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ORNL TM-2213

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Contract No. W-7405-eng-26

CHEMICAL TECHNOLOGY DIVISION

Process Design Section
LEGAL NOTICE

This report was prepared as an account of Government sponsored work, Neither the United
States, nor the Commission, nor any person acting on behalf of the Commiasion:

A. Makes sny warranty or representation, expresaed or implied, with respect to the accu-
racy, completeness, or usefulness of the information contained in this report, or that the use
of any information, apparatus, method, or process disciosed in this report may not infringe
privately owned rights; or ’

B. Assumes any liabilities with respect to the use of, or for damages resulting from the
use of any information, apparatus, method, or process disclosed in this report.

As used in the above, ‘‘person acting on behalf of the Commission® includes any em-
ployee or contractor of the Commission, or employge of such contractor, to the extent that
such employee or contractor of the Commission, of employee of such contractor prepares,
disseminates, or provides access to, any information pursuant to his employment or contract
with the Commission, or his employment with such contractor, ’

 

 

DESIGN OF AN ENGINEERING-SCALE, VACUUM DISTILLATION
EXPERIMENT FOR MOLTEN-SALT REACTOR FUEL

W. L. Carter
R. B. Lindauer
L. E. McNeese

'NOVEMBER 1968

‘OAK RIDGE NATIONAL LABORATORY
Odak Ridge, Tennessee
operated by
UNION CARBIDE CORPORATION
| for the | -
- | .. U.S. ATOMIC ENERGY COMMISSION

ESTRIBUTION OF Tdis QOCUMENS €5 Mmtm

 

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CONTENTS

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

PREOPERATIONAL INSPECTION ===mmmmmmmmmmmmmmmmmne mmmmmmmmeme e

Page
ABSTRACT . e ————— ]
INTRODUCTION ~- e e e e 2
DESIGN CRITERIA AND FEATURES ~=======m=m=m—mmm—mmmmmm e e oo é
Basic Design Requirements ==~=====m==—m=mm——emmmmc oo oo 6
Material of Construction =—=====-======- mme s 7
EXPERIMENTAL PROGRAM ====mmmmmmmm e e e e e e 8
‘Nonradioactive Operation =====m==m==mmmm e e e e e e 8
Radioactive -Operation ===~======——===eeccmeemm e - ——————— 10
METHODS -OF OPERATION ==~amemmmmm e e e m e e e e 10
~Semicontinuous Operation ========ememmemmimm e e e e ————— 1"
Batch Operation ===——=m===mmmemmem oo e e e 11
DESIGN OF EQUIPMENT =—-==m===mmmemam e mm e e e e oo 14
Feed Tank ~=====m==memmannaaa- e ————————— e = 14
Condensate Receiver ==—===—=======-mmesm—m— e m e oo e oo m e 16
Still and Condenser =—==msmmmmemmcmec— e 19
Cold Trap =========mm===- -——— e e e e e 27

- Vacuum Pump: e 27
Sampler =~-- e : - 30
Heaters =—=~=~—===cecea=- o e . e e e 8 e 0 30
Thermal Insulation ====—=====cmmmmme e e e e e oo e e 33
METALLURGICAL CHARACTERIZATION OF HASTELLOY N =--=====-=-=-- 33
Creep-Rupture Properties =—=-========mmmmmmmm e oo oo oo 34
Ductility ————- o S 34
Metallographic Examination ====—========-- ' - 38
STRESS ANALYSIS —=s—cmemmmmm e e e mc s e m e e e e e e e mwmm e 38
" Vacuum Still and Condenser =—====—===c====ux - e e 38
Feed Tank and Condensate Receiver =======~ - —emmme= 39

" INSTRUMENTATION =---=cmemmcmem e e e - e e e s 39
Temperature Measurement ———=========v==--- e -- 40
Temperature Control =====m=mmecmm e e e e e e 40
Temperature. Annunciafors ==========m==e = - ————————— e e 48
Pressure Measurement ======me=me—cnm oo e e e e 48
Pressure Control ===~=====meee=u= - ———————————— s 49
Liquid Level Measurement and Control =----==~=======ac-- —————— 49
51

 
 

 

 

 

 

 

 

iv

" CONTENTS (continued)

 

 

 

 

 

 

 

 

. Page
EQUIPMENT INSTALLATION ==<r—ecmmeeeommees ———————— Y
Unitized Construction ======emeaeemaeax —————————— ———— - 52
Hood Installation =====weeemmmeercemeea mm——— s -=- - 52
- Cell Installation e m—————— ——— -—- 52
FINAL DI'SPOSIT-ION e 55
ACKNOWLEDGEME NTS -- m———————————— rmm—mnm————— 55
REFERENCES - - ——————————— —————————————————— 57
APPENDICES ——— e e ———————————e 59
~ Appendix A Physical Properhes of Hastelloy N ~===m=aa—am- — 61
Appendix B Physical Properties of LiF, BeFy, ZrF4, and Thelr i
. - Mixtures and MSRE Salt A =m==mmeemcm e caacaeae 66
Appendix C Estimation of Pressure Drop for Salt Vapor in the
| Still=Condenser System ======-- cmm——— 72
Appendix D Estithation of Time to Heat Condensate Receiver and
- ‘Feed Tank to Operating Temperatyre ====~===~-= wo——— 79
‘Appendix E Estimation of Heat Rejection Rate By Condenser =~===== 90
Appendix F Stress Analysis of Vacuum Still and Condenser ~——----- 95
-Appendix G Specifications for Heaters for Vacuum Distillation ==~- 1M

Appendix H Equipment Drawmgs —m——mme . ——— m—m——————— -—- 116

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DESIGN -OF AN ENG.NEERING-SCALE, "VACUUM DISTILLATION
EXPERIMENT FOR MOLTEN-SALT REACTOR FUEL

W. L. Carter
R. B. Lindaver
L. E. McNeese

ABSTRACT

Experimental equipment has been designed for an engineering=- -
scale demonstration of vacuum distillation of molten-salt reactor fuel.
The distillation is carried out at about 1000° C and 1 mm Hg to
separate LiF-BeF, carrier salt from less volatile fission products,
primarily the rare earths, Uranium tetrafluoride is not present
during the distillation. - The experiment is designed for continuously
feeding a molten-salt-fission=product mixture into a still at the
same rate that distillate is being removed, thereby concentrating
fission products in the still. Also, the still may be operated batch-
wise to give large concentration factors. Frequent sampling of the

~ distillate furnishes data on the separation between carrier and fission
products as a function of concentration in the still bottoms.

‘The equipment consists of a 48-liter feed tank, a 12-liter
still, a 10~in. diam x 51-in. condenser, a 48-liter condensate receiver,
plus associated temperature, pressure and level control instrumen-
" tation.  All vessels and parts contacted by molten salt are made of
Hastelloy N.  The unit is electrically heated by shell-type, ceramic
heaters.

About 90% of the experimental program will be devoted to

. nonradioactive operation using mixtures of LiF, BeF,, ZrF,, and
selected rare earth fluorides. The experiment will be concluded
by distilling a 48~liter-batch of uranium-free spent fuel from the
~ Molten-Salt Reactor Experiment. o |

 
 

 

 

INTRODUCTION

- This report describes the design and proposed use of experimental equipment
to demonstrate vacuum distillation of fuel carrier salt from a .molten-salt reactor.
The purpose of this experiment is to demonstrate the feasibility of distilling a large
portion of the carrier from contained fission product fluorides. - Vacuum distillation
is the key step in one method of processing a molten-salt breeder (see Fig. 1)
because it separates the bulk of the valuable LiF~BeFy carrier from less volatile
fission products, primarily the rare earths, and recovers this carrier salt for recycle
to the reactor. Feasibility of dnshllmg fluoride salts was established in batch,
laboratory experiments by Kelly this design is of an experiment that will demon-
strate the operation on an engineering scale.

In the interest of simplicity, fabrication time, and economy, no attempt was
made in this experiment to reproduce the actual operating conditions, such as
high internal heat generation rate in the molten salt, or to use a still design of the
type to be used in a processing plant for a breeder. Such advances are the next
logical step after an engineering~scale demonstration. However, it is the purpose
of this experiment to show that molten salt, containing fission products, can be fed
continuously to the still at the rate at which it is being distilled, with the simul-
taneous accumulation of fission products in the bottoms. Furthermore, the still can
be operated batchwise to concentrate fission products in some small fraction of the
salt volume. In this way the still meets a requirement of a still for processing
breeder fuel since large fission product concentration factors are necessary to mini~
 mize the amount of carrier salt discarded as waste.

The experiment is designed to obtain throughput data and relative volatility
data between rare earth fluorides and the carrier components of molten salt fuel,
which are LiF, BeF,, and ZrF4. Zirconium fluoride will not be a component of
breeder reactor fu % but it is mcluded here because the still will be operated with
salt of the composition of the Molten-Salt Reactor Experiment (MSRE), which is
65 mole % LiF, 30 mole % BeF,, and S mole % ZrF4. Progress of distillation is
followed by sampling the flowing condensate at several times during the course of
an experiment. Samples can be removed under vacuum without interrupting the
run and will be analyzed to determine the amount of separation being obtained
~ between components being fed to the still. It is also possible to sample the contents
of the still, but this necessitates interrupting the run during the time a sample is
being removed. .

The experimental program is in two parts: About 90% of the time will be

- devoted to nonradioactive operation, and the remaining 10% to radiocactive

operation in distilling a-small quantity of fuel carrier salt from the MSRE, The first |
phase is expected to log about 500 hr of operation. The same equipment will be u
used in the radicactive experiment after being thoroughly inspected at the conclusion

of nonradioactive operation.  Radioactive runs will be carried out in an MSRE cell

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ORNL DWG. 66-82 R2

 

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NoF { MgF.
OREES, SORBER
'REACTOR f | v UFg+Fp |
o Ee | . [+voLaTiC
BLANKET. g
~\_ | FLuornaTOR FP'S
\LiF-BeFy-UFy 7 ~ 550°C
F2. |
LiF-BeFa-UFa o SPENT
5 T | - LiF+BeF, NaF + MgF,
\ | o ond VOLATILE FP's
Off |
Gas
‘ | 0.5-Imm Hg
*-Make-Up | »1000°C
_ |LiF-BeFy-UF,
. | REDUCTION
T ~ 600°C
y
FUEL
MAKE -UpP Y v
DISCARD WASTE
FOR REMOVAL  RARE EARTHS
OF VOLATILE IN LiF

 

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Fig. 1. Principal Steps in Processing Irradiated Fuel from a Molten Salt Reactor.

 

 
 

4

on a 48-liter batch of uranium=-free MSRE fuel that has been decayed at least

 two months.

Components of the experiment are a feed tank (48 liters), still (12 liters),
condenser, condensate receiver (48 liters), associated temperature_and pressure
instrumentation, and o vacuum system. The still, condenser, and receiver are
fabricated as a unit. The vessels are mounted in an angle~iron frame, which is
3 x 6 x 7 ft high, allowing transport of the entire facility as a unit once
instrumentation, power, and service lines have been disconnected. . The equupment
is heated by shell-type electric heaters which are enclosed in 4 to 8 in. of thermal
insulation. - |

An experimental run is carried out by charging a molten mixture of carrier
salt and fission product fluorides into the feed tank, which is held at a temperature
slightly above the salt liquidus, which is 450°C for MSRE carrier salt. Concurrently
the still, condenser, and condensate receiver are heated and evacuated, and the

~ space above the liquid in the feed tank is evacuated. The final pressure is adjusted

to about 0.5 atm in the feed tank and 0.2 to 5 mm Hg in the rest of the equipment,
depending upon the desired operating pressure. When the still temperature reaches
900°C, a 12 liter charge is forced into the still through a heated line; and the
temperature is raised to the operating temperature range of 950 to 1000°C.

The still pot is the highest point of the system and is an annular volume surround-
ing the top of the condenser (see Fig. 2). Salt vapors flow into the top of the
condenser and condense along its length by losing heat to the surroundings. Freezing
is prevented by supplying the necessary external heat to keep the condenser surface
above the liquidus temperature. In leaving the condenser the distillate passes
through a small cup from which samples can be removed for analyses. Sampling can
be done under vacuum without interrupting an experiment.

Liquid-level instrumentation in the still allows control of feed rate to correspond

to the distillation rate, which is estimated to be 400 to 500 em3 distillate per hour.

Determining the actual distillation rate for molten-salt systems is an important part
of this experiment.

All vessels and lines that contact molten salt are. fabricated of Hastelloy N.
In the region of the still and upper section of the condenser, the normal use témper-

" ature for this alloy may be exceeded by as much as 200°C. Consequently, the

vessels are to be examined thoroughly by dimensional, radiographic, and ultrasonic
methods before and after nonradicactive operation.

Provision is made for hanging test specimens of candidate metals of construction
in the still. The materials that will be tested are:

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| | CO!‘E~I¥E<%L Vol.=12 liters
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ARGON INLET

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CONDENSERSY
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CONTAMINATED FEED—=—-=x
LiF. = 65.6 mole % E i
BBF2329.4 n " 3
ZrFpe 50 " " |
FISSION PRODUCTS ¢

    
 
 
 

 

 

 

 

 

 

 

 

 

P S RN LY, 5
RO 3 AN

CONDENSATE TANK
Vol. =48 liters
P20.5 mm Hg
T=500°C

Vol. = 48 liters
P=6 psia
Tx500°C

 

Fig. 2. Vacuum Distillation of LiF-Ber-ZrF4.

COLD TRAP

 

 

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SER LiF -BeFp -ZrF,

 
 

 

 

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1. ‘Hastelloy N (referee sample of still composition)
2. Moly TZM (a Ti-Zr-Mo alloy)
3. Haynes Stellite No. 25
4. Graphite (grade AXF-SQBG, isptropic) |
5. Ni-18 Mo=0.2 Mn-0.05 Cr |

Samples will be removed and inspected at the end of nonradioactive operation.
DESIGN. CRITERIA AND FEATURES

Basic Design Requirements
- |

Factors which influenced ':equipment design included the following:

1. The total operating time and the total volume of salt distilled during
- operation with irradiated material should be sufficient to conclusively
demonstrate the feasibility of molten=salt distillation.

2. Operation with irradiated material should be preceded by successful
operation with unirradiated material.

3. The same equipment should be used for work with irradiated and
unirradiated materials.

4. The equipment size should be compatible with space suitable for
containment of Bef, during nonradioactive operation.

Other factors of importance included:
1. Either semicontinuous or batch operation should be possible.

2. Condensate samples should be taken during an experiment without
upsetting operating conditions.

3. The latent heat of condensation of the molten—salt vapor should be
removed from the condenser by loss of heat to the surréundings.

4. The pressure drop in the passage connecting the vaporization and
condensation surfaces should be low.

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The experimental program will consist of both nonradioactive and radicactive
- operation, with the former being about 90% of the program. Nonradioactive
operation will be carried out over a period of three to six months in the

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Unit Operations Section, and then the equtpment will be moved i in jg_fg_ to the
MSRE site to demonstrate vacuum distillation of irradiated MSRE carrier salt. |
Equipment size was governed by the space in an available hood, and the overall
installation is limited to about 6 x 3 x 8 ft in length, width, and height

respectively. Unitized installation of all components within a supporting frame-

work was designated to facilitate transport between sites. Radioactive operation
will be carried out in the spare cell of the MSRE.

The duration of the radioactive experiment is an important factor because of
the technological significance that can be associated with a conclusive demonstration
using recently irradiated fuel. For this purpose, an operating period of 10 to 14 days
was considered adequate, and, during this time, 48 liters of the fuel carrier salt will

be distilled.

Another design feature is that provision be made for sampling the condensate
stream at any time during the course of a distillation experiment. This requirement
is made so that the composition of the still vapor can be measured as a function of
still composition and/or temperature. Condensed vapors flow contindously through

~ a cup at the condenser outlet (see drawing M~12173-CD-011D in the Appendix)

from which a 10-g sample can be taken by lowering a thimble into the cup. The
sampling operation is carried out at the operating pressure, causing no interruption
or upset in the run.

Simplicity of design and ease of operation were primary considerations in
planning this experiment. The only auxiliary systems are the necessary heaters,
instruments, and vacuum equipment. Vapor condensation is brought about by
radiative and convective heat loss to the surroundings, obviating the need for an
auxiliary, high-temperature cooling system. This somewhat limits the maximum
distillation rate, the calculated range being 350 to 500 cm3/hr with 3.5 to 4~in.

insulation around the condenser.

Material of Construction

All major pieces of equipment and connechng lines are built of Hastelloy N.
This material has excellent resistance to corrosion by molten LiF-BeFy=ZrF, mixture
at the lower temperatures (500 to 700°C) of the experiment. A limited amount of
data at the higher operatlng temperatures (200 to 1000° C) indicate that the
corrosion resistance is probably quute good at these temperatures. This characteristic

“of Hastelloy N will be evaluated in the distillation experiment.

The still and condenser, which will be exposed to the higher temperatures, are -

constructed of 3/8-in.~thick plate to allow for uncertainty in the strength of Hastelloy

N in the neighborhood of 1000°C. The ASME Unfired Boiler and Pressure Vessel

‘Code makes no provision for the use of this alloy for service above 700°C. This

 
 

 

 

8

design is based on the creep data of McCoy* and the stress analysis of Hahs and
Pickel,* which substantiate the use of this equipment for an operating time up to

- 1000-hr duration. At no time will the unit be exposed to a positive internal
pressure, the largest AP being 1 atm external pressure.

Use was made of on-hand material from the MSRE stockpile of Hastelloy N
plate, sheet, tubing, rod, and pipe. Design and fabrication changes were made

- to conform to the available material, For example, cylindrical vessels are made

of rolled and welded plate instead of the more obvious choice of using standard
pipe if it were available; directional changes are made with mitered joints because.

- pipe fittings were not available; some nozzles are made of tubing or drilled rod

when a more conventional choice would have been standard pipe.
EXPERIMENTAL PROGRAM

The vacuum distillation experiment will be carried out in two phases. The
first phase will consist of a large number of nonradioactive experiments to thoroughly
evaluate the still, obtain operating experience, and gather data that are pertinent
to the distillation process. The second phase will be a 10 to 14 day demonstration

in which irradiated carrier salt of the Molten Salt Reactor Experiment will be
distilled in a cell at the MSRE site.

Nonradioactive Operation

- The experiment is described by the simplified flow diagram presented in Fig. 2;
a detailed flowsheet is given in Appendix H, Drawing No. E~12173-CD-012D.
The system consists of a feed tank, still, condenser, condensate receiver, cold trap,
vacuum pump, and auxiliary instrumentation for controlling pressures, temperatures,
and liquid level. All vessels and lines are heated with ceramic, clam-shell-type:
heaters or Calrod-type elements. |

Initially the system is purged and filled with argon to remove oxygen, .and all
vessels are heated to about 500°C. A 48-liter charge of molten LiF-BeFy=ZrFy
of MSRE carrier salt composition containing a fission product fluoride is then put
into the feed tank, and the entire system is evacuated. Pressure above the salt in
the feed tank is adjusted to about 5 psia, sufficiently low to prevent salt from being
pulled into the still when the still is at full vacuum. The evacuation is continued

 

*H. E. McCoy, Metal and Ceramics Division; C. A. Hahs and T. W. Pickel,
General Engineering Division. See later sections of this report treating the
metallurgical study and stress analysis.

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until the still, condenser, and condensate receiver are at the desired operating

pressure of 0.2 to 2 mm Hg. Concurrently with the evacuation, the still
temperature is raised to about 850°C, the temperature at which the salt charge
has a vapor pressure of around 1 mm Hg. The condenser temperature is adjusted
100 to 200°C lower than the still temperature to facilitate condensation of the
salt vapor without solidification. Condenser heat is applied in four zones so that
a high-to-low temperature gradient can be maintained down its length, The
condensate receiver is heated to 500 to 550°C, a temperature that will keep the
condensate molten but not cause undesired vaporization into the vacuum system.

When all parts of the sysfem have reached the desired temperature ond pressure,
12 liters of the feed salt are transferred through a heated line into the annular
section of the still by pressurizing the feed tank with argon. The gas is added
slowly through a capillary, and a liquid-level device, which senses the upper level
in the still, stops the argon addition when this level is reached. The still
temperature is controlled so that the vapor pressure of the salt is near 1 mm Hg; and,
as distillation progresses,changing the salt composition, this temperature is allowed
to increase to keep the vapor pressure at about 1 mm Hg. Pressure at the condenser
exit is held at about 0.5 mm Hg. The calculated distillation rate is about 350 ml/hr.

The liquid-level instrument in the still is set to detect a low level that
corresponds to vaporization of 2 liters and to begin argon flow into the feed tank to
push more salt into the still. The upper-level setting stops the addition, and this
cyclic operation is repeated throughout the run. Smoother, more continuous
operation can be obtained by regulating the argon flow to the feed tank to be very
near the predicted vaporization rate so that salt flows into the still at about the
same rate that it is being vaporized.

In leaving the condenser, the condensate flows through a small cup that is
centered beneath a sample tube. A 4~cm3 sample is obtained by lowering a
1-1/2-in. by 3/4=in.~diameter thimble into the cup. Sampling is done under

‘operating conditions with no interruption in the experiment; a double-valve

arrangement (shown schematically in Fig. 2) permits removal of a sample from the
system without upsetting the still pressure. The sample cup is continuously flushed
with fresh condensate, giving a sample that is representative of the still vapor at
the time the sample is taken. -

Flnally, the condensate collects in a receiver from whu:h it mrght be recycled

~ for subsequent experiments. Level-detecting instrumentation allows an independent

check of distillation rate. The condensate receiver can be sampled for a cumulative
analysis only if the run is terminated because the tank must be pressurized to force
the salt out the drain line. The vacuum line passes through a baffled trap cooled
by liquid nitrogen to remove particulates or vapors that might clog the vacuum pump.

- The still residue cannot be withdrawn during the course of an éxperiment. A
dip tube is provided for draining all but about 154 em3 from the conical bottom

 
 

 

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section when a positive pressure is applied above the liquid surface. However, if
desired, all liquid fed into the still may be evaporated. The maximum still temper-
ature (1000°C) is high enough to vaporize the least volatile component (LiF) of the
carrier but considerably below the point at which rare earth fluorides have a
significant vapor pressure. Fission product fluorides, which the carrier salt contains
during some runs, are allowed to accumulate in the still. A flush salt can be used
to purge the still between different types of experiments. |

Because of the toxic nature of beryllium, nonradicactive experiments are
carried out in a hood, and all work areas are monitored for beryllium contamination.
Containment is based on maintaining adequate air velocities at all hood openings.

