EPA-660/2-74-059
June 1974
Environmental Protection Technology
Submerged Combustion Evaporator
For Concentration of Brewery
Spent Grain Liquor
Office of Research and Devtboatnt
U.S. Environmental Protection Agency
Washington, O.C. 20480
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RESEARCH REPORTING SERIES
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was consciously planned to foster technology
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<*. Environmental Monitoring
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This report has been assigned to the ENVIRONMENTAL
PROTECTION TECHNOLOGY ; series. This series
describes research performed to develop and
demonstrate instrumentation, equipment and
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degradation from point and non-point sources of
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EPA-660/2-74-059
June 1974
SUBMERGED COMBUSTION EVAPORATOR
FOR CONCENTRATION OF
BREWERY SPENT GRAIN LIQUOR
By
John L. Stein
Roap/Task 21 BAG 11
Project 12060 HOW
Program Element 1B2037
Project Officer
i
Robert L. Hiller
Environmental Protection Agency Region VI
Dallas, Texas 75201
Prepared for
OFFICE OF RESEARCH AND DEVELOPMENT
U.S. ENVIRONMENTAL PROTECTION AGENCY
WASHINGTON, D.C. 20^0
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ABSTRACT
One of the major waste streams in many breweries is the liquor resulting
from spent grains dewatering prior to drying. This liquor may account
for a third or more of the B.O.D.i- and suspended solids generated by a
typical brewery.
Initial studies of the spent grain liquor problem indicated that recovery
rather than treatment was the best approach. A number of evaporators
were evaluated to determine which design was most satisfactory for
concentrating the liquor. A submerged combustion evaporator was selected
on the basis of engineering analyses and pilot scale tests.
A full scale unit was installed at the Houston Brewery of Anheuser-Busch,
Inc., in 1970. This evaporator was modified several times to overcome
failures of the burner downcomers brought about by high temperatures.
Before a final solution to these problems could be demonstrated, the
project was terminated. Fuel costs above $1.60 per million kg-cal
(kQ<£ per million BTU) coupled with thermal efficiencies approximately
3.5 times better for conventional four-effect evaporators indicated
that a conventional evaporator would be more economical.at these fuel
price levels.
This project was submitted in fulfillment of Project Number 12060 HCW
by Anheuser-Busch, Inc., under the partial sponsorship of the Environmental
Protection Agency. Work was completed as of March 1973.
11
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CONTENTS
Abstract ii
List of Figures iv
List of Tables v
Acknowledgments yi
Sections
I Conclusions -*-
II Recommendations 3
III Introduction ^
IV Experimental Program -^
V Evaluation of Process -^
oh
VI Discussion ^
VII References ^0
VIII Glossary 32
IX Appendices 3^
111
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FIGURES
No. Page
1 The Brewing Process 5
2 Process Flow Diagram 13
3 Submerged Combustion Evaporator 15
U Final Downcomer Design 22
IV
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TABLES
No.
1 Principal Waste Streams from the Brewing Process 7
2 Evaporator Performance Using Water-Cooled Downcomer 17
3 Evaporator Performance Using Non-Jacketed Downcomer 19
U Evaporator Performance Using Inconel 601 Downcomers -
Series 1 20
5 Evaporator Performance Using Inconel 601 Downcomers
Series 2 21
6 Evaporator Performance Using Jacketed Downcomer
with Dilution Air 23
7 Projected Effluent Improvement 27
8 Economics of Adding Spent Grain Liquor Concentrator
to Existing Drying Operation 28
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ACKNOWLEDGMENTS
Pilot plant studies of the submerged combustion evaporation process
were carried out "by the Anheuser-Busch Technical Center. Design,
construction, and start-up of the full-scale evaporator were under
the supervision of the Anheuser-Busch Central Engineering Department.
Personnel from the Houston Brewery were responsible for the operation
and upkeep of the evaporator during the test phase.
Personnel from the Thermal Research and Engineering Corporation of
Conshohocken, Pennsylvania, provided valuable assistance and
cooperation during the latter phases of the project.
