orel-tm-79 copy ini'o

OREL-TM-79

Copy Ini'o .

Contract Wo. W-7^05-eng-26

Reactor Division

WATER TEST DEVELOPMENT OF THE FUEL PUMP FOR THE MSRE

P. G. Smith

DATE ISSUED

MAR 2 71962

OAK RIDGE NATIONAL LABORATORY

Oak Ridge, Tennesseeoperated by

UNION CARBIDE CORPORATION

for the

U. S. ATOMIC ENERGY COMMISSION

OAK RIDGE NATIONAL LABORATORY LIBRARIES

3 44Sh DS467SE 5

Ill

CONTENTS

List of Figures

Abstract

Introduction

Experimental Apparatus

Pump . .- .

Test Loop

Carbon Dioxide Stripping Devices ......

Instrumentation. ...

Description of Tests

Head-Flow-Power-Speed Performance ......

Carbon Dioxide Stripping Tests .........

Pump Tank Liquid and Gas Behavior

Fountain Flow

Stripper Flow .....

. Gas Bubble Behavior in the Pump Tank Volume

Priming

Coastdown Characteristics

Test Results

Head-Flow-Power-Speed Performance

Carbon Dioxide Stripping Effectiveness . . .

Pump Tank Liquid and Gas Behavior ,

Fountain Flow . ,

Stripper Flow ,

Gas Bubble Behavior in the Pump Tank Volume

Priming . . . .


Conclusions

Acknowledgments

References

e No

v

vii

1

2

2

2

6

9

12

12

12

ik

Ik

Ik

Ik

Ik

15

15

15

19

22

22

27

27

29

31

31

32

32

Pag'

IV

Page No.

Appendix • • 3^

Nomenclature . . 35

Table I ........ 36

Table II . . . 37

Table III ... 38

Computations for:

Table I.. kO

Table II . . kl

Table III . . . k2

V

LIST OF FIGURES

Fig. No. Captions Page No

1. Cross Section of Pump 3

2. Discharge Connection to Loop ..... k

3. Photo of Test Loop 5

k. Stripper Configuration 1 7

5- Stripper.Configuration 2 8

6. Stripper Configuration 5 10

7 • Venturi Calibration 11

8. Motor Calibration . 13

9. Hydraulic Performance, 13-in. Impeller . . .16

10. Hydraulic Performance, 11-in. Impeller ...;... 17

11. Prerotatioh Baffle 18

12. Head, Input Power, and Speed Versus Flow, 11-in.Impeller 20

13« Hydraulic Performance, 11-in. Impeller, EfficiencyContours Superimposed ................. 21

1^. Relative Effectiveness Versus Sweep Gas Flow .... 23

15- Half-Life Versus Stripping Flow 2k

16. Relative Effectiveness Versus Jet Velocity 25

17• Cross Section of Upper Labyrinth 26

18. Fountain Flow Versus Speed, 11-in. Impeller 28

19. Pump Inlet X-Section . 30

VI1

ABSTRACT

A vertical centrifugal sump-type pump.utilizing commercially

available impeller and volute designs was selected to circulate the

fuel salt in the Molten Salt Reactor Experiment (MSRE) . Tests were

conducted in water to determine the adequacy of the pump design, to

assist design of the prototype fuel pump, and to investigate the

effectiveness of xenon removal with high velocity liquid jets con

tacting sweep gas in the pump tank. Hydraulic head characteristics

were within +1 to -3 ft of manufacturers data for a given constant

speed. Adequate and necessary provisions were devised to control

the liquid and gas bubble behavior in the pump tank. The results of

priming and coastdown tests are reported. During the gas removal

tests, the fuel, xenon, and helium in the MSRE were simulated with

distilled water, carbon dioxide, and air, respectively. The best

configuration removed carbon dioxide from water at approximately 99/0

of the ideal removal rate when the stripping flow was 65 gpm and the

sweep gas flow rate was k scfm.

WATER TEST DEVELOPMENT OF THE FUEL PUMP FOR THE MSRE

P. G. Smith

INTRODUCTION

The Molten Salt Reactor Experiment (MSRE) is to be a low-pressure,

high-temperature, graphite moderated circulating fuel nuclear reactor

using fissile and fertile materials dissolved in molten fluoride salts

and is designed for a heat generation rate of 10 Mw (l, 2, and 3) . Its

goals include proving the safe and reliable operation of this nuclear

reactor concept and demonstrating the maintainability of molten salt

machinery. The investigation reported herein is concerned with the pump

required to circulate the fuel salt in the MSRE.

A centrifugal sump-type pump consisting :of a rotary element and

pump tank was selected for this application. The rotary element in

cludes the vertical shaft and underhung impeller, the shaft bearings,

and the means for lubricating and cooling the bearings . The pump tank

includes the volute (casing), suction and discharge nozzles, other

nozzles for accommodating inert gas purge, fuel sampling and enrichment,

liquid level sensing devices, a flange for mounting the rotary element,

and various liquid bypass flows for degassing and removing xenon poison

from the circulating fuel salt. The device used for removal of xenon

will be referred to as a "stripper" . Much of the design of the fuel

pump was derived from the past experience with similar pumps for

elevated temperature service which were developed during the Aircraft

Nuclear Propulsion Program at Oak Ridge-National Laboratory (k, 5,

and 6).