Radioactive Operation

At the conclusion of the nonradioactive experiments, the equipment will be

moved intact to the spare cell at the MSRE site for a similar experiment using

irradiated salt. Distillation is carried out in the same way as described above;
however, all operations must be remote. A 48-liter batch of LiF-BeFo-ZrF

MSRE carrier salt, which has been fluorinated to remove uranium and volatile fission
products, will be transferred from the chemical processing cell through an existing
pipe line into the feed tank. The salt will then be distilled over a period of

- 10 to 14 days. Frequent samples will be withdrawn for analysis. It is anticipated

that the extensive operating experience with nonradioactive experiments will allow
specifying operating conditions to obtain maximum decontamination and trouble-free
operation.

The cell ventilation system is used for disposol of gases from the experiment.
This system contains the necessary fllters for removing activity from the gas before
exhausting it to the atmosphere.

METHODS OF OPERATION

The distillation system can be operated in either of two modes: semicontinuous
operation followed by batch operation or batch operation with heel retention. These |
methods are not necessarily the best for MSBR processing; they are, however, well’
suited for demonstration of molten salt distillation at the MSRE site,

Instrumentation for measuring liquid level in the still includes a liquid-level
probe which operates when the still inventory is between 10 and 12 liters and a
level probe which operates when the still inventory is between 0.78 and 6 liters. |
Salt can be fed to the system continuously or intermittently; however, no provision is g
made for removing liquid from the vaporizer during the operation. During a given

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run, the total salt volume which will be distilled by either method of operation is
approximately 48 liters.

Semicontinuous Operation

For semicontinuous operation, the still will-be charged with 12 liters of MSRE
fuel salt (65 mole % LiF—30 mole % BeFy—5 mole % ZrF4) containing rare earth
fluorides. An additional 36 liters of fuel salt will then be fed to the still at a rate
equal to the desired distillation rate. The liquid volume in the still will be main-
tained between 10 and 12 liters during this period. After feeding 36 liters of salt,
the salt feed will be stopped and vaporization will be continued until the salt liquid
volume is 0.78 liter.

The variation of BeFy concentration in the condensate and the fraction of rare
earth flyoride vaporized are shown in Fig. 3 for this mode of operation. The liquid
volume in the still was assumed to be perfectly mixed and the relative volatilities of

- BeF, and rare earth fluoride were assumed to be 4.0 and 5 x 1074, respectively.

The BeF, concentration in the condensate is observed to decrease from an initial
valuve of 67 mole % to 35 mole % at the end of semicontinuous operation and then
to drop sharply to essentially zero during batch operation. The fraction of rare
earth vaporized is seen to continuously increase to a value of 0.0018 at the end of
operation. Approximately 98.5% of the salt fed to the still will be vaporized.

Batch Operation

For batch operation with heel retention, the still is charged initially with
12 [iters of MSRE fuel salt containing rare earth fluorides. Vaporization is then
carried out until the liquid volume in the still is 0.78 liter. Fuel salt (11.22 liters)
will be fed to the still to yield a total liquid volume of 12 liters and the above
sequence repeated.  Four cycles of batch operation with heel retention can be

- carried out with 48 liters of salt.

The variation of BeF, concentration in the condensate and the fraction of rare
earth fluoride vaporized is shown in Fig. 4. The liquid volume in the still was
assumed to be uniform in concentration and the relative volatilities of BeF, and
rare earth fluoride referred to LiF are assumed to be 4.0 and 5 x 10-4, respectively.
The fraction of rare earth fluoride vaporized is based on the total quantity of rare

“earth fluoride which has been fed to the still during a given cycle. The BeF,

concentration is observed to decrease from an initial value of 67 mole % to
essentially zero during each cycle. The fraction of the rare earth fluoride vaporized
after four cycles is 0.0027. Approximately 98.2% of the salt fed to the still will be
vaporized..

 
 

 

 

 

MOLE FRACTION BeF, IN VAPOR

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i ! | 1 | ! ! |
5 i0 15 20 25 30 35 40 as
‘ QUANTITY OF SALT VAPORIZED, LITERS ’
Fig. 3. Semicontinuous Vaporization of Fluoride Salts.

(-n

¥

¥
 

 

P

r#

rfi?‘.

IN VAPOR

a

w

MOLE FRACTION BeF,
- L9

13

ORNL DWG. 67-3677

 

o

 

I 1 ! 1 ] i

 

 

 

5 10 15 20 25 30 33

QUANTITY OF SALT . VAPORIZED , LITERS

Fig. 4. Batch Vaporization of Fluoride Salts.

43

(FRACTION OF RARE EARTH !ELU(&RIDE VAPORIZED) X103

 
 

 

 

 

14

The distillation experiment will be operated with unirradiated fuel salt for
approximately 500 hr prior to operation with MSRE fuel salt which will require
approximately 150 hr. Experimental work using nonirradiated fuel salt will
provide general information on optimum operating conditions for the subsequent
work using irradiated salt as well as specific data such as relative volatilities of
rare earth fluorides and fuel salt components, vaporization rates and factors
affecting rate, and concentration polarization at the vapor-liquid interface.
Experimental work using irradiated fuel salt will provide additional information on
relative volatilities of rare earth fluorides and other fission product fluorides and
will point out problems associated with the remote operation of a dlshllahon system
with lrradlafed material.

" DESIGN OF EQUIPMENT

The major pieces of equipment for this experiment are designed for semicontinuous
or batch operation to concluslvely demonstrate vacuum distillation of molten-salt

reactor fuel on an engineering scale. The vessels are sized so that batch runs of

30 to 36 hr duration can be made. A batch operation can consist of distilling up
to 12 liters of salt, whereas a semicontinuous experiment can distill up to 48 liters
and operate for more than one week. The following paragraphs discuss the perhnenf
design characteristics of each piece of equipment.

Feed Tank

Design Features

The feed tank is described in Fig. 5, and the following values characterize the
vessel and its operation:

Total volume 58.6 liters
Operating volume (full) | 48,0 liters
Operating pressure | 5.0 to 6.7 psia
Operating temperature _‘ 500 to 550°C
Heater capacity - 20 kw

Material ~ Hastelloy N
Material thickness (sides, top, 1/4 in.

and bottom)

Detailed design of the feed tank is shown on Drawing No. M=-12173-CD-013-D in
Appendix H. |
" fi 4

 

ORNL DWG. 66-10983

 

@—VENT
1" SCH, 40 PIPE

Ny INLET
3 O.D.xI9 GA. TUBE

 
  
   

 

 

 

 

 

26

 

 

 

 

   

 

 

 

 

 

   

 

 

 

 

  

f--l] H FEED INLET
: - - 30.0.x15 GA. TUBE
I { th I
i t 1] |
| ! Hy 3
| H |
| i I
| It | |
| I |
t 1t | |
! it 1 !
f it | |
! iyt I 1| -
' I | |
L ed oo h H! ' o
IH il i 72° TYR
Ih! | |
I l | 1
| ! | I
I ' | |
| I :
I i |
oo
| | 1] .
i 1 :
I ity |
i 11
il Ly )
L i ALL DIMENSIONS
I W\ IN INCHES
[
{
'LJ THERMOCOUPLE WELL
= 1 0.0.x196a.TUBE

 

 

 

 

 

FEED OUTLET
$00.x15 GA.TUBE

 

PLAN VIEW

 

 

 

 

Fig. 5. Molten Salt Distillation Experiment. Schematic diagram of the feed tank.

Gl

 

 
 

 

 

 

16
Thermal Design

The thermal design of the feed tank was concerned only with determining the
required heat input rate to give a tolerable heat-up time from room temperature to
operating temperature (~ 500°C). After the vessel and contents have been heated
to 500°C, the only heat required is that needed to balance the heat loss to the
- surroundings. The heat-up time was calculated for several heat input rates, and
these are plotted in Fig. 6. An arbitrary upper limit of about 2 hr was chosen for
the heat-up period, and on this basis a 20-kw heat input is specified. The
calculations are based on the tank's bemg full (48 hfers) of L|F-BeF2-ZrF4 (65- 30 -
5.0 mole %) mixture.

At operating temperature, the calculated heat loss from the feed tank is 1.2 kw -
through the é=-in.~thick insulation. Heaters are arranged so that about 6 kw are

applied to the tank bottom, 4 kw to the top, and 10 kw to the sides.

A more complete treatment of the thermal analysis is given in Appendix D.

Operating Pressure

 

The feed tank is connected to the still via an open line that rises to a point
higher than the still and loops down to the still.” When the feed tank is filled,
molten salt must be raised 5.25 ft to the top of the loop; when near empty, salt must
be raised 7 ft (Drawing No. M=12173-CD-010-D in Appendix H). Since the still
operates at a pressure of about 1 mm Hg, the salt (sp gr = 2.22 at 500°C) will be
drawn into the still unless the feed tank is partially evacuated. . Feed tank pressure
must be kept in the range 5.0 to 6.7 psia, depending on the salt level in the tank.

Condensate Receiver

Design Features

The condensate receiver is described in Fig. 7, and the following values
characterize the vessel and its operation:

Total volume 57.5 liters

Operating volume (full) 48 liters
Operating pressure : 0.5 mm Hg
Operating temperature ’ - 500 to-550°C
Heater capacity 20 kw
Material . Hastelloy N
Material fhlckness (sides and neck) /4 in.

(bottom) 3/8 in.
 

 

 

wh

e

ORNL-DWG - 68-797

 

240}—

200

 

 

 

 

160
- TANK WALL HELD AT 600° ¢
0
-
>
=z
= 120p— °\
w ° 7T00°C
§ | -(;_--
-

80— )

INSULATION THICKNESS=6"
40}—
0 | 15 L 20

'HEAT INPUT TO TANK WALLS (kw)

Fig. 6. Calculated Time Réqunred to Heat the Feed Tank or Condensate
Receiver from Room Temperafure to 500°C When Tank Contalns 48 liters of

L|F-BeF2-ZrF4 Salt.

 
1" SCH.40 PIPE

ORNL DWG. 66-10984
VACUUM LINE

0.D.x.042 WALL TUBE

 

THERMOCOUPLE WELL

  

$0.0.4.042 WALL TUBE

THERMOCOUPLE WELL

 

18

 

 

2 ADD'N.

THERMOCOUPLE WELL
20.0.x.042 WALL TUBE
FUEL DIP LINE & N
$0.0.x.072 WALL TUBE

 

 

ALL DIMENSIONS
IN INCHES

 

 

LEVEL PROBE TUBE

3

— e ——— —— —— —— e

 

 

 

 

 

 

 

 

 

-
v

 

 

‘13 SCH.40 PIPE
| 10 2:2:
—

 

illation.Experiment. Schematic diagram of the

t

 

 

 

 

 

 

 

 

 

 

 

 

Molten Salt Dis

Fig. 7.
condensate receiver.

 

 
 

oy

0

19

Detailed design of the condensate receiver is shown on Drawing No. M-12173-CD-~
009-D in Appendix H.

Thermal Design

The same thermal design was used for the condensate receiver and the feed tank
because the dimensions and use of the two vessels are almost identical. The receiver
is surrounded on the sides and bottom by heaters rated at 20 kw, capable of heating a
full charge of salt from room temperature to 500°C in about 2 hr. At operating
temperature, heat loss to the surroundings through é-in. insulation is about 1.1 kw.

The heaters are arranged so that about 6 kw are applied to the tank bottom and
14 kw to the sides.

The temperature of the condensate tank is kept just slightly above the liquidus of
the contained salt so that the salt vapor pressure is negligible, A high temperature

~at this point would cause salt vapors to flow into the vacuum system.

Operating Pressure

Pressure in the condensate receiver must be kept lower than the vapor pressure
of the salt in the still so that these vapors will flow from the still into the condenser.
The receiver is kept at a pressure in the range 0.2 to 0.5 mm Hg, allowing a pressure
difference of at least 0.5 mm Hg between the still and receiver.

Still and Condenser

The still and condenser are designed as a unit with the condenser's vapor inlet
actually extending into the still. The still reservoir is the annular space between the
vapor line and the outer wall.  No provision is made for removing still bottoms from
the annulus during the course of an experiment; however, a dip-tube is provided to
allow removal of liquid between experiments. As shown in Fig. 8, the still and

~ condenser are joined in-an angular configuration; this was necessitated by the limited

headroom in fhe operational area.

' Design Features

 The data given.in Table 1 characterize the Still-condenser'unit and its operation.
Detailed design of the unit is shown on Drawmg M-12173-CD-011-D and M-12173-

CD-014-D in Appendix H.

 
 

 

 

ORNL DWG. 66-109885

THERMOCOUPLE WELL
1/270.D, TUBE x 19 GA.

   
   
   

LEVEL PROBE FEED LINE

 
    
 
 
 
 
 

 

 

 

 

 

 

 

 

 

LEVEL PROBE
I3 SCH. 40 PIPE

- DRAIN 8 SPECIMEN HOLDER
THERMOCOUPLE WELL  ,2"0 p TUBE x19 GA.
172*0.D. TUBExI9 GA. ‘ ,

 

 

VIEW AwA

 

SAMPLE TURE
I3 SCH. 40 PIPE

ALL DIMENSIONS IN INCHES

 

 

o«
¥ |
SAMPLE RESERVOIR —/L.

 

 

 

 

aag

 

Fig. 8. Molten Salt Distillation Experiment. Schematic diagram of the vacuum still and condenser,

I3 SCH. 40 PIPE 4"0.0.x.072 WALL
STILL TuBE |
a
41 HANGER |
_ : BRACKET

0z

 
 

 

 

.U 21
. Table 1. Design Data for the Vacuum Still and Condenser
“’2.
. Still
Material Hastelloy N
Dimensions 14 in. diam x 16 in. high
‘Wall thickness 3/8 in.
Insulatiofi thickness 8in.
Thermal conductivity of insulation 0.1 Bty hr=1 f=1 o -1
Opéraring volume in annulus 12 liters
- Depth of salt for 12-liter volume 8.08 in. (measured from top
of conical bottom)
Height between high- and low=level control |
points 1.62 in.
Volume of salt between high- and low-level
control points ‘ 2 liters
: Operating temperature 900 to 1000°C
¥ Operating pressure 0.5 to 1 mm Hg
Surface wetted by 12 liters of salt (excluding -
vapor line) | 2.64 12
Surface area of salt 0.52 t2
Heat flux during distillation ~1615 Bty hr1 fi-2
Distillation rate (c_'.ulculafed) ~5.24 x 10-4 g/cm2 sec
- Time required to evaporate 12 liters of salt ~30 hr
- Heater rating | o 15 kw
Condenser
Material Hastelloy N
Dimefisibns 10 in. OD x 51 in. long
“ Wall thickness 3/8 in.
- Surface area (outside) | 11.3 2
' Insulation thickness 4 in.

Thermal conductivity of insulation

(continued)

0.1 Btu hr=1 ft~1 ° -1

 
 

o 22
~ Table 1 (Cpntinued)

 

 

 

-{i
Operating pressure 0.5 to 1 mm Hg |
Operating temperature 550 to 875°C !
Cooling method Conduction through insulation

to surroundings
Condenser duty 4000 to 5000 Btu/hr
Heater rating (equally divided in four zones
| over length) - 20 kw
Y
’
 

vl

a)

23

The still annulus is about 13 in. deep by 2 in. thick and, when charged with
12 liters of salt, will be filled within about 1.43 in. of the top. Heat for distilling
the fluoride mixture is supplied by electric heaters surrounding - the sides and top. The
heat flux is small, being only about 1615 Btu hr™ V12 at o distillation rate of 420
cmS/hr.  The top of the still is kept a few degrees hotter than the still liquid to
preclude condensation.

In designing the still, care was used to avoid junctions that would produce large
stresses in the metal parts when the unit is heated from room temperature to 1000° C,

- The still=condenser unit elongates about 1 in. when heated over this temperature range.

The unit is supported by a cable and counterweight attached to the still so that move~
ment is not restricted.

The condenser is made relatively large (10 in. OD) to facilitate heat loss by the
greater surface areq, thereby increasing the attainable distillation rate. A cylindrical
core is placed inside the condenser to channel salt vapor into the annulus adjacent to
the outside wall where it is condensed and cooled. Three radiation shields are placed
inside this core at the high-temperature end to decrease the amount of heat received -
by the condenser from the 1000° C zone of the still.

Temperature Measurement

Temperature measurements are made at a number of points on the outside surfaces
of the still and condenser by attaching thermocouples to these surfaces. These exterior
readings should be very close to the temperatures inside the vessel because of the very
low heat flux (~ 1615 Btu hr=1 §1~2); the calculated temperature drop across the wall
is only 1.5°C. However, interior temperature measurements are made in the still
liquid at three different elevations by introducing thermocouples into wells extending
through the vessel head. The temperature of either a surface or interior thermocouple
can be selected as the reference temperature at which the still is operated.

- As to the condenser,,only outside~surface thermocouples are installed and selected
ones are used to control the wall temperature. There will be a temperature gradient
along the length of the condenser to allow the condensed vapor to cool to a temper-

“ature of only 25 to 30°C above the liquidus as it drops into the condensate receiver.

When the condensate composition is that of the MSRE carrier salt, LiF-BeF ~ZrFy
(65-30-5.0 mole %), the condenser temperature can be as low as 500° C; byt for
experiments in which nearly 100 mole % LiF is distilled, the condenser surface needs
to have a minimum temperoture of about 875°C. .

Operating Pressure and Distillation Rate

The upper limit of 1000°C on the operating temperature requires that the still
pressure be no greater than 1 ' mm Hg during most of a distillation experiment if

 
 

 

 

L

24
vaporization is to occur.  The initial salt composition has a vapor pressure of perhaps
10 mm Hg at 1000° C, but the more volatile BeFy quickly boils out, leaving an equi-
librium mixture whose vapor pressure is about 1 mm Hg. A pressure gradient is main-

tained through the condenser by evacuating the condensate receiver to 0.5 mm Hg or
less. The volumeiric flow rate of vapor from the still to the condenser depends upon

the pressure differential. The graph in Fig. 9 is a plot of the calculated flow rate of -

condensate as a function of the pressure at the condenser outlet. The pressure at the
liquid surface in the still was taken to be 1 mm Hg, and the vapor composition was

‘assumed to be that of MSRE carrier salt, namely, L|F-BeF2-ZrF (65-30-5 mole %).
The calculations indicate that the still will have a capacity of about 400 em /hr when

4~in. insulation surrounds the condenser.

. The same plot also shows the calculated distillation rate as a function of the
temperature of the condensing surface for insulation thicknesses of 3 in. and 4 in.
Satisfactory operation of the still is realized in the area to the left of these temper-
ature curves. Although the pressure curve was calculated for vapor of MSRE carrier
composition, it may be used with little error for vapors richer . in LiF. . For pure LiF
vapor the pressure at the condenser outlet needs to be about 3.5% lower than that of
MSRE carrier for comparable flow rates. However, the condensation temperature
must be considerably higher (>855°C) to preclude freezing.

Heat Rejection by Condenser
As stated above, the condenser rejects the latent heat of condensation of the salt

vapor by conduction through the thermal insulation to the surrounding atmosphere.
For this purpose the insulation is purposely made thinner (4 in.) than on other parts of

the equipment. The temperature of the condenser is maintained above the salt liquidus

by providing adequate heat input to the condenser. The rate of heat rejection is
directly dependent on the temperature difference between the condenser wall and the
surroundings, and the curves of Fig. 10 show this relationship over the temperature
range of interest in this experiment. The temperature at which the wall is held
depends on the vapor composition; that is, the wall temperature must be above the
liquidus yet low enough so that the vapor pressure of the condensate is small in com-
parison with the total pressure in the condenser. Salt of MSRE carrier composition
can be condensed in the temperature range 550 to 700°C; whereas, compositions

- containing greater than 90 mole % LiF require condenser temperatures of 800° to

900° C.

~ The dashed curves in the figure give the condensation rates for a vapor of MSRE
carrier composition and of pure LiF for values of the heat rejection rate. The
volumetric rate for the carrier salt was calculated for condensate at a reference
temperature of 600°C; for LiF the condensate temperature was taken as 875° C.

O

L 3]
PRESSURE CONDENSER OUTLET {(mm Hg)

 

 

&J‘ & o

ORNL - OWG - 68 -804

 

THICKNES

   

o
®

 

of—  INSULATION

S

|

'4
o
o
)

 

 

|- —|650
0.6 |
0 —ls00
/ / CONDENSER LENGTH = 3-0"
l | VAPOR: LiF -~ BeFz - ZrF4
| 64.7- 301" - 5.2 mole%
0.2H- STILL PRESSURE = | mm Hag.
V ! - —{580
0 _ | | I l 1 I | 520
300 400 500 600 700 800 900 1000 1100 1200

DISTILLATION RATE (cm3/hr) AT 600°C

~Fig. 9. Distillation Rate as a Function of Pressure at Condenser Outlet and Condenser Wall

Temperature.

CONDENSER WALL TEMPERATURE (°C

Ge

 

 

 
 

 

CONDENSER WALL TEMPERATURE (°C)

 

 

26

ORNL DWG.68-808-RI

 

2001~ \nsuLATION
THICKNESS =4"/=357 =3!
850 ‘ ' — 800
WALL TEMP |
800 - CURVES _ 4700
/7
ANSRE SALT
750 | / -600
/ 7
/ LIF rg%DENSER WALL

rFHEATER |
NSULATION
kz0.I Btuzft.hr.of — 500

3

|
\
*—1\
\

 

 

 

 

 

CONDENSATION RATE (c¢m3/hr)

 

 

 

 

 

d '

650 [~ —

, [ 400
/

600 |- —1300

500 : | I 6.5+ lt

 

 

3000 4000 5000 6000 7000 8000
HEAT REJECT IO_N. BY 3-0' LENGTH OF CONDENSER (Btu/hr)

Fig. 10. Condensation Rate of MSRE Carrier Salt as a Function of Wall
Temperature and Insulation Thickness.
 

