tube Thennocouple Installation 2-39 in Kuhn et al. [1994]

2.4-3 Test Section Thermocouple and Spacer Locations for Kuhn 2-40

, et al. [1994] Experiment 3.1-1 Data Plotted in the Form of the Vierow-Schrock [1991] 3-13 Correlation. The Factor 1-f/f iis Plotted Versus Local Air Mass Fraction (Used with permission) 3.3-1 A Comparison of the Air / Steam Nusselt Numbers Produced by 3-14 the Siddique [1992] Correlation Versus the Experimental Nusselt Numbers (Used with permission) 3.4 1 A Comparison of the fi Correlations of Vierow and Schrock 3-15

[1991) and Ogg (1991] Plotted Against Mixture Reynolds number d

3.4-2 Comparison of the f2 Correlation of Vierow and Schrock [1991] 3-16 and Ogg Plotted Against Air Mass Fraction 3.5-1 Plots of the Vierow (1990] and Ogg [1991] Data Plotted Along 3-17 with the Vial Correlation 3.5-2 Plots of Both the Siddique [1992] Data and the Combined Data 3-18 Base Along with the Vial Correlation 3.6-1 Plots of f /fi ishear Versus Film Reynolds Number for the 3-19 Pure Steam Data of Kuhn et al. [1994]

3.6-2 Plot of the Kuhn Steam / Air Data Along with the Kuhn et al. 3-20

[1994] Correlation for 6S Steam / Air Runs (The ordinate is equivalent to 1- f2 )

3.6-3 Plot of the Steam / Air Mixture Experimental Degradation Factor 3-21 Versus the Degradation Factor Predicted by the Kuhn et al.

[1994] Correlation X

NEDC-32301 Page 3.6-4 Plot of the Kuhn Steam / Helium Data Along with the Kuhn et 3-22 al. [1994] Helium Correlation for 24 Steam / Air Runs (The ordinate is equivalent to 1- f2 )

3.6-5 Plot of the Steam /llelium Mixture Experimental Degradation 3-23 Factor Versus the Degradation Factor Predicted by the Kuhn et al. [1994] Helium Correlation 3.6-6 Plot of the Heat Transfer Coemeient Predicted by the Kuhn et 3-24 al. [1994] Steam / Air Correlation Versus the Heat Transfer Coemeient Predicted by the Vierow and Schrock Correlation 3.6-7 Comparison of the f2 Correlation of Vierow and Schrock and 3-25 Kuhn et al. [1994] Plotted Against Air Mass Fraction 3.6-8 Plot of the Heat Transfer Coemeient Predicted by the Kuhn et 3-26 al. [1994] Steam / Air CorTelation Versus the Heat Transfer Coemcient Predicted by the Correlation Currently in TRACG 3.6-9 Plot of the Heat Transfer Coemcient Predicted by the Kuhn 3-27 et al. [1994] Steam / Air Correlation Versus the Heat Transfer Coemcient Predicted by the Vial Correlation 3.6-10 Plot of the Heat Transfer Coemeient Predicted by the Kuhn et 3-28 al. (1994] Steam / Air Correlation Versus the Heat Transfer Coemeient Predicted by the Ogg Correlation 3.6-11 Plot of the Heat Transfer Coemcient Predicted by the Kuhn et 3-29 al. [1994] Steam / Air Correlation Versus the Heat Transfer Coemcient Predicted by the Chen [1987] Correlation xi

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NEDC-32301 1  !

l 1. INTRODUCTION i

Investigations by the University of California at Berkeley (UCB) and by ,

Massachusetts Institute of Technology (MIT) have been conducted in order to experimentally investigate thermal-hydraulic conditions similar to those that will occur in the tubes of the SBWR Passive Containment Cooling System (PCCS) condensers. A correlation of the data is used in the code TRACG to help predict the performance of the SBWR PCCS. This report describes and summarizes the test programs and their results to date. Reporting details of data and the various apparatus is not within the scope of this report. That information is best described first hand by the original authors Vierow l

[1990], Vierow and Schrock [1991), Siddique [1992), Ogg [1991), Schrock et al. (1994],

and Kuhn et al. (1994]. This report summarizes results of each of the programs with reference to the SBWR design and in light of the increased knowledge available at the writing of this report.

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1.1 Background

The PCCS is a post-LOCA, low pressure, decay heat removal system of the SBWR as described in Wilkins et al. [1992] and Vierow et al. [1992]. It is designed to remove decay heat from the containment and maintain pressure and temperature at or below design limits for a minimum of three days. A large volume suppression pool j absorbs the energy released in the initial blowdown phase and limits the initial containment l pressure rise. The PCCS condensers remove essentially all of the decay heat during the long-term phase.

The PCCS condensers are bundles of vertical tubes attached to an inlet header at the top and a discharge header at the bottom. They are located in a large pool of water outside the containment boundary and represent an extension of the boundary. Each PCCS tube receives a steam and noncondensable gas mixture from the drywell and condenses the steam. The condensate flows down to a Gravity-Driven Cooling System (GDCS) pool, while the remaining gas flow is vented to the suppression pool. The gas flow to the heat exchanger is driven by the combined effects of condensation and the pressure difference between the dnpvell and the suppression pool pressure at the depth of the vent line (0.75m nominally). Thus, in general, the flow through the tubes is forced flow and not natural circu'ation driven.

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1.2 Necessity of Test Program The PCCS tubes are an essential part of the SBWR passive heat removal systems.

In order to develop and qualify modeling tools which evaluate the performance of the I overall system, experimental data are needed. Before the initiation of this investigation, experimental data for steam condensation inside of tubes in the presence of noncondensables were rare. The data that were available only showed average heat transfer results. To make appropriate use of detailed thermal-hydraulic codes, such as TRACG, requires correlation of local heat transfer data. An understanding of steam condensation in the presence of noncondensables necessitates that local quantities such as noncondensable mass fractions, local condensate flow rate, and local heat flux be resolved.

1.3 Scope of Testing The intent of this experimental program was to obtain a base oflocal heat transfer data for the range of steam /noncondensable flows expected in a DBA LOCA. This database has been used to develop a correlation suitable to TRACG and other codes and to support the evaluation of post-LOCA performance of the SBWR containment. The tubes used in the tests were prototypical in size, with the exception of the initial test at UC Berkeley, which had a 1-inch diameter tube instead of a 2-inch diameter tube.

The noncondensable gas that would be present in a DBA LOCA would be essentially all nitrogen from the inert containment atmosphere (negligible quantities of hydrogen and oxygen are produced by radiolysis). Under severe accident conditions, hydrogen may be produced by a steam-zircaloy reaction. For safety reasons and for experimental ease, these noncondensables were represented by air and helium, respectively. Air and helium have similar properties to nitrogen and hydrogen, respectively, and are expected to closely mimic the effects of nitrogen and hydrogen on the condensation process. The pressure range for the experiments was from 0.03 to 0.51

MPa (0.3 to 5 atm.). The inlet steam flowrates ranged from 8 to 73 kg/hr. The air inlet mass fractions ranged from 0 to 0.40 while the helium mass fractions ranged from 0 to 0.15. The cooling side of the heat exchanger was accomplished by forced convection of subcooled water.

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NEDC-32301 1.4 Status of Test Program The tests conducted at UC Berkeley and MIT were scheduled for completion in October 1993. This report was intended to be the final repon on the subject. However, both universities experienced delays, largely caused by equipment failures. Both universities have fmished taking data and are in the process of reducing and analyzing the data. UC Berkeley will issue a final report in April 1994 and MIT will issue a report on their current work in the first half of calendar 1994. This present report includes much of the results of the latest UC Berkeley work.

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2. TESTS 1

Three separate series of tests were conducted at UC Berkeley and two series of tests were conducted at MIT. What follows in this chapter summarizes the equipment and the results of these tests. A more detailed discussion may be found in the appropriate references (Vierow [1990], Vierow and Schrock (1991], Siddique [1992], Ogg [1991],

Schrock et al. [1994] and Kuhn et al. [1994]).

2.1 Vierow (UC Berkeley)

The first test program was performed by K.M. Vierow at UC Berkeley. The experiment utilized a natural circulation loop with a 1-inch diameter copper condensing tube. Detailed documentation and results may be found in Vierow [1990] and Vierow and Schrock [1991].

2.1.1 Apparatus The experimental facility had the following basic components: pressure vessel / boiler; steam inlet lines; lower plenum; riser; condensing test section; condensate drain system; and instrumentation. Figure 2.1-1 shows a schematic of the system and Figure 2.1-2 illustrates the instrumentation. With the exception of the drain line, all components were insulated in order to minimize heat loss. The body of the electrically heated boiler was a 2.74m long,12-inch (0.305m) IPS (International Pipe Standard)

Schedule 5 stainless steel pipe. A 12-inch (0.305m)IPS Schedule 10 pipe cap was welded i to the top and the bottom. A blowdown line consisted of a 1.27 cm outside diameter (OD) stainless steel tube that led to a water-filled reservoir. The pressure relief valve was i l

set to open at 100 psig. The air intake line was taken off the blowdown line, upsteam of the relief valve.

Three immersion heaters were installed through a 6.4 cm coupling at the bottom of the pressure vessel. The heaters were 1 cm OD stainless steel, sheathed Calrod type I

heaters. The heaters were able to produce a combined power level greater than 20 kW, which was the maximum power used in this experiment. Steam was carried from the boiler to the lower plenum by a 2.54 cm OD stainless steel tube. The lower plenum was used to mix steam with air before entering the test section. The steam / air mixture exited the plenum and entered a riser made of 5.08 cm tube,2.41m in length. The mixture then 2-1 i

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NEDC-32301 passed through two 900 bends and entered the condensing test section. The test section consisted of a double-pipe, concentric-tube heat exchanger. The inner tube through which the steam / air mixture flowed was a 2.21 cm ID,2.54 cm OD copper tube of 2.39m length, )

0.25m of which was not available for condensation. The condensate and the noncondensables exited the test section into the lower plenum through the downcomer.

The condensate flowed out through a double-pipe, concentric-tube heat exchanger and into a graduated cylinder. The noncondensables were recirculated with incoming steam back through the test section.

The coolingjacket was constructed of four sections of approximate length 0.5m of 5.08 cm stainless steel tubes flanged together. The flanges extend out from the tube on both the inside and the outside. The outside sections were bolted together. The inside sections of the three pairs of flanges had a 2.59 cm inner diameter to allow the flanges to just slide over the condenser tube. Each side of the flange pairs had 12 0.715 cm diameter holes spaced equally around the flange. The flange pairs were separated by a small distance and the holes were intentionally misaligned in order to promote mixing. The cooling water entered the bottom of the cooling annulus through custom-made heat exchanger fittings and exited at the top. The coolant flow rate was controlled to provide nearly complete steam condensation and also maintain a coolant temperature rise suflicient to determine local heat transfer rates.

All thermocouples were copper-constantan (T-type) except for six iron-constantan (J-type) in the boiler. The thermocouples used to measure fluid temperatures were 24-gauge, 0.159 cm OD, stainless steel Omega probes mounted through CONAX gland fittings sealed with Teflon disks. Nine thermocouples were mounted on the condenser tube outer wall. Three thermocouples measured the temperature in the cooling annulus afler each of the three flange pairs. These three thermocouples plus thermocouples in the coolant water inlet and outlet combined for a total of five coolant water measurements.

Pressure transducers were located in the lower plenum and at the top of the loop as shown in Figure 2.1-2.

In each of the experiments at the two universities, the calculation of the local heat transfer coeflicients was done in a similar manner. The local heat transfer coeflicient is defined as:

h(x) = q"(x)/ (Tsat(x)-Tw(x)) (2.1-1) 2-2

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NEDC-32301 where Tw(x) is the temperature of the inner wall of the condensing tube, Tsat(x) is the local (in the axial dimension only) saturation temperature of the steam / air mixture, and x is referenced to the top of the condensing section. The local heat flux, q"(x), is found from:

IV,c, dl;(x) q,,(x) = - (2.1-2) no, dx where Tb(x) is the bulk temperature of the cooling water at an axial location, W e is the coolant mass flow rate and cp is the specific heat at constant pressure of the coolant. The temperature Tsat(x)is not measured directly but must be determined by knowledge of the

, amount of steam that has condensed. The mass flow rate of the noncondensable remains constant along the length of the tube. The steam mass flow rate decreases because steam 1

is condensed. Thus, if the amount of steam condensed can be determined then the partial pressure of the steam (and therefore the saturation temperature) is known as a function of axial position. This assumes that the total pressure remains constant along the length of the tube. This is a valid assumption because the pressure drop through the condensing section is very small. A friction factor of 0.025 produces a pressure drop of 75 Pa for run 1.1-1 of Kuhn (data shown in Appendix). The condensate mass flow rate as a function of axial distance is:

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, II',c,( T,(0)- T,(x))

if'(x) = (2.1-3) is where h'rg is a corrected form of the heat of vaporization, hrg, to account for condensate subcooling:

4 h'rg = hrg + Constant cp(Tsat-Tw) (2.1-4)

The Constant quoted in textbooks and literature ranges from 3/8 to 0.68 and different constants were used with different experiments. The sensitivity of the results to the value of the Constant is small because the heat of vaporization is large compared with the correction part of the equation. The inner tube wall temperature is computed by a conduction correction from the outer wall temperature. The partial pressure of the steam

is now easily determined, which then specifies Ts at. Thus, h(x) can now be calculated.

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2.1.2 Discussion of Results 4

Vierow ran a total of 35 tests. A test matrix is shown in Table 2.1-1. In 18 of those tests the system reached a steady state and the condenser tube wall temperature monotonically decreased with distance from the entrance to the condensing section. In 12

tests which reached a steady state, the condenser tube wall temperature increased with distance from the entrance and then, between 24 and 48 cm downsteam, the temperature monotonically decreased to the cooling water temperature. This was termed a

" temperature inversion" and was an unexpected finding. Typical plots of cases with and without temperature inversions are shown in Figure 2.1-3. Temperature inversions occurred when the air mass fraction was low and were more in evidence as the heater

, power was increased. In three cases, system oscillations occurred during stanup with the system settling to a steady state, and in two cases oscillations occurred which did not die out. Both of these took place when the air content was high.

The flow oscillations are described in both Vierow (1990] and Vierow and Schrock [1991). Plots of tube wall and coolant outlet temperature with time are shown in Figure 2.1-4. While the flow oscillations are phenomenologically interesting, they are not l

applicable to the SBWR PCCS design. The Vierow experiment was a pure natural

< circulation driven flow (i.e., flow ceases when heat transfer ceases). The SBWR PCCS tube flow is forced circulation driven by the pressure difference between the drywell and the wetwell, even for small inlet noncondensable mass fractions.