The initial phase of development and testing of the fuel pump was

conducted with water to ascertain the capability of the pump to meet the

hydraulic requirements of the fuel circuit and.to remove from the circu

lating fuel the xenon which will be generated by the fissioning process.

Data were taken on the head-flow-power-speed performance of the pump for

two impeller outside diameters, 13 and 11 inches. Various baffles were

devised to control splash, spray, and gas bubbles caused by the operation

of the bypass flows in the pump tank. The ability of the pump to prime

was determined at various liquid.levels of interest. The coastdown

characteristics of the pump were measured from various speeds and flows.

Attempts were made to measure indirectly the effectiveness with which

xenon poison might be removed from the circulating fuel using high

velocity liquid jets in contact with gas in the pump tank. During this

particular test the fuel and xenon were simulated, respectively, with

distilled water and carbon dioxide; this gas is much more soluble in

water than xenon is in molten salts of interest and. in addition provides

for convenient measurement of solubility.

Pertinent information from these water tests were incorporated in

the design of the prototype fuel pump and will be subjected to elevated

temperature testing at MSRE design conditions.

• EXPERIMENTAL APPARATUS

The experimental apparatus includes the pump, the test loop, and

the stripper configurations. A description of each follows:

Pump

The pump is shown in Fig. 1 and includes a centrifugal impeller and

volute with the impeller supported at the lower end of a vertical shaft,

grease-lubricated bearings for supporting the shaft, bearing housing,

pump tank bowl, and volute support. The pump tank bowl was fabricated

of plexiglas to permit visual observation of the behavior of the liquid

and the gas bubbles . Labyrinth-type seals were utilized on the impeller

inlet shroud and on the impeller support shroud. The impeller support

shroud labyrinth seal was supported on the impeller cover plate, which

was sealed-to the volute by an elastomeric O-ring. The volute discharge

was connected to the pump tank discharge nozzle through a flexibly

mounted bridge tube. The connection arrangement is shown in Fig. 2.

Test Eoop

The test loop is shown in Fig. 3, which consists of the pump, piping,

venturi flowmeter, throttle valve (globe type), stripper flow circuits

LOWER LABYRINTH

UNCLASSIFIED

ORNL-LR-DWG 60816

STRIPPER

3 CONFIGURATION 5

LIQUID LEVEL

Fig. 1. Cross Section of Pump.

PUMP TANK

DISCHARGE NOZZLE

PUMP TANK WALL-

4

Fig. 2. Discharge Connection to Loop.

UNCLASSIFIEDORNL-LR-DWG 60817

(not shown), and a.cooler. The pump was driven with a 60 hp d.c.

variable speed motor. The vertical inlet pipe to the pump was fabri

cated of plexiglas to permit visual observation of the inlet flow con

ditions . A bundle of 1-in. diameter thin-wall tubes, 6-in. long,.was

added to the lower end of this pipe to reduce rotation of the water

column. The. cooler was installed in parallel with the main loop throttle

valve. A part of the main loop. flow.was bypassed through the cooler to

control the system temperature. The bypass flow was controlled by a

throttle valve located.in the bypass flow.circuit. Stripper configu

ration flow was supplied through a-tap located.just downstream of the

pump tank discharge nozzle. The stripper flow as well as the flow from

the impeller upper labyrinth passed through the pump tank and re-entered

the system at the impeller inlet. Throttle valves were used.to control

the stripper flow. Following the initial tests an orifice was added to

the nearly vertical section of the. loop between the discharge and the

venturi flow meter to decrease the pressure drop through the main throttle

valve.

Carbon Dioxide Stripping Devices

Tests were conducted wherein a portion of the pump discharge flow

was introduced into the gas volume of the pump tank through high velocity

jets (strippers). A number of configurations were investigated, starting

with a single stream and progressing to configurations which gave in

creasingly more fresh liquid-gas interface.

The strippers tested and identified in Table I (Appendix) are

described as follows (in each test two strippers were used):

1. Configuration 1 is shown in Fig. k. The flow discharged from

one side of the can through l/^-in. .holes. For this test the holes were

submerged below the liquid surface in the pump.tank.

2. Configuration 2 is shown in Fig. 5• The lower end of the entry

tube was closed and the beaker was packed with Inconel wool. The strip

ping/flow entered the pump tank gas space in tangential direction as a

spray. One beaker contained 8^ spray holes, l/8-in. in diameter, and

the other contained 30 spray holes, l/U-in. in diameter.

UNCLASSIFIED

ORNL-LR-DWG 60818

PUMP TANK ^LIQUID LEVEL--.

s s

li

• ^=r^ tT-^E^ZTt~

~~T"

r^r^". ^

SIXTY %-in. HOLES ^—»~^*/

li

3/4-in.IPS-»' | 5 n. e1/2in.

? 1GRAVITY

' ' '

-^ 5 in *-

Fig. 4. Stripper Configuration 1.

T-GRAVITY

r

PACKED WITH INCONEL WOOL-

£

K

1

UNCLASSIFIED

ORNL-LR-DWG 60819

-PUMP TANK

LIQUID LEVEL

__kDRAIN HOLES

Fig. 5. Stripper Configuration 2.