 

I {9

r“\
.

a)

i

27
The curves of Fig. 10 are based on an effective condenser length of 36 in.; the

actual length is 51 in. The diagram on the figure depicts the wall configuration
used in the calculations. |

Thermal Design

 The governing requirement in determining the amount of heat that should be
supplied to the still and condenser is the time that can be tolerated in heating from
room temperature to operating temperature. Independent calculations were made for
the still section and condenser section for this transient period to find the relation
between time and installed heater capacity. This relation is shown on Fig. 11.  From
these data arbitrary choices of 15 kw for the still and 20 kw for the condenser were
made. These heat input rates will permit heating the unit to 1000°C in about 1.5 hr

~ if desired; however, a heat-up time of 2 to 4 hr will probably be employed. The

20-kw capacity on the condenser is adequate to allow using a thinner insulation than
the specified 4 in. if it is desirable to increase the distillation rate (see Figs. 9 and 10.)

~ In steady=state operation the heat demand by the still is only a small part of the
installed capacity. For example, the vaporization of 500 cm3/hr of MSRE carrier
salt requires about 1.5 kw, adding a calculated heat loss from the still of 1.1 kw,
there obtains a steady state requirement of 2.6 kw. Similarly for the condenser
liquefying MSRE salt at 700°C, the calculated heat loss to the surroundings is 2.1 kw.
Subtracting the latent heat of vaporization of the salt (1.5 kw) gives a steady-state

demand on the heaters of only 0.6 kw.

Heaters are arranged on the still so that about 11 kw are applied to the vertical
sides and 4 kw to the top. Separate controls are provided so that the top can be held
at a slightly higher temperature than the boiling salt to preclude condensation and
refluxing. The 20 kw on the condenser are divided into four approximately equal
parts covering the entire length. Each section has separate temperature control.

Cold Trap
The cold trap is inserted in the vacuum line upstream of the vacuum pump to
remove mists and vapors that could impair operation of the pump. The unit is shown
in Fig. 12. It is cooled by liquid N2 in the jacket surrounding the baffled vapor
chamber. Liquid No additions are made manually upon a signal from a level device
in the jacket. Nitrogen vapor is vented to the surroundings.
Vacuum Pump

The vacuum pump is a Cenco Hi-Vac capable of evacuating the system from

“atmospheric pressure to 0.5 mm Hg in about 3 hr. This time corresponds with the

 
 

 

 

28

ORNL -DWG-68-8ll

 

 

 
 
 
 
  
  

 

180k t\ INSULATION CONDUCTIVITY=0.l Btu/hr.ft. °F
o\ HEAT CAPACITY OF HASTELLOY N =0.16 Btu/Ib.°F
EMMISSIVITY OF HASTELLOY N= 0.6
so} \
o
©
140
1201 '
. ° °
»
}_‘_" CONDENSER SECTION
O WEIGH = 290LB.
£ 100F ~4" INSULATION
Z 3" INSULATION
O
o
S
o 80fF
I
I STILL
& WEIGHT (INC. SALT) = 215 Ib
- INSULATION THICKNESS = 8
o 60F :
-
w
=
e
40}
20
0 -l 1 B | l 1 . ]
0 S

10 (5 20 25 30
HEATER RATING {(kw)

 

Fig. 11. Time Required to Heat Vacuum Still and Condenser from Room
Temperature to 1000°C,
 

 

o

 

L}

ae)

29

ORNL DWG, 66-10986

LEVEL PROBE o rh
4 scH 40 PiPE ) @ _.o THERMOCOUPLE WELL

< $SCH. 40 PIPE

LIQUID Ny INLET

Ng VENT
4 SCH. 40 PIPE

% SCH. 40 PIPE

 

LEVEL PROBE
1scn. 40 miree

 

 

s .
283

”,L‘ 5" SCH. 40 PIPE

    

" ALL DIMENSIONS
IN INCHES .

 

 

DI H UM LINE.
1"SCH. 40 PIPE

Fig. 12, Molten Salt Distillation Experiment. Schematic diagram of the
liquid N, cold trap. o ‘

 
 

 

 

30

transient heat-up time for the system. Heating and evacuating would be carried

out simultaneously.

Sampler

Nonradioactive Operation

The two photographs of Figs. 13 and 14 show the sampler. The unit is installed
directly above the sample cup at the condenser outlet (see Fig. 8). ~The small line
above the top valve is used to evacuate the chamber just prior to sampling; the
3/4-in.~diam by 1- 3/4-|n.-long capsule is then lowered by means of the crane into
the sample cup, filled with molten salt, and retracted to a position above the flange.
After freezing, the sample is removed for analysis by closing the lower valve and
opening the flange. The frequency of sampling is limited by the time required for
these operations. | '

This sampler was designed for use in molten salt test Ioop experiments and is’
being reactivated for this experiment.

Radioactive Operation

The same sampling device will be used to sample radioactive salt at the MSRE
site when irradiated fuel is distilled. The 1-1/2-in. pipe, through which the sample
capsule is lowered, will be lengthened to extend through the cell roof plugs, and
shielding will be installed around the valves and flange that are above the roof plugs.
A sample of condensate will be obtained as described above. The sample is then put
into a shielded container for transport to the hot analytical laboratory.

Heaters

Electric heating elements are used on all vessels and lines. For the vessels, the
heaters are fabricated of ceramic, refractory material in which the elements are
totally embedded. The heaters were molded by the manufacturer® to fit the geometry
of the vessels and to be removable without disturbing any nozzles or other connections

~ to the equipment. All ceramic heaters are capable of holding the vessel that they

surround at 1000° C,

A copy of the specifications to which the heaters were purchased is included in
Appendix G.

 

*Cooley Electric Manufacturing Compcmy, 50 South Shelby Street, Indianapolis,
Indiana
 

 

 

 

 

83

31

 

PHOTO 68259

Fig. 13. Sampler for Vacuum Distillation Experiment,

 
 

 

;
j
i
;
i
i
|
i
i

 

 

32

PHOTO 68263

 

Fig. 14, View of Sampler Showing Sampling Capsule.

 

w
 

%)

AN

 

 

33

Wherever heat was needed on pipes or vent lines, the hnes were’ fraced with
tubular eleciric elements. .

: -Thermul Insulation

Two types of thermal msulatlon are used. Adjacent to the heaters where the
temperature might be as high as 1200°C, a 2-in.~thick blanket of Fiberfrax* is used;
outside this layer, Careytemp 1600** is applied to the desired total thickness. The
Fiberfrax used here is Type 970-JH, having the cemposmon 50.9% AlyOg, 46.8%
S|O2, 1.2% B2QOg3, 0.8% Na20, and 0.3% inorganics by weight. H coni‘alns no
organic binders and is recommended for temperatures to 2300°F. Careytemp 1600 is
an expanded silica insulation reinforced with inorganic fibers and is recommended for
use to temperatures of 1600°F. Molded, segmented, cylindrical shapes are used to
cover the equpment. The outside surface is finished with asbestos cement and glass
cloth plus a bonding c:dhesrve to give a glazed appearance.

 

The following tubulcmon 2 lists the thermal conductivjty of these msulahng
materlclls -

, .‘Dé'ns'igy - Thermal Conductivity at lndncated Mean Temperature
- {Ib/ft3) (Btu=in. hr=1 ft-2 °F"]) |

600°F  1000°F  1200°F 1400°F  1600°F

P ———

 

 

Fiberfrax | ' , o
Blanket form 6 -0 58 - 0.86 1.09 1.34 1.62
Paper form 12 0.48 - 0.69 0.8 L0 1.27
Careytemp 1600 076

i

METALL_URGICAL CHARACTERIZATION OF HASTELLOY N

The metallurglcol propertiesSs 4 of Hastelloy N at elevated temperatures are well -
documentated in the temperature range 600 to 800° C where it is commonly used.
However, data in the neighborhood of 1000° C are nonexistent since there have been

“no previous occasions to consider the alloy for use at such a high temperature. . In

this experiment the still will be at about 1000° C during most of its operation, and the
upper porhon of the condenser.will be at 800° C or higher a large part of the time.
However, in light of the initial distillation work of Kelly 1 using small stills made of
Hastelloy N, this alloy appeared suitable for the engineering-scale unit. Furthermore,

 

* A product of Carborundum Company, Niagara Falls, New York.

- **A product of Philip Carey Manufacturing Company, Cincinnati, Ohio.

 
 

 

34 o L)
- a time=consuming alloy developmental progrcm would have been. necessary to identify
‘@ more sunfcble material. ,

The results of an abbreviated testing program indicated that Hastelloy N should
be satisfactory for a short~term experiment and gave the data that were needed to
ensure a safe design. In addition, these tests revealed characteristics of Hastelloy N,
which, although not of serious consequence in this short experiment, would make this
~alloy unsuitable for use at 1000°C in a reactor processing plant. Three such properties
are the oxidation resistance, intergranular cracking, and the effect of thermal
cycling on high~ and low- temperature ductility.

Creep~Rupture Properties .

A brief, creep=rupture program? was undertaken by McCoy* to determine data
at 982°C (1800°F), and the results are given in Table 2, These data were obtained
on test specimens of a typical heat of air-melted Hastelloy N (Heat 5065). The
specimens were small rods having a gage section 1in. long by 0.125 in. diam.

The cumulative time that the vacuum still would be at 1000° C during the lifetime
of the experiment was estimated to be 1000 hr, and it was agreed that a satisfactory
design point would be one that limited the still to 1% creep over this length of time,

- The data of Table 2 were plotted as shown in Fig. 15 to extend the creep-rupture
‘characteristics over the expected lifetime. The curves show that the stresses producing
rupture and 5% creep over the 1000=hr period are reasonably well defined; whereas,
the 1% and 2% curves, in particular, are not defined sufficiently by the experimental
data. More data are needed for times greater than 100 hr. Nevertheless, the
allowable design stress was chosen by extrapolating the 1% curve to 1000 hr to obtain
a value of about 780 psi; this figure was rounded off on the lower side to 700 psi
which was used in the design calculations.

Ducfili.ty

* The ductility of Hastelloy N at 982°C (Fig. 16) exhibits a minimum for test
specimens having rupture lives in the approximate range of 50 to 200 hr, The
minimum ductility is slightly greater than 20%. The reduction in area decreases
rapidly with increasing rupture life to a value of about 15%. The increase in the
elongation for long rupture lives is thought to be associated with the exfenslve
lntergrcnular cracking that was observed.

 

*The data and discussion of this section are a summarization of the work of H. E. U
McCoy, Metals and Ceramics Division. His contribution to this design is gratefully
acknowledged. |
 

3! o P . _ - i .

Table 2. Creep Properties of Hastelloy N at 982°C ¢

 

 

%

Test ~ Time to Indicated Strain (hr) Reduction

No. olpsi) 1% 2% 5% 20% Rupture ‘e (%/hs) e (%) in Area Remarks

5768 2000 35 73 . 185 495  6M49 00276  4AL50 1622 ----

5765 3000 1 7.6 33 17 123.9 0.123 22,36 13.4 Temperature control not
- VE _ ' ' adequate at start of test.

5762 4000 0.7 2.0 11 47 51,5 0.282 21.88 15.47 Temperature control not

o ‘ adequate at start of test.

5761 6000 075 1.3 3.2 10.5 1615 165 48.44 36,57 ----

5763 10000  <0.1 0.2 0.5 1.9 295 9.0 50.0 37.86 -

5867 1880 35 72 165 407 520.8 0.026  52.0 15.6 -

5868 3000 12 25 40 154 157.9 0.081 22,22 15.6 ----

 

%Heat 5065 tested in the o#-received condition (1/2 hr at 1176° C mill anneal).

 

GE

 
 

 

36

ORNL-DWG 66- 11455
20,000

10,000

5000

STRESS ( psi)

2000

1000

 

500
0.1 { 10 00 1000

TIME (hr)

Fig. 15. Creep-Rupture Properties of Hastelloy N at 982°C Test
Specimens from Heat No. 5065.
 

 

Wik

al

RUPTURE STRAIN (%)
[4]
o

60

50

H
o

n
o

10

37

ORNL DWG 66-11457

 

 

 

 

 

 

 

 

 

 

 

O ELONGATION

 

 

 

 

 

 

 

 

 

60
— D
=Ty \Q\ 50
c —
| 1 40 ®
—flrl et \ ) o
\ <
L
! @
A \ / <
\ / 30 z
=
HEAT 5065 . S
Q
D
0o
L
o

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

A REDUCTION IN AREA 120
‘ __ A
A
10
- 0
! 10 100 1000

"RUPTURE TIME {(hr) -

Fig. ']6.7 _buctility of Hqsfélloy N at .982'°C.

 
 

 

38

~ Metallographic Examination

“Metallographic examination revealed that the quantity of precipitate after test-
ing at 982°C and 2000 psi was much greater than that present before testing. The
tested material contained larger particles of precipitate, which are thought to be
induced by the thermal and mechanical history;  also the smaller precipitate in the
as-received metal appeared to be a different composition than that found in the tested
sample. The precipitate apparently does not impair the ductility at 982°C, but its
effect on low-temperature ductility was not established. This effect could be
important in a vessel that undergoes a number of thermal cycles.

STRESS ANALYSIS

This experiment requires the use of Hastelloy N considerably above its usual
upper temperature (600 to 700°C) in molten-salt service. To ensure the adequacy
of the design, a thorough stress analysis* was made using the data of McCoy discussed
in the preceding section. The principal concern was with the still=condenser unit
which experiences temperature as high as 1000° C in some areas. - For the feed tank
and condensate receiver, which are not expected to be above 600°C, the stress
analysis was confined to calculating the resistance of the flat heads to externdl
pressure for full vacuum operation.

Vacuum Still and Condenser

This analysis was based on the 1% creep property of 700 psi allowable stress at
1000° C and the rupture property of 1650 psi at this temperature (see Fig. 15). In
addition, it was assumed that the unit would undergo 50 to 100 thermal cycles during
its 1000-hr lifetime. The analysis considered the stresses induced on the walls, head,
and nozzle penetrations by full vacuum operation; the stresses imposed by the dead
weight of the system and the method of support; and thermal stresses due to heat flux
through the wall and expansion-contraction from thermal cycling.

‘The conclusions of this study are that:

1. the vessel be limited to a total 0percmng life of 1000 hr and to processing
npnradnoachve salts;

 

 

*This secfioa is a summary of the work of C. A, Hahs and T. W. Pickel, General
Engineering and Construction Division. Mr. Hahs's detailed analysis is included in
Appendix F.
 

 

*1

4}

39

2. the vessel be observed after the nonradioactive experiments to determine
the effects of external oxidation and internal corrosion, and that the
effects be evaluated to determine if protective measures are required;

3. before use the vessel be given a thorough inspection (ultrasonic, dimen-
sional, photographic, visual, or other nondestructive tests) and that the
initial inspection be compared with a similar inspection after the non-
radioactive operation. |

An inspection of the still-condenser unit will be conducted before use and
compared with an inspection after the nonradioactive tests. This precaution is being
taken because of the lack of experience in using Hastelloy N at these elevated
temperatures, and, before use with radioactive salt, the integrity of the vessel must be
ensured. Even though conclusion 1 above states that the still not be used for distill-
ing radioactive salts, it was thought that this portion of the program was important and
should not be abandoned. Consequently, the vessel will be thoroughly inspected
aofter nonradioactive operation, and, if further integrity of the vessel is ensured,
radioactive operation will proceed as planned.

The ASME Boiler and Pressure Vessel Code Sections [l and VIII does not
include the operating conditions specified for this equipment; the analysis was made
on the basis of meeting the intent of the Code, specifically Section VII. The final
design meets the intent of the Code, and the calculated stresses are below the 700 psi
aliowable stress. No fatigue analysis of the vessel was made because the data for
such an analysis were not available. However, the vessel will undergo a number of
thermal cycles, and fatigue may be an important factor in the design. This useful
information will be obtained from the experiment.

Feed Tank and Condensate Receiver

Stress calculations for these vessels were made for the flat heads only since
these were the weakest areas of the two tanks. The feed tank is 15.5 in. OD by
16.5 in. high.,  The physical data of Appendix A, Table A-4, were used to confirm
the use of 3/8-in.~thick plate for these. heads in the 500 to 600°C temperature

range.
INSTRUMENTATION

- The vacuum distillation expenment is operated primarily from temperature and
pressure measurements; fo a lesser degree, level measurements are also used. There

are two distinct zones over which temperature must be measured and controlled:
a 500 to 600°C range for feed and condensate and an 800 to 1000° C range for the

 
 

 

 

 

40 | B - )
salt in the still. Pressure is controlled at about 0.5 qtm-in the feed tank and in the
- 0.3- to 1-mm-Hg range in the rest of the system.  Thermocouples are liberally

employed on vessel surfaces and internally to the vessels for monitoring all areas of
the equipment. Identifications and descriptions of all instruments are given in
Table 3. : | o

Temperature Measurement

For the high temperature part of the system (still and condenser) where exacf
temperature measurement is most important, platinum~rhodium thermocouples are used -
because of their high stability. Throughout the system standard Chromel-Alumel
thermocouples are used for signals to the temperature controllers in order to standard-
ize on readily available Chromel~Alumel controllers. For control in the high-
temperature zones, the control points will be changed to make the Chromel-Alumel
thermocouple agree with the Pt=Rh thermocouple in that zone if any temperature shift
is observed. The less expensive Chromel=Alumel thermocouples are the primary units
on the feed tank, condensate receiver, and salt lines; however two Pt=Rh thermo-
couples are installed on each tank to indicate any drift. All thermocouples are
enclosed in a 1/8-in.-diam Inconel sheath, and insulated junctions are used.

Most of the thermocouples are attached to the outer surface of the vessel or
pipe by inserting the junction into a tab welded to the vessel. Before installation
each thermocouple is tested to ensure that its function has not been impaired. In
- addition to the surface thermocouples, there is one thermowell in the feed tank, four
in the still, and three in the condensate receiver. These are made of 1/2-in.-OD
by 0.042-in.-wall Hastelloy N tube. There is also a thermowell drilled into the base
of the sample cup below the-condenser for monitoring condensate temperature, since
it is desirable to keep this temperature as low as practicable to avoid excessive salt
vapors leaving via receiver vent.

For readout there is one 24-point recorder for the Pt-Rh thermocouples and
one 24-point recorder for the Chromel-Alumel thermocouples.

The other required temperature indication is of the liquid N5 cold trap in the
condensate receiver off-gas line. There is also a liquid No pressure bulb in the
~ jacket of the cold trap to actuate an alarm at low Ny level. Upon manual addition of
liquid N2, a high=level signal from a similar bulb actuates another alarm. . A
Chromel-Alumel thermocouple is used as an alternative level indication at both points.

Temperature Control

There are nine individually heated zones on the feed tank, still, condenser, and o
receiver. Heaters on each of these zones are controlled separately by a Pyrovane =’
Panel Board  Application

o

)

N

Table 3. Identification and Description of Instrumentation

 

 

Ly

Input Output :
Number Number ] Range Range Location Scale Function Type of Device
1 Pi-5 3-15 psig Panel 0-20 psia Monitor still pressure above range of PE-1 3-15 psig receiver gage
2 -5 3-15 psig Panel 0-40 in. H20 Menitor condensate raceiver level 3-15 psig receiver goge
3 P17 3-15 psig Panel 0-10 mm Hg Monitor sampler pressure 3-15 psig receiver goge
4 Pl-2 3=15 psig Panel 0-10 psia Monitor Ar pressure in feed tank 3-15 psig recelver goge
5 - Pdi=1 3-15 psig . Panei 0-2 psia Monitor level in feed tank by reading AP 3-15 psig recelver gage
6 LR~1 3-15 psig Panel 0-40 in. H,O Monitor salt level in feed tank Foxboro 2-Pen Pneu.-Recorder
é LR-5 © 3-15 psig Panel 0-40 in. HZO Menitor condensate level in condensate recelver Foxboro 2-Pen Pneu.-Recorder
7 - PR=1 0-14 mv Panel 0-2 in. Hg Menitor, record and control still vacuum Foxboro Electric=Recorder
8 PR-2 3-15psig Pane| - 0-10 psia Monitor ond record Ar pressure in feed tank Foxboro 2-Pen Pneu.~Recorder
.8 PR-5 3-15 psig Panel 0-20 psia Mc;nggor]und record still pressure above range Foxboro 2-Pen Pneu.-Recorder
‘ o - :
9 TR-1 | 0-44.9 mv Panel 0-2000°F Monitor various temperatures in system Brown 24-Pt, Recorder
{Ch/Al thermocouples)
10 LR-2  0-50 mv AC Pane! 8-10in, HyO  Control salt level in still Fox. Resistance Dynalog Rec.
1 PC-1 0.2-2 in. Hg Panel Muyltirange Monitor and transmit to PR-1 signal NRC Alphatron Vacuum Gauge
‘ proportional to still vocuum .
13 TIC-9 0-44.9 mv Panel 0~-2000°F Control temperature of salt in feed tank Honeywell Pyrovane
14 TR-2 0-10,7 mv Panel 0-2000°F Monitor various temperatures in system Brown 24-Pt, Recorder
(Pt/Rh thermocouples)
15 | LR-3 0-50 mv AC Panel 0-8 in. H20 Monitor ond record low level of salt in still Fox, Resistance Dynalgy Rec.
16 LR-4 0-50 mv AC Panel 0-20 in. HZO Monitor and record condensate level in receiver Fox. Resistonce Dynalog Rec,
17 TIC-2 0-44,9 mv. Pane! 0-2000° F Control temperature along condenser Honeywell Pyrovane
18 TIC-3 0-44,9 mv Panel 0-2000°F Control temperature along condenser Honeywell Pyrovane
19 TIC-4 0-44.9 mv Panel 0-2000°F Control temperature along condenser Honeywell Pyrovane
20 TIC-6 0-44,9 mv Panel 0-2000°F Control temperoture of condensate receiver Honeywell Pyrovane
0 TIC-7 0-44.9 mv Panel 0-2000°F Control temperature of top of still Honeywsll Pyrovane
22 TIC-8 0-44.9 mv Panel 0-2000° F Control femper;:lfure of salt in still Honeywell Pyrovane
23 HCO-11 0-208 VAC  0-208 VAC  Panel Provide line heat for condensate receiver Variae Unit
~ . outlet line
24 HCO-12 0-208 VAC  0-208 VAC  Panel Provide line heat for line between Variae Unit

condensate receiver and cold trap

 