The non-oscillatory runs from Vierow can be divided into those with temperature inversions and those without. A partial explanation of the temperature inversions is made in Vierow [1990] starting on page 59. Siddique at MIT [1992] and the latest tests at UCB, Kuhn et al. [1994) (both forced circulation experiments) do not repon the existence of such a temperature inversion. Schrock [1993] postulates that it is a result of the setup of the flow in a manner which appears to be unique to natural circulation. The data from runs with a temperature inversion were not included in the Vierow-Schrock correlation

("Tsukuba" correlation), discussed in Section 3.1, on the above-mentioned basis that they are inapplicable to the SBWR with its forced venting mechanism.

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NEDC-32301 2.1.3 Experimental Uncertainties The two most prominent uncertainties in this experiment were: (1) determining the inlet air mass fraction and, (2) determining the coolant bulk temperature. In order to obtain the air mass fraction at the condenser entrance, the air holdup was determined from approximate calculations as explained in Vierow [1990]. This likely contributes to the data scatter shown in Section 3.1. There is also some uncertainty in the determination of the coolant bulk temperature from the available temperature measurements. The procedure relies on the flow becoming well-mixed due to the fluid having to flow through pairs of flanges with non-aligned holes. One helpful bit of knowledge gained from this experiment was insight on the axial shape of the heat flux curve. As a result, subsequent UCB tests used a nonuniform thermocouple spacing with measurements concentrated near the entrance, where most of the condensation occurs.

2.2 Siddique (MIT)

Siddique at MIT also investigated steam condensation inside tubes in the presence of noncondensables. He utilized a forced flow system with a 2-inch diameter condensing tube. Detailed documentation and results may be found in Siddique [1992].

2.2.1 Apparatus The experimental facility has the following basic components: pressure l vessel / boiler; steam inlet lines; condensing test section; condensate drain system; throttle i valve; and instrumentation. Figure 2.2-1 shows a schematic of the whole system and Figure 2.2-2 illustrates the test section. The electrically heated boiler was a cylindrical stainless steel vessel 4.5m high by 0.45m inside diameter. Power was supplied by four immersion type sheathed electrical heaters, each nominally rated at 7 kilowatts. A high precision wattmeter measured the power input to the boiler. The noncondensables were l supplied to the base of the boiler through a pressure regulating valve, a calibrated rotameter, and a flow control valve. Mixing of the steam with the noncondensable gas was achieved in the boiler vessel. The steam / gas mixture left the vessel through an isolation valve located near the top of the vessel. The mixture temperature, pressure and l flowrate were measured before entering the test section. The condenser tube was a stainless steel tube with a 50.8 mm OD and a 46.0 mm ID and 2.54m in effective length.

Condensate was collected in the condensate separator / collector drum. The l

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I NEDC-32301 noncondensable gas and the uncondensed steam, if any, were vented from this drum to the to the atmosphere via a throttle valve. The cooling jacket was constructed of 62.7 mm ID stainless steel (SS) tubing. As in Vierow, the cooling water flowed upward through the annulus, while the steam /noncondensable mixture flowed downward through the condensing tube. The cooling water was pumped through the test section and then to a drain after passing through a rotameter and a flow control valve. To prevent thermal stresses, a sliding 0-ringjoint at the lower end of the condenser was used to allow relative movement between the condenser tube and the coolingjacket tube.

All thermocouples were iron-constantan (J-type). Temperature measurements were made of the inside and outside condensing tube wall temperature and of the cooling water at nine locations spaced 30.5 cm apart along the length of the condenser.

Temperature measurements of the gas mixture were also made along the centerline of the condenser, but were not used in the data reduction. The inner wall thermocouples were 0.8 mm OD SS sheathed probes embedded in drilled holes filled with silver solder. The holes entered the tube wall at an angle and were drilled so as to locate thejunction of the thermocouple at less than 0.2 mm from the inner surface of the tube wall. The outer wall thermocouples were the same type of probes as the inner wall probes and were each embedded in a longitudinally machined groove with the dimensions 0.9 mm wide by 0.4 mm deep and 12.7 mm in length. The hole was brazed with silver solder. All of the tube wall thermocouple leads entered the test section at the top and were strung through the coolingjacket annulus to the axial location for that particular thermocouple. Details of the thermocouple locations are shown in Figure 2.2-3.

i The cooling water temperature measurements were made using a 1.6 mm OD SS sheathed rigid thermocouple probe that was inserted through the cooling jacket shown in Figure 2.2-3. In order to get an accurate measure of the bulk coolant temperature, good mixing was required in the annulus. The easiest way of accomplishing this is to supply I cooling water at a rate so that the flow is turbulent within the annulus. However, for this configuration, the flowrates required would not have allowed a sufliciently large temperature difference between the inlet and outlet coolant flow water. Siddique's solution to this was to bubble in small amounts of air through the annulus so that good mixing could be accomplished while achieving a large enough coolant water temperature rise. Siddique did not specify the amount of air which was added to the water.

Measurements of the inlet and outlet cooling water temperature were also made.

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NEDC-32301 The data reduction methods used by Siddique are similar to those used by Vierow (as explained in Section 2.1.1). Thermocouples located on both the inside and the outside of the condenser tube wall were intended to be a redundant method of obtaining the heat flux through the wall. However, large scatter in the tube outer wall temperature measurements occurred and the method was abandoned.

2.2.2 Discussion of Results Siddique ran 52 air / steam and 22 helium / steam tests. He reported neither oscillations in the test experiment nor a temperature inversion. His inlet air mass fractions ranged from 0.09 to 0.42. A test matrix is shown in Table 2.2-la and 2.2-lb.

Comparisons of heat transfer coeflicients of Siddique and those produced from the l correlation in Vierow [1990] are shown in Figure 2.2-4. Note that the correlation used I for comparing the UCB data is not the "Tsukuba" correlation of Vierow and Schrock [1991], but is an unpublished correlation from Vierow's thesis. 1 Notwithstanding, it is still useful for this comparison. It is clear from both plots that the I MIT data predict much higher heat transfer coeflicients than does the correlation in Vierow (1990]. This will be explored in more detail in Section 2.2.3.

Siddique tested helium / steam mixtures as well as air / steam mixtures. He reported that, for the same mass fraction, helium degrades the heat transfer more than does air. For j the same mole fraction, air degrades the heat transfer more than does helium. This is a useful, but not a surprising result. The gas-side heat transfer is controlled to a large extent by the partial pressure of steam near the condensate / gas interface. The lower the partial i

pressure of steam is (for a given total pressure), the lower the heat transfer will be. The partial pressure of steam at the interface is controlled by the partial pressure (or equivalently volume fraction and therefore mole fraction) of the noncondensable gas at the interface. This, in turn, is controlled by two factors: (1) the bulk amount of the noncondensable gas in moles and (2) its ability to diffuse away from the interface.

Because helium has near an order of magnitude greater moles per unit mass than does air, one would expect it to degrade the heat transfer more than air does on a mass basis. As i steam condenses, a concentration gradient of noncondensable gas appears near the condensate / gas mixture interface. The ability of the noncondensable to diffuse in steam will then determine the partial pressure of the noncondensable at the interface for a given bulk molar fraction. Therefore, a gas that diffuses well in steam will degrade steam I

2-7

NEDC-32301 condensation heat transfer less than a gas that diffuses poorly. Helium diffuses much better than air in steam and, as a result, does not degrade heat transfer as much as air does on a molar basis.

Plots comparing the ratio of Nusselt numbers of the system nm with helium and the system run with air are shown in Figures 2.2-5 and 2.2-6. Siddique did not experience any differences running the system with helium versus air. No unusual profiles, no transients, and no stalling were reported.

2.2.3 Experimental Uncertainties Data from the current tests at MIT (not presented in this report) as well as analysis of Siddique's data at UCB reveal some questions about the data reduction which resulted in large heat transfer coefficients near the entrance of the tube. In analyzing the data for the Vial correlation (Section 3.4), UCB discovered that Siddique extrapolated the coolant temperature at the upper end of the test section. The first cooling jacket thermocouple was located at a distance of 41 cm from the entrance of the tube. Siddique reported condenser tube wall temperatures at a distance of 10 cm from the inlet but did not report a coolant water temperature. He took the bulk temperature of the coolant at x = 0 to be the value recorded by the thermocouple located on the coolant exit pipe. It was not clear that this was indeed measuring the bulk temperature of the coolant. Trying to fit a coolant temperature curve for x < 41 cm using the coolant exit temperature was difficult to justify, and thus only the data at locations greater than or equal to x = 41 cm were included in the Vial correlation. Golay [1993] agreed to this treatment of the data. With this data excluded, the large differences in heat transfer near the entrance of the tube (Figure 2.2-4) are eliminated. Possible additional sources of error not reported by Siddique are: (1) uncertainties in obtaining the bulk coolant temperature measurements and (2) design problem associated with the coolant flow outlet.

Siddique's method ofinjecQg air bubbles into the coolant to promote turbulence is a reasonable procedure but the documentation of the experiments does not provide suflicient detail for a complete evaluation. A detailed evaluation is included in the current MIT experiment. Another possible concern about obtaining the bulk coolant measurements is that all the thermocouple leads for the condenser tube wall are led up through the annulus and exit at the top. This is a problem which is diflicult to avoid, but 2-8

NEDC-32301 nevertheless, the leads can potentially disturb the flow and possibly cause stagnant regions near the condenser tube.

Figure 2.2-7 shows details of the test section upper end. The figure shows that there is a region above the coolant outlet where cooling may take place. An improved design would have the coolant outlet flush with the top end of the available condensing tube. The problem is compounded by the possibility that air may collect at the top of the coolant annulus and inhibit heat transfer. Also like Vierow, the coolant outlet is located at only one circumferential location. This could affect the coolant hydrodynamics near the coolant outlet (and inlet) resulting, in erroneous bulk temperature measurements.

2.3 Ogg (UCB)

Ogg at UC Berkeley utilized a forced flow system with a 2-inch diameter condensing tube. Detailed documentation and results may be found in Ogg [1992].

2.3.1 Apparatus The apparatus in Ogg's experiment consisted of a campus steam supply system, a

. gas supply system, test section, separator, cooling water system, piping, and instrumentation and data acquisition system. A schematic of the overall system is shown in Figure 2.3-1. The steam was supplied by the 120 psig UC Berkeley campus steam system. Air was supplied by a 100 psig building air supply and the helium was supplied from high pressure cylinders. The steam and the noncondensable gas each flowed through separate 1-inch (2.54 cm) IPS lines with metering sections for both high flow rates for low flow rates. Downstream of the metering sections, the gas and the vapor were mixed and were delivered to the test section.

The condensing tube was a 3.5m long 5.08 cm 321 stainless steel tube with a 0.071 cm wall thickness. To provide an adiabatic entrance length, the top 0.787m was insulated. The bottom 0.278m of the tube was also not available for condensation, which left 2.44m for the active length. Like Vierow and Siddique, forced convection cooling water flowed upward in the annular space between the condensing tube and a cooling waterjacket. Thisjacket was constructed from five sections of 6.35 cm OD stainless steel tubing with a 0.305 cm wall thickness. These sections were flanged together in a similar manner as Vierow. The flanges formed mixers which were just upstream of a cooling 2-9

NEDC-32301 water thermocouple. An outlet plenum mounted at the bottom of the test section directed the condensate, the noncondensable gas and any uncondensed steam to the separator.

Separation of the condensate from the gas phase was accomplished with a 1/2-inch (1.27 cm) Armstrong float trap, which only allowed liquid to pass. Measuring the condensate flow rate served as a check of the steam metering system.

A 3/4 HP centrifugal Grundfos pump supplied the cooling water to the cooling water jacket. The cooling loop also supplied water to cool the condensate. Afler exiting the top of the cooling jacket, the water was cooled by a shell and tube heat exchanger.

The system was a closed loop in order to conserve water.

Sixteen copper-constantan (T-type) thermocouples were used to collect temperature measurements in the experiment. Ten were brazed to the outside condensing tube wall and were spaced in a logarithmic manner along the length of the tube. The remaining six thermocouples were stainless steel sheathed and were placed afler the flanges inside the cooling water annulus. The spacing was also logarithmic with the closer spacing at the top of the test section. All the thermocouple wires entered the test section through the nearest flanged section. The data reduction methods used by Ogg were similar to those used by Vierow (as explained in Section 2.1.1). Ogg also had a movable wet bulb probe, but the measurements were not used in the data reduction.

2.3.2 Discussion of Results The full test matrix is shown in Table 2.3-1. Ogg reports that the system operation was very well behaved for all flow conditions. No oscillatory behavior was observed.

Ogg states that the most notable phenomenon present in the experiment was the condenser tube wall temperature inversion at the test section inlet. A typical profile is shown in Figure 2.3-2. The temperature inversion in Vierow [1990] was only present for cases of low air mass fractions. In Ogg, the inversion occurred in virtually all of the cases and it was of a different shape than that of Vierow. The Ogg data show an initial decrease in tube wall temperature followed by a peak then a decline. Vierow's inversion had an initial increase followed by a decrease. Ogg, like Siddique, found that the degradation in heat transfer on a molar basis with helium was less than the degradation caused by air. A comparison of the Ogg data with Vierow data will be made by comparing the correlations in Section 3.3.

2-10

NEDC-32301 2.3.3 Experimental Uncertainties and Analysis The Ogg results were never published or presented in any journal or conference because of some inconsistencies in the results. Some of the runs, particularly the pure steam runs, lacked reproducibility. Thus, the if correlation of Ogg is not viewed with a high degree of confidence. In addition, upon teardown of the Ogg test section, it was noticed that a thermocouple on the condenser tube wall had come loose. The results are relevant, but should be viewed with some skepticism. Lessons learned from this experiment provided the basis for improvements which were applied to the final tests done at UC Berkeley by Kuhn et al. [1994].

2.4 Kuhn (UCB)

J. S. Z. Kuhn, under the direction of Professor Schrock and Professor Peterson, sought to construct an experiment which incorporated all the lessons learned from Vierow, Siddique, and Ogg. Detailed documentation will be found in Kuhn et al. [1994].

2.4.1 Apparatus The steam supply system and the data acquisition instrumentation were nearly identical to that of Ogg. An additional steam trap was put on the steam supply line in order to insure that all the moisture was removed. Most of the differences were found in the test section. The general schematic is shown in Figure 2.4-1.

In the Ogg experiment, the condenser tube wall bare thermocouple jusiiaa were brazed to the outer wall. In Kuhn's experiment, thermocouples were inserted into a groove machined into the condenser tube wall and the groove was filled with silver solder in a manner similar to the Siddique installation (Figure 2.4-2). A heat conduction calculation was made to determine the inner and outer tube wall temperatures. The thermocouples were 0.5 mm OD SS sheathed J-type. The grooves were 12.7 mm in length. This improved installation technique is expected to result in more accurate temperature measurements and eliminate the possibility of detachment of the thermocouples from the condenser wall. The locations of the test section thermocouples are shown in Figure 2.4-3. The thermocouples located at the inner wall of the cooling jacket were 1.6 mm OD SS sheathed type thermocouples embedded in a plastic jacket.