3• Configuration 3 was the same as No ..2, except for the size of

spray holes, and the number of holes. Each stripper contained 162

spray holes, l/l6-in. in diameter, with the beaker suspended such that

the spray.was circumferential.

k. Configuration k was the same as No. 3> except the number of

holes was reduced by a factor of two and the spray,was directed radially

inwards toward the pump shaft.

5 • Configuration 5 was a toroid constructed of pipe as shown in

Fig. 6, and located in the pump tank as shown in Fig. 1. Each stripper

contained two rows of 80 holes each, l/l6-in. in diameter.

INSTRUMENTATION

Instrumentation was provided to measure venturi pressure drop,

discharge pressure, pump shaft speed, water temperature, motor input

power, fountain flow, stripper flow, pH value of the water, and pump

tank liquid level.

Three different methods were used in measuring the venturi pressure

drop: mercury manometer, difference between individual pressures measured

at the inlet and throat, and by differential pressure transmitter. Cali

bration of the venturi was provided by. the vendor, and it is shown in

Fig. 7- Individual pressures at the inlet and throat were indicated on

Bourdon tube gages, 0-30 psi range, l/8 psi subdivision, and l/k<?o ac

curacy. The differential pressure transmitter was read out on a dif

ferential gage, 0-50 psi range, l/2 psi subdivision, l/k^o accuracy. The

flow is estimated to be accurate within ± jfo-

The discharge pressure was measured on a Bourdon tube gage, 0-100 psi

range, l/2 psi subdivision, and l/k'fo accuracy.

The pump shaft speed was measured.by use of a 60-tooth gear mounted

on the shaft, a magnetic pickup, and a .counter which indicated directly

in rpm.

The water temperature was measured with a dial-type thermometer,

0 to 2^0 F range, 2 F subdivision.

Motor input power data was obtained by two methods: power recorder,

0 to kO kw range, 0.8 kw subdivision and power analyzer which indicated

120

i 100

a.<

60

20

11


1

r

y

//

•

y

-•'

.l--0*^*m"^

200 400 600 800 1000 1200 1400 1600 1800 2000 2200

0, FLOW (gal/min)

Fig. 7. Venturi Calibration.

12

current and.voltage. The power measurements were in error during most

of the testing with the 13-in-o.d. impeller which preceded tests with

the 11-in. impeller. During this period, investigations were conducted

to.locate and correct the source of error. Satisfactory power measure

ments were obtained with the 11-in. impeller. The motor calibration

curve is shown in Fig. 8.

The fountain flow was measured by directing the flow through 90°

V-notch weirs and measuring the height of the flow column.

The stripper flow was measured by use of rotameters.

The pH value of.the water was indicated with a Beckman pH meter,

Model H^2, range 0 to.Ik pH.with an accuracy of.0.03 pH.

The pump.tank liquid level was indicated with a scale marked off in

0.1-in. divisions. Zero level corresponded with the center line of the

volute.

DESCRIPTION OF TESTS


Hydraulic performance data were obtained over a wide range of

operating conditions with impellers of 11- and. 13-in. outside diameter.

Two methods of operation were used: speed was varied (700 to 1300rpm)

at constant system resistance for several values of resistance with the

13-in. impeller, and system resistance was varied at constant speed for

several values of speed (700 to 1300 rpm) with the 11-in. impeller. Data

were obtained for computing head, flow, brake horsepower, and efficiency.

Carbon Dioxide Stripping Tests

A number of tests were performed with both impeller diameters to

ascertain the change in effectiveness of CO removal caused by various

stripper configurations, flow rates, jet velocities, and sweep gas flow

rates. Carbon dioxide in dry-ice form was added to the circulating dis

tilled water in the system until saturation was achieved, after which

time the stripper flow was started. Readings of pH of the water were

taken versus time to determine the time required to reduce the CO con

centration by a factor of two. A total of 37 tests were performed.

13

UNCLASSIFIED

ORNL-LR-DWG 6082160 1 1 1 1 1 , —r— .

850 rpm »^50

2400 rpm -j*n

4060-hpdc G.E. MOTOR

SERIAL NO. 7287063 "

i

1-30

0.

20

10

0

10 20 30 40

OUTPUT (hp)

50

Fig. 8. Motor Calibration.

60 70

Ik

An expression was derived to give the theoretical time required to

reduce the C0p concentration by one half. Comparison of the theoretical

and experimental data is reported as relative effectiveness of the

stripper.


Fountain Flow

Considerable testing was performed to,observe the flow of water from

the impeller upper labyrinth (flow up.the shaft and return to the system

through the pump tank volume) and to develope adequate control of the re

turn of this flow.into the pump tank liquid, keeping the splatter of water

and gas bubble formation to a minimum (see Fig. l).

Clearances were varied between the shaft and the impeller upper

labyrinth and the impeller upper shroud and seal plate. The corres

ponding fountain flows were measured.

Stripper Flow

The flow through the various stripper configurations was measured

and baffling was developed to control splatter and gas bubble formation.


Throughout all of the testing the formation and behavior of gas

bubbles were observed, in the pump tank volume. Baffling was devised.to

prevent entry of gas bubbles into the pump inlet.from the pump tank

volume.