 

 
 

 

 

Panel Boord  Application Input Ovutput
Number Number Range Range Location Scale Function Type of Device
25 HCO-13 0-208 VAC  0-208 VAC  Panel Provide line heat for line between feed tank Variae Unit
and still
26 TCO-2 0-208 VAC  0-208 VAC  Parel Control temperature along condenser Powerstat
27 HCO-16 0-208 VAC  0-208 VAC  Panel Provide line heat for salt feed line into Variae Unit
feed tank ‘
28 HCO-17 0-208 VAC  0-208 VAC  Papel Provide heat for top of feed tank Variac Unit
29 HCO-18 0-208 VAC  0-208 VAC  Panel Provide heat for bottom of feed tank Variac Unit
30 HCO-19 0-208 VAC  0-208 VAC  Panel Provide heat for bottom of condensate receiver Variac Unit
32 TCO-3 0-208 VAC  0-208 VAC  Parel Control temperature along condenser line Powerstat
33 HCO-10 0-208 VAC  0-208 VAC  Ponel Provide line heat for sampler line Variae Unit
34 TCO-4 0-208 VAC 0-208 VAC  Panel Control temperature along condenser line . Powerstat
36 TCO-6 0-208 VAC  0-208 VAC  Panel Control temperature of condensate receiver Powerstat
37 HCO-14 0-208 VAC  0-208 VAC  Panel Provide line heat for transmitter LT-1 Variae Unit
38 TCO-7 0-208 VAC  0-208 VAC  Panel Control heat input to top of still
39 HCO-15 0-208 VAC  0-208 VAC  Panel Provide line heat for transmitter LT-1 Variae Unit
40 TCO-~-8 0-208 VAC  0-208 VAC Panel Control temperature of stiil Powerstat
41 TCO-8 0-208 VAC  0-208 VAC - Panel Control temperature of still Powerstat
42 - TCO-9 0-208 VAC  0-208 VAC  Panel Control temperature of feed tank Powerstat
43 TCO-9 0-208 VAC  0-208 VAC  Panel Control temperature of feed tank Powerstat
HCV-1 Containment Sparge feed tank
Cubicle
HCv-2 Contoinment Vent feed tank
Cubicle ‘
HCV-3 Containment Purge feed tank vent line ond equalize LT-1
Cubicle
HCv-4 Containment Evacvate between sampler line valves
Cubicle
HCV-5 Containment Sparge condensate receiver
‘ Cubicle
HCV-8 Containment By-pass vacuum pump
Cubicle .
HCV-9 ~ Containment Vacuum pump suction valve
Cubicle '

ey

 
o) . kg

oA,

 

 

Panel Boord  Application Input Output
Number Number Range Range Location Scale Function Type of Device
HCV-10 Containment Vocuum pump discharge valve
Cubicle ‘
HCV-20
HCV-21
PS-1A Panel Provide alam on low vocuum Microswitch
PS-18 Panel Control vacuum pump Microswitch
Ps-2 3-15 psig Panel Provide alarm on high Ar pressure in feed tank Barksdale pressure switch
PS-5A 3-15 psig Panel Close FSV-1 on loss of vacuum Barksdale pressure switch
- PS-58 3-15 psig Panel Provide alarm on loss of vacuum Barksdale pressure switcl,
PT-2 3-15 psig Containment Monitor Ar pressure in feed tank Foxboro d/p cell
: ) Cubicle
PT-5 3-15 psig Containment Monitor still pressure outside range of PE-1 Foxboro d/p cell
Cubicle ‘
PT-7 3-15 psig- Containment Monitor sompler tube pressure Foxboro d/p cell
Cubicle
LE-2 0-50mv AC  Still Sense salt level at upper section of still Special level probe
LE-3 0-50mv AC  Stil Sense salt level at lower section of still Special level probe
LE-4 0-50 mv AC  Condensate Sense level in condensate receiver Special level probe
i receiver
XwM-2 ) Panel Supply fow voltage, high frequency current Hewlett-Packard Power Supply
XwM-3 ) (1000 cycles/sec) to LE-2, LE-3, LE-4
XwM-4 ) . :
LS-13% Contoct Cold Trap Sense N, level in trop and actuate hi-level Special level switch
closure alam
LS-138 Contact Cold Trap Sense N, level in trap and actuate low-level Special level switch
closure alam
Pl-1 Field 0-15 psig Indicate Ar supply pressure Pressure indicator
Pl-3 Field 0-30 psig Indicate control valves header pressure Pressure indicator
- Pl-6 Field 0-30 psig Indicate Ar pressure to feed tank Pressure indicator
- Pi=7 3-15 psig Panel 0-10 mm Hg Indicate pressure in sampler tube Receiver gage
PI-9 0.2-2 in. Hg Field Multironge Used for colibration check on PC-1 Mcleod vacuum goge
FC-1 Containment Limit Ar flow rate Capillary

Cubicle

ey

 

 
 

 

 

Panel Board  Application Input Output .
Number Number Range Range Location Scale Function Type of Device
LCV-2A Panel Actuate LCV-2B 3-way solenoid valve
LCV-28 Containment Control level of salt in still Pneumatic control valve
Cubicle '
Hv-1 Pane! Argon to feed tank Manual valve
HV~2 Panel Argon to eondensate receiver Manual valve
HV-3 Field Liquid N2 addition Manwual valve
Fi-1 Panel 0-10 |/min Indicate Ar flow into feed tank ' Rotameter
FI-2 Panel 0-10 |/min Indicate Ar flow into condensate receiver Rotameter
during ogitation or condensate removal
FSV-1 Panel Shut off Ar supply to feed tank on loss of vacuum Prneumatic control valve
FSv-2 Containment Prevents backflow into system from off-gas system Check valve
Cubicle ‘
FSV-3 Panel Control FSV=-1,. Operates on loss of vacuum Solencid valve
detected by PS-5A '
PV-1 Panel Regulates Ar pressure to feed tank ‘Pneumatic regulator
PV-3 Panel Regulates air supply pressure for all Pneumatic regulator
. pneumatic control valves ‘ _ t
LT-1 0-40 in. H20 3-15 psig Containment Monitors feed tank salt level Foxboro d/p cell ’
Cubicle
LT-5 0-40 in, HZO 3-15 psig Containment Monitors condensate receiver level Foxboro d/p cell
Cubicle
-1 - TA-102 Contact Contact Panel Alarms on low feed tank temperature Annunciater
‘ closure closure
1-2 TA-110 Contact Contact Panel Alarms on low still feed line temperature Annunciator
‘ closure ¢losure : ‘ ‘ B
1-3 TA-134 Contact Contact Panel Alarms on low condensate receiver temperature Annunciator
closure closure
1-4 Contact Contact Pane! Annunciator
_ closure closure :
1-5 . Contact - Contact Panel Annunciator
closure closure
1-6 Contact Contact Panel Annunciator
' closure closure '
. » - 1 1 $

 
- ¥)

Panel Board  Application

 

-

 

Input Output
Number Number Range Range Location Scale Function Type of Device
2.1 TA-112 Contact Contact Panel Alarms on low still temperature Annunciator
_ closure closure
2-2 TA-1B Contact Contact Panel Alatms on low condenser temperature Annunciator
‘ closure closure ‘ _
2-3 TA-28 Contact Contact Panel Alarms on low condenser temperature Annunciator
clasure closure
2-4 - TA=3B Contact Contact Panel Alarms on low condenser temperature Annunciotor
' closure - closure .
2-5 TA-48 Contact Contoct Panel Alarms on low condenser imeperature Annunciator
closure closure
2-6 TA-78 Contact Contoct Panel Alarms on low still tempersiure Annynciator
_ closure clsoure '
31 PA-1 Contact Contact Panel Alams on low vacuum in still Annunciator
closure closure
3-2 PA-2 Contact Contact Panel Alamms on high Ar pressure in feed tonk Annunciator
closure closure '
3-3 TA=5 Contact Contact Panel Annunciator
. closyre closure
3-4 LA-136 Contact Contact Panel Alorms when liquid N, trop is filled Annynciator
' ~ closure closure
3-5 LA-138 Contact Contact Panel Alarms on low liquid N2 level in cold trap Annunciator
closure closure .
3-6 Contact Contact Panel! Annunciator
_ closure closure _
4-1 Contact Contact Panel Annunciator
closure closure
4-2 Contact Contact Panel Annunciator
closure closure
4-3 ~ Contact Contact Panel Annunciator
closure closure
4-4 Contact Contoct Panel Annunciator
closure closure
4-5 Contact Contact Panel Annunciator
closure closure
4-4 Contact Contact Panel Annunciator
closure closure

Gy

 

 
 

Panel Board  Application Input Output *
Number Number Range Range Location Scale Function Type of Davice
TE-131 0-2000°F Conde.nscfle Monitor temperature Ch/Al
receiver
TE-132 0-2000°F 0-10.7 mv  Condensate Monitor temperature Pt/Rh
‘ receiver ‘ _
TE-133 0-2000°F 0-10.7 mv Coude.nsate Monitor temperature Pt/Rh
receiver
TE-134 0-2000°F 0-44.9 mv Cond:ensafe Monitor temperature Ch/Al
receiver
TE-136 0-2000°F 0-44.9 mv ‘ Cold Trap Alarm on high liquid N, level in cold trap Ch/Al
TE-138 0-2000°F 0-44,9 mv Cold Trap Alarm on low liquid N, level in cold trap Ch/Al
TE-141 0-2000°F 0-10.7 mv Condenser Monitor temperature Pt/Rh
TE-140 0-2000°F 0-44.9 mv Condensate receiver Monitor temperature Ch/Al
Exit line
TE-1A 0-2000°F 0-44,.9 mv Condenser Monitor temperature Ch/Al
TE-1B 0-2000°F  0-10.7 mv Condenser Monitor temperature Pi/Rh -
TE-2A 0-2000°F  0-107mv  Condenser Control Ch/Al
TE-~2B © 0-2000°F 0-10.7 mv Condenser Monitor Pt/Rh
TE~-3A 0-2000°F 0-44.9 mv Condenser Control Ch/Al
TE-~3B 0-2000°F 0-10,7 mv Condenser Monitor Pt/Rh
TE~4A 0-2000°F 0-44.9 mv Condenser Control Ch/Al
TE-4B 0-2000°F 0-10.7 mv Condenser Monitor Pt/Rh
TE-7A 0-2000°F 0-44.9 mv - Still Control Ch/A}
TE-7B 0-2000°F 0-10.7 mv Still Meonitor Pt/Rh
TE-8A 0-2000°F  0-449mv  SHill Control Ch/A}
TE-88 0-2000°F 0-10,7 mv Still Monitor Pt/Rh
TE-9A 0-2000°F 0-44.9 mv Feed tank Control Ch/Al
TE-98 0-2000°F 0-44.9 mv Feed tank Monitor Ch/A1
TE-58 0-2000°F  0-44.9 mv Monitor Ch/AI
TE-6B 0-2000°F  0-44.9mv Monitor Ch/Al
TE=-139 0-2000°F 0-44.9 mv Monitor Ch/Al
TE-6A 0~2000°F  0-44.9mv Monitor Pt/Rh

v

 
Panel Board

 

 

Application : Enpuf‘ * Output
. Number Number Range " Range Location Scale Function Type of Device -

TE-100 0-2000°F  0-44.9mv  Feed tank Monitor femperature Ch/Al
TE-101 0-2000°F 0-10.7 mv Feed tonk Monitor temperature Pt/Rh
TE-102 0-2000°F 0-44.9 mv Feed tank Monitor temperature Ch/Al
TE-103 (0-2000°F  0-44.9mv  Feed tank Monitor temperature Ch/Al
TE-104  0-2000°F. - O0-44.9mv Feed tank Monitor temperature Ch/Al
TE-105 0-2000° F 0-10.7 mv Feed tank Monitor temperature Pt/Rh
TE~106 0-2000°F  O-d44.9mv LT line Monitor temperature Ch/Al
TE-107 . 0-2000°F - O-44.9mv  LT-1line Monitor temperature Ch/A]
TE-108 0-2000°F - 0-44.9mv StiH input line Monitor temperature Ch/A1
TE-109 0-2000°F  O-449mv  Still input line *Monitor temperature Ch/A1
TE-110 0-2000°F  0-44.9mv  Still input line Monitor temperature . Ch/A1
TE-111 0-2000°F . 0-10.7mv Skl " Monifor temperature Pt/Rh
TE-112 0-2000°F  0-10.7mv  SHll Manitor temperature Pt/Rh
TE-113 0-2000°F . 0-10.7mv  SHll Monitor temperature Pt/Rh
TE-114 - 0-2000°F  0-107mv  Still Monitor temperature Pt/Rh
TE-115  0-2000°F  0-107mv  SHll Monitor temperature Pt/Rh
TE-116 0-2000°F = 0-107mv  Still Monitor femperature Pi/Rh
TE-117 0-2000°F - 0-10,7mv  Still Monitor temperature Pt/Rh
TE-118 0-2000°F  0-107mv Skl - Monitor temperature Pt/Rh
TE-120 0-2000° F 0-10.7 mv still Monitor temperature Pt/Rh
TE-122 '0-2000°F ~ 0-449mv  Still Monitor femperature Ch/Al
TE-123 0-2000°F ~ 0-10.7mv ' Condenser Monitor femperature Pt/Rh
TE-124 0~2000°F  0-10.7 mv Condenser Monitor temperature P1/Rh
TE-125 0-2000°F . 0-10.7 mv Condenser Monitor temperature Pt/Rh
TE-126 '0-2000°F  0-44.9mv  Condenser Monitor temperature Ch/Al
TE-127 0-2000°F 0-44.9 mv Sompler line Menitor temperature Ch/Al

. TE=128 0-2000°F 0-10.7 mv Condenser Monitor temperature Pt/Rh
TE-129- 0-2000°F 0-44.9 mv Condensate receiver Monitor temperature Ch/Al
TE-130 0-2000°F 0-44.9 mv Condensate receiver Monitor temperature Ch/Al

Ly

 

 
 

 

 

 

48

on-off controller. The voltage to heaters in each zone is controlled by Variacs.
There are seven heated lines on which heaters are controlled by on-off, manual
switches and Variacs. All heater controls are mounted on four 24-in. standard

_ instrument racks which adjoin two additional racks containing the temperature
recorders plus pressure and level instruments.

Tem peruture Annunciators

" Each of the nine heated zones on the equipment and the salt feed line to the
still are provided with low-temperature annunciators. The alarm-points are set to
provide indication of instrument or heater fcnlure before the temperature falls low
enough to freeze the salt.

Pressure Measurement

Feed Tank

An absolute pressure D/P cell connected to the feed tank vent line in the con-
tainment cubicle measures the pressure in the feed tank. This pressure will vary -
between 5 and 7 psia as the salt is pressurized into the still, the increase in pressure
being caused by the decreasing level in the feed tank. Pressure in excess of 7 psia
probably indicates a restriction in the still feed line.

Condensate Receiver

 

The pressure in the condensate receiveris used as an indication of the ‘pressure
in the still ofter adding the calculated AP through the condenser. Measurement of
the pressure in the still itself was felt to be impractical because of the high temper-
ature and because introduction of an inert purge into the still would make control of
vacuum more difficult. The pressure tap for this measurement is on the 1-in. vacuum
line very near the condensate receiver. Two pressure instruments are used: - (1) an
MKS Baratron pressure measuring device with ranges of 0 to .003, 0 to 0.01, O to 0.03,
0to 0.1, 0t0 0.3, 0 to 1, 0 to 3, and O to 10. mm Hg; and (2) anabsolufe
pressure D/P cell covering the range from 0 to 15 pan.

| Samele Line

A pressure transmitter measures the pressure between the two valves in the
1-1/2-in. salt sample line. During operation at vacuum these valves may not seal
tightly enough, and it may be necessary to maintain this pressure near the operating
pressure. '
 

 

49

Pressure Control

The system pressure is controlled by feeding argon to the inlet of the vacuum
pump. The Baratron pressure instrument is used to regulate the flow.

In order to protect the still against excessive internal pressure (at high temper-
ature, pressures in excess of 2 atm could be unsafe), the argon supply to the system
will be cut off if the system pressure exceeds 1 atm. The absolute pressure trans-
mitter in the condensate receiver off-gas line is used for this purpose.

Liquid Level Measurement and Control

Feed Tank

The pressure differential between the outlet of a dip tube extending to the
bottom of the tank and the gas space above the salt is used to measure the salt level.
Difference in level provides a check on the salt distillation rate. The dip~tube purge
is provided by the argon which displaces the salt being fed to the still. The feed
tank and condensate receiver liquid levels are transmitted to a two-pen recorder.

Still

A conductivity-type level probe (see Flg 17) is ‘used i in the shll for measuring
and controlling the liquid level. This probe is similar to the single=point level
probes being used in the MSRE drain tanks but with two concentric tubes instead of
one for the excitation length because of the limited head room in the still. Tests
have shown that a variable output is obtained over at least ane-third the length of

‘the sensing probe., A 6-in. sensing probe is therefore used to control the liquid

level between 1 in. and 3 in. below the top of the annulus. The bottom joint of the

“two concentric tubes in the excitation length is located at this upper control point.
~ When the salt is below this point, the control valve in the argon line to the feed tank

is open and argon flows through a capillary restrictor: to the feed tank. The restrictor
is sized so that the gas displaces salt to the still at a rate slightly in excess of the

~ desired distillation rate. A recorder shows the rising liquid level. When the bottom

joint of the excitation length is reached, the valve closes and the level falls for about -

- 2 hr until it reaches the bottom of the sensing probe. At this point a signal causes the

valve to open to start charging salt to the still again.

A second conductivity probe with a straight excitation length extends as close as

possible to the tapered bottom of the still pot ‘This provides salt level measurement

during the final boildown. .

 
 

 

 

 

50

ORNL - DWG-68-818

   
    
    
  
 
   
 
   
 

  

SEALED
PENETRA

TO AMPLIFIER
AND READOUT

1000 CYCLE
EXCITATION

STILL TOP

CONCENTRIC
TUBES .

‘MAX. LIQUID LEVEL

MIN. LIQUID LEVEL

Fig. 17. Liquid Level Probe.
 

 

)

N

oy

ol

Condensate Receiver

 

A third conductivity probe is installed in the condensate receiver to permit
following the distillation rate. -~ The probe is long enough to provide continuous
measurement for the entire volume of the tank. It was felt that the alternate choice
of a continuous bubbler-type instrument would require too much purge gas, causing
excessive pressure drop in the line to the vacoum pump. A bubbler-type instrument,
however, is installed for periodic checks and calibration of the conductivity probe.

- PREOPERATIONAL INSPECTION

The use of Hasrelloy N at temperafures of 800 to 'r000°C is not well enough
known to predict the condition of the vacuum distillation equipment after extended
periods of operation. Since the second phase of the experiment invoives the use of
radiocactive materials, it will be necessary to thoroughly inspect the vessel after non-

~ radioactive operation. The basis or reference for this inspection is a set of radio~
~ graphic observations plus direct and ultrdsonic dlmenslonal measurements made on the

assembled eqUtpmenl before initial operahon.

~-An inspection program was planned that completely described the still, condenser
and condensate receiver assembly. - As shown on drawings No. -M-12173-CD-019D,
M-12173-CD-020D, and M~=12173-CD-021D of Appendix H, a mapping of 247 points
for radiographic and ultrasonic measurements of wall thickness is specified on the
vessel surfaces. In addition, locations in the form of center-punched tabs are provided
for 55 length and diameter measurements. Data points are concentrated in regions
where highest material stresses are expected.

The referenced drawings contain a record of the initial measurements, showing
that thicknesses were measured to the nearest 0,001 in, and linear measurements to the
nearest 1/32 in. Because of equipment and geometrical limitations, it was not possible
to check every ultrasonic measurement with a direct measurement., Length and
diameter measurements were made after the unit had been installed in supporting
framework at the location where it was to be operafed Thls precauflon precluded a

_measuremenf blas due to handlmg and transport.

Afrer nonradloactwe operation, msulahon and heaters wull be removed and alI
measurements and observations will be repeated - The new data will be recorded on

~ the referenced drawing for easy comparison with initial values. At that time the

su:tabll:ty ol" fhe equnpmenr l"or furfher experlments will be decided,

 

*lnspechans and measurements were made by R. M. Fuller and co-workers of the
Inspection Engineering Division.

 
 

 

EQUIPMENT INSTALLATION

Unitized Construction

The entire dlshllahon unit conslstmg of the feed tank, still, condenser,

~ condensate receiver, and.cold trap with the associated heaters, insulation, and
thermocouples is installed in a 3 ft x 6 ft 4 in. x 8 fi - high angle-iron frame
~designed to be moved as a unit. The base supports for the feed tank and condensate
receiver are bolted to the botiom of the frame. . The still is supported by a counter’
weight on a pulley to allow for thermal expansion during Operafion but will be
rngldly supported while in transit. The cold trap, being small, is supported by the
1-in. vent line from the condensate receiver. An electrical junction box and

two thermocouple junction boxes are provided on the frame.

| Hodd- Ihstal Iafiori

The distillation umt W||| be msl'alled ina wclk-ln hood, 4 ft 4 in. x 8t x 9 ft
high, located in Building 3541, for nonradioactive operation. The lZ-ft-Iong
instrument and heater control panel, the containment cubicle for D/P cells, remote.
valves, and the vacuum pump are mounted near the hood. The vacuum pump dis-

- 'chqrges through absolute filters. The directly operated sampler, described above,

 

is located inside the hood. Nonradioactive operation W||| test all of the equipment
to be used in the radioactive demonstration.

Cell Installation

At the completion of nonradioactive testing, the unit will be thoroughly in-
spected to determine its suitability for radicactive operat:on If this inspection is .
affirmative, all electrical, instrumentation, and piping connections will be broken
and the unit moved to Building 7503. . The unit will be installed in the spare cell
to the east of the fuel processing cell, as shown. in Figs. 18 and 19. Electrical and
thermocouple leads will be brought through penetrations in a roof plug to the high--
bay area over the cell where control panels are located. These panels contain
heater. controls, temperature recorders, and pressure and level readout msfruments.

| Salt is chorged. to the,feed tank through line No. 112, which is connected to .
~ the fuel storage tank and contains a freeze valve. All other piping connections
including the sample line passes through a roof plug to the high-bay area where the
sampler, vacuum pump, liquid Ny supply, and instrumentation are located.