2-11

NEDC-32301 The thermocouples protruded approximately 1 mm into the cooling jacket in order to measure the coolant temperature at the adiabatic coolingjacket wall.

The main wr.cerns that arose from the three previous experiments were (1) the possible variations in the degree of mixing (axially and circumferentially) in the cooling jacket and (2) the associated effort in determining the bulk cooling water temperature.

Improvements were made in each of these areas in the design of the Kuhn cooling jacket.

In previous experiments there was one cooling water inlet and one cooling water outlet.

In this experiment there are two inlets and four outlets spaced 900 apart (shown partially in Figure 2.4-3) in order to minimize circumferential nonuniformities. The cooling jacket was constructed of a longitudinally split steel jacket. A plastic cooling jacket was first used, but this was damaged due to inadvertent addition (by a student performing a separate experiment) of steam in the condenser without any cooling water flow. The longitudinally split cooling jacket allowed the thermocouple wires to exit the jacket radially near the axial location of their measurement instead of being led out the top or through intermediate flanges. Nylon spacers were used to fix the radial location of the cooling jacket (Figure 2.4-3). The spacers and a small number of thermocouple wires were the only flow obstructions present in the cooling jacket flow annulus. There were no flanges / mixers to promote mixing as in Vierow and Ogg. The coolant flow rate was kept high enough to be naturally turbulent. The coolant bulk temperature was calculated with the aid of a computational fluid dynamics model. The model included the well-tested k-c turbulence model, which performs well in simple flows such as the annular flow in the cooling jacket. The model accounted for variations in fluid properties with temperature.

With the benefit of the coolant annulus flow model, the following iterative process was developed to determine the local heat flux:

(1) Fit adiabatic wall temperature to obtain an approximate heat flux:

q"(r) ~ - W'c" dT"(x) (2.4-1) nD, dr (2) Calculate inner tube wall temperature:

r,q"(r)ln D"'

' '/

7;.,,, = 7;. + (2.4-2) k, 2-12

NEDC-32301 (3) Calculate outer tube wall temperature:

D' i;q"(x)in g-7l,o = T,.,,, + (2.4-3) k, (4) Calculate cooling water bulk temperature:

Tc , = T,, - f(T uo , T,,W,)(T,o - T,) (2.4-4) where f(7l,,, T,,W,) is calculated by the coolant annulus numerical routine.

l (5) Fit cooling water temperature to obtain the improved value of heat flux:

W,c, dTc"(x) q"(x) = -

(2.4-5) nD, dx (6) Repeat steps (2) through (5) to convergence.

Further details on the numerical procedure are as follows:

(1) Velocity Distribution in the Annulus:

dP 1B & (2.4-6)

- - + -- (r ,f L) + pg = 0 d: r& &

j By solving this momentum equation, the fully developed velocity profile vz(r) is obtained when eff is derived by solving the turbulent k-c equation in j which temperature dependence of properties was taken into account.

(2) Temperature Distribution in the Annulus:

6T BT 1B GT pc,,(v,a- + v,cr--) = r & (rk,f&-) (2.4-7) 1 2-13

- . ~ . - . . .- - .- .- - . - _ _ - . - .. .

I i

NEDC-32301 or dT JT^ BT (2.4-8) pc,v' &6 =r& I B (rk, GT) for v = 0 and

- - =-

with boundary conditions Ts = Ts, at : = 0 T = T, at r=l{

T=T, at r = }{,

k, = k(r) for laminar flow (Thermal conductivity k(T))

k, = k(r)+ k,(r) for turbulent flow

= k(r) + cep, ,

(3) Bulk Temperature The cooling water bulk temperature by definition is given as:

i

.g, T(r)v,(r)dr ,

Tc , = ' "' ,

y, (2.4-9)

,a v,(r)dr and the cooling water bulk temperature ratio fis defined as:

f = T, - Ts =

T.-T* (2.4-10)

T,- T, T_ - T, and this is used in Equation 2.4-4 to obtain T b rom f ' measured values of the outside tube wall temperature and the coolingjacket adiabatic temperature Ta- -

2.4.2 Results -

The complete results will be available in Kuhn et al. [1994]. At the time of this report only limited results were available in a plotted form. These results will be discussed in Section 3.6. A test matrix is shown in Table 2.4-1.~  ;

I 2-14

. . . . - . _ - ~ . . - -

NEDC-32301 Table 2.1-1 -I TEST MATRIX FOR VIEROW l

1 Run Inlet Air Pres. Inlet steam Run Inlet Air Pres. Inlet steam I

No. Mass (MPa) flowrate No. Mass (MPa) flowrate Frac. (kg/hr) Frac. (kg/hr) 1 0.00 0.047 12.9 19 0.14 0.304 12.3 2 0.00 0.061 13.0 20 0.18 0.244 7.57 3 0.00 0.059 8.53 21 0.054 0.173 12.2 l 4 0.0086 0.111 12.9 22 0.038 0.159 19.0 l 5 0.023 0.108 8.16 23 0.081 0.262 19.2 l 6 0.00 0.148 8.21 24 0.082 0.378 18.6 7 0.016 0.108 8.16 25 0.00 0.050 18.5 8 0.012 0.112 13.0 26 0.095 0.374 18.7 9 0.14 0.172 8.30 27 0.013 0.119 23.1 ~

10 28 0.039 0.274 23.5 11 0.13 0.214 8.07 29 0.00 0.050 23.9 12 0.11 0.220 13.0 30 0.049 0.318 23.8 13 0.15 0.181 8.12 31 0.055 0.412 23.8 14 32 0.055 0.452 28.8 15 0.00 0.047 12.8 33 0.002 0.049 28.3 16 0.00 0.053 8.30 34 0.025 0.310 29.6 17 0.00 0.030 12.8 35 0.014 0.163 28.9 18 0.00 0.04 8.48 36 0.045 0.419 28.8

• Rows not filled indicate tests for which steady-state was not achieved.

1 2-15 l

NEDC-32301 Table 2.2-1a l

TEST MATRIX FOR AIR / STEAM RUNS OF SIDDIQUE i

l Run Inlet Air Pres. Inlet steam Run Inlet Air Pres. Inlet steam No. Mass (MPa) flowrate No. Mass (MPa) flowrate Frac. (kg/hr) Frac. (kg/hr) 1 0.09 0.107 8.93 27 0.27 0.243 20.70 2 0.15 0.112 8.83 28 0.31 0.252 20.35 3 0.18 0.117 8.76 29 0.36 0.266 20.65 4 0.24 0.122 9.15 30 0.10 0.387 19.95

. 5 0.29 0.128 9.12 31 0.15 0.403 19.73 4

6 0.33 0.133 9.09 32 0.20 0.421 19.92 7 0.08 0.209 9.39 33 0.25 0.438 20.37  !

8 0.14 0.217 9.30 34 0.32 0.469 19.90 9 0.19 0.227 9.24 35 0. I 1 0.109 25.34 10 0.26 0.239 8.97 36 0.14 0.114 27.08 11 0.33 0.260 9.38 37 0.19 0.118 28.63 l 12 0.42 0.287 8.80 38 0.24 0.124 28.84 13 0.11 0.389 7.98 39 0.30 0.131 28.76 14 0.18 0.410 8.04 40 0.35 0.137 28.97 l 15 0 24 0.432 7.95 41 0.10 0.213 30.41 16 0.30 0.454 8.00 42 0.15 0.221 30.97 l 17 0.34 0.475 7.92 43 0.20 0.230 30.35 i 18 0.12 0.110 20.02 44 0.24 0.239 29.91 l 19 0.17 0.114 19.85 45 0.31 0.254 29.41 20 0.21 0.119 19.82 46 0.34 0.264 29.61 1 21 0.25 0.123 19.99 47 0.10 0.386 31.91 22 0.31 0.130 19.68 48 0.15 0.402 31.75 23 0.35 0.136 19.82 49 0.20 0.416 31.90 24 0.11 0.214 20.42 50 0.25 0.437 31.61 '

25 0.15 0.221 20.84 51 0.30 0.457 31.41 l 26 0.22 0.233 20.67 52 0.35 0.485 31.09 a

2-16

i NEDC-32301 l l

! Table 2.2-1b l

l TEST MATRIX FOR HELIUM / STEAM RUNS OF SIDDIQUE <

l I

i l

l Run Inlet He Pres. Inlet steam l No. Mass (MPa) flowrate l

Frac. (kg/hr) 1 0.02 0.114 9.16 2 0.04 0.126 9.14 3 0.07 0.140 8.97 4 0.10 0.157 8.90 5 0.02 0.221 8.77 6 0.05 0.244 8.72 7 0.08 0.273 8.68 ,

8 0.11 0.303 8.63 9 0.03 0.400 8.78 10 0.04 0.428 8.65 11 0.06 0.466 8.60 12 0.02 0.118 18.51 13 0.04 0.134 18.21 14 0.05 0.144 If>.59 15 0.07 0.157 20.09 l

16 0.02 0.214 18.54 17 0.05 0.252 18.72 18 0.07 0.271 18.47 19 0.09 0.293 18.04 20 0.02 0.398 20.46 21 0.04 0.437 20.37 22 0.05 0.465 20.30 l

i l

2-17 l

NEDC-32301 Table 2.3-1a TEST MATRIX FOR . AIR / STEAM RUNS OF OGG Run Inlet Air Pres. Inlet steam Run Inlet Air Pres. Inlet steam No. Mass (MPa) flowrate No. Mass (MPa) flowrate Frac. (kg/hr) Frac. (kg/hr) 8.1 0.0 0.I15 72.7 15.1 0.05 0.286 72.7 8.2 0.0 0.104 61.4 15.2 0.05 0.143 61.4 8.3 0.0 0.0983 50.0 15.3 0.05 0.124 50.0 10.3 0.0 0.0979 38.6 15.4 0.10 0.139 38.6 11.1 0.0 0.100 27.3 16.1 0.10 0.153 27.3 11.2 0.0 0.0989 15.9 16.2 0.15 0.123 15.9 11.3 0.40 0.106 15.9 17.1 0.02 0.252 72.7 11.4 0.15 0.106 27.3 17.2 0.02 0.145 61.4 12.1 0.10 0.110 72.7 17.3 0.02 0.133 50.0 12.2 0.10 0.I11 61.4 17.4 0.05 0.126 38.6 12.3 0.10 0.110 50.0 18.1 0.05 0.118 27.3 12.4 0.15 0.108 38.6 18.2 0.02 0.105 27.3 13.1 0.40 0.122 38.6 18.3 0.10 0.110 15.9 13.2 0.15 0.119 50.0 18.4 0.05 ___0.106 15.9 13.3 0.15 0.132 61.4 19.1 0.01 0.186 72.7 13.4 0.15 0.144 72.7 19.2 0.01 0.154 50.0 14.1 0.40 0.122 50.0 19.3 0.01 0.180 61.4 14.2 0.40 0.107 27.3 19.4 0.02 0.139 38.6 2-18

NEDC-32301 Table 2.3-1b TEST MATRIX FOR IIELIUM/ STEAM RUNS OF OGG Run Inlet Air Pres. Inlet steam Run Inlet Air Pres. Inlet steam No. Mass (MPa) flowrate No. Mass (MPa) flowrate Frac. (kg/hr) Frac. (kg/hr) 20.1 0.01 0.274 72.7 23.2 0.005 0.135 61.4 20.2 0.01 0.216 61.4 23.3 0.005 0.156 50.0 f

20.3 0.01 0.I27 50.0 23.4 0.01 0.I37 38.6 20.4 0.02 0.160 38.6 24.1 0.01 0.107 27.3 21.1 0.05 0.145 27.3 24.2 0.01 0.105 15.9 i

21.2 0.02 0.109 27.3 24.3 0.005 0.132 38.6 21.3 0.05 0.110 15.9 25.1 0.02 0.307 72.7 j

~

21.4 0.02 0.104 15.9 25.2 0.02 0.192 61.4 23.1 0.005 0.189 72.7 25.3 0.02 0.176 50.0 1

2-19

NEDC-32301 1

Table 2.4-1a TEST MATRIX FOR PURE STEAM RUNS OF KUHN l

Run Pres. Inlet steam Run Pres. Inlet steam No. (MPa) flowrate No. (MPa) flowrate l

1 (kg/hr) (kg/hr) 1.1-1 0.101 60 1.3-1 0.101 40 1.1-lR 0.101 60 1.3-1R1 0.101 40 1.1-2 0.203 60 1.3-l R2 0.101 40 1.1-2R 0.203 60 1.3-2 0.203 40 1.1-3 0.304 60 1.3-2R1 0.203 40 1.1-3 R 0.304 60 1.3-2R2 0.203 40 1.1-4 0.405 60 1.3-3 0.304 40 1.1-4R1 0.405 60 1.3-3R1 0.304 40 1.1-4R2 0.405 60 1.3-3 R2 0.304 40 1.1-4R3 0.405 60 1.3-4 0.405 40 1.1-5 0.507 60 1.3-4R1 0.405 40 l 1.1-5R1 0.507 60 1.3-4R2 0.405 40 1.1 5R2 0.507 60 1.3-5 0.507 40 l 1.1-5R3 0.507 60 1.3-5R1 0.507 40 1.2-1 0.101 50 1.3-5R2 0.507 40 1.2-2 0.203 50 1.4-1 0.101 30 1.2-3 0.304 50 1.4-2 0.203 30 1.2-4 0.405 50 1.4-3 0.304 30 1.2-4R1 0.405 50 1.4-4 0.405 30 1.2 -5 0.507 50 1.4-4R1 0.405 30 l 1.2-5R 0.507 50 1.4-5 0.507 30 l

l 2-20 l

l

1 NEDC-32301 l l i Table 2.4-1b TEST MATRIX FOR AIR / STEAM RUNS OF KUHN i -

i Run Inlet Air Pres. Inlet steam Run Inlet Air Pres. Inlet steam a

i No. Mass (MPa) flowrate No. Mass (MPa) flowrate i Frac. (kg/hr) Frac. (kg/hr) 2.1-1 0.01 0.405 50 2.2-11 0.30 0.101 50 2.1-2 0.02 0.405 50 2.2-12 0.35 0.101 50

2.1-3 0.03 0.405 50 2.2-13 0.40 0.101 50 2.1-3R 0.03 0.405 50 3.1-2 0.01 0.203 60 I 0.04 50 3.1-3 0.304 60 2.1 -4 0.405 0.01 2.1-5 0.06 0.405 50 3.1-4 0.01 0.405 60