Priming

The priming characteristics of the pump'were checked at various

static,liquid levels-in the pump tank. The ability of the pump to hold

prime as the liquid, level in the pump tank was being lowered was in

vestigated. Data were obtained of head-flow-speed performance and of

15

change in starting level for various starting levels as the pump was

accelerated from zero to design speed.


A number of coastdown tests were made from various pump operating

conditions. The power supply to the pump drive motor was interrupted

while the pump.was operating at specific .speed and flow conditions, and

the time required to reach reduced system flow and pump speed was de

termined .

TEST RESULTS


Hydraulic performance data were obtained over a wide range of head

and flow conditions at several speeds for the 8.in. x 6 in. volute, using

impellers of 13- and 11-in. outside diameter. These tests with the 13-in.

diameter impeller were conducted without a baffle in the pump.inlet. The

13-in. impeller performance is presented in Fig. 9, which is a plot of

head versus flow at.various speeds. The flow is total flow consisting1

of system flow, fountain flow, and stripper flow. The corresponding

data are tabulated in Table II (Appendix). Aliis-ChaLners data are also

shown for comparison. The heads obtained are increasingly lower than

Allis-Chalmers data with decreasing flow at constant speed.

The performance obtained with the 11-in. diameter impeller is pre

sented in Fig. 10, which is a plot of head versus flow at various speeds.

The flow is total flow consisting of system flow, fountain flow, and

stripper flow. The corresponding data are.tabulated in Table III (Ap

pendix) . Data for three different inlet configurations are shown: in

two configurations a prerotation baffle was located at the inlet to the

impeller; and the other configuration had none. The baffle consisted of

two plates arranged, in a cross as shown in Fig. 11; it had the effect of

increasing the head at the lower range of flows on a constant speed line .

There was essentially no difference in the results obtained with the two

16

UNCLASSIFIED

ORNL-LR-DWG 60822

0 200 400 600 800 1000 1200 1400 1600 1800 2000 2200 2400

<?, FLOW (gal/min)

Fig. 9. Hydraulic Performance, 13-in. Impeller.

88

80

72

64

56

£ 48o<UJI

. 40

a?

32

24

16

17

UNCLASSIFIED

ORNL-LR-DWG 60823

ALLIS CHALMERS MFG. CO. IMPELLER-VOLUTE

SIZE 8x6; TYPE E; IMPELLER P-482, 11-in. OD

. ALLIS CHALMERS DATA

ORNL DATA

o WITHOUT INLET BAFFLE 4-19-61

• WITH INLET BAFFLE (4-in. LONG) 4-20-61 _A WITH INLET BAFFLE (21/2-in. LONG) 6-19-61

0 ' 200 400 600 800 1000 1200 1400 1600 1800 20000, FLOW (gal /min)

Fig. 10. Hydraulic Performance, 11-in. Impeller.

18

UNCLASSIFIED

ORNL-LR-DWG 60824

FLOW

Fig. 11. Prerotation Baffle.

19

sizes of baffles. Curves of head and pump.input power versus flow at

various speeds are shown in Fig. 12. The input power change versus

flow for constant speed operation is slight.

The prerotation baffle was not fully tested with the 13-in. im

peller. Were such a baffle used with the 13-in. impeller, performance

would be more nearly coincident with the published Aliis-Chalmers data.

From the power data obtained with the 11-in. diameter impeller,

efficiency contours were computed which are shown in Fig. 13, super

imposed on a plot of head-flow-speed data.

Carbon Dioxide Stripping Effectiveness

In the stripping tests, data were obtained to determine the time

required to reduce the CO concentration by one half (half-life) . The

change in pH value of the distilled water was measured over a range from

k to 6 versus time . For plotting purposes the pH values were converted

to the logarithm of the molarity of CO to determine the half-life.

Theoretical half-life (t = 0.69 v/Q ) was computed for each tests

and compared with the experimental half-life to give relative effective

ness .

The results of.the carbon dioxide stripping tests are presented in

Table I (Appendix) . Related in the table are data pertaining to the

stripper configurations, by-pass flows, liquid level in the pump tank,

sweep gas flow rate, system volume, jet velocity, experimental half-life,

ideal half-life, and relative effectiveness.

The first six tests were preliminary; the flow was simply bypassed

through the pump tank without passing through strippers. These tests

were performed to provide a base from which to proceed, with strippers.

Values of relative effectiveness ranged from 10 to kO percent.

Tests 7 through .16 were concerned mainly with varying the stripper

configuration. Other variables may be noted in the data shown in the

table. Values of effectiveness ranged from 15 to 68 percent.

From the results of tests through No. 16, configuration 5 (Fig. 6)

was derived and used for the remainder of the tests, 17 through 39•

~ 30

S 20

10

0

72

64

56

48

r 40

32

24

16

20


- •- ». m1300 rpm • « < •"

1150•_ •— _• .»-•—

860• .»—•— .• -• —•—

d

N̂^**

s%

^v. fie0

48.5. ft, 1150 rpm; 17.5 gal

11-in. IMPELLER, 8 »6 IMPE

'min FOUNTAIN F

LLER-VOLUTE

"LOW

2V2 -in. PRE ROTAIIC N BAFF LE

0 200 400 600 800 1000 1200 1400 1600 1800 2000

0, FLOW (gal/min)

Fig. 12. Head, Input Power, and Speed Versus Flow, 11-in. Impeller.