Additional concrete shielding will be provided in the cell surrounding the unit
to prevent excessive radiation in the operating areas to the east and south of the cell. \/
 

it}

53

MSRE HEATER
CONTROL PANELS

ORNL DWG 67-3653 RI

 

NN

 

077

SPARE CELL FIXED

SUPPORT
PLUG

   
 
  
  
 

CHEM. PLANT EXHAUST

 

 

 

 

    

 

 
  

  

 

 

 

HOT
_ EQUIPMENT
STORAGE \
CELL \
§ FILTER—>
« —] CELL
§ - ~—EXHAUST
60" HIGH _ INNN\¥ CHEM.
- WALL PLANT
CHARCOAL
TRAP

DECONTAMINATION
CELL

    
 
   

 

   

 
 
  

2

JE BLOC

------- bt
s

  

    

 

L))

FUEL PROCESSING CELL

Fig. 18. Layout of MSRE Spare Cell.

\\\\\\\\\\\\\\\\\\\\\\\\\\\\\\\\\\\\\\\\s

PENETRATIONS
FOR ELECTRIC
LEADS AND

™ INSTRUMENTATION

ELECTRIC
SERVICE
AREA

_CONDENSATE
RECEIVER

~CONDENSER

- STILL
L FEED TANK

 

DRAIN TANK
CELL

 
 

 

 

 

HIGH

54

ORNL - DWG- 68130

 

 

—SAMPLER

 

0-8|

 

— LEAD SHIELD

ELEV. 852-0"
BAY AREA /7 3

 

 

 

 

 

FROM FUEL
o

STORAGE
TANK

Fig.

 

 

 

   
  
 

BARYTES
CONCRETE
BLOCKS :

 

 

 

ELEV. 840-0"
C -

 

 

 

 

 

 

 

°o°°°.0o°v

 

 

 

 

 

 

 

 

L ELEV. esiio"
Ifuo E

 

oo ©

SATE. RECEIVER

Og oo o0
9000 ®

 

 

 

19. South Elevation of MSRE Sparer Cell Showing Distillation Unit

and Sampler Locations.
 

N}

g%

e}

.

55
Since the salt will have been fluorinated before distillation, no volatile activities
are expected to pass through the liquid No trap. The vent from this trap and the
three instrument lines for pressure measurements in the feed tank and receiver are -
routed to a sealed, monitored cubicle in the high-bay area. This cubicle contains
all equipment and instruments that are connected directly to the process equup-
ment (vacuum pump, control valves, and instrument transmitters) as shown in Fig. 20.
In case of activity backup in the lines, a radiation alarm will indicate the difficulty
and the lines or cubicle can be purged. The top and one side of the cubicle is
sealed with a gasketed, removable cover to facilitate maintenance.

FINAL DISPOSITION

At the end of the radioactive salt distillation, the salt will be distilled until the
level is just below the low-level probe. All heat will then be turned off the
equipment and the salt allowed to freeze.in the still and the receiver. The feed tank
will have been emptied as much as possible. The vacuum pump will be turned off and
the system allowed to reach atmospheric pressure and temperature under an argon
blanket. -

The level probe line to the receiver is heated and insulated and can be used
to remove a composite sample (or the entire amount of condensate). In that case a
shielded, sample-transport cask will be connected to the line in the high-bay area

and the salt pressunzed from the receiver. -

After the system is cool, all electricol and thermocouple leads will be severed
as close to the unit as possible. The flanged lines will be disconnected and blanked;
tubing lines will be cut and crimped.. The entire unit will be removed from the
cell using remote maintenance techniques and taken to a burial ground for storage.

' ACKNOWLEDGEMENTS

The authors grctefully acknowledge the assistance of the following individuals
who were interested in this experiment and contributed to its design: R. E. Whitt
and B. C. Duggins for the design and selection of instrumentation; C. A. Hahs,

T. W. Pickel, and W. R. Gall for stress analysis on the assembled equipment;
H. E. McCoy for essential, high-temperature data on Hastelloy N; J. W, Krewson

~ for special instrumentation for liquid-level measurement; and members of the

Chemical Technology Dwnsuon MSR commlttee for helpful criticism during design
reviews. , |

 
 

 

o 56"

—\ac Pump

 

Not Shown:

Instrument Air Supply Lines
Instrument Output Air Lines
Air Lines To Valves

Motor Electrical Supply
Cubicle Radiation Monitor

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

ORNL DWG. 68-8€9

 

 

 

 

 

 

 

 

 

 

 

 

 

 

To. Feed Tank Dip Tube (1/2" T }—1
To Feed Tonk Vent {(I"P)

 
 

 

 

 

 

 

 

 

 

 

 
 

System Pressure pfx:;::'; Receiver Sompte Line
{Medium Range} (Low) LL. Pressure
PT-5 PE-~I LT-5 Hov-a PT-7
] Lo HI >4 From LD
HCV-T HCV~-4 Header
6? NCV-9 - 1 -From Somple
HCY-1A A @_. : Line
HCV-8 rN T »
> —
HCV-I0 -
HVA
le——] o-30"
Feed Tank Feed Tank &1 o
« kL. Pressure -
PT-2 l _ CC/MIN
4 Vacuum
Y Pump Air
Open Valve to Vent
Cubicls During Operation.
Close Valve to Leak

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

From Ny Trep{1"P)

 

 

 

 

To Receiver Dip
Tube (3/4'T)

Fig. 20. Diagraom of Sealed Cubicle,

 

Test Cubicle.

  
  

 
 

 

a%

)}

12.

57
REFERENCES

|
1. M. J. Kelly, "Removal of Rare Earth FISSIon Products from Molten Salt Reactor
Fuels by Distillation,” a talk presented at the 11th Annual Meeting of the
American Nuclear Society, Gatlinburg, Tennessee, June 21-24, 1965.

2, R. C. Robertson, MSRE Design and Operations Report, Part |, Description of
Reactor Des:gn, ORNL TM-728, pp. 217-18 (January 1965).

3. J. T. Venard, Tensile and Creep Properties of INOR - 8 for the Molten Salt
o Reactor Experiment, ORNL-TM- 1017 (February 1965).

 

4, R. W. Swmdeman, The Mechanical Properhes of INOR 8, ORNL-2780
(January 10, 1961).

5. R, B. Briggs, Molten Salt Reactor Program Semiannual Progress Report for |
Period Ending August 31, 1966, ORNL-4037, pp. 125-30 (January 1967).

6. K. A. Sense, M. J. Snyder, and R. B. Filbert, Jr., "The Vapor Pressure of
Beryllium Fluoride," J. Phy. Chem. 58, 995-6 (1954).

7. W. R. Grimes, Reactor Chemistry Division Annual Progress Report for Period
Ending December 31, 1965, ORNL=-3913, pp. 24~33 (March 1966).

 

8. 'R. B. Briggs, Molten~- Salt Reactor Program Semiannual Progress Report for
- Period Endmg August 31, 1965, ORNL - 3872, p- 126 (December 1965).

 

9. W. R. Grimes, Reactor Chemistry Division Annual Progress Report for Period
Ending January 31, 1963, ORNL-3262 (May 4, 1962).

 

-10. J. H, Perry (ed. ), Chemlcal Engmeers Handbook 4th ed., McGraw - Hill,

New York 1963.

11, R. B. Lmdauer, Revuslons to MSRE Deslgn Data Sheets, lssue No 9 "ORNL-CF-
- 64-6~43, p. 9 (June 24 1964). |

~

ASME Boiler and Pressure Vessel' Code, Section VIII, .Ru‘.les for Construction of
Unfired Pressure Vessels, 1965 ed., published by the American Society of
Mechamcal Engmeers, Umfed Engmeermg Center, 345E. 47fh St., New York.

13. R. J. Roark, Formulas for Stress and Strcun, 3rd ed., McGraw H||| New Yor|<,
1954,

14, L. E. Brownell and E. H. Young, Process Equipment Design, John Wiley & Sons,

Inc., New York, 1959.

 
 

 

 
 

 

w“w

»

8%

h)

59

APPENDICES

 
 

 

 

o e
 

w}

0

3}

 

w)

6l
APPENDIX A

Physical Properties of Hosfelloy N

Table A-1- - Chemical Composition

Table A-2 ~ Density and Melting Range

Table A-3 - Thermal Conductivity

Table A-4 Modulus of Elasticity

Table A-5 Specific Heat o

Table A-6 Mean Coefficient of Thermal Expansion
Table A-7 Mechanical Properties |

Table A--'I._ Chemical Composition

 

 

Weight %
Nickel | " Balance (~66-71)
Molybdenum B 15,0 t0 18.0
Chromium o - 6.0to 8.0
Iron, max. 5.0
Titanium plus Aluminum, max. | 0.50
Sulfur, max. , | : 0.02
Manganese, max. | 1.0
Silicon, max. 1.0
Copper, max. - 0.35
Boron, max. | | - 0.010
Tungsten, max. | | 0.50
Phosphorus, max. . o 0,015
Cobalt, max. B 0.20
Vanadium, max. | | 0.5

" Catbon | - 0,04 to 0.08

 

 
 

 

 

 

| - 62 -
Table A-2. Density and Melting Range

Density at 25°C, g/cm3 | - | 8.79 -
| Ib/in.3 0317
Melting range, °F | 2470 to 2555

°C - 1353 to 1400

 

Table A-3. Thermal C_onductivi_fy

 

 

Temperature (°F) "Bty ft hr=1 =2 °F
212 - 6.600
400 | | - 7.409
- 600 ~ 8,293
800 | 9.160
1000 - 10.37
1050 | : 10.81
1100 - 11.10
1150 11.41
1200 11.71
1250 ~ 12,02
1300 12.68
1350 13.26

1400 - 13.55

 
 

 

 

_Table A-4. Mo

63
dulus of Elasticity

 

 

 

 

 

Temperature (°F) psi x 1070
57 31.7
430 29.3
770 27.8
- 930 - 27.1
1070 26,3
1170 26.2
1290 24.8
1470 23.7
1570 22.7
1660 21.9
1750 20.7
1800 19.7
1830 19.1
1920 17.7
. Table A-5. - Specific Heat
Temperature (°F) Btu Ib~1 e g~!
140 0.0977
212 0.1005
392 0.1052
572 0.1091
752 0.1120
896 0.1139
1004 0.1155
1058 0.1248
1094 0.1347
1148 0.1397
i 1220 0.1387
1256 - 0.1384
1292 - 0.1380

 

 
 

. V M .
Table A-6. Mean Coefficient of Thermal Expansion

 

 

 

Temperature (°F) ~ in/in~°F | AT (°F) "AL/L (in./in.) |
70-400 6.45 x 1076 330 2.13 x 1073
70-600 6.76 x 1076 530  3.58 x 1073
70-800 7.09 x 10706 730 5,18 x 1073
70-1000 743 x 1076 930  6.81 x 1073
70-1200 7.81 x 1006 1130 8.83 x 107°
70-1400 8.16 x 1076 1330 10.85 x 1075
70-1600 8.51 x 1076 1530 13.02 x 10~°

70-1800  8.85x 1076 1730 1531 x 107°

 

 
65
Table A-7. Mechanical Properties

 

1/4 Min. Spec.  2/3 Min. Spec. 4/5 Rug Str. Stress for Max. Allow.
Temp. Tensile Strength  Yield Strength  for 10 0.1 CRU  Stress

 

_(°F (psi) (psi) (psi) (psi) ~ (psi)
0~ 100 25,000 26,700 - 14,500 25,000
200 24,400 24,100 - - 24,000
300 23,900 . 22,800 | - - 23,000
400 23,500 21,700 - - 21,000
500 - 23,100 20,800 - - 20,000
600 22,700 20,000 - - 20,000
700 22,250 19,300 - - 19,000
800 21,800 18,700 - - 18,000
200 21,200 18,150 - 18,150 - 18,000
1000 20,500 17,650 | 16,000 - 17,000
1050 . 19,900 17,400 14,500 - -
1100 19,100 17,200 12,400 14,500 13,000
1150 18,100 17,000 10,400 10,200 -
1200 17,100 16,800 8,300 7,400 6,000
‘1250 16,100 16,600 6,200 5,400 -
1300 15,000 16,400 4,800 4,100 3,500
1350 13,800 16,300 3,600 3,100 -

1400 12,700 16,200 2,900 2,400 1,900

 

 

.ow

 
 

 

 

66
- APPENDIX B

Physical Properties of LiF, BeFy, ZrF4,and Their Mixtures

Fig. B-1 Calculated Densities of Molten LiF, BeF,, and ZrFy

Fig. B-2 , Density~Temperature Curves for LiF-BeFp=ZrF Mixtures
Fig. B-3 Vapor Pressure-Temperature Relatidnships for LiF, BeF,
. - ZrFy, and Their Mixtures |

Fig. B-4 | Calculated Viscosity of LiF-BeF,-ZrF, Vapoi'
Table B-1 - Latent Heat of Vaporization of LiF, BeF,, ZrF4, and_

Their Mixtures

Table B-2 Thermal Properties of MSRE Salt A
 

 

[

iy

L))

LH

{9/ cm3)

DENSITY

67

ORNL-DWG -68-824

 

2.00 —\

.80—

.60~

140}—

 

.20

   
   

(BOILING POINTS CALCULATED FROM VAPOR PRESSURE DATA)
(DATA FROM REF. 9, ORNL - 3262) ‘

1159 °C
b.p.at 760mm

   

/-lGTG"C
! b.p.at 760 mm

  

LiF

  

 

- 3.80

3.60

3.40

3.20

3.00

 

 

500

]
1000 | 1800 2000
TEMPERATURE (°C)

Fiflg. B-1, Calculated Dénsifiés of Molten LiF, BeF, and Zr

F4.

2.80 .

(g7/em3)

DENSITY

 
 

 

 

 

{(gm/cm3)

DENSITY

- 2.20

210

68

ORNL-DWG-68-825

 

2.00

1.90

LiIF- BeFp - ZrFq
90.0-7.5-2.5
MOLE %

 

1.80

 
  

   

LiF- BeFp - Zr Fq
. 64.7-30.-52

|({DATA FROM REF. 7, ORNL-3913, P. 29)

LiF-BeF2-Zr Fq
2-90-8 MOLE %

  
      

MOLE %

  

 

 

400 600

800

1000

TEMPERATURE (°C)

Fig. B-2. Density~Temperature Curves for LiF-Ber-ZrF 4

1200
 

 

L]

69

ORNL -OWG - €68-841 R}

 

{mm Hg)

VAPOR PRESSURE

 

  

/

(Data from ref. 6,7,8) -
/| BeFa: Logp =10.491 - 10,953/
f [ ZiFg Logp = 13.3995 - 12,376/T
7 LiF: Logp = 30.619 - 15,450/T - 6.039 Log T
7/ 64.7 - 30.1 - 5.2 mixture: Log p = 8.803 - 9,936/T

 

 

N /I 90.0-7.5-2,5mixture: Log p = 8.940 - 11,480/T
, I,, P=mm Hg and T = °K :
/ | | _
. 17 1 1 1 1
700 800 900 1000 1100 1200 1300 1400

TEMPERATURE  (°C)

Fig. B-3. Vapor Pressure-Temperature Relationships for LiF, BeF-2, ZrF 47

and their Mixtures.

 
 

 

(°C)

TEMPERATURE

70

ORNL-DWG~68- 840 R!

 

1050

1000 |-

950

 

900

 

  
  
 

VAPOR COMPOSITION
LIF ~ 64.7 mole %
BeFq— 30.1
ZrFg~- 5.2

(CURVE CALCULATED BY CORRELATIONS OF
EQS. 3-104 & 108 PAGE 3-230, OF REF. 10)

 

] ] i 1 ] L 1

 

.022

o
023 .024 025 026 027  .028 029
VISCOSITY (centipoises) |

Fig. B-4. Calculated Viscosity of LiF-BeFZ-ZrF 4 Vapor.
 

 

oy

71

Table B-1. Latent Heat of Vaporization of LiF, BeFy, ZrF, and Their Mixtures

(Values estimated from vapor pressure data)

 

 

~ Composition cal/g=-mole
LiF 44,000
BeF, 50,400
 LiF-BeF,ZrFy (64.7-30.1-5.2 mole%) 46,2000
LiF—B_er-ZrF4 (90.0—7.5—2.5 mole%) _ 44,600°

 

ACalculated by assuming that the latent heat of each component in the
mixture is proportional to its molar composition.

‘Table B-2. Thermal Profiérti'es of MSRE Salt A

(data from Ref, 11)

 

 

Heat capacity of solid (212° to 806° F)
Heat capacity of liquid (887° to 1472°F)

Composition of Salt A Mole %

LiF 70 -

BeF, 23.6
ZrF, 5 |

- ThFy 1

UF, 0.4

. Melting point | | 840°F
Latent heat of fusion at 840°F 139 Btu/lb -

0 0.132 + 0.000433 t (°F)

0.575 - 0.0000999 t (°F)

 

 
 

 

 

72
APPENDIX C

Estimation of Pressure Drop for Salt Vapor
in the Still-Condenser System

The highest pressure in the still-condenser system during distillation is about
1 mm Hg which occurs just over the. surface of the liquid in the still. A vacuum
pump connected to the condensate receiver develops a lower pressure. in this
vessel to induce vapor flow through the condenser.. Because the ‘average pressure
in the condenser is low and the diameter is relatively large (9.25 in. D), the
possibility was foreseen that vapor could channel, resulting in incomplete conden-
sation. It was not desirable to make the condenser smaller in diameter because the
larger surface is needed for heat rejection; therefore, to avoid channeling, a core
" was placed in the condenser (Fig. C-1) to route vapor to the condenser wall,

The calculations that follow were made on the sysfem shown schematically in
Fig. C-1. They consider pressure drops for various flow rates beginning at the vapor
line opening in the still to the neck of the condensate receiver. The objective of
the calculations is to determine the annulus width that easily passes the amount of
vapor that can be condensed. In other words, the condenser-is to be made non-
channeling but with sufficient annular area that pressure drop is not the controlling
characteristic. The results indicate that a 3/4-in. annulus very nicely fulfills
these requurements, whereas a 1/2-|n. annulus l:mlts the distillation rate to about

500 em / hr.

Properties of the System

In addition to the dimensional properties of the system, the following data are
tabulated:

Vapor composition, mole %

LiF | 64.7

BeFy | 30.1

ZsF4 - 5.2
Molecular weight of vapor, g/mole - 39.66
Vapor temperature, °C 1000
Pressure in still, mm Hg 1.0
Vapor density at 1000°C, Ib/ft3 312 x 1070
Vapor viscosity at 1000°C, centipoises 0.0257
Condensate temperature, °C 600

Condensate density at 600°C, g/ cm3 | 2.17
73

'ORNL DWG. 68-852 RI

 

    

 

 

 

 

 

   
 
  

 

 

 

STILL
Y
{{ife— 2" ANNULUS
LAl
20" ||4u ‘i%*“m‘_ FEED
0.75"
" TO VACUUM
ATT5,00, CONDENSER " TPUMP
925"1.D.
CORE !
CONDENSATE
RECEIVER

Fig. C-1. Diagram of Still-Condenser System SHowing Dimensions Used in
Pressure Drop Calculation, -

 
 

 

74

The pressure drop is calculated in three steps: (1) the AP in the vapor line

from its entrance to the beginning of the core, (2) entrance loss into the annulus,

and (3) AP in the annulus. It was chosen to find the pressure drop for a conden-

sation rate of 800 ecm3 liquid per hour for a sample calculation.

 

AP in Vapor Line

_ 800 cm* cmS 2,17 g Ib

Vapor flow rate, w = 3500 sec X cm3 X ng- = 0,001063 I.b/sec

The vapor is in laminar flow so use the correlations of PerryIo Table 5-11,

hage 5-21, to find the pressure drop in the vapor line.

The weight rate of flow is

1rD4N

128 ¢
where D = diameter = 0.771 ft.

N is defined by

 

g M pRop)
N = =S \ 1 2
2zRTp | L !
where g = conversion factor = 32/17 ft-Ib/Ib force-secz,
M = molecular weight = 39.66 Ib/Ib mole,
z = compressibillty factor = 1.0,
'R = gas constant = 1,543 ft—lb/" R=1b mole,
- T. = temperature = 2292° |
p = viscosity = (0.0257) (6 72 x 10~4) = 1.73 x 10'5 Ib/ft sec,
L = average length = 1.42 fi, |
Py = upstream pressure = 1 mm Hg = 2.7845 Ib/f12,
» P2 = downstream pressure, |b/ft2 '

Using the above values, it is found that

\ | o
N=7I2( -2 | | 3)
 

 

- 75
From Eq. 1,
_ 128 w _ (128) (0.001063)

N
x D? mmmfi (4)

Using Eqgs. 3 and 4, the downstream pressure is found to be

Py = 2.7815 Ib/ft2 Z 0.9989 mm Hg. (5)

Contraction Loss Entering Annulus

The correlation given in Perry 10, Fig, 5-34, page 5-31, was used to
estimate this effect. The hydraulic diometer Dy, of the annulus is 0.125 ft;
the “equivalent” length L_ of the annular entrance is taken as one~half this
value or 0.0625 ft. The correlation term for Fig. 5-34 is

LeH
D} G

 

where G = mass flow rate in annulys = ——————— = 0,00764 Ib/sec¥ff2.
area of annulus

Other terms have been previously defined.
The value of the correlation term is

L
> = 0.00904,
DR G

 

which is used in Fig. 5-34 to determine that

 

_P2 3-1=15 S e
V29, - ) L -
“where p = vapor density = 3.12 x 10°5 Ib/f3,

V = vapor velocity in entrance = 245 ft/sec,
P2 = pressure just upstream of entrance = 2,7815 Ib/ft2
P3 = pressure after entrance losses, 1b/Fi2,

From Eq. 6, the pressure after entrance losses is
Py = 27087 Ib/ft2 < 0.9728 mm Hg. 7)

 
 

 

77

flow rates above and below this range, and the results are plotted in Fig. C-2.
Also included in the figure is a curve showing the pressure drop for an annulus
width equal to 1/2 in. For an annulus this narrow, the pressure drop in the

400 to 600 em3/hr operating range is significantly greater than for the 3/4-in.
annulus. In fact, it appears that in a 1/2=in. annulus the distillation rate might
be limited to about 550 cm3/hr. The 3/4~=in. spacing was chosen for the con-
denser design because this eliminates pressure drop as a factor in controlling
distillation rate.