]

i 2.1-5R 0.06 0.405 50 3.1-5 0.01 0.507 60 2.1 -6 0.08 0.405 50 3.2-1 0.05 0.101 60 2.1 6R 0.08 0.405 50 3.2-2 0.05 0.203 60 1 2.1-7 0.10 0.405 50 3.2-3 0.05 0.304 60 l 2.1-8 0.15 0.405 50 3.2-3R1 0.05 0.304 60 l 2.1-8R 0.15 0.405 50 3.2-4 0.05 0.405 60 i 2.1-9 0.20 0.405 50 3.2-5 0.05 0.507 60

! 2.1-10 0.25 0.405 50 3.3-1 0.10 0.101 60

2.1-10R 0.25 0.405 50 3.3-2 0.10 0.203 60 2.1-11 0.30 0.405 50 3.3-3 0.10 0.304 60 l 2.1-12 0.35 0.405 50 3.3-4 0.10 0.405 60 2.1-12R 0.35 0.405 50 3.3-5 0.10 0.507 60

{

! 2.1-13 0.40 0.405 50 3.4-2 0.20 0.203 60 j 2.2-1 0.01 0.101 50 3.4-2R1 0.20 0.203 60 2.2-2 0.02 0.101 50 3.4-3 0.20 0.304 60 1

2.2-3 0.03 0.101 50 3.4-5 0.20 0.507 60 l 2.2-4 0.04 0.101 50 3.5-2 0.40 0.203 60 i 2.2-5 0.06 0.101 50 3.5-2R1 0.40 0.203 60 2.2-6 0.08 0.101 50 3.5-3 0.40 0.304 ,60

2.2-7 0.10 0.101 50 3.5-3R1 0.40 0.304 6) 2.2-8 0.15 0.101 50 3.5-4 0.40 0.405 60

2.2-9 0.20 0.101 50 _

3.5-5 0.40 0.507 60 s 2.2-10 0.25 0.101 50 2-21 1

i l . _ _ . _ , . _ . . _ . _ . , . , . -

NEDC-32301 Table 2.4-1b TEST MATRIX FOR AIR / STEAM RUNS OF KUHN (continued) 1 Run Inlet He Pres. Inlet steam Run Inlet Air Pres. Inlet steam No. Mass (MPa) flowrate No. Mass . (MPa) flowrate Frac. (kg/hr) Frac. (kg/hr) 4.1-2 0.01 0.203 30 4.3-5 0.10 0.507 30 4.1-3 0.01 0.304 30 4.4-2 0.20 0.203 30 4.2-2 0.05 0.203 30 4.4-3 0.20 0.304 30 4.2-3 0.05 0.304 30 4.4-5 0.20 0.507 30 4.2-5 0.05 0.507 30 4.5-2 0.40 0.203 30 4.3-2 0.10 0.203 30 4.5-3 0.40 0.304 30 4.3-3 0.10 0.304 30 4.5-5 0.40 0.507 30 Table 2.4-1c TEST MATRIX FOR HELIUM / STEAM RUNS OF KUHN Run Inlet He Pres. Inlet steam Run Inlet Air Pres. Inlet steam No. Mass (MPa) flowrate No. Mass (MPa) flowrate Frac. (kg/hr) Frac. (kg/hr) 5.1-1 0.003 0.405 30 5.2-3 0.01 0.405 45 5.1-2 0.005 0.405 30 5.2-4 0.03 0.405 45 5.1-3 0.01 0.405 30 5.2-4R 0.03 0.405 45 5.1-4 0.03 0.405 30 5.2-5 0.05 0.405 45

_ 5.1-5 0.05 0.405 30 5.2-5R 0.05 0.405 45 5.1-6 0.10 0.405 30 5.2-6 0.10 0.405 45 5.1-7 0.15 0.405 30 5.2-6R 0.10 0.405 45 5.2-1 0.003 0.405 45 5.3-1 0.003 0.405 60 5.2-lR 0.003 0.405 45 5.3-2 0.005 0.405 60 5.2-2 0.005 0.405 45 5.3-3 0.01 0.405 60 5.2-2R1 0.005 0.405 45 5.3-4 0.03 0.405 60 5.2-2R2 0.005 0.405 45 5.3-5 0.05 0.405 60 1 2-22

. . _ .=_. m . _ . . .. - ~_ _ _. . .. ._. . . .- . _ _ .

~

" V26 Vl4

^; 13 w ~'

% ~

%) e

, 30 'TO DRAIN w a a e l b z >; l 27 m .

3 a

• z h a s i

3 3 I 7 m E

o l o ClTY 3 a- 3 28 V29 T g Vl5% w 4  :: < WATER rn S _

y _._

V2C 25 b c,

is - -

,., e ~

T U h~ i d -

, V -n V33 V33 AIR M

o

'I

~

5 -

~

__.  : [V31 V34 V353  : 6-2 -O -

u x  : :vis 3MI 2si y

-++

1_.c 10 39 v22 N CITY v4 yli N12  :: 39

51 OO ,

a

' -++ ,, ,,

P35 a 38 '

WATER

'L-------- --- '

P2 20 " 17 37f' -

42 32 I 4i 47 o 48 To eMa E VE[ ?f I

Figure 2.1-1a. Schematic of Vierow [1990] Experiment (Used with permission)

- - . _ . _ . . . _ . . - _ _ . _ _ . - _ _ . _ - _ _ _ _ _ _ _ _ . _ . _ _ _ _ _ _ _ _ _ _ - - ________s _

NEDC-32301

' KEY TO SYSTEM SCHEMATIC Component Description 1 Water feed line fmm reservoir P2 Reservoir fill pump V3 Pump bypass valve V4 Regulanng valve fort reservoir fill line 5 Immersion heaters 6 Reservoir fillline 7 Steam / water pressa reservoir 8 Fillline to purge pressure sense line of air V9 Regulating valve for filling pressure sense line 10 Reservoirlevel sense lines V11 Valve to purge pressure sense line of air V12 ' Valve to purge pressure sense line of air 13 Steam / air separator V14 Pressure relief valve V15 Airintake valve 16 Orifice meter on 1/2 inch steam supply line 17 Steam / air purge line on 1/2 inch seam line V18 Valve on 1/2-mch steam supply line 19 Orifice meter on 1 inch steam supply line 20 Steam / air purse line on 1 inch steam supply line V21 Regulating valve on steam / air purge line V22 Valve on 1 inch steam supply k'ne 23 Lower chamber V24 Gate valve 25 Downcomer V26 High point vent valve 27 Condensation test section 28 Test section coolant inlet line V29 Regulating valve for test section coolant 30 Test section coolant outlet line V31 Pressure relief valve 32 Testloop blowdown line to barrel V33 Air intake valves V34 Manometer toloop isolation valve P35 Vacuum pump 36 Sight glass 37 Condensate drain line 38 Condensate heat exchanger 39 Condensate coolantinlet line V40 Regulating valve for condensate coolant inlet 41 Condensate coolant outlet line P42 Condensate pump V43 Pump bypass valve.

V44 Regulaung valve for condensate pump V45 Regulating valve for condensate pump V46 Three way valve to direct condensate flow 47 Condensate measurement tank and weighing scale 48 Return line to supply barrel V49 Manometer to vacuum pump isolation valve 50 Mercury manometer-51 Pressunzed air bottle 52 Water ReservoirQuench Tank Figure 2.1-lb. Key to System Schematic of Vierow [1990] Experiment (Used with permission) 2-24

l T35 +

A PT20 v

M ***

gT25 fg ,

_T38 TO DRAIN E z TM t _T26 w 3 3 5 i T27 E E 5 I7 28 n

z >' wTB r-

<r . 7 29 o

j W

O in T22

[77 30 3; o T_Z 3 y . 7 32 F34 o

g y g 4 r 7 33 ,, CITY T_E p w -

_ WATER 4 F , -

- lT21 rn 3 in O

w U h --

9 U *

-t1 1

w FE ' PTIB

^^

• _ AIR o

-^

r , , ,

A '

,'p' TIS -

PG40

-->+ "

n M < - ,

v GI u ' - -

FIO PTil

-~

O

~

• • - PT2 w

' -++ ,l TE o wkfER

' Tl2 TR

[------------;

T39 todametD X 2 FIGURE f E X PERIMENT AL INSTRUMENTATION Figure 2.1-2a Experimental Instrumentation of Vierow [1990] Experiment (Used with permission)

l NEDC-32301 KEY TO INSTRUMENTATION DIAGRAM Component Description Number PG0 Visual J auge for vessel gauge pressure M2 Diff. P" on reservoir level sense line T3 Pressure vessel water TC T4 -> 19 Pressure vessel wall TC's F10 Flow meter on 1 inch steam supply line Mll PT on 1-inch and 1/2 inch steam supply line T12 1-inch steam su ply inlet TC F14- Flow meter on : /2 inch steam supply line -

TIS 1/2-inch steam suppl T16 LowerchamberTC yinletTC PG17 Visual pressure gauge on lower chamber M18 M on lowerchamber F19 Flow meter on steam / air entering test section M20 Diff. M for absolute pressure at top of loop T21 Test section coolant inlet TC T22 -> T24 Test section coolant bulk temperature TC's

'T25 Test section coolant outlet TC T26 -> T33 Condensor tube outer wall temperature TC's F34 Flow meter on test section coolant line i l

T35 Test loop high point TC T36 Condensate TC T37 Condensate TC T38 Condensor tube outer wall temperature TC T39 Condensate drain TC PG40 Gauge on pressurized air bottle i F = flow meter i l

PG = pressure gauge PT = pressure transducer TC = thermocouple Diff. = differential l

l Figure 2.1-2b. Key to Experimental Instrumentation of Vierow (1990] Experiment (Used with permission) 1 2-26 l

- - _ = - .

l i

NEDC-32301 i TYPICAL STEADY. STATE TEST SECTION TEMPERATURE PROFILES i

Steady-state Temperature Profile Run #29 150 a

a b 100 a

g! 50 0

0 30 60 90 Position Along Condensing Test Section (in.)

Steady-state Inverted Temperature Profile Run #17 150 a

D 100 1 l I

E

& ' ' "

• a f . 50 0

0 m e g Position Along Condensing Test Section (in.)

Figure 2.1-3. Typical Steady-State Condenser Tube Wall Temperatures for Vierow [1990] Experiment (Used with permission) 2-27

Temperatures During Oscillation .

Run # 10 Real Start Time = 15:50:01 -e- T25 200 '

-M- T26

+ T38 b b 't 1 150 e i 1

o y 4 On ~

Q ggn I + . 3

)

3 I

h/ d 1 r s

- l 4

50 ' 250 300 O 50 100 150 ,

200 time (sec) ,

Figure 2.1-4. Sample Thermocouple Time Records for an Oscillatory Run of Vierow [1990] (Used with permission)

_ _ _ _ _ _ _ - _ _ _ _ _ _ _ _ . _ _ _ _ _ - _ _ _ _ _ _ _ _ _ _ - - - - _ _ - - - _ _ _ _ _ - . _ _ _ _ - _ _ _ - - - . .= . -- __

r , vario ,m .

I Cadmg Wasa (btlet isolation T ' '

va. P Blodwn ll T Vdn ,,

y

, 4 ,

T,*

see mcenerator ,, ce Ta ^* . i 7, o,.

. i n i i

, e e e ll a e 1

]

1I g

va.

@ throede p , no , = m C'" b

$ f' e __T c L-k '>"""*

• ""' h C+

Pr -

• ]' "

C+

+3 3

=

=

f- - - -

[

s_ a

. Rotameter  % P DesignmeesPreneureTransdww j c m. "d" L c-a van

} so Ypi 1",,l' r %n wh Figure 2.2-1. Schematic of Siddique [1992] Expenment (Used with permission)

NEDC-32301 Inlet of Ner. cert r.able Gas / Steam Mxture h

i 1

~

Cooing Water Outlet n 11 11 I;

/

l4 lll l

11 7=$ z.s =

Il _  !!_ F j

~

lj jI~

ll ll

,i _

I, _ "y" cooang wetw

~

thermocoupee

'j l'- - ,

Center une ll l

1. ^

l li N ll ll 5=

2.54 m NlN II-7 /YI '! - E wl=

e One thermocouple each lj lI h on the inside and the Me ll ll U

outside tube wan lt _ l[_

li~ o lli I m=

ll ll p

~

ji Il o x.s =

ll ll

" U 11 11 N=

11 ll coonne water wet i I I I Figure 2.2-2. Test Section and Thermocouple Configuration for Siddique Experiment (Used with permission) 2-30

NEDC-32301 I

l l

Noncondensable Gas / Steam Mixture U

/( l

./ l

/[

s s s

l wg Ws s s iron /constantan

> /

Center une Thermocouple l

s

[ {'

s MI T s l

Sheathed l 1 r

Thermocouple Gas Sampling Point s l 1ron/Constantan s s s N

\

l N

v N s Coolant Flow s

N U

% _ jbndenser Tube Stainless Steel 304 pipe Stainless Steel 304 62.7 mm ID 46.0 mm 10,50.8 mm OD Figure 2.2 3. Detail of Test Section Instmmentation for Siddique [1992] Experiment (Used with permission) 2-31

NEDC-32301 15000 O h UCB

• h MIT u e .

h g 10000-E . .

2 c:

.5 g

8 uw .

a

• g 5.

- c.

]

~

. tir; ',! .

=&_ .

o.

O.0 0.2 0.4 0.6 0.8 1.0 Mixture Bulk Mr Mass Fraction Figure 2.2-4. Plot of Heat Transfer Coefficient as Predicted by the Siddique Correlation and the Vierow [1990] Correlation (not Vierow and Schrock) Versus Mixture Bulk Air Mass Fraction (Taken from Siddique (1992] and used with permission) 2-32

NEDC-32301 3.0 Ja=4.038 2.5 -

Re=10000

Re=5000

- Re=1000

- Re=500 M

g 1.5 -

i 1.0 -

s 0.5-4 0.0 . . . .