- 40

C 32

21

UNCLASSIFIED

ORNL-LR-DWG 60826

0 200 400 600 800 1000 1200 1400 1600 1800 2000

<?, FLOW (gal/min)

Fig. 13. Hydraulic Performance, 11-in. Impeller, EfficiencyContours Superimposed.

2g

In tests 17 through 2k, the flow and jet velocity were varied simul

taneously, at a constant sweep gas flow rate. The relative effectiveness

varied, from 27 to 99 percent.

In tests 10, 13, Ik, .17,:18, and 25 through 29, sweep gas flow rate

was varied with the other variables held constant, and two stripper con

figurations were used. The relative effectiveness varied from ^7 to

72 percent. These data are plotted in Fig. Ik, Relative Effectiveness

Versus Sweep Gas Flow, for two configurations.

In tests 30, 32,,33, 35, and 39, the stripping flow was varied with

the other variables held constant. The relative effectiveness varied

from 70 to 90 percent. The results from these tests are shown in Fig. 15,

Half-Life (defined on page 18) Versus Stripping Flow. Experimental and

theoretical curves are shown.

In tests.30, 31, 3k, and 36, the jet velocity was varied with the

other variables held constant. The relative effectiveness varied from

27 to 90 percent. The results are shown in Fig. 16, Relative Effective

ness Versus Jet Velocity.

Configuration 5 was selected, for the MSRE fuel pump, and was in

corporated in the. design of the prototype fuel pump. Tests 37 and 38

yielded effectiveness values of 52 and 55 percent, respectively. These

tests were performed at the following conditions, .reasonably attainable

in the MSRE: stripping flow rate of 65 gpm,,and sweep gas flow rates of

0.05 and 0.07 scfm, respectively.


Fountain Flow

Observations of the fountain flow from the impeller upper labyrinth

(Fig. 17) revealed the need to control it;, the slinger impeller was

causing an undesirable spray. This spray was contained and controlled

by use of a cover enclosing the, labyrinth and slinger impeller, and

having drain ports located at its lower end.

Approximate measurements of the fountain flow were made using weirs

located in the windows -carrying the flow from the fountain into the pump

100

> 60

vu 20

23

JET VELOCITY CONSTANT

STRIPPING FLOW CONSTANT

q, SWEEP GAS FLOW (fr/min)


Fig. 14. Relative Effectiveness Versus Sweep Gas Flow.

1.6

~ 1.2c

E

l±J

V 0.8

<I

0.4

24

—I T"

TEST NUMBER

EXPERIMENTAL

JET VELOCITY CONSTANT

SWEEP GAS FLOW RATE CONSTANT

STRIPPING CONFIGURATION CONSTANT

10 20 30 40 50

STRIPPING FLOW (gal/min)


60 70 80

Fig. 15. Half-Life Versus Stripping Flow.

100

£ 80

ijj

>

>

60

40

w 20

25

,7«18

36

STRIPPING CONFIGURATION CONSTANT

SWEEP GAS FLOW RATE CONSTANT

STRIPPING FLOW CONSTANT

10 15 20 25

v, JET VELOCITY (ft/sec)


30 35 40

Fig. 16. Relative Effectiveness Versus Jet Velocity.

TOP EDGE

OF IMPELLER

26

SLINGER IMPELLER

CLEARANCE C

UNCLASSIFIED

ORNL-LR-DWG 60830

SHAFT-

Fig. 17. Cross Section of Upper Labyrinth.

27

tank. Values of fountain flow for several labyrinth clearances are as

follows:

13-in. Diameter Impeller, Ih-50 gpm, 1030 rpm, 50 ft Head

Configuration

Number Clearance "A" Clearance "B",

1 0.015 0.015

2 0.015 0.0k)

3 0.015 0.0U0

k 0.015 0.060

Configuration k was used with the 11-in. diameter impeller and the

fountain flow was measured at various speeds along a .constant resistance

line defined by 1300 gpm and h-5 ft. The fountain flow versus speed is

shown in Fig. 18. Configuration k was adopted for use on the prototype

MSRE fuel pump.

The direction of the fountain flow was observed over the range of

conditions from which head-flow-speed data were obtained with both the

11-in. and 13^in. impellers. The flow of liquid was found always to be

outward from the shaft annulus into the pump tank, which is the desired

direction.

Stripper Flow

Considerable splatter of liquid resulted from impingement of this

flow onto the volute and volute support. Control of this splatter was

obtained through use of baffles installed on the stripper and on the

volute support.


Entrance of the fountain and stripper flows into the pump tank liquid

caused gas bubble formation in the liquid. Control was obtained through

use of a baffle installed on the volute which deflects bubbles radially

Clearance "C", Flow, gpm

0.090 7.5 - 10

0.090 10 - 12

0.250 10 - 12

0.250 , 15 - 17.5

*

Each configuration was basically the same. Only the clearances

were different

5o

£

O

20

18

16

14

12

10

28

UNCLASSIFIED

ORNL-LR-DWG 60831

11-i

130

n.-dia IMPELL

O-gal/min LO

ft HEAD

.ER

DP FLOW

'*m

45-

'

*•

S

800 900 1000 1100

SHAFT SHAFT (rpm)

1200 1300

Fig. 18. Fountain Flow Versus Speed, 11-in. Impeller.