 
 

ORNL DWG. 68-864 RI

 

o O -
> g o o

Pressure At Condenser Outlet (mm Hg)

o
o
T

 

  
  

3/4" Annulus

172" Annulus

Condenser Length =3 ft
Vapor. LiF -BefFy -Zr F4

64.7 30. 5.2 mole %
Still Pressure = Imm Hg
Vapor Temperature=[000°C

 

  

 

 

0
300

;400 - 500 600 700 ‘ | 800 - 900 1000 Hoo
‘ Distillation Rate {(cm3/hr at 600°C )

Fig. C-2. Distillation Rate as a Function of Pressure at Condenser Outlet.

1200

8/

 
 

©

79
APPENDIX D

Estimation of Time fo Heut'C_ondehsote' Receiver
and Feed Tank to Operating Temperature

5

The condensate receiver and feed tank are so nearly the same size and geometry
that one calculation of time~temperature characteristics is assumed to apply to both
vessels., The purpose of the calculation is to find the proper rating for heaters
attached to the outside of the vessel that permit heating from room temperature to
500°C in about 2 hr. The results of the calculation, presented above in Fig. 6,
page 17, show that a heat input of about 20 kw is required; the followmg discussion
illustrates the computahonal procedure.

Data and Computational Model

The condensate receiver, shown schematically in Fig. 7, page 18, ond detailed
in Dwg. M~12173=-CD~009 of Appendlx H, was chosen as the model for the calculation.
Elements of the model are shown in Fig, D-1. The vessel as installed is covered with
ceramic heaters that provide a uniform heat source to the vertical sides and bottom;
however, for calculational convenience it is assumed that all heat enters through the

~ vertical sides, the sides being made longer to include the heated area that would be

on the bottom. It is assumed that the vessel contains a full charge (48 liters) of salt
having the properties of MSRE Salt A (see Table B~2, Appendix B). This salt was
chosen because heat capacity and heat of fusion data are available and its composi-
tion very closely approximates that of MSRE carrier salt.

The following data are pertinent properfies of the vessel and its contents:

Vessel material L ST ‘Hastelloy N
Vessel weight, lbs S o | 125

Vessel surface areq, ft2 | R | o 16,89
Average specific heat of metal, Bty lb"] °F"] o o - 0T
Average thermal conduchv:ty of meral Bty hr~} °F"]r | 10.3

- Emissivity. of metal.. D ] o 0.5
Weight of salt {48 liters), lbs : - 235

" Melting point of salt, °C . . | ' 450
Heat of fusion, Btu/lb | ' 139
Average specific heat of solid salt (70 to 842° F) Btu lb"'.| °p-1 0,316
Average specific heat of liquid salt (842 to 932°F), Bty Ib~} °F-1 0.486

Thermal conductivity of insulation, Btu hr ft"‘ °p-1 0.1

 
 

80

ORNL DWG. 68-855

 

i SALT - | -VESSEL WALL
HEATER

 

   
      
 

EQUIVALENT
LENGTH OF
VESSEL=I.7 ft.

   

 

".............I.l..............

 

— T3in. —'I INSULATION
*—— 7.75in. ——» t=6in
e—— r, = 8.75in.

e————————— rp=14.75 in.

 

 

 

Fig. D-1. Model for Calculating Time to Heat Condensate Receiver to
Operating Temperature. |

 

 
 

©

"

Definitions

Am

e .

L
"

—

X o _x
0o 3

9,

-

81

.qh = heater outpg't, Btu/hr

heat transfer areq, ft2
emissivity
length of vessel, ft

radius to outside of heater, ft

radius to outside of insulation, ft ., |
thermal conductivity of insulation, Btu he=1 f=1 °F-1
heater temperature, °R | |

salt temperature, °R

metal temperature, °R

temperature at outside surface of i_nsuldtion, °R

time, hr |

spemf:c heat of solt Btu b1 oF-1

specnflc heat of mgfal, Bty Ib=1 °F-1

weight of salt, b

weight of metal, Ib | _ .
thermal co‘nducflvify of metal, Bty hr=1 fi=1 °F-1

coefficient of heat transfer for salt fllm, Btu hr-1 ft=2 o f~1

thickness of metal wall ft

- Heat Balance -

The oufpuf of the heaters is radiated to the vessel or is lost by conduchon
) through the lnsulahon.

2wkl T, - AR | 0
~'Intr2/r|’

¥
1
i

—0173x10'8A (Tf: 14 +
"')

 

 
 

 

 

| 82 ,
The energy received by the vessel wall is partially used to heat the metal and

partially to heat the salt inside the vessel. In a‘small time increment dO there
would be a small rise in temperature of the vessel and the salt, and we can write

=W cCd +w. c dr + TR =T) 4
ssosoomom - @

m ‘ ]"F2/r])_

Both T, and T_ are variables in this equation, and one must be eliminated before
integration. T we make the simplifying assumption that the amount of heat
going into the salt is proportional to the amount of heat going into the metal,

~ the proportionality constant is probably the ratio.of the relative conductances
of the metal and the salt film adjacent to the wall. In this case the propor=
tionality constant becomes - -

UG

k /x ' | |
m’ T - 10.3/0.0208 | |
r— = L = 24.72, - ©
¢ |
The value of h_ (= 20 Bty hr=1 ft=2 °F~1) is estimated from physical properties.

Using the value 24,72 as the proportionality between the first two ferms to
the right of the equality sign in Eq. 2, we write |

   

W C dT okl (T, -T) .
U do = ——_22._7?—‘+'Wm Cm dTm + n - @

Upon rearrangement and integration this becomes
Tl!n o . ';’:e-u '

dT
m

20kl [T, - T
@G - In (r2/r1)

®

 

 

 

 

 

o

‘The initial conditions are T, equals room temperature at time equals zero;
final conditions are T , ¢ predetermined upper limit for the temperature of the
vessel wall, and €', fl?_]e time reduired for the vessel wall to reach temperature
T’ . - 7 .

m
 

83
Time to Heat Metal Wall to 600°C

Since the metal temperature rises much faster than the bulk or "mixed"
temperature of the salt, it is necessary during this transient period to limit the
metal temperature to some reasonable value, for example, 600 to 700°C, and
hold the temperature at this value until the salt melts and heats to operating
temperature, which is taken to be 500°C. While the metal is being heated, the
relationship between metal and bulk salt temperatures can be found from the
assumption used to get the proportionality factor of Eq. 3.

 

 

oo S __amean _ 0.00477 ()
T =T~ 2472W_C_. = (24.72) (235) (0.495) ™
T = 0.00477 (Tm - To) +T. @

The value 6f C, (=0.495 Btu Ib=1 °F=1) ysed in Aqu 6isa wéighted specific
heat which inciudes in one number the effect of heating the solid, of the heat
of fusion, and of heating the liquid to 500°C.,

The left member of Eq. § contains the variables T and Ty, which are
related through Eq. 1 for any chosen heater capacity qy,; other quantities in
Eq. 1 are defined in Fig. D~1"and the paragraph titled Definitions. If we
choose a heater of 15 kw (51,195 Btu/hr) capacity and a surface temperature
for the insulation of 530°R, we obtain for Eq. 1:

(20) (0.1) (1.7) [Th - 530}

] - g
51,195 = (0,173 x 10°8) (6.89) (0.5 (T: rfn TR

 

 

51,195°= 0.596 x 10'8(7: -+ 2.046‘Th - 530) o ®

We need to use Eq. 8 to eliminate either Ty or T from Eq. 5 and then
integrate Eq. 5; however, the fourth-power relationship in Eq. 8 makes integration
of Eq. 5 difficult unless graphical methods are used. Equation 8 is plotted in
Fig. D-2; the "mixed" temperature of the salt, computed by Eq. 7, is shown on the
same plot. When values are substituted into Eq. 5, we obtain

 
 

 

ORNL DWG. 68-863 RI

 

 

 

 

 

2300 . T I . T r
2100+ -
1900 -
1700 -1540
~1500 4538
o
0
e
31300 -1536
E ——
m m
?, °
~ 1100 4534 ©
© 2
< 2
= e
900 4532 £
@
'-.
©
700 530 @
wc ] 1 1 1 ] 1
IT00 1800 I900 2000 2100 2200 2300 2400

Heoter Temperature (°R)

Fig. D-2 Temperature of Vessel Wall and Salt as a Function of Heater
Temperature (15~-kw Heater). -
 

85

Tr'n = ]57]°R | Gl- , af

 

. ! o de _ [ e 09
51,195 - 2,046 (Th'-saoj - = [ (25 oY - | a3

530°R 0 o

Wthh when integrated graphncolly with the aid of Fig. D-2, gives a value of

= 18.5 minutes. This is the time for heating the vessel to 600°C (1571°R).
Dur:ng this transient period, the "mixed" temperature of the salt has risen only
about 5°R to 535°R (~25°CQ). '

Heating Salt to 500°C While Holding Vesse'lb.Walls at 600°C

 

Choosing at this point to hold the vessel walls at 600°C by on-off control
of the heaters, we examine the mechansim for transferring heat from the heaters
through the walls and then into the salt. The rate at which heat is recenved by
the wclls, assumed fo be by radiation only, is '
ok 10PA (74 -7 ) :

m h m

The rate of heat transfer into the salt depends upon convection which is

hoA (T - 1) .

These two expressions must be equal since the wall temperature is held constant.
Therefore,

A (T -T) = 0.173 x 1078 A e(T4-T4). - (10)
mlilm s m hm . A .

In Eq. 10, T_ increases with time, and the heat transfer rate into the salt

. :drops off because of the decreasing value of (Tm - T ) At the outset this

. temperature difference is large enough to permit all radlated energy to be
conducted into the salt. However, eventually (T = T) becomes small enough
that the heater outpyt must be curtailed (through the on=off control that holds
wall temperature constant). - During the time that the large value of (T - T) |
prevails, the energy balance is ,

 
 

 

 

 

B 86
-8

0.173 x 10 A

A e (T - T4) do =W C dT.
m | h m s s s
‘Infe_grqting from the lower limits 6 and T;, respectively, the time (18.5 minutes)
and temperature (535°R) at which the metal reaches 600° C, to the upper limits
6" and T, we have '
_ : _ W _ !
o185 _ W& - T
S5 i
80 g73x 108 A . (74 -
- m | h m,

 

 

| (23’5) 0.495) \Ts - 535)
0.173 x 10°° (6.89) ©0.5) [1940)* - (157)*]

 

;‘0.00242 (T: -535} : o ()

The linear relation of Eq. 11 holds until the magnitude of (Tm - T)
decreases to the point at which convection transfer controls.. The salt temperafure
at which this oceurs is found by equating the radiation heat transfer rate to the
convection transfer rate as was done in Eq. 10, We define this temperature fo be
Te and obtain it by solving Eq. 10,

0173 x 107 e( r4, | | |
T -1 =— » T | (12)

- m

 

The value of T: is

571 - 7" = B8 x 1078 0.5 [a9a0* - as7nt]
s 20 -

 

T"- = 1222°R (406° C) o | - (13)

The elapsed time for the salt to reach 406°C is found from Eq. 'Il to be 8" = 118
| minutes.

- Above a salt temperatyre of 406° C the heat transfer rate decrecses with
time, and the time-temperature relationship is found by equating the energy
passing through the salt film to energy absorbed in the salt.
 

| 87
h A (T -T)dB=WCdT ) o (18)
cm m S , s S s .

Integration from mmal conditions 6" and T* to the desired final temperature
Tef gives

 

-Tm-T:' hCAm |
7. “wc ©-9 (13)
m sf s s

Upon substitution of numerical values Eq. 15 becomes

I 1571 - 1222 _ (20) (6.89) (e _1ng

1571 -1 of (235) (0.495) 60

 

= 1.185 (ef ---‘g}j@). ' (16)

Using Eq. 16, the time (6f) required to heat the salt to 500°C is 152 minutes.

- The relationships between time and temperatures of the heater, vessel wall,
and salt were calculated from Egs. 8, 11, 12, and 16 and are plotted on Fig. D-3.
Two curves are presented for the salt temperature, one for the vessel wall at a
constant temperature of 600° C and a second for a constant temperafure of 700°C,
The difference in time between the two cases is insignificant.

Choosing the Heater Slzes for the Condensate Receiver, Feed Tank, Still, and
Condenser

~ Condensate Receiver and Feed Tank. — The calculations discussed above
‘were repeated for heating jackets of 10 kw and 20 kw capacity around the sides
and bottom of the condensate receiver.. These data, presented previously in
Fig. 6, page 17, were used to fix the heater capacity for the condensate receiver
 and feed tank. It was chosen to heat each tank with 20-kw heaters, having the ~
distribution over the vessel surfaces specified in Paragraphs 4.6.2 and 4.6.3 of
Appendix G. Since some heat is applied to upper surfaces that are not-contacted
by salt, the heater effectiveness for heating the salt is not the total 20 kw but
perhaps about 16 kw. The required time (Fig. 6) for brmgmg the vessels to

- temperature is then clbout 140 minutes.

~ Still and Condenser. — An analysis similar to that described in this
Appendix was made for the still and condenser, giving the time versus heater -
rating curves shown in Fig. 11, page 28 . A 20-kw heater was chosen for the
condenser and a 15~kw heater for the still giving a heat-up time of about 1.5 hr.

 
 

 

 

 ORNL DWG. 68-865

 

 

   
   
 
      

 

 

i } 1 i i ' 1
1000 Heater -
800 -
o
~ 600 -
-
2 Metal Wall
o
2
E 400 -
o
-
; Salt Temporature For .
“Metal Waill Held At 600°C
700°C
200 -
0" ! ] : L » J _ 1 i 1
0 20 40 = 60 80 100 120 140 160
- Time (min.)
Fig. D=-3. Temperature-Time Curves for Heating Up the Condensate Receiver with a 15-kw Heater,

88

 
 

 

W)

.

89

~ Calculations for the still-condenser system were straightforward since it was not nec-

essary to consider heating and melting a mass of salt. The small volume (12 liters) of
salt that might be in the still was included in the weight of the metal thus simplifying

the calculations. '

 
 

 

 

 

. 90
APPENDIX E -

Estimation of Heat Rejection Rate by Condenser

The condenser is designed to reject heat by conduction through the insulation and
convection to the' atmosphere. This characteristic was chosen for the design since it.
offers the simplest and most economical cooling method. . More efficient methods, such
as forced circulation of an inert gas or liquid metal, were evaluated and found to re-
quire a significant investment in circulating plus auxiliary heating and cooling equip-
ment. -

The following calculations illustrate the straightforward approach to finding the
heat rejection capability of the condenser. A 3-ft length was chosen for the calcu~-
lations since this was estimated to be the effective length of a unit that would fit the
available space; the actual condenser length of the completed design is 51 in.

- Independent variables in the condenser wall temperature and insulation thickness.
The object of the computations is to find the most suitable combination of these
variables for the desired distillation rate; results for condensing MSRE carrier salt and
pure LiF are presented in Fig. 10, page 26. For 4=in.~thick insulation and wall
temperatures between 600 and 850°C, the 3-ft length of 10~in.~OD condenser can
dissipate 5000 to 7000 Btu/hr; this is equivalent to condensing 500 to 600 cm3/hr of

-MSRE carrier salt. A 4~in. thickness is specified for the insulation on the installed
unit; this may be increased or decreased with little inconvenience if operating
experience does not agree closely enough with calculations.

Model for the Calculation

Heat given up by condensing salt inside the condenser must pass across an air gap
to the heater, through the heater, and then through the insulation to the surroundings
as diagrammed in Fig. E-1. The heater is used to heat the condenser from room
temperature to the desired condensation temperature. Once thermal equilibrium is
established, the heat of condensation maintains the unit on temperature, For this
calculation it is assumed that heat is radiated from the condenser to the heater and
then passes by conduction through the heater and surrounding insulation before being
dissipated to the atmosphere by convection and radiation.

Definitions .

In addition to the dimensions shown on Fig. E~1, the following terms are defined:

q = heat transfer rate, Btu/hr
 

 

INSULATION

Thermal Conductivity Of Insulation
Thermal Conductivity Of Heater

Figo E-lo

21

ORNL DWG.68-859 RI

 

0.1 Btu/ft hr.°F
8 Btu/ft hr.°F

Cross Section of Condenser, Heater and Insulation.

 
 

 

 

92

A = area normal to heat flow, ft2

T = temperafure; °.R. |

k = thermal conductivity, Btu ft~' he! oR!

€ = emissivity

L = length, ft

‘r ='radius, ft |

hc = convective heat transfer coefficient to surroundihgs, Btu .P-\l;_l 52—2 °_Fl-]
h-r = radiative heat transferrcoefficienf to surroundings, Btu hr ~ ft = °F

Subscript 1 refers to conditions at condenser surface
Subscript 2 refers to conditions in heater

Subscript 3 refers to conditions in insulation

Subscript 4 refers to conditions at outer surface of insulation

Subscript 5 refers to conditions of surroundings

Heat Balance

In the closed confines of the insulated system heat transfer from the condenser
surface to the ceramic heater should be almost entirely by radiation. For this the
rate is given by |

t

qy = 0.173 x 1078 A, e iTA' - IR ()

Cpnduction through the heater is

| 92 | 'In(ra/rz) :

Conduction through the insulation is
T - T |
ookt T Ty ®
B~ T Inly/r) | |

 
 

 

L}l

%)

®

93

Radiation plus convection from the outer surface of the insulation is

_ ! Voot -
%= ZuryLih +hi (T, 15}. (4)

Solutions to Equations

Equations 2,3, and 4 are linear in temperature and are conveniently handled
by determinants. To simplify the writing we define constants a.. and express Eqgs.
2,3, and 4 as follows: ' -

T

ayTg = a1 T3 ¥ a3 Ty = ay (5)
91 T2 * 92 T3 = 93 T4 = %3 . (©)
ag Tyt agp Ta +aga Ty =gy + ag5 T 7)
In these equations
2k, L - - ,
an = o2 = T | ®
| 2k, L. I |
Unn = Qnn = == S . ‘ ' . )
22~ “23 " Tn(ry/ry) . .
daq = 2n r4L.(hc .+ hr), _ | . . . (10)_ |
013 S99 9% =0 AL

| When thermal equilibrium is'establishqd; qy =qp = q3 = 9y and Eqgs. 5, 6,
and 7 can be solved simultaneously. The convenient quantity to obtain is Ty, since
this temperature is needed to find the radiation rate from the condenser. The

. solution is

_929%2%3 " 93 %2%3 " 9 * %375 129

T2 A,y Onm Oa.
- “11 722 733

 
 

 

 

 

94
q 9 9 | | . -
=2+3+4+T5. | - o - (12)
M %2 s ‘
- Since each of the q's is equal to q;,
_o oo I
e Yoo T s | - 9

\°1 %2 %33

In Eq. 13 the desired quantity is qy, the heat that can be rejected by the condenser.
Therefore Eq. 13 can be used to eliminate Ty from Eq. 1 to obtain an expression in
which qy is the dependent variable. This gives

 

 

/ | V0 a -
RN sllg ety —10—-=1
j S, 0173x 10 A e

In this equation, Ty, the temperature of the condenser wall, is the independent
variable; Tg is the temperature of the atmosphere surrounding the unit. |

Presentation of Resulis

Equation 14 was used to calculate the rate of heat loss from the condenser for
several values of the wall temperature; these results are given in Fig. 10, page 26.
Insulation thickness, which affects the constants agg and agq, Was treated as a
parameter over the range 3 to 4 in. to completely cover the range of interest for
this experiment. The rate of condensation is greater at the higher condenser temp-
eratures because the larger temperature drop between condenser and surroundings
causes more heat to flow. On the other hand, a higher condensate temperature
implies a higher vapor pressure, which is undesirable from the viewpoint of salt
mist migrating into the vacuum system. | | |
 

 

95
APPENDIX F

Stress Analysis of Vacuum Still and Condenser*
The stress analysis was made to comply with the intent of the ASME Boiler and
Pressure Vessel Code, 12 Section VIIl. This analysis examines all areas of antic-

ipated stress concentration due to external pressure (internal pressure = 0.5 mm Hg),
nozzle penetrations, weight of vessel plus contents, and thermal effects.

Allowable External Pressure for Elliptical Head

ORNL DWG. 68-9088

 

Design data reference: Paragraph UA 4, Section VIII of ASME Pressure Vessel
Code, 1965 edition.

The design pressure for elliptical heads shall be 1.67 x operating pressure.
Design Pressure = (1.67) (15) = 25 psi.  See paragraph UG-33, (1).

Required thickness of elliptical head (1):

_ _PDK - e |2+ [B)2
' = ZE-0.2p where K = (V6) [“ (EF) }
whereh?-lg,

ID_ 14,

h = Z -7 in 7’=;I3.5 in.,

 

*Work performed by C. A. Hahs, General Engineering Division.

 
 

 

 

96

 

 

 

2 2
- K= (/8 [2 + %) } = (1/6) [2 + (7%;'-3-)-) ] = 1.0,
Lo PDK _ 25(14) (1) _ 0.251 in. Maximum |
= 2SE-0.2P 2 (700) (1)-0.2 25) N

Actual thickness (t;) = 0.375 in.
Theoretical Stress (Sy1,):

s = PDK + 0.2Pt _25(14) (1.0) + 0.2 (25) (0.3?5) _
“th 2 Et 2 (1) (.375)

Allowable internal pressure (P;)):

2 SEt _ 2 (700) (1) (.375)

v “KD + 0.2t _ 1.0 (14) + 0.2 (0.375) 37.3 psi.

p
Allowable external pressure = %773 = 22.4 psi,

Actual maximum external pressure = 15 psi.

Thickness of head is satisfactory.

Allowable External Pressure and Reinforcement for 1 1/2~in. Sched. 40 Pipe Nozzle

| I/2 in. Sch 40 Pipe

Elliptical
Head

 

470 psi.