Personnel from the EPA Office of Research and Development Headquarters
and Region VI provided assistance throughout the project.
vi
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SECTION I
CONCLUSIONS
\
The experiment showed that the concept of using a submerged combustion
evaporator for concentrating brewery spent grain liquor is feasible,
although all of the design problems involved in this application have
not been completely resolved. Concentrates of 20 percent total solids
can be produced from feedstocks of 2.U to 3.2 percent solids.
Extensive pretreatment of the spent grain liquor was shown to be
unnecessary. Screening of the liquor using a standard vibratory screen
was adequate to assure a feed soluble-insoluble total solids ratio of
1.0 or greater, the ratio proven necessary to hold fouling and demister
plugging to a minimum.
Although the testing program was cut short prior to final evaluation
which included air emissions testing, it was demonstrated that smoke and
odor could be minimized with proper combustion controls. Entrainment was
unavoidable during operations without the stainless steel mesh demister
pad, but plugging was unavoidable with the pad located at the base of
the stack where it was subjected to considerable splashing. At the time
of termination of the test program plans had been made to relocate the
demister pad to a portion of the stack not subject to splashing.
The use of an air-cooled burner dbwncomer proved to be the only satis-
factory method insuring reasonable downcomer life under the conditions
experienced during this test. Non-cooled downcomers were subject to
rapid deterioration because of the high skin temperatures developed.
Single-pass cooling with water resulted in considerable heat losses
and poor thermal efficiency. The closed loop system tried did not
satisfactorily transfer heat to the liquor from the downcomer walls. The
air-cooled downcomer which circulated air through the downcomer walls
and into the firebox eliminated these problems. Evaporation was satis-
factory, equipment service life was acceptable, and the thermal efficiency
was maximized. Inconel 601 was judged to be a better downcomer material
than Type 316 stainless steel.
Submerged combustion evaporation can be economically attractive in
situations where fuel may be obtained at less than $1.60 per million Kg-cal
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per million BTU), but when fuel costs exceed this amount conventional
evaporative processes are favored. Where high-cost fuels must be used
the efficiency of the conventional evaporator outweighs the capital costs
associated with this type of evaporator and its ancillary preprocessing
equipment. Although the submerged combustion evaporator is perhaps the
most efficient single-effect evaporator, conventional four-effect units,
such as are now being used on concentrate spent grain liquor, offer
efficiencies about 3-5 times those of the submerged combustion evaporator.
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SECTION II
RECOMMENDATIONS
Because of the demonstrated low thermal efficiency of the submerged
combustion evaporator and the current critical shortages of oil and
natural gas, further experimentation with this system would not
appear warranted at this time. Due to the shortage of petroleum fuels
which has developed in the past year, it is unlikely that many breweries
would be able to secure sufficient supplies to operate a submerged
combustion evaporator, or even if such supplies were available that
these plants could economically operate such a system due to the
greatly increased costs of oil and gas.
Recent experiences have shown that conventional evaporators, such as the
multiple-effect or recompression types, can be designed to overcome
most of the problems which the submerged combustion evaporator eliminated.
These evaporators can be operated efficiently and economically. For
this reason, it is recommended that future efforts in the area of spent
grain liquor recovery be directed toward the refinement and improvement
of conventional evaporative techniques, with the goal of reducing the
number of processing steps required for the spent grain and liquor.
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SECTION III
INTRODUCTION
The brewing industry in the United States operates some 130 breweries
across the country and produces approximately 156 million hectoliters
(133 million barrels) of beer per year. The effluent control problems
of the industry have been accentuated in recent years due to the closing
of many small outmoded breweries in large metropolitan areas coupled
with the construction of large, more modern breweries in smaller cities
and towns. This trend has resulted in increased percentages of brewery
wastewaters in the influent of many municipal treatment plants which
have had little or no experience in the treatment of high carbohydrate
wastes.
BREWING INDUSTRY WASTEWATER PROBLEM
2
A process flow diagram for a typical brewery is shown on Figure 1.
Malt is crushed into fine particles and mixed in aqueous solution. A
similar process is carried out with the grain adjunct (rice, corn or
other grain derivative), except that the adjuncts are heated and brought
to a boil before being combined with the malt. The soluble fractions
are separated, and the starches are converted to sugars and the proteins
into amino acids. Upon completion of the mashing operation the grain
solids are separated from the malt extract, or wort. The spent grains
are then normally screened and mechanically pressed to remove as much
moisture as possible. The grain is then fed to a rotary kiln dryer and
the dried grain is then ready for shipment to cattle feed processors.