§9

outwards in the tank and by forcing these two flows to enter the

impeller inlet at the lowest elevation in the tank as shown in Fig. 19,

which may be compared to Fig. 1.

Priming

Priming tests were conducted with the 13-in. impeller in which the

pump was accelerated from zero to 1030 rpm in approximately 30 seconds,

noting the change in pump tank liquid level and observing attainment of

normal pump head and flow performance. The following operating levels

were noted for the listed starting levels:

Static Liquid Level Operating Liquid Level

(in .) (in .)

13-in. impeller

+2 +1.2 .

+1.5 +0.6

+1 -0.9

+0.5 -2.1

11-in. impeller

+2 +1

+1 -1.5

0 would not prime

Normal hydraulic performance was achieved at the end of pump accele-4.0 7«

ration for all runs except the 0.5-in. starting level with the 13-in.

impeller and the zero level with the 11-in. impeller. The 13-in. impeller

required an additional minute for priming at the 0.5-in. level and the

11-in. impeller would not prime at the zero level. These data should not

be used for reactor system computations unless differences in volumes of

system trapped gas are accounted for.

Reference level is center line of the volute. + is above center

line .

30

Fig. 19. Pump Inlet X-Section.

UNCLASSIFIED

ORNL-LR-DWG 60832

31

Other priming tests were performed jby lowering of the liquid level

in the pump tank slowly with the pump running. A test was performed tilth

the 13-in. diameter impeller operating at 1+50 gpm, 50 ft head, and

starting liquid level at .1 l/2-in. above center line of the volute. In-

gassing began at approximately k l/2-in. below the center line of the

volute. At 5 l/2 in. below the center line of the volute, the system

flow dropped to 700 gpm, and 6 l/2 In..below the center line of the

volute, the flow reduced to zero.

A test was performed with the 11-in. impeller operating at 1250 gpm,1 5^>.7»

.4-5 ft and starting liquid level at 1 1/2 in. above the center line of the

volute. Ingassing began at approximately 3 in. below the center line of

the volute. Vigorous ingassing and loss of head and flow began at 3 l/2 in.

below the volute center line.


• Coastdown tests were performed on the.drive motor and pump with the

13-in. impeller to determine the,time required for the unit,to stop.after

opening the drive motor circuit from the electric supply. Tests were

performed on the same flow resistance line for operating speeds of 1150,

1030, and 860 rpm at flow rates of 1630,. 14-50, and 1210 gpm, respectively.

Coastdown times to zero speed ranged from 10.1 to 10.k sec, and for flow

reduction to 540 gpm, the times ranged from 1.5 to 2.0 sec.

CONCLUSIONS

From the experimental hydraulic characteristics, the total head was

found to deviate from, reported data by +1 to -3 ft. It was found necessary

to insert a prerotation baffle in the inlet to improve the head at reduced

flows.

Based on the water test results, a 11.5-in. diameter impeller will

be required to meet the reactor design head and flow (48.5 ft and 1200 gpm).

This dimension will be more precisely determined during the prototype fuel

pump tests.

32

Fountain flow was observed over the whole range of operation and

found ,to be outward from the upper labyrinth into the pump tank, which

is the desired direction. Gas bubbles created by the fountain and

stripping flows were removed in the pump tank with assistance from the

various baffles.

With regard to priming, the pump would prime (full head and flow)

instantaneously with speed at static levels of 1 in. or more above the

center line of, the volute.

Gas stripping was accomplished in the pump tank with a relative

effectiveness of up to 99 percent. Sweep gas flow rate, stripping flow,

and jet velocity were found to have quite pronounced effects on the

stripping rate of a given stripper configuration. It was concluded that

the zenon removal rate will be primarily dependent on the fraction of

fuel processed rather than on improved stripper configurations.

The hydraulic characteristics were found to be adequate for the

anticipated requirements of the fuel circuit of the MSRE. The required

control of liquid and gas behavior in the pump tank was accomplished by

the use of baffles.

ACKNOWLEDGMENTS

The following specific contributions are acknowledged which comprise

the main talents required to complete the investigations: L. V. Wilson,

design; F. F. Blankenship, devised stripping tests; R. F. Apple, chemical

aspects of stripping tests; and J. M. Coburn, test operation, data taking,

and computations .

REFERENCES

1. R. B. Briggs, MSRP Quar. Prog. Rep. for Period August 1, i960

to February 28, 1961, ORNL-^3122, June 20, 1961.

2. R. B. Briggs, MSRP Prog. Rep. for Period March 1 to August 31,

1961, OREL-3215, January 12, 1962.

3. S. E. Beall, W. L. Breazeale, B. W. Kinyon, Molten-Salt Reactor

Experiment Preliminary Hazards Report, ORNL-CF 61-2-46, February.28, 1961.

33

k. A. G. Grindell, W. F. Boudreau, H. W. Savage, "Development of

Centrifugal Pumps for Operation with Liquid Metals and Molten Salts at

1100-1500 F", Nuclear Science and Engineering, Vol. 7, No. 1, i960,

PP 83-91.

5' H. W. Savage, Components of the Fused-Salt and Sodium Circuits

of the Aircraft Reactor Experiment, ORNL-2348, Feb. 15, 1958.