0.0 0.2 0.4 0.6 0.8 1.0 Bulk Mole Fraction of Noncondensable Gas l

Figure 2.2-5. Ratio of Nusselt Numbers When Helium is Present Versus When Air is Present Plotted Versus the Mole Fraction of Noncondensable Gas (Taken from Siddique [1992] and used with permission) 2-33

NEDC-32301 J

l 1

1 0.40 Ja=0.038 0.38 - ,

Re=10000

Re=5000

Re=1000

- Re=500 0.36 -

j i

0.34 -

g 0.32 -

)

0.30 -

0.28 , , , ,

0.2 0.3 0.4 0.5 0.6 0.0 0.1 Bulk Mass Fraction of Noncondensable Gas Figure 2.2-6. Ratio of Nusselt Numbers When Helium is Present Versus When Air is Present Plotted Versus the Mass Fraction ofNoncondensable gas (Taken Rom Siddique [1992] and used with permission) 2-34

I NEDC-32301 i

6-1/8"

= (155.5mm) 2-7/8"

=

= (73.0mm)

,= 2.05" _1 i (52.1mm) ~' 1

., _  :' '//'

h r ,

h

,1/16*

, (1.6mm) 3f4 '

(19mm) 1a ,

j' g 2 f(25.4mm) l , s xxx, nxx' k ,

jg l 1.5" Dt of bWt orde:

l ,

i "I 4.5'(114.3mm)

Du of bolt hees:

1/4*(6.3mm) cotar to ,

3j4.(19.0mm) -

I jocket poo, mates e J ,

De of bolts:

[

• W / l 5/0'(16mm)

' "~

me.cfhNet &&cf!? ,

base .

2-7/16*(61.9mm) 2"(50. Bunn) OD SS 304 RTBE l BWG #13 Eight.1/16' (1.6 mm) NPS.

g

/ u' ._ _

Attage strenged at equel speanssume 1 1/2' NPS socket for the cmwderence l **d"9 *

• 2-1/2", sch 40s

! ss304 Mpe i D 2.469'(62.7 mm) 4 00 2.87s*(73.0 mm) i i

. Figure 2.2-7. Detailed Sketch of the Upper Part of Siddique's [1992) Test Section (Used with pennission) i

(

2-35 4

..,-u. 4 _ m u. a_ . ..a.. m. 4 a _ c ee m .._-am_<m..- .c+- c-. 4 ._s NEDC-32301

t:: w ; w

_ .l

I ge  ;} N ,.

h [ 'g. 3 s

4 1 g1: 1 Il __

, _ij~

i -

I "T" 1

3

==

a A ,

i r ._

a ,

is E O' O >*- E I $ S g j1

$4 a g oo g o om o q o o -

.;  ; = ,g

.T9 ee e e e e4 2 c.

e

~

2 [ I 08 28

( O~I h{

Qa: E y i }

!i -

5 8.

5=

$i

ft = ai  :

8 * - .

f#[ -

m .p Tb 5 "-l 8 g:t $ Y 1:3 Vd .

d g

II

, _.- ; => n h

• 6 l t! I og kl.l3 i

M "- If n

il li

s:si sl.I 2-36

NEDC-32301 1

Axial temperature profiles (Run 13.4,9/28/91) l I I i

110= g

.. =

I_ f; _

r - -

100- f

l T,,, a 3

90- We= 73.2 kg/hr Wa= 14.5 kg/hr Tw,,,

80= We= 927 kg/hr TS pres. = 143 kPa

/-[

TS D/P = 0.4 kPa P T.,.i;

• 70=

i 60 l

\

50= ,

40 -

)

' i -

30- 1 I l I I I i I

50 100 150 200 250 i 0 Axial pos. (cm)

Figure 2.3-2. Typical Temperature Profiles from Ogg [1991]

s (Used with permission) s 2-37

KcY Wet bulb probe

, y P - Pressure gauge XP - Pressure transducc4 XP3 T - Thermocouple To ottier HX - Heat exchanger crperiment t DP - D/P transducer Ill A f A V11 V12 1 I; U do- -b+@-

l V10X 0 psig supply ll v3 v4: vs vs u Test ,

,, , ,, lI section gl y h L XPi XP2 lI g

V_18 V_19 '

MW Separator Expansion ^ ^

IT) '

V1 V2 V8 / tank II

% f II N# '

Q

$ 100 psig 7aC gl Co U

oc air supply --

O g

()

-$ap" f f Y$ "dAS I L3 l

D ) . - -

b V17

• h Y '<2 s _ _

^

u.abi, ..

bulb probe suppression ,

I pool Cooling #~'~ nx

~-

Pump - .s V24 tower V27

~~

3 jb HX

' N i D29 ' ' v22 i

T D4- V21 V28 City water V m

- X v30 y

He cylinder  ;

Condensate drain i

Figure 2.4-1. General Schematic Drawing of Kuhn et al. [1994] Experimental Apparatus

. - . . . _. .. , ,. .. _ . _ . _ - ..__ - - - _ , - _ . ~ , - . - . - . - _ . . __- _____ __2

NEDC-32301 0.7 mm y r I

I i- . 0.25 mm 4 --> <-

1/16" sheathed f+ 'I thermocouple A

< st Silver solder 50.8 mm

~ ,

W t N

j l

l 1

I f 1.65 mm I sA 4 l E

--> y 0.58 mm I y

. - V l

e^ ll Ili E

y l g 0.02" 00 SS sheathed

- ,j

, i J-Type thermocouple y-4 I' I

I i l l

l l Figure 2.4-2. Sketch Showing the Condensing Tube Thermocouple Installation in Kuhn et al. [1994]

2-39

NEDC-32301 Tube packing gland Thermocouple inserted Axial Location

( cm )

O- in cooling water cooling witu 0.0 - -

D n- outlet

---

g 7 4.0 9.0

- a -]g"<-- tecket packing gland

- - -- C-' - - ' K) ----

17.0

- - ' 1) ----

30.4 - --- C~'

44.6 - - - - Cr> - - -*- 6 ----

1/4" nylon screw (spacer) 7i 60.0 - - ' .-t --' ---

61.5 - - - - C->

~

0.02" OD SS sheathed f

79.8 - - - - C- e - --s g)4 - -

J tyoe thermocouple embeded oncondensingtube 1/16" OD SS sheathed 99.6 95.0 - - i -

- - -- CL

> ---a "[l - - T type thermocouple embdd on plastic jacket ee I

I 115.0- - -l - '

121.3 - - - - 6- . ---a- 6 - - - - - l

< Coofing Jacket

-i 13 7.0- - t m 14 s.1 - - - - E ---a 4----

< CondensingTube I

171.5 - - - - C -'-

-d' ---

e : 0.02" OD J type TC O : 1/16" OD T type TC l m W nspacu 2 01.5 - - - - C -> - - - *6 ---

l l

3 l

'a .:

t Cooling water 241.8 -

' - -) --

inlet Q s'\

~Q? u Figure 2.4-3. Test Section Thermocouple and Spacer Locations for Kuhn et al. [1994)

Experiment 2 40

NEDC-32301

3. CORRELATIONS 3.1 Vierow and Schrock ("Tsukuba")

^

The correlation currently in TRACG is based on a slightly modified version of the correlation presented in Vierow and Schrock [1991]. The database used was the database developed by Vierow [1990]. The Tsukuba correlation, as noted in Section 2.2.2, differs

from that presented in Vierow [1990]. The Tsukuba database excluded the runs which did not reach a steady-state condition, as well as the runs with the temperature inversions.

The data were correlated as a two-part correction to a reference local heat transfer coefficient. This reference heat transfer coeflicient is termed the "Nusselt" heat transfer coeflicient. This reference value is calculated by dividing the condensate thermal conductivity by the local liquid film thickness as calculated from the model of smooth interface, gravity-driven laminar film flow:

4 3p,T Y

l j 6, = (3.1-1) 4 rRPt (Pr ~ P,)> ,

i where F is the film flowrate per unit circumference. The data were correlated such that hexp = f bref ; href = kpSi (3.1-2) where fis the correction factor (also called a degradation factor). The correction factor is divided into two parts such that f = i2 f f . The factor f iis the correction factor which accounts for the enhancement of heat transfer due to interfacial shear, interfacial waves and deviations from the Nusselt model. The factor 2f is the correction factor which accounts for the effects of heat transfer degradation due to the noncondensable gas mass fraction. The Vierow and Schrock correlation then is:

f 3= (1 + 2.88x10-5 Re m I'I8)

(3.1-3) b f2= (1 - C Ma )

3-1

\

NEDC-32301 where (for steam / air mixtures)

C = 10 b=1.0 for hi a< 0.063 C = 0.938 b = 0.13 for 0.063 < hia < 0.60  !

C = 1.0 b = 0.22 for hi a> 0.60 i hi ais the bulk air mass fraction (air mass / total mass) at any axial location and Rem is the local gas / steam mixture Reynolds number, pDV/pm. The experimental data are shown plotted in the form of the correlation in Figure 3.1-1. The ordinate,1-f/f i, is equivalent to 1-f2such that when the correlation is plotted b is the slope of the curve and C fixes the position of the curve.

l l

3.2 TRACG The correlation used in TRACG is a modified version of the Vierow-Schrock I

correlation. The f 2correlation is changed only slightly to avoid discontinuities-l l

b (3.2-1) l f2= (1 - C hia) where (for steam / air mixtures):

C = 10 b = 1.0 for hi a< 0.06586 C = 0.938 b = 0.13 for 0.06586 < hia < 0.4911 C = 1.0 b = 0.22 for hi a> 0.4911 The f iterm is modified as follows:

f i= 1 + 2.88 x 10 -5Rem1.18 for Ref s 1000 (3.2-2) fj = 1 for Rer> 2000 1/3 also 6, = 32.3

1. ' 3 for Rer> 2000 (3.2-3)

<P1 ET ,

l 3-2 l

l

i l NEDC-32301 l

l l

l linear interpolation between Refilm of 1000 and 2000 .

i I

additional restriction of if s 3

(

where in this case Rer= 4F/pr Because the if correlation of Vierow and Schrock exceeds a value of 3 (near Rem =

12,500), the TRACG correlation generally predicts lower heat transfer coeflicients in the high heat transfer region near the tube inlet. l 3.3 Siddique Siddique correlated his data in the form:

l

,nu h ,M. 4 .4 jy-i 2" g(yp (x)D' = 6.123 Re* 223 (3.3-1) k, M,, ,

where Ma,w is the mass fraction of air at the wall (or interface), Ma,b si the bulk mass fraction of air, and Ja = [Cpmixture(Tb -Tw)]/hrg. The correlated data are shown in Figure 3.3-1. The MIT correlation assumes that the condensate thermal resistance is a I negligible compared with the gas side resistance. This requires that the interface temperature equal the wall temperature which then allows Ma,w to be calculated. It has been shown that this is not true for all conditions.

3.4 Ogg Ogg [1991] correlated his data in a manner similar to Vierow and Schrock. The fi correlation was obtained from pure steam data. Knowing fi , the f 2correlation was derived from air / steam data. His correlation is:

f i= 1 + 0.0012 Rem 03 (3.4-1) f2= 1- C Mab 3-3

NEDC-32301 i

where:

l C = 1.165 b = 0.26 for M a<0.3 C = 0.905 b = 0.05 for 0.3 < Ma < 0.9 C = 1.0 b = 1.0 for Ma>0.9 A comparison of the Ogg correlation with the Vierow-Schrock correlation is shown in Figures 3.4-1 and 3.4-2. The f 2comparison shows that the two correlations are in reasonable agreement on the issue of the degradation due to the presence of noncondensable gas. The comparison of f icorrelations shows that Vierow-Schrock predicts a significantly higher amount of shear enhancement than does the Ogg correlation.

The helium / steam data were correlated also making use of the if correlation:

f2= 1 - CMab (3.4-1) where:

l C = 1.59 b = 0.29 for M a< 0. I 1 C = 0.865 b = 0.014 for 0. I 1 < Ma < 0.86 l

C = 1.0 b = 1.0 for Ma > 0.86 M ais the helium mass fraction in this case. 1 i

l l

3.5 Vial l Under the direction of Professor Schrock, Eric Vial [1993] developed a correlation from the combined databases of Vierow, Siddique, and Ogg. His effort involved only the development of a correlation and did not involve any additional experimental work. Each  !

of the databases had certain data points excluded from the combined database.

Vierow:

. Only the runs without the " temperature inversion" were used.

3-4

1

NEDC-32301

. At the inlet of the tube: 0.0103 < Ma< 0.148 7138 < Rem < 26300 Siddique:

. The data for the first 41 cm were excluded.

. At 41 cm from the inlet

0.131 < Ma < 0.525 1283 < Rem < 19905 Ogg:

. Only the data for the points located downstream of the temperature inversion region are taken into account; namely beyond the first 45 cm.

l

. At 45 cm from the inlet: 0.012 < Ma < 0.407

! 3247 < Rem < 39560 i

l Vial's correlation was of a similar form as Vierow & Schrock and also Ogg. The correlation is:

f i= 1 + 1.2x10-8 Rem2 for Rem < 5000 (3.5-1) f i= 0.76728 + 1.06543x10-4 Re m for Rem > 5000 f2= l- C M ab where:

C = 1.0946 b = 0.2344 for Ma<0.4 C = 0.9562 b = 0.0969 for 0.4 < Ma < 0.9 C = 1.0 b = 0.5229 for Ma>0.9 s

3-5

i NEDC-32301 l

The standard deviation is defined:

l i

' " ' f, - f,)

• s= f""' >

N = number ofpoints (3.5-2)

N-1 s = 0.3826 for the Vierow data set s = 0.4854 for the Siddique data set s = 0.4647 for the Ogg data set s = 0.4613 for the combined data set The data sets are plotted along with the new correlation in Figures 3.5-1 and 3.5-2.

i 3.6 Kuhn l l

From the results of Kuhn, UCB decided that a different form of the if correlation was required. The Kuhn pure steam data were not well correlated by the old form of the f icorrelation, which was only a function of mixture Reynolds number. The new fi is now a combination of the heat transfer enhancement due to interfacial shear and other factors:

fi = i f, f, i (3.6-1) where f,i is a function of film Reynolds number f,, = 4(Rer ) (3.6-2)

The f,i factor is the theoretical approximation derived from smooth intedace laminar film theory with interfacial shear. The f,i factor accounts for other influences such as interfacial disturbances, deviations from linear temperature profiles, and temperature 3-6

NEDC-32301 1

i dependent properties, etc. The f 2correlation remains in the same form as Vierow-Schrock, Ogg, and Vial. The complete data reduction of Kuhn is given as follows: l (1) Experimental Heat Transfer CoefTicient:

9 (3.6-3) h,(x) = 7,, , (x)' T,,,(x)

(2) Condensate Flow Rate:

x1)"q"(x)dx W,(x) = (3.6-4) hf F(x) = II'(x) (3.6-5)

M.