The wort is sent to the brew kettle where it is boiled and mixed with
hops. All enzymes are destroyed and the resins which impart flavor are
extracted from the hops. Following this operation, the hops are
screened from the wort and either mixed in with the spent grains or
disposed of separately. The hot wort is then cooled and prepared for
fermentation. Proteins which were coagulated in the brew kettle settle
to the bottom of the wort receiver and become known as trub. The trub
may be mixed with spent grains or sewered.
Fermentation of the wort is then initiated with the addition of yeast.
Sugars are converted to alcohol and carbon dioxide, and an excess of
yeast is produced. Carbon dioxide may be recovered for counter-
pressurization of lager tanks and possibly for carbonation of the beer
further along in the process, or it may be drawn off for sale with any
excess vented to the atmosphere. The yeast may be reused several times
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Figure 1. THE BREWING PROCESS
Filter Aid
Recovered
V.'aste Stream.
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before it is discarded. Upon completion of fermentation, the beer is
ready for aging and additional carbonation, brought about by injection
with carbon dioxide or through a second fermentation step. The beer is
then clarified and filtered, using either cotton or diatomaceous earth
filters. Following this step, the beer is ready for packaging.-^
The principal waste streams resulting from this process are shown in
Table 1. The characteristics of the combined brewery waste stream are
highly variable, both from plant to plant and within a specific brewery.
The wastes from different plants vary depending upon the raw materials
used, process equipment employed, residual disposal techniques, etc. The
effluent from a particular plant may vary as a function of which of the
various processes are operating at any particular time. Generally speak-
ing, brewing wastes are abundant in degradable organic matter and contain
abundant amounts of suspended and dissolved solids. Variability in the
amounts of biochemical oxygen demand (B.O.D.c) and suspended solids
contained in the wastewater is caused by the numerous batch processes
involved in brewing.
Due to the variability and strength of brewing wastewaters, successful
conventional treatment of these wastes alone using trickling filters and/
or activated sludge has been difficult and costly to achieve. Most
breweries have long recognized the benefits to be realized by combining
their wastes with domestic sewage, and the practice of combined treat-
ment is widespread. (Only two breweries in the United States operate
their own treatment facilities.) Different treatment plant operating
techniques are needed, however, as the proportion of brewing wastes, as
with many other wastes, increases in the total volume of waste handled
by the municipal treatment plant. Virtually all treatment plants
today also find themselves being required to meet more stringent effluent
standards, and, hence, are going "upstream" in an effort to reduce the
total load on their facilities.
SPENT GRAIN LIQUOR
One of the most significant sources of high strength organic wastes in
the brewing industry is the liquor resulting from the spent grain
recovery process. In this process, waste grain from the mashing process
is screened and pressed to remove as much moisture as possible by
mechanical means, and then dried to produce saleable animal feed. The
liquor remaining from the screening and pressing operations is character-
istically high in B.O.D.,- and suspended solids, and somewhat variable
as to the ratio of soluble to insoluble solids. Breweries with grains
drying operations can usually attribute 30 to 60 percent of their total
B.O.D.IT and suspended solids discharge to screen and press liquor.
Attempts to eliminate the grain liquor problem to date have been limited
in their success. Some breweries have eliminated their drying operations
and sell their grains wet. Wet grain feeding operations can, however,
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Table 1. PRINCIPAL WASTE
STREAMS FROM THE BREWING PROCESS11
Source
Washings from kettles, cookers,
and grain separators
Screen and press liquor
Trub
Yeast
Clarification precipitates
Spent filter aid
Beer
Cleaning solutions
B.O.D.5
mg/1
200-7,000
15,000
50,000
150,000
60,000
90,000
1,000
S . S . ,
mg/1
100-2,000
20,000
28,000
800
100
if, 000
100
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become nuisances. When grains are hauled to an independent drying
operation the spent liquor problem has only been moved, not eliminated.