ORNL DWG. 68-9089
 

 

97

_ 0.145°
P -0555(3) = 0,55 x 19.7 x 10 (1920) 4580 psi

all
For value of E, see Appendix A, Table'A-4.
Required thickness of ellipfic_dl head'tr' = 0.251 in. (See page 96).

Required thickness of nozzle b

- ]5(1 590)
PR 2 _=1500.795) _ 11.92 .. 51725 in
rm  SE-0.6P 700 (1)-0.6 (15) =~ 700-9 TTeeT Tt ’

Area reinforcement required = (d) (‘tr) = (1.590) (0.251) = 0.399 in.2

i

Area reinforcement available = Al' = (E1 't-'tr)‘ (d) [('I) (0.375)-0.251] (1.880)

n

(0.124) (1.880) =.0.233 in.2

(t - ) (51)

Vg

I

(0.145 ~ 0.01725) (5) (0.375)

i

- (0.1277) (5) (0.375) = 0,238 in.2

n

Total reinforcement cn)ailablei A1 '+ A2-= 0.471 in.2

Reinforcement is ddequate. |

 
 

 

 

 

98 | | - U

Allowable External Pressure and Reinforcement for.1/2-in.-OD x 3/16~in.-1D Tube

ORNL DWG. 68-9090

 
  

— Elliptical
Head |

0.147)3

P allowable = 0.55¢ (1] 0.500

6
0.55 x 19.7 x 10 (

10.8 x 10° (0.294)°

10.8 x 10° (0.0254) = 0.275 x 10 psi.

Required thickness of elliptical head = fr = 0.251 in. (See page 96).

Required thickness of nozzle (tm):

__PR___ 15(0.103 1545
o = SE-0.6P 700 (1-0.6(15) o1 0022 in.

 

Area of reinforcement required = A = (d) (tr)
= (0.207) (0.251) = 0.052 in.2

Area Available (A:) :7

A:_ = (E;t - *r) (rn + 1) (2)
 

 

 

99
(1 x 0.375 - 0.251) (0.146 + 0.375) (2)

(0.124) (0.521) (2) = 0.129 in.2

Therefore, reinforcement is adequate.

Stresses and Collapsing Pressure for Sides of Still
ORNL DWG. 68-9091

 

 

 

 

 

 

$

'

v

N
TS

 

 

 

L————- 14 in.————= j+=—3/8 in.

Stresses Sy and S, were calculated by the method of Case 1, Page 268 of Roark 13

~

_ P

_ 15 (7.187)
2

0.365

S = 295 psi

13 -~

S

= 147.5 psi

N

) t

The collapsing pressuré may be evaluated from Eq. 8.26, page 144, of the
text by Brownell and Young. 14 This equation is developed for design of long,
thin cylindrical vessels operating under external pressure. A factor of safety of
4 may be applied to the theoretical value. Equation 8.26 includes this safety factor
of 4. _ : o '
- . 3
P allowable = 0.55E (t/d)3 = 0.55 x 19.7 «x 106 0.979 % _ 192 psi.
| \ | | 14,375
Note that this value provides a factor of safety against collapse of 12.8 based on
an external design pressure of 15 psi.

 
 

 

 

100

‘Wall Thickness and Reinforcement for Feed Nozzle

._..| I..;.3/8 in. ORNL DWG. 68-9092

NSNS )

  

    

I/2 in. Sch 40 Pipe

  

Qutside of Still

SN IINTS

Shell thickness required (t,):

PR _ 15 (7.010) _105.1 _ )
N = SE-0.6P ~ 700 (1)-0.6 (15) 691 0.152 in.

Actual thickness = 0.375 in.
Nozzle thickness required {t_):

, PR 15 (0.311 + 0.010)

m  SE-0.6P _ 700 (1)-0.6 (15) = 0.00697 in.
Actual thickness = 0.109 in.
Area of reinforcement required (A):

A= () () = (0.642) (0.152) = 0.0976 in.2

Area reinforcement available:

f

A= (E]t - fr)d | [(1) (0.365) - 0.152] (0.642)

10.213 (0.642) = 0.1366 in.2
 

 

t:

PO 15 (14) 210

101
Reinforcement is adequate.

Author's note:
Since Mr. Hohs made this calculation, a design change made the feed

nozzle 1 in. OD x 3/4 in. ID.

Thickness of Conical Bottom of Annulus

ORNL DWG. 68-9093

r———zin——-l———aasm.—-l

     
 

3/8 in.

Outside Wall
of Still

3/8in.

Vapor Line to
Condenser

 

Required thickness of head (See Par. UG 32-9, Section 8, of ASME Boiler
and Pressure Vessel Code): - -

Assume half apex angle is 30°.

= 0,175 in.

 

2 Cos 30° (SE - 0.6P) = 2Cos 30° (700-0.6(15) - 2(0.866) (700-9)

 
 

 

 

 

 

102 , | :
Assume external pressure = (1.67) (design pressure) = (1.67) (15) = 25 psi,

_PD 25 (14) _ 350 - 0.295 in.

' = 2Cos 30° (SE - 0.6P)  2Cos 30° (700 - 0.6 (25) 2 (0.866) (685)

 

Actual thickness = 0.375 in.

Allowable External Pressure on Condenser

ORNL DWG. 68-9094

 

Reference: Process Equipment Design, p. 142, by Brownell & Young. 14
Allowable pressure P for long cylindrical vessels operating under external

pressure may be calculated with a factor of safety of 4 applied to Eq. 8,25
giving the following:

| 3
P allowable = 0.55 E (T)L)

= 0.55 (19.7 x 106) (g—%—g-) = 642 psi.

Note: The maximum external operating pressure is 15 psi.

) _ PR _ 15(4.635) _ .
Maximum hoop stress = = T To0395 ]85.4 psi

- Thickness of condenser shell is therefore adequate.
 

 

103
Allowable External Pressure and Reinforcement for Sample Line

ORNL DWG, 68-9095

- | 1/2in. Sch 40 Pipe

1.900in. O.D.
1.610 in. I,D.
0.145in. Wall

 
    

e oo L

     
 

  

375 in:

Condenser...’/
Walil

 

B o S OS———2—

 

Dimensions normal to condenser surface:

1.900

;M_cx'imum _opening = C—o-s-—é-b—o = 2.1 95 ;i-fl.

1.61 0 o

~Minimum opening = Tos 30° 1,854 iin.

Allowable external pressure - P ¢ -

113 o In va 3
| Caerre BN _agr woang o ané. [0:145)

= 0.55 x 19.7 x 106 (0.0755)3

 
 

 

 

104 .
= 0.55 x 19.7 x 10© (0.00423) = 4660 psi
Nozzle Reinforcement Requirements:
Reinforcement calculations will be rfiude cfisuming the nozzle passes rthrough

" the shell af right angles. The nozzle wall thickness remains 0.145 in.; however,
an OD of 2,195 in. and ID of 1.854 in. is used in the calculations.

 

 

 

 

o 15 (9 250) |
_ R 3 _69.4 _ .
Shell t = SE-0.6p “700 - 0.6 (15 ~ &1 0.100 in.
Nosgle = __PRn _15(1.854/2) _ 1500.927) _ o 0007 10
oNezzle T SE<0.6P 700- 0.6 (15 . 6é91

Area of reinforcement required = di = 1.854 (0.100) = 0.1854 in.2

Al

i

area available

(E,t-t)d = (0.375 - O, 10) 1.610 = 0.275 (1.610) = 0.443 in.2 ¢

No additional area calculation is shown since A] is sufficient.

Stress Imposed by Dead Weight of Vessel

The following calculations are made to ensure that the structural design of
the vessel is sufficient to allow it to be supported as shown on page 107.

Weight Calculations of Still Components:

Area 8-1/4 in. diam = = (8.25)2/4 = 53.456 in.2
Area 8 in. diam = n (64)/4 = 50,265
. Difference = 3.191 in.

Weight of 8-1/4 in. OD x 8 in. ID Cyl. = 3.191 in2 x .317 Ib/ta. 3 =. 1.011bfin.
Area of 10 in. OD Cyl =x (102/4 -~ =78.54in.2

Area of 9-1/4 in. ID Cyl. = = (9.25) /4 = 67.20
leference = T1.34 in.2

Ll

»

Weight of 10 in. OD x 9-1/4 in. ID Cyl. = 11.34 in.2 x .317 Ib/in.3 = 3.595 Ib/in. -

Weight of heaters on éondenser wall = 75 Ilb.
 

 

105

Weight of insulation on condenser wall = 45 |b,
Combined we_ight of heaters and insulation = (—7%7—%?-?& = 2.56 |b/in.

Assume salt deposit on condenser wall = 0;335 Ib/in.

Total combined weight of condenser shell, inner shell, heater, and insulation
= 7.5 Ib/in. | |
Blank from which elliptical head is made may be 22.25 in. ID.

Weight of top cylindrical section 14 in. ID x 14.75 in. OD x 7.5 in. long:

Area 14.75 in. diam. = 170.874 in.2

Area 14 in. diam = 153.938
Net Area = 16.936 in.2

Weight = 16.936 in.2 x 7.5 in. x 0.317 Ib/in.3 = 40.3 Ib.

Weight of conical section:

ORNL DWG. 68-9096

&
o
M
| ©

K

  

Volume of conical section = w (11.187) (4.375) (0.375) = 57.65 in.3
Weight = 57.65 in.3 x .317 Ib/in.3 = 18.55 Ib.

 
 

 

 

106
Weight of vapor line:
'ORNL DWG. 68-9097

 

 

LIS 3/8in,—=

 

/Qo.n.x 9 1/4in. 1.0,

Area 10 in. diam = 78.540 in.2
Area 9-1/4 in. diam = 67.200 in.2
11.340 in.2

Weight = 11.34 x 16.375 x 0.317 = 58.8 |Ib

Additional weight:

Weight of heater equipment = 50 b

Weight of insulation = 90 |b
Weight of salt = 18 |b
158 Ib

Total weight of top section of still:

Weight total = 46,2 + 40.3 + 57.65 + 58.8 + 158.0
= 360.95 |b
 

 

| 107
Method of Support for Still and Forces Active on the Still:

ORNL DWG. 68-9098

47 - ~Wt=2360.95 Ib

 

 

 

o fWi= 7.5 1b/in.

 

 

 

 

 

 

 

8 3/8 in— _ 51 1/4 in, ——————n
Ro | |

b 3611

p ' | 7.51b/in.

 

 

 

 

b
b——— 59 s/8 m.——_—-’

 

RI + R2 = 361 Ib + 51.25 (7.5)

=361 © + 384.5 = 745.5 |b

 

2Mp =0
TN
59.625 R, = 51.250(361) + .'(5'2'25) (384.5)
59.625 R, = 18500 + 9,850
f R, = 28,350 = 475 Ib

59.625
R] = 745.5 - 475 = 270.5 Ib

 
 

1

108

360 Ib

Stresses and Moments in Condenser Shell:

ORNL DWG. 68-9099

 

 

a

 

t475.5lb

 

- 7.51b/in.

 

| |
2701b

 

 

 

 

—l 8.3750n.

 

2701b

 

 

 

~— 23.

LM,

 

575 in.—>

866 - 5420 + 11,160

4874 in.~-1b

- (7.5) (15.2) (7.6) - (361) (15) + (475) (23.575)

| = moment of inertia for 10 in. OD x 9.25 in. ID condenser

| T el
z R

; Stress Sb

- v =3 [0 - we25]

= % (625-455) = % (170) = 133.5 in4

=-—I— = TB—3-.-5_— = ]82.5 psi
 

 

 

109
Hoop Stress = 185.4 psi (See page 102)

Methed of support is sahsfactory.

| Thermal Stress Calculation

At across wall of still = 5°C o

At of 5°C ~ 10°F .

Still temperature = 1832°F, |

Coefficient of thermal expansion at 1832°F = 8.85 x 1076 in./in.~°F
- (See Appendlx A, Table A-6),

Modulus of elasticity at 1832° F=19.7 x 108 Ib/in.2

_AtaE 1ox885x10-6 197x106_ :
St =0 = 3 (1-0.33) w = 1320 psi.

The maximum principal stress of 367 ? psi is the combined bending
stress, 182.5 psi, as shown on page 108 and the hoop stress, 185.4 psi, as
- shown on page 102,

It should be noted here that the sum of the principal stress, 367.9 psi,

- and the maximum thermal stress, 1320 psi, is 1688 psi, which is 38 psi more
than the stress rupture value of 1650 psi shown on Fig. 15. Since the thermal
stress is self-relieving, these values are sufficient, -

Additional test data will be ebtaihed in the nonradioactive experiments,
and the "used” physical condition of the still will be studied before this
equipment is used for a radioactive salt experiment.

- ‘Minimum Thickness of Flat Head on Feed Tank

| Reference Paragraph 34-C-2 , P ?e 19 Section VIII of ASME Boiler and
Pressure Vessel Code, 12 o

. Mlmmum thlckness of flat heods (t)

" 0perahng temperature of vessel = 500°C or 923°

t.=dVCcp/s

- C= 0.4 See (e) page 21, Sechon 8 of the above reference
'd = ID of shell

 
 

 

 

110

S = maximum allowable stress

= 17,000 psi at 1000°F

_ /0405 _ | 6 _ -4
t=15\Fo0- = YViseos - PV x 10

]

115 (0.01876) = 0.282 in.

Actual thickness = 0.375 in.

" *Thickness of head is satisfactory.
 

 

SO
APPENDIX G

SPECIFICATIONS FOR HEATERS FOR VACUUM
DISTILLATION EXPERIMENT FOR FLUORIDE SALTS

1.0 Scope

1.1

1.2

General

These specifications (identified as Specification No. CT=63, October 31,
1966) state the requirements for several electric heaters to be mounted on
vessels described by the following drawings. These drawings are component
parts of these specifications: -

References (see Appendik H for first four draw‘ings listed).

Drawing Number

M-12173-CD-009-D Condensate Recéwér — Assembly and Details
M=-12173-CD-011-D  Vacuum Still and Condenser Assembly

- M=12173-CD-013-D Feed Tank for Vacuum Still

M-12173-CD-014-D  Sample Reservoir and Thermocouple Well Details
ORNL DWG. 68-866 Coil Location Within Heating Element

2,0 Codes and Standards

~ The latest revisions of the following Codes and Standards shall apply to these
~ specifications: ASA, NEMA, and ASTM.

3.0 Type of Service o

-3.1

Te’mperature and Operdti'cm

The vessels on whlch the heaters are placed will be required to operate at

temperatures as high as 1000°C for extended periods of time. Also during

the course of the experimental program the heaters will undergo cyclic

 operation between room temperature to 1000° C at a frequency of one cycle

3.2

per day. The heater shall be designed for a lifetime of at least 5,000 hr.
Vessels |

All vessels will be fabricated of Hastelloy N for which the mean coefficient
of thermal expansion may be taken as 8.85 x 1076 in./in.~°F between

 
 

 

 

 

v

1/8min> le—

'

 

 

 

 

 

Heli-Arc
Weld

Figo G- ] .

178" min.—

e—1/8"min.

   

nz

" ORNL DWG.68-866

   

 

 

 

 

 

Coil

 

 

 

\—|/4" To 172" Long
Cross Bar

Typical Splice
Full Penetration
Weld - Ground Flush

Coil Location within Heating Element.

 

 

*
 

3.3

70 and 1800°F.

113

Radiation

The h-eaters_' will not be dsed in service that will cause radiation damage.

4.0 Specifications

4.1

4.2

4.3

Mechanical Features

(o) T'he'heahng elements shall be imbedded (totally enclosed) in a
thermally conductive refractory material. In general, the total
number of heaters should be kept as low as practicable.

(b) The heaters will be supported by and on the vessels by the Company (UCNC)
~and shall be of the .type that can be removed and replaced without
disturbing the vessel or any nozzles on the vessel. Direct access to
the vessels may be assumed for removal and replacement of heaters.
Heaters shall be designed for 1/4 + 1/8 in. clearance of vessel walls and
surfaces to allow space for thermocouple leads and to supply heat
uniformly over these surfaces within the limitations allowed by nozzles
and supports. |

(c) The vessels are equupped with various nozzles which will be maintained
at temperature as requured by heaters suppl ied by the Company

Heat Capacnty
Heat capacity of the heaters shall not be greater than 1 cal/g° C.
Electrical Accessories

The manufacturer is not required to furnish any power supply or control

""equipment. These will be furnished by the C{SmPC'"Y'

4.4

Thermal Insulation

. The manufacturer is not required to furnish thermal insulation.

4.5

'Elect_ricol Requirements

(@) Available power is 230 v, single-phase, 60-cycle alternating current.

- (b) . The manufacturer shall specify the power rating of each heater.

 
 

 

 

 

114

4.6 Geometrical Considerations

~ 4,6.1  Still and Considerations

4.6.2

4.6.3

(@) The markings on this drawing indicate the zonal heat requirements.
Total heat input to the still section is 15 kw; this rating may be
increased for manufacturing convenience by as much as 15% but
no decrease will be allowed. The top of the still shall have a
heat input of 4 kw; the remaining 11 kw shall be applied to the
sides. Heaters for the top section shall conform to the geometry of
the dome-shaped top. - When the still is operating at a temperature
of 1000°C the maximum loss rate to the surroundings of 1.5 kw may
be assumed. |

(b) Total heat input to the condenser section is 20 kw with a 15%
increase being allowed if needed for manufacturing convenience.
~ This total requirement is to be divided into three approximately
equal zones as shown on the drawing. When the condenser temp-
erature is 1000° C, the maximum heat reqmremenf including losses
to the surroundmgs wnll be '|0 kw.

Condensate Receiver, Drawing No. M=12173-CD-009-D.

This vessel will be heated along its bottom, vertical sides, and top.

A total heat input of 20 kw is required with a 15% overage being
allowed. The heat input is to be distributed over the vessel as follows:
approximately 30% on the bottom, 50% on the sides, and 20% on the
top. When the vessel is at a temperature of 1000°C, the maximum heat
requirement including losses to the surroundings will be 3 kw.

Feed Tank, Drawing No. M-12173-CD-013-D.

This vessel will be heated along its bottom, vertical sides, and top. A total
heat input of 20 kw is required with a 15% overage being allowed. The heat
input is to be distributed over the vessel as follows: approximately 30% on

~ the bottom, 50% on the sides, and 20% on the top. When the vessel is at a

temperature of 1000°C, the maximum heat requnrement including losses to the |
surroundings will be 3 kw. '

4.7 Special Features

(c) Terminal leads shall be at least 3 ft long and shall have a cross-sechonal

area more than twice that of the heater element and shall not be less than

No. 14 AWG.,
 

b))

(c)

115

Terminal leod wires shall be imbedded a minimum length of 1 in. into the
ceramic refractory and shall have a cross bar as shown on the accompanying
Fig. G-1. \

All weld joints shall be heli-arc welded mcludmg splices in the terminal
lead wires.

5.0 Inspection and Test

5.1

Visual |
Visual inspection shall be made to determme fhat
(a) the ceramic ;s not_ ‘cracked or_broken,

(b) the ceramic is not swelled or warped, and

~ (c) the terminal lead wires do not move or rotate in the ceramic.

5.2

5.3

Liquid Penetranf

quwd penetrant (dye check) inspect all terminal lead splice welds
and remove or repair all dye indications.

Radiography - :
Each completed unit shqll be 100% radlographed to establish that:

(a) _.‘the heotmg element has a minimum spacing of 1/8 in.;

- (b) a minimum clearance of 1/8 in. is maintained between the heating

54

5.5

element and surface of the refractory;

(c) the terminal leads are imbedded a minimum length of 1 in. in the

refractory;

- {d) Exposed rodlogmphs sha|| be shlpped wnth the heahng elements.

Electrical Test

. The electrlcal resistance of each h'eating‘ element shall be measured,
" recorded, and compared with the design resistance. The resistance

shall be measured at room temperatyre.

VObservahon of Tests

The tests descrlbed in th;s section shall be performed by the manufacturer
at the manufacturer's plant prior to shipment. The manufacturer shall

notify the Company at least five working days prior to start of tests so

that a representative may be. present to witness the tests,

 
 

 

 

116
~ APPENDIX i|-|

Equn pment Drawings

The following eqmpmenf drawings are included in this Appendlx ‘Each

drawing bears the primary title MSRE Distillation Experlment drawing numbers and

 

subtitles are as follows:

- -M-12173-CD-009-D  Condensate Receiver Assembly and details.
-M-12173-CD-010-D Installation of equipment and piping in Supportmg Frame.

M-12173-CD-011-D  Vacuum Still and Condenser Assembly. -

-F=12173-€CD-012-D Flowsheet for Vacuum Dlstlllqhon of Molten Salt Reactor

Fuel (Hood Experiment)
M-12173-CD-013-D Feed Tank for Vacuum Still.

- M=-12173-CD-014-D  Sample Reservoir and Thermoco.uple Well Details.

M-12173-CD-015-D  Lliquid N Cold Trap for Vacuum Line.

--M=12173-CD-016-D  Equipment Support Frame.

M=12173-CD-017-D  Temporary Vessel Support (for Transporfmg)
F-12173-CD-018-D Flowsheet for Vacuum Distillation MSRE Fuel Salt

(Radioactive Experiment).

- M=12173-CD-019-D  Location of Points for Dimensional and Radiographic

‘Measurements on Still and Condenser Assembly.
M-12173-CD-020-D  Tabulation of Data from Dimensional and Radiographic
Measurements on Still and Condenser Assembly.

M-12173-CD-021-D  Location of Points for Linear Measurements and Tabulation

of Data for Still = Condenser - Assembly.

Drawings M-12173-CD-020-D and M-12173-CD-021-D as presented herein
contain a complete tabulation of the data recorded immediately after construction

* of the still assembly. These data are to be compared with similar measurements made

after the still has been operated at temperatures up to 1000° C for extended periods
of time. This second set of data will not be available before publication of this

~ report and cannot be included herein. However, when the measurements and

observations are made, the results will be recorded on a revision of these drawings for
a permanent record.

The following drawingsare referenced but are not included in this Appendix.
Each drawing bears the primary title MSRE Distillation Experiment; drawing numbers
and subtitles are as follows:

 

- §-20794-EB-137-D High-Density Concrete Shleld Plug Plan and Sections.