(3) Calculation of two film thickness, Si and 62: I l For the case without shear the film thickness is given by Equation 3.1-1.

l Rearranging to solve for F yields:

l T= Pf(Pf - Pg) (3.6-6)

With interfacial shear the predicted film thickness,62, is given implicitly by: I 2

i2 l

I = 3_ Pf(Pf - Pg)d + PrT S (3.6-7)

Pf 3 2pf l where Ti= f R PgVm (3.6-8) l f R= 0.046 Rem - (3.6-9) leading to the interfacial shear prediction 0.023 'p" r, - Re.i s (3.6-10) p, < D, ,

or rearranging Equation 3.6-7 gives:

! 3-7 l

NEDC-32301 I

)

i I= pf(1 - +

of pf )3 2ur (3.6-11)

F with (3.6-12)

Ref = Pf Now in dimensionless form 2

Si = LS (3.6-13)

, r, r, = r 3 (3.6-13b)

P. L gpf 1

< Pf ,

with characteristic length 23 3 L= Uf (3.6-14)

Then Re f P,

( 1 - P,,, / f

[ 3 r*6*,2 2

(3.6-15)

(4) Determination of the Correlation for f iFactor from Pure Steam Runs:

h f=i (3.6-16) h,i k

h,, = (3.6-17)

Assume fi is the combination of the heat transfer enhancement due to interfacial shear and other factors:

f=f1 1 shear *flother (3.6-18) 3-8

NEDC-32301 I

f hexp = hexpS2 (3.6-19) ishear = h T2 kr where S2 is obtained numerically from solution of Equation 3.6-7. Assume flother is a function of film Reynolds number f

f lother=g = 4(Ref) (3.6-20) 1 shear with 4(Rer)=1+ C3Ref (3.6-21) j (5) Determination of the Correlation for Degradation Factor h

f= =ff i 2 (3.6-22) h si with f 3= 4(Rem, Ref) (3.6-23) f = 1 - C2 M,'

2 (3.6-24) l Mixture Reynolds number 1

l

! Re,(x)= 4 W'"(x) (3.6-25)

, xDp, where i

X,p' (1 - X')p" (3.6-26) p" = X, + (1 - X,) , + X, , + (1 - X,)

with l

i f < 31/2r sl/4f 1+ b b

< p,, g M,,

p, =

~ -

l/2 (3.6-27)

T 1 8 '1 + "M

• 4

_r M, s _

and 3-9

NEDC-32301 2

[ r sl/ 2 r 31/41 1+ b s p,) s hi,)

p, = 1/ 2 (3.6-28) 8 1 +b

_( AI,s .

The correlation of Kuhn is:

f= f fl2 (3.6-22) fi = i f, f, i f,, detennined from Equation 3.6-19 f,i = 1 + 7.32x10-4Ref (3.6-20) b f2= (1 - C hia ) (3.6 24) where C = 2.601 b = 0.708 for hi a< 0.1 C = 1.0 b = 0.292 for hia > 0.1 For helium the fi correlation remains the same as the air correlation. The 2f correlation for helium is:

f2= l- C hi ab where:

C = 35.81 b = 1.074 for hi a< 0.01 C = 2.09 b = 0.457 for 0.01 < hia< 0.1 C = 1.0 b = 0.137 for hi a> 0.1 3-10

NEDC-32301 The fy correlation is plotted versus film Reynolds number along with the pure steam data in Figure 3.6-1. The correlation (and plot) were created from 33 pure steam runs. The standard deviation of the data from the fi correlation is 7.4%.

Figure 3.6-2 shows the f 2correlation (plotted as 1-f ) 2and the 68 steam / air cases from which it was calculated. The standard deviations for the data for the two different regions are shown on the plot. The experimental total degradation is plotted versus the degradation predicted by the Kuhn correlation in Figure 3.6-3. The extent of the data spread is evidenced by the standard deviation of 18% . This is considerably smaller than the standard deviations for the Vial correlation. The standard deviation of Ogg's data with his correlation was 27%. Figures 3.6-4 and 3.6-5 show the corresponding graphs for the steam / helium cases. The standard deviation is shown in Figure 3.6 5 to be 13%.

A comparison of the heat transfer coemeient predicted by the Kuhn correlation is made with the heat transfer coemcient predicted by Vierow and Schrock (Tsukuba) for the Kuhn experimental conditions in Figure 3.6-6. The crosses represent predictions of the correlations for the conditions of the 68 steam / air runs. Note that the Kuhn correlation predicts a consistently lower heat transfer coemeient than does Vierow-Schrock. The f 2correlation of Vierow and Schrock and the f2correlation of Kuhn are plotted versus air mass fraction in Figure 3.6-7. The plot shows that less degradation caused by the presence of air is predicted by Kuhn than is predicted by Vierow and Schrock. Because the Vierow-Schrock correlation was not applied directly in TRACG it is also useful to compare the TRACG correlation results with those of Kuhn. Figure 3.6-8 compares the Kuhn et al. correlation with the Vierow-Schrock correlation with the restriction that fi 5; 3. The additional changes for 4F/p > 1000 were not included. Most of the data are for values of 4F/ less than 1000. The restriction on fi brings the two correlations into better agreement, though Kuhn still predicts lower heat transfer coemcients. The impact of the different predictions will be discussed in Section 4.1.

Similar comparisons of Kuhn with Ogg and Vial are shown in Figures 3.6-9 and 3.6-10, respectively. The Kuhn correlation also predicts lower heat transfer coemeients than do these two correlations. Finally, a comparison was made against a general correlation for steam condensation inside of tubes found in Chen et. al. [1987). Though the applicability of this correlation to the present conditions may be questioned, the 3-11

NEDC-32301 comparison is made in order to satisfy the desire to compare the Kuhn correlation with any in the existing literature. Figure 3.6-11 shows that Kuhn also predicts a lower heat transfer coefficient than does Chen.

3-12

NEDC-32301 1

4 p.

i m g-g .{. . ..g m.

g.

. . . . . . .. . 3. 7g..... ..

15 E

.l 1 5'

~

t

i u- ip E u i,

.u . , g_!. L g .,. . g i 2 i  ! - x a5 - g - --- - + - + -

        -                                                    m 8

e .

                                                  ~

m j i a a a E B j i i 0.1 0.1 1 O.01 Local Air Mass Fraction Figure 3.1-1. Data Plotted in the Form of the Vierow-Schrock [1991] Correlation. The Factor 1-Oft is Plotted Versus Local Air Mass Fraction (Used with permission) 3-13

NEDC-32301 100000 , 4 l 4 O B 10000 - .h ' O ~ u t: - j O kj 1000 ,

              -          O O       O O        O
               .                            O OO O

OO o 100 .. 1000 10000 100000 100 Nu Experimental Figure 3.3-1. A Comparison of the Air / Steam Nusselt Numbers Produced by the Siddique [1992] Correlation Versus the Experimental Nusselt Numbers (Used with permission) 3-14

NEDC-32301 comparison or f1 correlations 10 9 8 7 ' e ygg

• 5

                             /                                             _ _ _ _ _ _ ogg 3
                                           ~~~____ -

1- # 0 0 10000 20000 30000 40000 50000 Mixture Re Figure 3.4-1. A Comparison of the f Correlations i of Vierow and Schrock (1991] and Ogg [1991] Plotted Against Mixture Reynolds number 3-15

NEDC-32301 Comparison of f2 correlations

        $'N 4
               *~
                                                                \ ,

y&s Cf \ - - - Ogg N 0.01 0.001 0.2 0.4 0.6 0.8 i 0 Air mass fraction Figure 3.4-2. Comparison of the2 f Correlation of Vierow and Schrock [1991] and Ogg Plotted Against Air Mass Fraction 3-16

1 i l l lViliROWl lg,l

       ,_                                                                             i-                                                                                                             l
                        , '. s
                         , . ... n. ..s . . .. . .

w:;. 1

                          *. 2,

• e
• 1 's r

                                      * . . . a.
                                                          ..                           ,.                                         pf5 *
                                                                                                                                                                    . I $.

l

        .-              s t.           j. . .
                                                                                                                                                             ~. . .           ..
                               .:e..
                                         ~
                                                                                                                 -. .... .m%.,_.. . . - u..

y r. C r .. l,, 'N..*.,.... l

                                                                              ~~
  %                                                                                        .    ~.                      .

as 3 ., ., ...

                                                                                                                                                          ....                                     i c                                 .

g s.- . . ..,. . . . .  % g ,. .. g . . , .

                                                                                                                                 .            ...*                                       In e

g O e .. .. . . c.y Y J . u

                                 .                                                                   ,         ,                                                         .               N q v-                                                                                                              .                                                                       u
                                                                                                                                                       -                                 oa
       '~i 0 0t i   i ; ii;;

01 i i ; i ; ;i'T I

                                                                                      *i 0 08 ot                                          i Gas mass fraction Ma                                                                         Gas mass fraction Ma l

Figure 3.5-1. Plots of the Vierow [1990] and Ogg [1991] Data Plotted Along with the Vial Correlation

ISIDDlQUEl lVIEROW, OGG, SIDDIOUEl

                                                                                                                    '~
      '~
                                                                       ,,.,..5. . . .
                                                           . *. . , e/e s
                                                                                        ...     .. e-; .
                                                                                                                     ..                                  ,,.atp,,. .-:%......
                                                                                                                                                                                , 4$

2.y < .

                                                                                                                                                                                      .    +..
       ..          ..                               . ,3        ***

3.s.1 .y ';* -*' ,

e. - ; ,PS;;.,_

                                                                                                                                                                - ' ', . z.. .W,::-

I

                                                    .s ...i .           * .* 4
                                                                       ..-f...Mit'
                                                                                                                      *-                     ny::::..tl' S*

!. c,j .. , - .

                   +                                                                                                        .,          ,                          .
                                                       .        . .'.e.:

4 e..

                                                                                                                                                  ..         ...-/-                   ,
                                                                    's..                                              '            '
                                                           , . *3 j,                    *                                                        ,*.                                *
                                                      ,s.         .                               .               p                                                     ', * .

l .-

                                                    .                                                             t

_e . , .

                                                    ... i                                                    s                                        ..
   )                  .                      6             .

T R _. , m 7

                                                                                                                                                         -                                               D

,a o. s.:  !  !, U .' l N co i .. G3 O i  % i i;iii '~i i i i iiiiii i i i ; i ii'1

         'i                                    i              i        i 0 01                                            0t                              i 0t                                                                                                  t Gas mass traction Ma                                                                                  Gas mass traction Ma Figure 3.5-2.                                  Plots of Both the Siddique [1992] Data and the Combined Data Base Along with the Vial Correlation

l33 Pure steam runs l 2.0 - _; 33 Runs 1.9 -- , - - +- -.4 +--.- ... . . . 9 1.8 - ! --

                                                                             +               y              ;            -                   L ---                  - . - -

jjj 1.7 - 7- - -- f / fish.,= 1 +7.32* 10"*Re f *- - - - r ---- llI.) 1.2-5 1.6 - [ I d---. STD=0.0736 . _ _ . . . . _ . . _ . . . . _ . . . . . . 1.3-4 3 l 1.5 - - + > 1 i -, l3~5,4 j 1.4-5 b1.4-m

• l-- +

O t i

                                                                                             +

i t 6 4 + + i O _ __.. g_b -d ~~ 9 I 0-- i 2 0~-~& O c 1.3 - e +- e-8O O O t-~~~----!o % O Y u 1.2 -- t SO -@-- fo-O "!l oO - - O% O u E E @ g1.1- o O gg-Oo ----tOof O t O-o - o o . _. 1.0 - - ... _ ___ 0.9 - h --+

                                          ' O- _O_!_g 0._ _        _                           , __               __              . _ . .               _                          _.,

I 4-  ; -4 --- - - - , 0.8 - t O.7 - I ~

                                                     --+----+----l-

• k'- -+- - -<

0.6 - I t- -i- - 0.5 - k I I I i i i ll l l l 0 50 100 150 200 250 300 350 400 450 500

                                                                                             %.i i

Figure 3.6-1. Plots of f /fi ishear Versus Film Reynolds Number for the Pure Steam Data of Kuhn et al. [1994] l

l68 Steam-Air Mixture Runs l r " 1- L.-...-.... .i.. . .j. . [ . i

                                                                                                                                                                                              ..l. 4.. }..                           1__           -- 4                L........     ..
                                                                                                                                                                                                                                                                                                          ..5...

g.. b, *5-[ # I .- . b < 8-i-- j,...g.. ,. ,; .,.. a... .)3 t.g

                                                                                                                                                                                                                                                                                     .y_.4.~._v.-                ,

7 ; p ... .;... .4.....,..~.4_.9 4 .g gy, g, ,

                                                                                                                                                                                                                                                               '   *3
                                                                                                                                                                                                                                 - .; p             ;.
                                                                                                                                                                    !        .         . . .                  t..        < .i **                 . cr.                      :                :
                                                                                                                                                                                                                                                                                   -t -t-t-t-t-,

i : . e,.g,- sr . -- e s- - t t-- -t--t-- 7 , e. 5 -- t-

                                                                                                                                                                     ; , c{e
                                                                                                                                                                              - c,c,r, gi.

s

,. b N + *..... , 4- -+"

                                                                                                                                                               ,:                     ..                +          , . . -                                                                   w/o :

i .

                                                                                                          .t                             ,.,         .:.....L.,. g        ..
                                                                                                                                                                                               .. y y ; W
                                                                                                                                                                                                 .                                     ...:                + .. . .- ;                +- 3,4.g ..+_

4 i 3.5-2 i

                                                                                                                                               ~
                                                                                                                                                 . 'j *,

• i . * , #l ' *l +- 3.5-3 +.

L 3- s

                                                                                                                          ; . --j;.; .-+ - . ,yL- -.                                              --
                                                                                                          .i                              .              .
                                                                                 -                        s   -
                                                                                                                                                    'r'                        -     -- l-                    ?-

R 2 -- i- - - 1 *.s--*-L--*---

• IT1 i

g

                                                         ,                     .     =,        ..

i  : O. w  % i

u

 .                                                                                                                                                                                                                                                                                                                       to o                                                       -
                                                                                                               .i.                                                                         i                                                                                                                             u o                                                                                                                                                                                                                                                                                     *--+---4--2---*--                  O
                                                                                                           --'--------*--'-+---4----'--+---+-4---                                                                 ---

0 1,-_ _ - _ * ., . - -

~ -i- 4--;_ STD=0.1056 0.1 < Ma ~..-_4._.H r , _4 - -

s- -

                                                                                     ----.-.-I----+                                                      --------!               !                 L L---j - STD=0.3071                              0.1 > Ma                          -
                                                                                                                                                                                                                                                                                               '- +-... +        "..,
                                                                                                                                                                                                                                                             .                         -     ~               .L 1 p....,..