Brewers, then, have been forced to look at means for recovering the spent
grain liquor and attention has focused on concentration processes. The
use of a liquor concentration process allows the actual elimination of
the grain liquor as a waste stream. The concentrate is a syrupy sub-
stance which can easily be mixed with wet grains and dried.
PROCESS SELECTION
Concentration of dilute solutions is normally carried out by evaporation
of the solvent, with or without recovery of the vapor. Evaporators may
be classified as follows:
1. Those in which the heating medium is separated from the
evaporating liquid by tubular heating surfaces.
2. Those in which the heating medium is confined by coils,
jackets, double walls, flat plates, and other surfaces.
3- Those in which the heating medium is brought into direct
contact with the evaporating liquid.
Most industrial evaporators fall into the first or second category.
This group may be further subdivided into forced-circulation, long-tube
vertical, horizontal-tube, and other lesser known types.'
The forced circulation evaporator is suitable for a wide variety of
applications. In this type of evaporator liquid is pumped through a
tube bundle in a steam chest. As the liquid rises through the tubes, it
becomes heated and begins to boil, causing vapor and liquid to exit
from the tubes at high velocity. The vapor and liquid are ejected into
a vapor head to effect an effective separation of the two. Forced
circulation evaporators do have high heat-transfer coefficients and are
relatively free from scaling and fouling, but they are not universally
attractive because of their high capital cost and the high energy
requirements for recirculation. These evaporators frequently suffer
from plugging of tube inlets by deposits detached from walls of equipment,
poor circulation due to,high head losses, and corrosion and erosion.'
The long-tube vertical evaporator is a one-pass vertical shell-and-tube
heat exchanger which discharges into a small vapor head. Liquid may be
fed to the bottom of the tube, starting to boil part way up the tube
and then exiting as a mixture of vapor and liquid at the top where
separation occurs. In the case of the falling film version liquid is fed
to the tops of the tubes and flows down the walls as a -film. Vapor-
liquid separation normally takes place at the bottom. Long-tube vertical
8
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evaporators have the advantages of low initial cost, good heat transfer
coefficients, and short residence time. Their drawbacks include high
headroom requirements, problems with scaling liquids, poor heat transfer
coefficients with the rising-film version at low temperature differences,
and the necessity for recirculation for most falling-film versions.
Long-tube vertical evaporators are especially useful where heat sensi-
tive liquids are being concentrated (including many liquids in the food
and-beverage industry), where foaming is a problem, and where high
evaporation loads are encountered.7
Horizontal-tube evaporators may be used for severely scaling liquids.
In this design the liquid flows or is sprayed over a tube bundle contain-
ing steam. These evaporators are favored because of their low headroom
requirements, relatively low initial cost, and good heat-transfer coef-
ficients. Care must be exercised in design and operation or serious
scaling problems may develop. Horizontal-tube evaporators are not as
widely used for concentration as are forced-circulation or long-tube
vertical evaporators.'
The most widely used evaporator which does not depend upon a heating
surface is the submerged combustion evaporator. Here hot combustion
gases passing through the liquid transfer the heat. The submerged
combustion evaporator normally consists only of a tank, a burner and gas
distributor and a combustion control system. The evaporator is well
suited for severely scaling liquids because of the lack of any heating
surfaces. Because of the simplicity of design, the submerged combustion
evaporator is much less expensive to construct than those utilizing
heat transfer surfaces. High entrainment losses can be a problem; and
because the vapor is mixed with large quantities of non-condensable
gases, it is impossible to reuse the heat in the vapor. For this latter
reason, the use of submerged combustion evaporators is normally limited
to areas where low-cost fuel is plentiful.''
l
One type of concentrator which does not fit into the category of an
evaporator is the membrane concentrator. Membrane concentrators are
normally classified as a reverse osmosis or ultrafiltration devices,
depending upon the size of the solids which the membrane is designed
to exclude. Membrane devices function by pumping liquid feed at high
pressures through a permeable membrane. These devices are highly
efficient from an energy standpoint, since they effect a solid-liquid
separation without a phase change. They are, however, highly susceptible
to fouling and as a result the feed liquor must be virtually free of
suspended solids. Membranes presently available are highly sensitive
to pH and as a result special cleaning solutions, usually detergent-
enzyme formulations are necessary. This concentration technique has had
little use in the food industries, although the process has been proposed
for spent grain liquor recovery."