6. A. G. Grindell, "Correlation of Cavitation Inception Data for

a Centrifugal Pump Operating in Water and in Sodium-Potassium Alloy (NaK)",

ASME Trans., Series D, Dec. i960, pp 82I-828.

Nomenclature

Table I

Table II

Table III

Computations

35

APPENDIX

37

NOMENCLATURE

t, Half-life, min.

V, System volume, gal.

Q , Stripping flow, gal/min.s

C, CO concentration, pH reading

q., Sweep gas flow rate, ft-ymin.

e, Relative effectiveness, dimensionless

Q, Total flow, gal/min.

H, Total head, ft.

v, Jet velocity, ft/sec .

38

Table I. C02 Stripping Tests of MSRE Primary Pump Circulating H20

Impeller Diameter:Impeller Diameter:

System Water Flow:

Head: 50 ft

Water Temperature:

13 in. for tests 1 through 2411 in. for tests 25 through 391450 gpm

65 F

la 2 3 4! 5 6 7 8 9 10 11 12 13 14 15

Stripper Configuration By-Pass Flow (gpm) Half-Life, t (min)

LiquidLevelb(in.)

Sweep Gas

(Air)Flow

(cfm)

Direction of

Stripper Flow

Jet

Velocity

(ft/sec).

System

Volume

(gal)

Total

By-PassFlow

(gpm)

Test

No.No.

Number

of

Holes

Diameter

of

Holes

(in.|)Stripper Fountain Experimental Theoretical

Relative

Effectiveness

1 35 8 4.0 0 Submerged 96 42 15.0 1.57 10.5

2 35 8 4.0 0 96 42 16.0 1.57 9.8

3 18 15 4.0 0 96 32 12.0 2.06 17.2

4 18 15 4.0 0.1 96 32 8.0 2.06 24.2

5 ( 35 15 4.0 0.1 96 50 10.0 1.34 13.4

6]

0 15 4.0 0.1 96 15 11.0 4.45 40.5

7 1 60 1/4 26 15 2.5 0.1 4.6 91 41 10.0 1.55 15.5

9 2 84\30 J

1/8\1/4;

35 15 1.5 0.1 C ircumferential 8.9) •'6.2/

88 50 3.0 1.22 40.6

10 3 324 i/ie 35 15 1.5 0.1 18.5 88 50 2.6 1.22 46.9

12 3 324 lie 35 15 3.8 0.1 18.5 96 50 3.2 1.32 41.7

13 3 324 1/16 35 15 1.5 8.6 18.5 88 50 1.8 1.22 67.7

14 3 324 1/16 35 15 1.5 4.3 18.5 88 50 2.2 1.22 55.4

15 '5 324 l/ite 0 ' 15 1.5 0.1 0 88 15 6.8 4.06 59.7

16 4 162 l/l6 35 15 1.5 0.1 Radially in

ward

37.0 88 50 2.0 1.22 61.0

17 5 320 ±/k 35 15 1.5 4.3 18.5 88 50 1.7 1.22 72.8

18 5 320 1/^6 35 15 1.5 4.3 18.5 88 50 1.7 1.22 71.8

19 5 200 i/i6 50 15 1.5 4.3 46.2 88 65 ' 1.0 0.94 98.9

20 5 200 1/^6 50 15 1.5 4.3 46.2 88 65 0.9 0.94 99.0

21 5 320 1/^6 70 15 1.5 4.3 40.5 88 85 0.9 0.72 80.8

22 5 320 1/16 70 15 1.5 4.3 40.5 88 85 0.9 0.72 82.7

23 5 215 1/16 44 15 1.5 4.3 37.8 88 59 1.1 1.03 96.8

24 5 215 1/16 44 15 1.5 4.3 37.8 88 59 1.0 1.03 98.0

25 5 320 1/16 35 15 1.5 0 18.5 ' 88 50 2.5 1.22 48.8

26 5 320 1/16 35 15 1.5 0 18.5 88 50 2.6 1.22 46.9

27 5 320 l/l|6 35 15 1.5 0.05 18.5 88 50 2.5 1.22 48.8

28 5 320 1/16 35 15 1.5 0.07 18.5 ' 88 50 2.4 1.22 50.8

29 5 320 1/16 35 15 1.5 1.0 18.5 88 50 2.3 1.22 53.0

30 5 160 1/16 35 15 1.5 4.3 37.0 88 50 1.4 1.22 89.6

31 5 200 1/3J6 35 15 1.5 4.3 29.6 88 50 1.5 1.22 83.6

32 5 200 1/16 44 15 1.5 4.3 ° 37.0 88 59 1.4 1.04 73.833 5 228 1/3J6 50 15 1.5 4.3 37.0 88 65 1.2 0.94 78.3

34 5 240 1/16 35 15 1.5 4.3 27.0 88 50 1.6 1.22 76.3

35 5 274 l/l'6 60 15 1.5 4.3 37.0 88 75 1.2 0.81 70.2

36 5 280 1/16 35 15 1.5 4.3 23.1 88 50 1.7 1.22 71.737d 5 290 1/16 50 15 1.5 0.05 28.8 88 65 1.8 0.94 52.2

38d 5 290 1/16 50 15 1.5 0.07 '28.8 88 65 1.7 0.94 55.3

39 5 300 i/i,6 62 15 1.5 4.3 34.8 88 77 1.1 0.79 72.2

See appendix for computations relative to indicated columns.