4-.. 7 i

g. . - . . . . -

                                                                                                          ...i...                                             . - .-.. j-                                                               ..4......         - 4.                              .......;..
                                                                                                                                                                         -"+-i--*                                          --- -~~ L                              --
                                                                                                                                                                                                                                                                                                         -4        +         1
                                                                                                                                                                                                          "- {

5- .--

                                                                                      *                                                                                 .-.,4.-~....                      . . . . . .       .......-....:...                ..v
                                                                                                                                                                                                                                                                                                    ..s-....'...;

p 4 . . . . . .. 3- - - - - - - r-+ " + -+ - - - -

                                                                                                                                                                                                                                                                                                  ' - + - -

i. 2., 2 3 4 5 6 7 8 9 g 2 3 4 5 6 7 8 9 1 0.01 0.1 Ma Figure 3.6-2. Plot of the Kuhn Steam / Air Data Along with the Kuhn et al. [1994] Correlation for 68 Steam / Air Runs (The ordinate is equivalent to 1- f2)

l68 Steam-air Mixture Runs l 1.2 - --- T~~ r l- ~ i T

                                                                                             "~          "~         "             -~         ~~~               '

t i  !  !  !

                                                                                                                                                            +

1.1 - + f=f1 *f 2 +- - + - - - - -

                                                                                                                                                         +-                 ----*

f 1 = f 1 T*(1 + 7.3 2

• 10"*Re,f) + + ++

1.0 - +' f 2=1 -2.601 *Ma

• Ma < 0.1

                                                                                            ~ ' ~ ~ ~ - '        ~~'
                                                                                                                        +

f 2= 1 -Ma" Ma > 0.1 g,_ +++M _+._ 0.9 - STD=0.1764 + .g+ 0.8 -

                                                                                             +

E *pN #+4+$ - - - - - - - - - F 0.7 - - - - - --

                                                                          - -.        4H-p                     - + Q ~---
                                                                                                                                                              -i                          M o
                                                                                  +
                                                                            *         +                                                                                                   $

k 0.6 - +-- r 4- ----

                               -r-      ~                                                                   -
            ~- -

0.5 - - K  % 4)tt t- t --- "-

                                                                                                                            -+-
                                                                                                                                                              -t---           -

0.4 - t- i 0.3 - +

                         - - + -
                                    "+ y
                                                            ^
                                                                                             +          +            *                           - - -
                                                                                                                                                              +                 --

0.2 - -- I h +-~

                                                                 +
                                                                                             ~+-        4                                                        *                   -
                             -lE                                                                                      .
                                                                                                                      ~

0.1 -

                               -+

0.0 - 1 I I I I I I I I I I I I 0.0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1.0 1.1 1.2 I kunn. corr Figure 3.6-3. Plot of the Steam / Air Mixture Experimental Degradation Factor Versus the Degradation Factor Predicted by the Kuhn et al. [1994] Correlation

l24 Steam-Helium Mixture Runs l 1-

g. .. ; . . . . . t .._. . . . h .. .m _ ......m....a... .h.........y... . , . . . .,..

8_ ......_1...4._ . .. 4. ..... 4 .. . . . ;. . . . + . . + . . . . . + . . . _ + . . ........ . ?*" ' ' 11 ..

                                                                                                                                                                                                                     .+.._..+...+.........t..

7- - j --- + - - 4~4 - - - - - - - - . - - g *dt * ,

                                                                                                                                                                                           - I-d--                         --p-------+--+--

. ..-.e

• E.... ...h... ......--...b.h...yo- e 4-4 ha 4 d... w ..g... .4.. ..

                     !                                                                                          !-          .v.,                    .

• j 5- -

i--4-+ --i 7 -

                                                                   - - -- q ;---                         ,--4 +- I , - + *

• f ' I- - " d- +- -r- - h - "-- +-- i -

i 4- --:-- -+-+--4-*---**- -* . ' f-*--l-+ 4- - + - L---4 5 L ~

                             - - + - - :- - - - - + - --t*~*                                 *-= -                                    --+-"-+lL-++-                               --

4- - - r 3-

. y .,.. ,. .:

STD=0.0543 1 < Ma < 0.1 2 3 2- - - - 4 -- --+- --+ ~ STD=0.1514 0.1 < Ma < 0.01

                                                                                                                                                                                                                                                             ~'

D 0 y

                                                           .:-                                                                                                      STD=0.4971                         0.01 < Ma < 0.003 to u                           .. -              .

o w - o a I

                             .'                                                                                                               .-.~..l--*-                                          =       . . . , .               . . . . . . . .      . . .
                                                     ,.                                              +      . . . . . . . . . . . . .                                  .-4.--

_m . ..

            ....                                                                                                                                                       A-9-      -                                  -

t - - - ^

                                                                                                             ~4-              - - - - - -                   - -                                    -               "                     - - --- <

g. ..... . . . .

                                                                                                                             ..9.
                                                                                                     .       -. y .                  .. .                        .                                 .                  . . z. . .. .                  . . . . . .

7_ . . . . . . . 6- ' . - 1 - - - - - < -

g. .

l 4- . . . . . . . . . . . . , , , , , , , I 5 6 789 .i i .

                                                          .i                                         2          3                4                                                                 2            3       4     5 6 7 89 3           4         5 6 7 89 O.01                                                                                                         0.1                                                                                       1 IW1 Figure 3.6-4. Plot of the Kuhn Steam /IIelium Data Along with the Kuhn et al. [1994]

IIelium Correlation for 24 Steam / Air Runs (The ordinate is equivalent to l 1-f) 2

l24 Steam-Helium Mixture Runs l j,j _ ,_ ,. ,. , , ._ . - _ . . . - _ - . . , 1.0 - * - - - - r -4 --

                                                                                                                                 - -- d +          44               ,

_p

                                                                                                                                  + +
                                                                                                                                                      ++$; 4 +g.--

0.9 - t-

                                     *-               r                          r                           *-
                                                                                                                       - ++ y(+$--
                                                                                                                            +l             4-        ++                      +
                                                                                                        +

• 0.8 - ' - -- - -

p - - -

                                                                                                      ++                    +4++ f@

0.7 -

• 2- *-- - + , + + '-

                                                                                                                       +                                                          2
                                                                                          +

a 0.6 -

          +                  - - * -                  +-            -

ff-+- p ++--'-~~ - - - Y 5 + S S ' O.5- ' - - - - - +- +j .gb+-h -1; -- - - -

                                                                                                                                                            -+--                  g
                                                                    +++           4 + p--                                                                                         o
                                                                            +                                                + - -

0.4 - + + +- i -r +I-h-- ' i -

                                                                                                                                                        --+---

t ++

                                                     +                        f=f1 *f 2 0.3 -   +-           <

r -- [ 4b --

                                                ++                 +          f 1 = f 1 T * ( 1 + 7.3 2

• 10"* R e,f) 0.2 - *--- - -- - '~

f2=1-aMa a=35.81, b=1.074 0.003< Ma <0.01 f a=2.09, b=0.457 0.01 < Ma <0.1 i 0.1 - *- - ' a= 1.0, b=0.137 0.1 < Ma STD=0.1297 l 0.0 - - - ' -4~ -- - ---'- il i i i i I I I I I I I I l 0.0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1.0 1.1 l I Kuhn. corr l Figure 3.6-5. Plot of the Steam /IIelium Mixture Experimental Degradation Factor Versus the Degradation Factor Predicted by the Kuhn et al. [1994] fielium Correlation

i ! . ! . i .!

                                                                                 +-+-r-+-+

r- +- - - 10000- 4-+- +-+t + F- t L+t..+t+"-~~' a_ !_L .!._L.i. _. .-- L.. ._. 2...-. 4._2.. L2 . 2 J..-.- 1-+.  :

                                                                                                                                                                                                                      ~~
                                                                                                                  - - ' -                     --                               -~~"- ---
                                                                             -~-                    " ----
                                                             - ~~

8- - - - - - -

                                                                                                                                                                  +

e. t ;

                                                                                                                ~---*-                   - --
                                                                                                                                                                  - g+

s- ----<- r g ,z 4 ._.4 ;. . .7 .. I

                                                                          ._.._ -.+..;tt                                    4_ f   .
                                                                                                                                                                       '.h                L-      -
                                                                                                                                                                                                     -.+-e-4-.

9  % a E 3- +

                                                                        .f+!+Y  y+- +M+4                 i
                                                                                                             --                   ' ~,w:u:p,.p+:                    ..
                                                                    +        #                                              % !             +-W++

g

                                                                                               .g.... m i,           .....,..;...a...........           ....+.

g it;$MH y h ... -- ..,. ,.- - - , . .

                                                                                                                                                                                                          - - - , . ~ . . . . - .

rn O 2 7.-p y o f s .

                                                    *+              + p; + h.

2 m

                                                    + ++                                                                                                                                                                                                                                     8
                                               +

f$l 4++-

                                                    +. ,h+4 i     !+                   % +

i 4 1000- i++ Y+h~~ -

                           ....j      1-. .                  a...                                               + - - .             4 --                                                    1        4~.~ . .+ -.v- .

g. 4.. +4 -'

1 1 0- i i '-- -i f.4+. -- 4;---t--""; i J. . 1 . 4..

                                                              ! . .-                b.-.i
                                                                                                                                                                            ;                                  .-4                                       -

4.._4 .. i... . .. j. e 7

; +l t

                                                                                                                            "+-
                                                                                                                                                                                                     '-"--4'"

6- - h 4- i-fi Ii i'

                                           '                                                 ~ ~ ~ - ' '

5- e i e i i i e ig i i e i i e ig i e 4 i 5 6 7 8 2 3 4 5 6 7 89 2 3 6 7 89 1000 10000 2 u (W/m C)

                                                                                   ' 'Wwow. corr Figure 3.6-6.                    Plot of the Heat Transfer Coemeient Predicted by the Kuhn et al. [1994]

Steam / Air Correlation Versus the Ileat Transfer Coemcient Predicted by the Vierow and Schrock Correlation

I- h5EDC.32301 s t i I l l 1 3 i4 , 1 i a comparison of f2 Correlations i 1

                   '%                                                                                                         \

i '~ ~.~. ~ ~ . ~ *

                                                   .,,~~~.

1 0.1 , 4 N .V&S i l

w

  ~

N. j \ - - Kuhn s 0.01 si i ! 0.001 i

'              O                  0.2        0.4           0.6             0.8                 1 i

i Air mass fraction i i , Figure 3.6-7. Comparison of the f 2Correlation of Vierow and Schrock and Kuhn et al. a [1994) Plotted Against AirMassFraction 1 i k l l l 4 b-3-25 i

i i + 10000- -+-J l 1 4 +- i i-! i 9 4 .. . ; .. .. j .. .4 . 4.. .. i.. . . . . . .

                                                                                                                                                                                                                  ..+..+

i +

                                                                                                                                                                                      . . . . . . . . . .. -t . .It.gi.

e. .

                                                  .. l ..                                                   ...                                                              ..

3 4..._............. 7 . . . . _ . . .l .. .. 6 .. i- . } -. ..+.. . - o. . . - . . . . . . . . . . . . < 4

s. . . . . . -. 1............ .

C 4 . 1. . . . . , . , . . . . .. 9...

• I n

e +g + & t_., s 3 , .+ y - 2

                      $                                                             %+t_++;i.
                                                                                                                                  !                                                                                      m o,      2   .,                                   4

_ _4 . . . O g 4 3

                                                                                       ++                                                           i                                                                    9 s   $                                              + ++                                                                                                                                                  $
                                                 +        +                 4                                                                                                                                            9
                                                                   ,     + +4
                                                                                                                                                                        +

1000- - , - '- t -

g. ..

                                                                                #r

e. ...;..

4 .+. ..

                                                                                            .......           ..,.......                            p..

7 + - ..

                                                                       -t -      -.-    -

i-- .- --i-- -+. - . . . 6 + + t

                                                                                                                                                                        +

54 I d i 4 5 5 i &4 i i HTRAC-G(W/M b) Figure 3.6-8. Plot of the IIcat Transfer Coeflicient Predicted by the Kuhn et al. [1994] Steam / Air Correlation Versus the IIcat Transfer Coeflicient Predicted by the Correlation Currently in TRACG

10000- 4---4 [ t H 4-+-d h h +i o-

                              >     =         '                    ..
                                                                                 .l..                                                                                                                                                i                             ._    2. . i ._4.              t_..]                              +t.+                             4
                                                                                                                                                                                                                                     ?

Y--- - 8-7- t- &  ;-- - a-  ;- p- t- ;- t ; t-L - -+ j I--+_ -I 6-s- -, l- -r- L , - - - , p ^#ib

                                                                                                                                                                                                                                                                          -- M-W        ,+

5 + r ,. 4- -._, + 4,,+-+ ++ ++g 7 9+ r t---- t 3 .,,

                                                                                                                                                                                                                        +*+                      $_.#I I...

e f  : db g f +% Iff"' k f 2 y +$ k. ._ t + 8 m + ++

                                      + +                                                         4                                                                                            3                                                                                                                                                                                          2
                                                                                       +

1000- [ 4t++Y .

                                                                                                                                                                                                                                                                -+--t--t--+-+-                                                                                              1 t

9-

                                +--t4--+                              *--[-++----                                                                                                                                                                                                                           4 ---

8- g-----p -- i------ + 7_ . t - ... . . . _ . . .. _ . . . . . . . . . . . _ , . . . . . . . . . . . .

                                                                                                                                                                                                                                                                                                                                     ..7...  . . . _ . . _

s. ;.. .g_4 .. . . . _ . . . . _ . ...;.. ..

4._.9

                                                                                                                                                                                                                                                    ! ---- i --- ? -                                 -+-                                                                  -

5- -- - - l- : - - -

                                $     5h5$I                                                                                                                                                                          h                 $            $             $       hh$dI                                                         5                                    5 1000                                                                                                                                                                                                                        10000 Niatcorr Figure 3.6-9. Plot of the Heat Transfer Coeflicient Predicted by the Kuhn et al. [1994]

Steam / Air Correlation Versus the Heat Transfer Coeflicient Predicted by the Vial Correlation

                                                                                                                         '                                             '                                                          '                          i                                                     +        i 4'                  +                                          - - + - - + - + - -4 10000- b---+              -

? -+

2 :_ _1.._ : +++

1. i..a.... 4...

                                                                                                                                                                                                                                                             + ++
                                                                          ,. 1                   .

s- -- b I- b-- + 1- 4 - -r--+- -- i i - -- 4

                                                                                                                                                                                                                                      -} ~ -                                                                             --i l

s- + .

                                                                              +
                                                                                                                                                                                                           -                                      ' 1-5-.+         4---+--+- !                                                  +               -- 4 4                      F y_.                                  ,

4 ,

                                                                                                                                                                   +h                 .4..

[ I 1 p 3 e . 8,

                                                                                                                                                                                       +                                                                                                                                                                                       2
                                                                                                                                      - + E81+k                                                                          - - + - + -                                 +------                         - - - - - - - - - -
                                                                                                                                                                                                                                                                                                                            -i                                                 $

f 2- 4-------'----- - --- ;-- - -;- - +

                                                                                                                                                     +-
                                                                                                                                                     %                  k'                *
                                                                                                                                                                                           ~

o y g+ o eo w a  ;+ + s g i A_ +- -'

                                                                                                    !.i+!