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Although dryers also remove moisture from a liquid or semi-liquid feed,
they are not normally compared with evaporators because evaporators are
used only to transfer heat to liquids, whereas dryers transfer heat to
liquids and solids.
The decision to proceed with full scale investigation of spent grain
liquor concentration using submerged combustion evaporation was based
upon compatibility with existing grain drying and recovery equipment
and the success of preliminary pilot plant investigations. Prior to
the commencement of the design of a full-scale submerged combustion
system several other methods for the disposal of the spent grain liquor
were explored. These approaches involved the use of a dry grain
recycle system and a number of evaporative systems. One system involved
the elimination of screening or pressing of the grain; the wet grain
was mixed with dry recycled grain and then added to the dryer. This
process required considerable additional dryer capacity coupled with
greatly increased fuel costs. A modification was examined in which
the grain was screened but not pressed prior to mixing with the recycled
grain. An evaporator of the submerged combustion type was used to
concentrate the screened liquor so that it could also be mixed with the
recycled material. This process showed considerable merit for new
installations, but not for existing plants where the added dryer capacity
would be difficult to install and presses were already in place.
Two systems designed around evaporators were studied which were applic-
able to both new and existing breweries. The first involved the use of
a centrifuge to remove the suspended material from the screen and press
liquor prior to evaporation in a conventional multiple-effect evaporator.
The second utilized a vibrating screen to remove coarse solids from the
spent liquor before adding the liquor to a submerged combustion evaporator.
The multiple-effect evaporation system was estimated to be more costly
to install than the submerged combustion type, but slightly less
expensive to operate. Questions arose, however,- concerning the ability
of the conventional evaporator to tolerate the suspended solids in the
spent liquor, as well as the ability of either centrifuges or screens
to reduce the suspended solids concentration to an acceptable level.
It was concluded that the submerged combustion system could offer the
greatest degree of reliability and the lowest overall cost, and additipnal
research was directed toward this area.
Preliminary studies to determine the practicality of the process and to
identify potential problem areas were conducted in May, 1970, by the
Anheuser-Busch Technical Center. A pilot plant evaporator and a vibrat-
ing screen were obtained in order to carry out these studies. A series
of twelve tests was run with the 6l cm. (2*4- inch) vibrating screen.
These tests indicated that the minimum required concentration of 20 percent
solids could be guaranteed for most feed conditions and that concentrates
in the 30-35 percent solids range might be obtainable.
10 ~
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The studies showed that the feed soluble-insoluble solids ratio should
be maintained above 1.0 to avoid stack plugging and entrainment of
solids. It was found.that foaming was dependent on concentration and at
concentrations of 7 to 10 percent excessive foaming ceased. Burning
of grain was not a significant problem due to the small amount of surface
area available. It was considered that there would be no problem in
removing what grain material was burned and that the amount of material
would be insignificant in any event. It was also determined that the
evaporator would not violate any existing air pollution regulations.
Odors were detected in the pilot plant operation, but it was felt that
these should be localized in nature. °
11
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SECTION TV
EXPERIMENTAL PROGRAM
TEST FACILITY
Based upon the success of the pilot studies, a decision was made to
design a full scale evaporator installation and to seek a Research/
Development/Demonstration grant from the Environmental Protection
Agency. The grant was approved and a complete testing and evaluation
program was set up. The Houston Brewery of Anheuser-Busch, Inc., was
selected as the test site.
The system as designed following the pilot plant work is shown in Figure
2. Cooked grain mash is dumped into the grain separator, where the
wort used to make the beer is drawn off. Water under high pressure is
then used to force the grain from the grain separator to a dewatering
screen and then to a holding tank. Water from the first six minutes
of washing, which is high in B.O.D.c and suspended solids, is recycled
to the holding tank because it is impractical to by-pass the screen
or to carry the rinse water to the SWECO -R * screen which is located in
another building. The remainder of the wash water is sufficiently clean
to be sent directly to the sewer. Wastes from the brewing operation,
such as spent hops, are also sent to the holding tank.