Level referred to centerline of volute.

"Data from R. G. Apple,

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42

COMPUTATIONS

Table I.

Col. (10), Jet Velocity, ft/sec

q = v A v = .98 v Where v is Velocity through hole

A = .62 A A is area of hole

V. is Velocity of jet

Q. = .98 v (.62A) = .61 vA A is area of jet

vQ

.61 A

35s2i x lkk idmm ft

Test 17, v

.61 (321 holes) I(-^) in.2 x7-5 ^ x60

v = 18.5 ft/sec.

Col. (12), Total By-Pass Flow, gpm

Col. (10) = Col. (5) + Col. (6)

Col. (13), Experimental Half-Life, min.

Col. (13), Data obtained from Reactor Chemistry Division

Col. (-Ik), Ideal Half-Life, min.

-Q.t/Vc = c e s C = CO Concentration, pH reading

Q = Stripping Flow,- gpm.s

t = Half-Life Time, min.

V = System Volume, gal.

-Q t/vs

0.5 = e

In 0.5 = -ftt/v

0.6.9^ = Qt/V

t = 0.69^ v/q

sec

ft-' mln

43.

Test 17, t = °'£>9k(88) = lt22min.

Col. (15), Relative Effectiveness, "jo

• col (15) - Co1- [lk]LO±* UW •". Col. (13)

Table II.

Col. (3), Motor Input Power, Kw

Col. (3) = k Col. (2)

Col. (6), Motor Input Power, Kw

mi (6) - Eco1- (4)] [Col. (5)]GO±" [b) ~ 1000

Col. (8), Discharge Head, ft.

Col. (8) - Col. (7)(^§ x^^'/f2 =Col. (7) (2.31)in 62.4- —-

ftJ

Col. (ll), Venturi Pressure Drop, psi

Col. (11) .= Col. (9) -Col. (10)

Col. (13)> Venturi Flow, gpm

Col. (13) obtained from Fig. 7, using Col. (ll) or (12)

Col. (15) and (17), Stripper Flow, gpm

Cols. (15) and (17) = tCols..(l^and (l6)] ^

Col. (l8), Fountain Flow, gpm

Col. (l8) obtained from Fig. 18

Col. (19), Total Flow, gpm

Col. (19) = Col. (13) + Col. (15) + Col. (17) + Col. (18)

44

Col. (20), Change in Velocity Head, ft.

6 ?Col. (20) .=• 1.28.x 10 Q Where Q = Total Flow, gpm.

2g

-6 2 vd Vs ^Adr (Q/A )<1.28 x 10 DQSi-i-'= i_, ^_

* 2g 2g 2g 2g

. 2 .2 _ 2 .2ltd, n&»

16 Qg 1 1 '

•V d *: d S

2(32.2)rt£

Where d = discharge diameter

d = suction diameters

dd .= 0.505 ft.

d = 0.666 ft.

Q ,= ftJ/sec

16^'(7.5 x 60 f 1 1

2(32.2)«2 (.505)^ (.666)k

Col. (20) = 1.28x10 Q Where Q = gpm.

Col. (21), Total Head, ft.

Col. (21) = Col..(8) + Col. (20)

Table III,

Col. (3), Motor Input Power, Kw.

Col. (3) = k [.Col. (2)3

45

Col. (6), Motor Input Power, Kw.

Pol (6) = tCol..(lQ] [co1- (5)]' v ' 1000

Col. (8), Discharge Head, ft.

Col.

Col. (10

Col.

Col. (15

Col.

Col. (16

Col.

Col. (17

Col.

Col. (18

Col.

Col. (19

Col.

Col. (20

Col.

Col. (21

Col

Col. (22

Col

Col. (11) + Col. (12) + Col. (13) + Col. {Ik)100

(8) = Col. (7) (2.31)

), Venturi Flow, gpm.

(10) is obtained from Fig. 7 using Col. (9)

), Stripping Flow, gpm.

(15) =

), Fountain Flow, gpm.

(16) is obtained from Fig. 18.

), Total Flow, gpm.

(17) = Col. (10) + Col. (15) + Col. (16).

), Change in Velocity Head, ft.

(18), Same as Col. (20), Table II.

), Total Head, ft.

(19) .= Col. (8) + Col. (18).

), Pump Power Input, hp.

(20) obtained from Fig. 8, using Col. (6)

), Water Horsepower, hp;.

(21) = ^oTJ Qis in gpm.

H is in ft.

), Efficiency, $

(oo\ - [col- (21)1 mo(22} " [col.., (20)J 10°

17-5

.47

INTERNAL DISTRIBUTION

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ll. G. T. Colwell 39. J. R. Tallackson

12. A. P. Fraas kO. D. B. Trauger

13- C. H. Gabbard kl. R. S. Valachovic

.Ik. W. R. Grimes 4-2. J. H. Westsik

15- A. G. Grindell 43. L. V. Wilson

16. M. I. Lundin kk. c. E. Winters

17- R. N. Lyon 4.5-46. Central Research Library18. H. G. MacPherson 4-7-49. ORNL - Y-12 Technical Library,19. W. D. Manly Document Reference Section

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EXTERNAL DISTRIBUTION

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