4 4-4 4- af ~

Ih

                                                                                                                   +'                                                      ;-                                                                                           j                                                  -j 1000- 7                                                                                                                                                                                                                                                i 9-             .         .

e- +--  ;- s- ;  ; p 4 _l

                                                                                   .._.._.9..-9..... _ . _ .

I 4 7 .

                                                                                                                                                                                     - ~+                                ^4--               +---

t 6- 4 " 4 - ---- -" -~{4h'

                                                                                                                                                                                  .._- _ .a                  - . = . .                           . ..s .

s. . . 2.. . u a - .. ;.. ... . . . . , , .

4 5 6 7 8 9 2 6 7 8 9 2 3 5 10000 1000 kg.wrr Figure 3.6-10. Plot of the Heat Transfer Coemcient Predicted by the Kuhn et al. [1994] Steam / Air Correlation Versus the Heat Transfer Coemcient Predicted by the Ogg Correlation

                                                                                                                                                                                                                                                                                                                                             +
                                                                                                                                                                                                                                                                                                                                                -.~.~._

14x10 - 1 e f

                                                                                                                                                                                                                                                                                                                                      *+
                                                                                                                                                                                                                                                                                                                                              +
                                                                                                                                                                                                                                                                                                                                              +

12- $ ,

                                                                                                                                                                                                                                                                                                         +                        +
                                                                                                                                                                                                                                                                                                                        ++
                                                 -                                                                                                                                                                                                                                                       +              ++

9 ++ E s +1_ . .tr-10- _f +

                                                                                                                                                                                                                                                                                                      * +p+
                                                                                                                                                                                                                                                                                                              .                                                                          z j                                                                                                                                                                                                                                     ..

H- ..

                                                                                                                                                                                                                                                                                                  ++++*.                                                                                 f71 n

E = u x 2 p %q-- _+ -

                                                                                                                                                                                                                                                                                                                   . . . _ _                                                             Q f--
                                                                                                                                                                                                                                                                                                                                                                       ~ . . . . . . . .

b 8- w _.ggg+& A # ... . 6- ' F 4- . i ~ ~ ~ ~ ~ ~ ~ ~ ~ I f i 6 8 10 14x10' 2 Hchon.co,, (W/m C) Figure 3.6-11. Plot of the IIeat Transfer Coemeient Predicted by the Kuhn et al. [1994] Steam / Air Correlation Versus the IIeat Transfer Coemcient Predicted by the Chen [1987] Correlation

NEDC-32301

4. DISCUSSION 4.1 Impact on TRACG Analysis

The results presented in Section 3 show that the correlation in TRACG predicts a higher heat transfer coeflicient (htc) than the Kuhn correlation. The potential impact of this result on the post-LOCA containment performance analysis should be evaluated by 4

considering the overall thermal resistance from the steam inside the tube to the pool outside. Typically, the current TRACG correlation predicts that the inside resistance is about 25% of the total. From the results shown in Figure 3.6-8, the Kuhn correlation would raise the inside resistance to about 35% of the total resistance. The effect of this change is equivalent to a 20% reduction in the condenser heat transfer area. Kim et al. [1993], submitted to the NRC in February 1993, presented the results of a TRACG sensitivity study in which the PCCS heat transfer area was reduced by 33%. It was shown that the effect was to raise the containment pressure by 17 kPa (2.5 psi). For a 20% reduction in heat transfer area, the expected effect would be a 10 kPa (1.5 psi) increase. In the same reference, it was stated that improvements in the containment model had resulted l in a decrease in the peak containment pressure relative to that presented in GE-NE [1992], submitted to the NRC in August 1992. The magnitude of this decrease is larger than the expected increase from the use of the Kuhn correlation. Thus, the peak pressure predicted with the current model and the Kuhn correlation will be less than the value presented in I the SSAR. An additional indication of the relatively small sensitivity of predicted condenser performance to a reduction in the inside hte is provided by the comparison of TRACG predictions with GIRAFFE data presented in Andersen [1993], also submitted to the NRC in February 1993. Those comparisons, made with the Tsukuba correlation, show satisfactory agreement of the TRACG predictions with both the Step 1 steady-state condenser performance, and Step 3 integral system test results. 4.2 Applicability of Kuhn Correlation to IC Tubes The applicability of the Kuhn correlation to high pressure pure steam environments will be addressed initially here in this report and also in Schrock et al. [1994]. The IC tubes operate at pressures near 70 atmospheres. The maximum pressure tested in the university tests is 5 atmospheres. The data of Kuhn are well correlated over the range of 1 4-1

NEDC-32301 to 5 atmospheres. Because the IC tubes will generally experience minimal degradation due the presence of noncondensable gases, the 2 f correlation is not critical. The f,, correlation, on the other hand, is relevant and includes first order effects of pressure in Equation 3.6-10 in the 0.023/p gterm. As the pressure increases, the shear enhancement is reduced in a linear manner. The sensitivity of the TRACG analysis of the IC performance is expected to be very small because the limiting resistance is not the gas-side resistance. Because the ICs contain only small amounts of noncondensable gases and have thicker tubes, the gas-side resistance will be an even smaller part of the overall resistance in the IC's than it is in the TRACG PCCS performance analysis. 1 l I 1 4-2

NEDC-32301 5.0

SUMMARY

4 When this experimental program began, there was no known local heat transfer data or correlation for forced flow steam condensation inside of tubes in the presence of noncondensables. At two universities, five experiments using four different test rigs have now investigated this phenomenon. Lessons learned from each of them were applied to subsequent tests, such that the final test at UC Berkeley has produced a correlated data set 1 with a standard deviation of only 18%. The effect of the most recent data on the SBWR post-LOCA containment analysis has been evaluated by comparison with a previous , sensitivity study on PCCS heat transfer area. The results indicate that the effect is small and bounded by the peak containment pressure presented in the August 1992 SSAR. 4 4 4 4 5-1

NEDC-32301

6.0 REFERENCES

i Andersen, J. G. M. et al.,1993, TRACG Oualification, NEDE-32177P, Rev.1, Class 3, June 1993. Chen, S. L., Gerner, F. M. and Tien, C. L., 1987, " General Film Condensation - Correlations," Experimental Heat Transfer, Vol.1, pp. 93-107. GE-NE,1992, SBWR Standard Safety Analysis Reoort,25A5113, Rev. A, August 1992. Golay, M. W.,1993, phone conversation with W. R. Usry, October 1993. i Kim, H. T., et al,1993, Apolication of TRACG Model to SBWR Licensing Safety Analysis. NEDE-32178P, Class 3, February 1993. Kuhn, J. S. Z., Schrock, V. E., Peterson, P. F.,1994, in preparation. Ogg, D. G.,1991, " Vertical Downflow Condensation Heat Transfer in Gas-Steam

Mixtures", M.S. Thesis, U.C. Berkeley Dept. of Nuclear Engineering.

4 Schrock, V. E.,1993, Presentation to the NRC on the subject of the Single Tube Condensation Tests, San Jose, June 10,1993. Schrock, V.E., Peterson, P.F., Kuhn, J.S.Z., Yuann, R.Y., Ogg, D.G., Kageyama, T., Vial, E., and Vierow, K.M.,1994, Final Report of the UCB Study of Condensation Phenomenon in the Presence of Noncondensables, in preparation. Siddique, M.,1992, "The Effects of Noncondensable Gases on Steam Condensation Under Forced Convection Conditions", Doctor of Philosophy Dissertation, Massachusetts

; Institute of Technology.

Vial, E., and Schrock, V. E.,1993, "A Correlation Based on the Combined UCB and MIT Data Sets for Condensation Inside Tubes with Noncondensable Gas", UCB-NE-4193, April 1993. 6-1

l NEDC-32301 Vierow, K. M.,1990, " Behavior of Steam-Air Systems Condensing in Cocurrent Vertical j Downflow", M.S. Thesis, U.C. Berkeley Dept. of Nuclear Engineering. j Vierow, K. M. .tnd Schrock, V. E.,1991, " Condensation in a Natural Circulation Loop with Noncondensable Gases, Part I and II", Proceedings of the International Conference on Multiphase Flows, Tsukuba, Japan. Vierow, K. M., Fitch, J.R., Cooke, F.E.,1992, " Analysis of SBWR Passive Containment Cooling Following a LOCA", International Conference on the Design and Safety of Advanced Nuclear Power Plants, Tokyo, Japan. Wilkins, D. R., Hucik, S.A., Berglund, R.C., McCandless, R.J.,1992, "GE Advanced Boiling Water Reactors for the 1990's and Beyond", International Conference on the Design and Safety of Advanced Nuclear Power Plants, Tokyo, Japan. 6-2

NEDC-32301 a l N 9 APPENDIX Kuhn data used for pressure drop calculation 4 4 9 l

• l l

i l 1 l .l 4 l l l l l l

Run 1.1-1 116.1 KPa Tc i = 31.5 *C Tc-fit =D Ws = 60.2 Ku/hr Pinlet = 52.0 *C Point =11 Wg = Kg/hr Tinlet = 138.8 *C Tc.o =

                                                                                                                              .0                                                                                                                                                                                                                                                                                                                  STPD =                     .19 *C Wew = 999.8                                      Kg/hr Tcl          drew /dX                                             q'                     Wcond    Wst eam   Film-dx Ta        Tcw                                       Tc-Int                                                                             Two            'lw                                                     Twi                                                      Tsat Kg/hr      Kg/hr             m Lengt h                                                                                                                                                                                                                                                                                                                         *C                         *C                  'C/m                            W/m*2 cm                                        *C              'C                                                       *C                                                            'C           'C                                                             *C 7.041                     .548E+05                                     2.17     58.03    721E-04 51.0                                                                                94.1                                                       99.0                                                      103.9                                 136.8                                                                                                        .874E-04 17.0                                     47.5        51.4                                                                                                                       93.0 103.9                                 136.5                  6.945                    .540E+05                                     3.85     56.35 30.4                                     46.0        50.0                                             50.1                                                                      92.3      93.3                                                        98.2 6.845 .533E*05                                                        5.60     54.60  .992E-04 49.1                                                                     91.1       92.1                                                       96.9                                                     103.9                                 136.0 44.6                                     45.1        49.0                                                                                                                                                                                                                                                                                            135.4                  6.728                     .523E+05                                    7.66     52.54  .110E-03 48.1                                                                                                                       91.3      92.3                                                        97.0                                                     103.9                                                                                                                                       50.36  .120E-03 61.5                                     44.0                                                          47.9 103.9                                 134.7                  6.604                     .514E+05                                    9.84 42.8        46.9                                              46.7                                                                      90.6      91.6                                                       96.2                                                                                                                                                                                      12.15      48.05  .129E-03 79.8 90.4                                                       94.9                                                      103.9                                133.9                  6.472                     .503E+05 99.6                                     41.1        45.3                                              45.4                                                                       89.4 133.1                  6.330                     .492E+05                                  14.63      45.57  .137E-03 44.0                                                                      88.9     89.9                                                       94.4                                                     103.9                                                                                                                                       42.92  .145E-03 121.3                                     39.8        44.0 103.9                                 132.5                  6.178                     .481E+05                                  17.28 145.1                                     38.4        42.7                                              42.5                                                                       88.7     89.6                                                       93.9 103.9                                131.5                  6.014                     .468E+05                                  20.11       40.09 .154E-03     R 36.8        40.9                                               40.9                                                                      84.9     85.8                                                        90.1                                                                                                                                                                                     23.24       36.96 .162E-03 171.5                                                                                                                                                                                                                                                   87.6                                                     103.9                                130.6                  5.833                     .454E+05 201.5                                     34.8         38.9                                               39.1                                                                     82.6     83.5 O
                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                    +

4 M Length Re,I X Gas [1 Gas P steam P gas p(mix)a Re(mix) Htheor Hexp Dfactor R(in) ma 2*C/W R(tube) a m 2*C/W R(out) m* 2*C/ W h KPa KPa Kg/m 2 W/m*2.*C W/ m^ 2 . *C cm rrass % mole %

                                                                                                                                                                                                                                                                                                                                                                                                                                      .946E+04          .113E+05                                      1.199                     .882E-04     .109E-03   .821E-03
                                                                                                                                           .000                                                         000                                                       116.1                      .0                       .122E-04                                                      . 354 E+ 05
                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                             .109E-03   .835E-03 17.0          .145E*02                                                                                                                                                                                                         .222E-04                                                      .344E*05                                          .780E*04           .949E+04                                     1.217                     .105E-03
                                                                                                                                           .000                                                  .000                                                             116.1                      .0                                                                                                                                                                                                                                              .109E-03   .843E-03 30.4           .256E+02
                                                                                                                                                                                                                                                                                             .0                       .122E-04                                                       .333E+05                                         .687E+04           .766E+04                                     1.115 .131E-03 44.6            .371E*02                            .000                                                  .000                                                              116.1                                                                                                                                                                                                                               1.237                     .131E-03    .109E-03   .886E-03 116.1                      .0                      .122E-04                                                        .320E+05                                        .619E+04           .765E+04 61.5            .507E+02                            .000                                                         000
                                                                                                                                                                                                                                                                                                                                                                                                                                      .568E*04           .674E+04                                      1.186                     .148E-03    .110E-03   .914E-03
                                                                                                                                                                                                  .000                                                             116.1                      .0                       .122E-04                                                      .307E+05                                                                                                                                                           .935E-03 79.8            .649E*02                             .000
                                                                                                                                                                                                                                                                                                                                                                                                                                      .529E*04           .565E*04                                      1.069                     .177E-03    .110E-03
                                                                                                                                                                                                   .000                                                            116.1                      .0                       .122E-04                                                       .293E*05                                                                                                                                                          .976E-03 99.6             .795E+02                            .000
                                                                                                                                                                                                                                                                                                                                                                                      .278E405                                         .496E+04          .518E+04                                      1.044                     .193E-03    .110E-03
                                                                                                        .955E*02                            .000                                                   .000                                                             116.1                     .0                       .122E-04                                                                                                                                                                                                  .206E-03    .110E-03   .103E-02 121.3                                                                                                                                                                                                    .0                       .322E-04                                                       .262E+05                                         .469E*04          .485E+04                                      1.034 145.1             .113E*03                             .000                                                   .000                                                             116.1                                                                                                                                                                                                                                  .'766                  .295E-03   .110E-03   .101E-02 116.1                      .0                      .122E-04                                                       .244E+05                                         .443E*04          .339E*04 171.5 .128E+03                                         .000                                                   .000                                                                                                                                                                                                                                                  .280E+04                                          .666                   .357E-03   .111E-03   .102E-02
                                                                                                                                                                                                   .000                                                              116.1                     .0                      .122E-04                                                        .225E405                                        .420E*04 201.5              .146E*03                            .000

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