$~20794-EB-138-D High-Density Concrete Shield Plug Enlarged Plan and
o Sections.
S-20794-EB-139-D High=Density Concrete Shield Plug Lifting Hook Details
and Sections.

E-20794-ED-155-D  Electrical-Vacuum Distillation Experiment.
 

 

117

 

 

 

 

 

 

 

 

 

  

 

 

 

BAsK PLATE,

 

 

 

 

 

b

e

PARTIAL ELEVATION

 

 

] [Cowumes Cone & Somamars Yo %o o 75 Prm | 3067 Lt o] THEL

 

 

no,

JNWhesler
[~ DESIGNED |

— S

 

 

REVISIONS

DATE |APPD| APPD

 

 

 

 

APPROVED - TE

RaaE . ans

 

 

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TYPICAL LEG DETAIL :ssg MBLY ‘ . ” j{ ] ) ’
INSP‘CTION OF WELDE JOINING LEGS TO VESSEL Scale,- IE"'I, . %“O-D. x.o42.WAL'I. TURE . @
REQUIRES ONLY DYE PENETRANT CHECK OF —_—r u__l =
FIRSY Pass 8 LasT pass. No iNnsPrcTiOoN )
REGQUIRED ON WELDS JOINING BASE PLATES 10 , Maxs From /"-Dia Rop
LEGS ’ E::Evc.zf;;:ozzus Drite THey For Suir Fit |
| Wity F/a" 1A Tuse
QENERAL NOTES £ "B’ ADAPTER
L ALL MATERIAL TO BE HAsTELLOY N ! _lPeauirERD
Scace: "
2 WHEN REFERENCE 18 MADE TO ANY  NATIONALLY Actl‘P'rID ST?NDAI.D ertul;:el F
OR €ODL, THE LATEST REVIson ArPuiss. ASME cbor cass 1270N &1273
; REFERENCE DRAWINGS NO.
3.DesicN conDITIONS; ' L OAX RIDGE NATIONAL LABORATORY
DemicN Temperature - 350°C

 

  

7 /—J"RAD

 

 

" |"SeH 40 prPE

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

DesiaN prassunrs 0.5 mmHg
VESSEL HYDROSTATIC TEST 45 PSIO SegnNote €
VESSEL FREON TEST 1o PsIG ‘

4. MaTERIAL SPECS PER MET-RM=-2, MET-RM"4,; MET-RM-G, MET-RM-B-lc7,
MET-RM-B 334 & MET"RM-B 336 ‘

5.FasricaTion ; Wewping = ORNL cracs_PS'EL, PS-25 & P8-26
INsPeEcTioON - ORNL spec MET-WR - 200 scu “R"
G, ASSIMBLE WiTH sTILL B conpenstr unT (Dwa M-12173-CD-Oll*D) & makz
45 PSIG HyorostaTic & (O PSIG FRYON TESTS ON cOMBINED ASSEIMBLY

 

 

 

 

 

 

 

  

 

 

 

 

 

 

 

 

 

 

 

 

 

OPERATED BY
UniON CARBIDE NUCLEAR COMPANY
DIVISION OF UNION CARBIDE CORPORATION
OAK RIDGE, TENNESSEE

 

 

LINITS ON

mumgmh UNLESS

o Vig"
FRACTIONS & /-

DECMALS + .. —T
ANailES +_ O™DOQ'

 

MSRE DISTILLATION EXPERIMENT B3, 781

 

CONDENSATE RECEIVER
ASSEMBLY & DETAILLS

 

 

—— PR

   

 

 

scM.::NoTln

 

vl

 

 

 

 

L1 X Tartar. ool BBt
oty M-12175

 

 

 
 

é-4"

"T*NEEDLE VALVE WITH
wilD ENDS

i Fir, mtfi‘&; TNSPRCT SHADRD PORTIONS QOF PIPING .
B vawvi . i syop.’ Sex Note.§ Dwa MI2I73-CD-

110+ D PR EPLaILICATIONS.

_REFERENCE DRAWINGS .
OAX RIDGE NATIONAL LABORATORY
__ OPERATED BY '
UnioN CARBIDE NUCLEAR COMPANY
DIVISION OF - UNION" CARBIDE OORPORATION

‘, "[Mske. DisTIEEATION _
onows B INSTALLATION OF EQUIPMINT
bee £ T BEPIPING IAC BURPORTING. FRAME

AQLES x__ T

 

 

 
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119

 

 

 

 

 

 

 

 

    
 

 

 

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REFERENCE DRAWINGS

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OAK RIDGE NATIONAL LABORATORY
OPERATED BY

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UNION CARBIDE NUCLEAR COMPANY
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MSRE DISTILLATION EXPERIMENT

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Oax RipaE NATIONAL LABORATORY
OPERATED BY

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OAK RIDGE NATIONAL LABORATORY

OPERATED BY

UNiON CARBIDE NUCLEAR COMPANY
DIVISION OF UNION CARBIDE CORPORATION

OAK RIDGE, TENNESSEE

 

 

LIMITS ON DIMENSIONS UNLESS
OTHERWISE SPECIED:

FraciONS & Y32
DECIMALS £..Q05"
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0AX RIDGE NATIONAL LABORATORY
OPERATED BY

UnioN CARBIDE NUCLEAR COMPANY
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OAK RIDGE NATIONAL LABORATORY
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UNON CARBIDE NUCLEAR COMPANY
DIVISION OF UNION CARBIDE CORPORATION
OAK RIDGE, TENNESSEE

 

 

 

 

 

 

 

 

 

 

 

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§. Paintings All mild steel parts shall bs free of scale,
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SUPPQORT FRAMI h : -, cD-Qleé-n
REFERENCE DRAWINGS ‘ NO.
Oax RIDGE NANONAL LABORATORY
OPTRATED BY
Union CARBIDE NUCLEAR COMPANY

DMVISION OF UNION CARBIDE CORPORATION
OAX RIDGE, TENNESSEL

 

 

 

 

 

 

 

 

 

LTS on DMERSONY UMESS | MSRE DISTILLATION EXPERIMENT SSu it
OTHERWISE SPECIPIED: ) . LB
macnows & . Y32[ TEMPORARY VESSEL SUPPORY
DATE [AP#D] APPD : ' (FOR TRANSP :
- DECIMALS & e ASSEMBUY & DETALS . .
oy 2o — :
ot 3l PRI a-12175. [eojoiz D]

 

 

 

 

 

 

 
 

i"""IG Ga Coppan

Nz FEED

&--- A ' X19GA"

SUL T fediin S S RooT PEREL LY
Sair vor w J2.0
DIAMO.D. * M N g o
Heiawr  * [6in g5
Orsn_pPrsas® 0.5 :
OptR TEMP =
ELc HEAT B )5 KW
Disr RATE 0
INsuLTHR & BN

4 |60 A kL

Ling HEAT
1350 Warrs -
CanrooTypr

_FLOW.CONTROL CAPILLARY

2700 WaTtTs

ey
(Exisming) L

500 WaTry

© LINE HEAT

_ _LIQUIDN; TRAP -us

®-
- Hahvzk -
Zown O

BALT VAL - = 481

DIAM QD -« 455w CONDENSER

Hrmtanr, =22 1N ) .

 

List Sica 0w Alcewar
REVISIONS

Oren Prisa = '5- 7.0 PSIA
Qper TEMP, * 500-550°C
Ecne Hear * 20-kw

Diam O. 0.
LenaTn
OuTsiDE SURFACE

INSuL THK - ® &N

Tamp Zone 4
Teme moNw £
TeMr ZONE S
Teme zoned
"Tuemp zone 5
InsuL THR
EvLzc HEAT

THERMAL INSULATION

CangvtEmr 1900 BLOCK TYPE
k= 0. 8ru/rr-Hr -*F @ 1000°C

 

 

CONDENSING DUTY !

» 500~875°C

500-875 *C
500475 C

- 500-873°C

{
Sact'vol | s 481

Diavt OO0 161

Heiaur. . < 165N
Opgr Prias * O.5mm Hg

- Orer TEMP * 500-55Q°C

Egug.- Hear  =RO kw
INsyL Tk "B

 

REFERENCE: DRAWINGS

OAK- RIDGE NATIONAL LABORATORY

UNION CARBIDE NUCLEAR COMPANY

. DIVISION OF UNION CARGIDE CORPORATION
w ‘ .

DISTILLATION EXPERIMENT

L

 

 

 
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TR "D U, T AOG

 

 

PLAN . ROW "mA7

SRawi A" 4 PaniTy. & 45°

ArARg S T° Wad;Meawmin

. HeaZonmiey Frisa Coamin OF ¥ooso——
—Pw "B 12 Pamrs @ 20°
APaRY On  4° Raw, Mhliatd
o Hu\zothufl Fiora Ceuten O ing

 
    
 
  
 
 
  
  
 
  

Wawi "C* & Points As.

“MEAIRED HMomtouTany Frea
CEOTER. O Hako -

sj@

 

PLAN ° OF ~ STILL “RERD'

 

 

 

 

 

 

 

 

 

Auawn F48°* 'On 4" Rad.

 

Artam Fasmeatied \u Cdtatd
ABSCHASH  Tris Seempuy O

) S’ Wais AN Heas Wiw m:nnfl‘_
! Exresunts To Aoteuatauy Mar Sumine -

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Or Coniehn. SacTion, Actess. Fen Rasia-
UARenva hm- Cass Be Mase Tanu Nema*F*
A{ e On MoumADIoACT W& EafERusatuTS
Repaat Tus Ramoen-mn Descavnen Avend.

-**pumm. Fanmasiion Mans Dmut Taenutss Mosontmmnts
} Praty Devanatto By " LerYy Comnem OF

d "'D\fi“1 Wavtian * Covivan o .

'L Duminé, Fl.m.cntwu ‘Mane MEAsTREIAENTS Uutmasauicawy ' At
F\mn's DasisnaTey Tha Tamunatenas OO0 Dwe . WLIT4Ch- o:oa

ARG MITITA-CD. D‘IID Eraert Trioae: Manuan ' Ne M-mufltm‘u‘\'! .

runt RIsULTS 1k ArtmadiaTe - <‘.m.umu. '.

  

   
   
 

 

   
   
   
 

'Paw\-c "A‘r"wme( i
" ~

‘\altsu\m‘n g Lo ll\l'l Alt lQMmI\:“
Ry R CE R (K, e

T RieeAND A Muwun
D 0L T N e Pesiynil Waketa -

[ huu'uflr.‘ut T CPARER (RS & M) Cavly . 3 Insineate
COTWAY, PN T Dingeuy. . Orsotite The DispLACED wANTa
& Daviwer Uitmiseme witunsss Moasemameny Precasure Ouming

 

 

 

 

 

.‘._.:-_'FANMIGA‘(\QN Car Wisk " Piatues. Tha Samd  Themscst Measonswanls

  

PETrosE - Founb ™ Dimeexiay AT Fhm-n Dtflauncb Neva V- Anflt_.

. Reans Proicovas PreEcisswy,

G‘ TAFTRNEC NeumASIOACTIVE tmnm\‘urt, Maxg Ustiassut Thienate
L MEAWRAMLMTE AL s Nots 2 Amn Aus  Maceno REWATE. TN

T MPPROPRATE . Conumn, .

ST ST TTuwcKukes MER RIS in Decimnia o~ STATE A oTvun.

C NMeawRoduaty W lucdes Ao FRracTe s,

'1 AvTn Fagimespen; Eaocenarn . Wi  Sursicaa] Exsesshuy To
TERASLETLY MAR Ve W Hl'wulu Weun Luig At GeTrema
O Conie nis S kEtan T OF IR iAun  Rew YN On Csanunsgr. .
Arter Henraowacive EAPERIMENTY, R:nq T Raorocmanine,

 

       

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PLAN . ROWS

N
PLAW . ROWS “U" B y*

 

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“TE Poiusys Emuacey 'lim
Aol CIREGAFIRAME * OF
Riicmadh o :
“Cimevws » 13,933 wa.
Dwisews ¢ Z.AZTE wi.

  
 
   

 

Foen e e

i

 

Loeavinns =Linaan Muswetituts T Tanasne Do [ 07700 680

 

REFERENCE DRAWINGS . - MO

 

 

OAK RIDGE NATIONAL LABORATORY

OPERATED BY )
UnioN CARBIDE NUCLEAR COMPANY
DMIBION OF UMION CARBIDE CORPORATION
. OAX RDOE, TENNESSER

 

 

 

 

 

 

 

 

 

 

 

w ) y -, Mpa. WAL
LIMITS ON OIMENSIONS URMLESS | PASRE - DSTILLATION  EXPERTMENT' No s 1000 -]
FRACTIONS e LACATT T Peiuts Folt Dusawtisoh -vaw '

Radrosaapuic Mimbasmangy Oh, Stus: Al
DECIMALS % i Covogusi&n . Ansemaily
aaLes 2 e APPROVED
: er R & Lo 3/7

scaE- Nans 3 y%,hfl'lm - jeoloigT

 

 

 

 

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128

WALL THICKNESS MEASUREMENTS AND OBSERVATIONS WALL THIGENESS MEASUREMENTS QBSERVATIONS

DIRECT "] DIMENSIONAL |  RADICGRAPHY, OBSERVATIONS, LOCATION | DmeCT [ " " RADIOGRAPHY, CBIERVATIONS, LOCATION
INITIAL | INITIAL CHANGE AND REMARKS Of INITIAL. | INITIAL | GRERATIO ‘ AND REMARKS

A ; cA ower [— DIENSIONAL  RADIOGRAPHY. OMSERVANONK
tinches) | (inches) (Inches) . ‘ ' MEASIREMENT | {inches) | (inchas) | - (inches) 4 ‘ ' GHAN AND. REMARKS

WALL THICKNESS MEASUREMENTS AND OMSERVATIONS

—

—
—
—
—
—
o
—
—
e
—
—
—
—
—
—
—
—

OAK RIDGE NATIONAL LARORATORY
* "

m :
UNION CARBIDE NUCLEAR COMPANY
DIVISION OF UNION CARBIDE CORPORA
OAX TENNESSEE .

WIRE. DISTILLATION. EXPERIMENT. BLDG.
TABUCAT AR OF - DATA Frow -Dintas woay.

Aug Ravdt kabric MEAsuntiints O St
CTAwe - Conubaser  Asttmecy .

w

U Finer

IMTIAL DIMENSIONS - . : . \ )

 

 

 

 
*

I.OCAM DmeCt

T3

vy

s|=

g%

| X¥

N4

129

WALL THICKNESS MEASUREMENTS AND OSSERVATIONS

- RADIOGRAPHY, OISFRVATIONS,
INITIAL CHANGE AND REMARKS

”

WALL THICKNESS MEASUREMENTS AND OBSERVATIONS

LOCATION | -DIRECT ) DIMENSIONAL RADIOGRAPHY, OBSERVATIONS,
OF INITIAL | INITIAL | OPERATION CHANGE - AND REMARKS
1z -
zl. —
T2 . . —
3 -
28 - . —
398 . —
Mo —
2o —_—
Zil e —
- —

b

   

T4 Buyrwees @ T Mwuu'
- SPaatm 90° APARE

X

AL

FROM |-
POINT

LENGTH AND

INITIAL POSY
AS BURT | OPERATION
LENGTH

Mave Butyows By
Hasyoniay X Walo
HAvuss 25 Wio Reo
SussTITUTE .

LIMITS ON
OTHERWASE

FRACTIONS +
DECMALS &
Avars

=

Fiis Cmiwi
Amnmnni
Aue Comervuién

 

(wWeioine)
MatAL On Sumsacss,
An Acageyani

TR e W T . _wsMeD
REFERENCE DRAWINGS NO.
OAK RIDGE NATIONAL LABORATORY

OPERATED BY :
Union CARBIDE NUCLEAR COMPANY
OF UNION CARBIDE CORPORATION

TENNERSEE
umess | MEKE DTILATIOR EXPERvmenT BB
TOCeRAR N - OF Painte  Foll TUINERR Witk

RINGARITY
- ANE . TABULATI#N - OF Oata  Fon Snn-Cmfih-
Rusivin  Assumony

" . TS ~
 

130

- D~KKC-55179-D One-line Diagram Sheet-5 Motor Control Centers
, G3 and G4. -

E-FFB-49040  Plan at Elevation 852 Ft-Elevation AA,
49041 Installation of Equipment Between Elevations 831 ft and 852 ft.
49042  Containment Cubicle for Instruments.
49043  Containment Cubicle for Instruments, Piping Details Sheet 1.
49044  Containment Cubicle for Instruments, Piping Details Sheet 2.
49045  Containment Cubicle for Instruments, Piping Details Sheet 3.

| The first four drawings in the above list are concerned with modifications to
the roof plugs of the spare cell in the MSRE building (Building 7503). These
modifications were necessary before distillation of irradiated salt. The remclnlng
six drawings are details of the equipment installation.

Drawings listed below are referenced but are not mcluded in thls Appendlx

These drawings cover design and installation of instruments. - Each drawing bears

the principal title MSRE Distillation Experiment with the followmg numbers and
subtitles: ‘

I-12173-QE-001-D Instrument Application Diagram.
I-12173-QE-002-D Front of Panel Board Layout.
1-12173-QE-003-D Rear of Panelboard. | |
I-12173-QE-004-D Bill of Materials Panel Construction Nameplote and’
- Annunciator Tag Tabulation.
1-12173-QE-005-D Panel Cutouts.
1-12173-QE-006-D Elementary Wiring Diagrams.
I-12173-QE-007-D Panelboard Wiring Details = Sheet 1 of 2
1-12173-QE-008-D Panelboard Wiring Details = Sheet 1 of 2,
1-12173-QE-009-D Heater Control Schematic. '
I-12173-QE-010-D Relay Box Wiring Diagram. ' .
1-12173-QE-011-D Load Distribution Panel Wiring and Construction Detalls
I-12173-QE-012-D Pnuematic Tubing Schematics.
I-12173-QE-013-D  Thermocouple Patch Panel Box Details. |
I-12173-QE-014-D Relay Box and Door Details,
1-12173-QE-015-D Relay Box Assembly and Details.
1-12173-QE-016-D Dolly for Six Frames-Details.
I-12173-QE-017-D Miscellaneous Details.
[-12173-QE-018-D  Back Frame Cover Details.
1-12173-QE-019-D Level Probe Insulation Assemblies.
I-12173-QE~020-D Level Probe Assembly and Details.
1-12173-QE-021-D Level Probe Miscellaneous Details.
- 1-12173-QE-022-D Level Probe Junction Box and Details.
1-12173-QE~-023-D Level Probe Interconnection Wiring.
I-12173-QE~024-D Level Probe Junction Box Terminations.”
1-12173-QE-025-D Level Probe Exciter Junction Box.

 

 

 
 

.

 |-12173-QE~026-D

I-12173=-QE~027-D

1-12173-QE-028-D

|~12173-QE~029~D
I-12173-QE~030-D

1-12173-QE~031-D

I-12173-QE-032-D
I-12173-QE-033-D

1~12173-QE-034~D

|-12173-QE~035-D
I-12173-QE-036-D

I-12173-QE-037-D

 

131

Valve Position Indicators and Schematic Diagram.
- Temporary Layout Building 3541.
Valve Box Schemahcs
_Field Wiring.
Panelboard T/C Junction Boxes.
Metalphoto Name Tags for Panel.
* Metalphoto Name Tags for Panel.
Metalphoto Name Tags for Panel_
Heater Schematic.

Schemahc Wiring for Mulhpomt Spdx. Instr./Commutator
Control or Alarm Special Circuit Arrangement=TR-1.
Schematic Wiring for Multipoint Spdx, Instr ./ Commutator
Control or Alarm Special Circuit Arrangement-TR-2.

Valve Piping Schematic. |

 
 

 

 

133
_DISTRIBUTION. -

1. C. F. Baes 43.
2, H. F. Bauman 44,
3. S. E, Bedll 45,
4, M. Bender 46.
5. C. E. Bettis 47.
6. E. S. Bettis - 48,
7. R. E. Blanco 49,
8. R. Blumberg 50.
9. E. G. Bohlmann 51,
10.. G. E. Boyd 52,
11.. R. B. Briggs - 83,
12, R. E. Brooksbank - 54,
13, K. B. Brown 55.
14. S, Cantor 56.
~15. W. L. Carter 57.
16. C. I, Cathers 58,
17. C. W. Collins 59.
18. E. L. Compere 60,
19. W. H. Cook 61,
20-21, D. F, Cope, AEC-ORO 62,
22, F. L. Cuyller , | 63.
23. C. B. Deering, AEC-ORO 64-65,
24. S. J. Ditto 66.
25. W. P, Eatherly 67.
26. J. R, Engel - 68,
27. D. E. Ferguson 69.
28. L. M. Ferris 70.
29, C, H. Gabbard 71,
30, H. E. Goeller 72,
31. W. R. Grimes - 73.
32, A. G. Grindell - 74,
33. R. H. Guyman 75,
34. C, A. Hahs 76.
35.. B. A. Hannoford 77.
36. P. N. Haubenreich _ 78.
~.37. J. R. Hightower 79~80,
. 38, W, H, Jordan - 81-82,
39. P. R. Kasten - 83-85,
40. R. J. Kedl - 86,
41" M. J. Kelly 87-101 :
42, H. T. Kerr 102,
103.

20 Lo =

S. S. Kirslis

J. W. Krewson
J. A. Lane

B. Lieberman
R. B. Lindaver
M. |, Lundin

"H. G. MacPherson

R. E. MacPherson
H. McClain

« E, McCoy

F. McDuffie
E. McNeese
R. McWherter
L. Moore

. A, Nelms

L. Nicholson -
C. Oadkes

. M. Perry

. W. Pickel

. T. Robetts

C. Robertson
M. W. Rosenthal
Dunlap Scott

C. E. Sessions
J. H. Shaffer
W. F. Shaffer
A. N. Smith

J. R. Tallackson
R. E. Thoma |

srTrx

Mo

W. E. Unger

J. R. Weir
M. E. Whatley

“J. C. White

R, G. Wymer

E. L. Youngblood
Central Research Library
Document Reference Section
Laboratory Records
Laboratory - Recrods, RC
DTIE

Nuclear Safety Information

"~ Center, Y-12

Leb. and Univ. Div., ORO