The contents of the holding tank are then pumped to a dewatering screen
ahead of the spent grain holding tank. The spent grains are then sent
to a series of presses for further dewatering. Liquor from the dewater-
ing screen and the presses is delivered to a common sump, and then sent
through the SWECO-|^ dewatering screen. Here large particles which have
passed through the" presses are recovered, and along with any other
recoverable suspended matter, are returned to the spent grain holding
tank for recycle. Alternately, these solids may be sent to the
concentrate storage tank.
Liquor from the SWECO £> screen is sent to the evaporator feed tank, where
it is agitated until bMng sent to the evaporator itself. In the
evaporator the solids content of the liquor is brought to the 20-25
percent range. The concentrate is then delivered to the concentrate
storage tank where solids from the SWECO £ screen may be added.
* A product of SWECO, Inc., Los Angeles, California
12
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=. 7..
L_'_ J
F ri ,.j
i -i ' L i-
S c.^.« «*a \ va o^ s
st
13
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This concentrate is then delivered to a mixing screw conveyor where it
is combined with the spent grain pressings, spent yeast, "beer clarifica-
tion precipitate (if available) and recycled dry grain, and then sent to
the grain dryer. Once the grain has left the dryer, it is then cooled
and ready for recycle or shipment as Brewers Dry Grain.
Principal items of equipment for the process include the SWECO,^ screen
and the submerged combustion evaporator. The SWECO $-. screen is a 183 cm.
(60 inch) unit with two decks. The top deck is a 30-mesh screen and the
lower deck is a 7^mesh screen. The SWECO^ unit was chosen over other
types because of the extensive experience Anheuser-Busch has had with
the screen. The evaporator chosen was not of the same design as that
used in the preliminary studies. A 6.3 million Kg-cal/hr (25 million
BTU/hr) unit manufactured by Thermal Research and Engineering Corporation,
Conshohocken, Pennsylvania, was selected for reasons of lower first cost
and fire safety features. The evaporator tested uses natural gas only
as a fuel, although burners are available which will burn gas and No. 2
oil. The evaporator is shown in Figure 3-
TEST PROGRAM
Testing of the evaporator system was to be divided into equipment
evaluation and effluent analysis. The equipment evaluation phase
included development of complete material and heat balances for the
system. The efficiency of the entire process was to be assessed, as
well as the performance of the specific items of equipment. The effluent
analysis phase was designed to measure the impact of the spent grain
liquor recovery system upon the overall brewery sewer loading. Plans
called originally for an eight-month test period, four with the evaporator
in operation and four without. Two total brewery effluent samples were
to be taken each week during the entire period. The analytical para-
meters included five-day biochemical oxygen demand (B.O.D.^), chemical
oxygen demand (C.O.D.), total solids, total suspended solids, volatile
suspended solids, total Kjeldahl nitrogen, total phosphorus, nitrate,
and nitrite. In addition, this sampling program was to be augmented
with spot sampling of the individual waste streams in the grain drying
area. These spot samples were to be analyzed only for C.O.D. and total
suspended solids.
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Figure 3. SUBMERGED COMBUSTION EVAPORATOR
15
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SECTION V
EVALUATION OF PROCESS
In the course of the evaluation of the submerged combustion system,
critical problems developed with the burner downcomer. The downcomer
is a cylindrical duct which directs the hot gases from the burner into
the liquor. Much of the work on the process was devoted to the develop-
ment of a durable and efficient downcomer. Aside from the downcomer
problems the performance of the submerged combustion system was virtually
as predicted. Considering the extensive work done on downcomer design,
this section is organized to reflect the development of this crucial
element. Test results are summarized in the following sections. More
complete data tabulations will be found in the Appendices.
PHASE I - TESTS USING WATER-COOLED DOWNCOMER
Initial tests of the submerged combustion evaporator utilized a water-
cooled downcomer. The purpose of the water jacket was to reduce the
skin temperature of the metal downcomer sufficiently to avoid buckling.
A single-pass cooling system using city water was used with the intention
of switching to a closed loop cooling system once the evaporator was
proven out. The test data are summarized in Table 2.
PHASE II - TESTS USING JACKETED DOWNCOMER AND CLOSED LOOP COOLING SYSTEM
In an effort to reduce the heat losses from the jacketed downcomer and
the single-pass water cooling system, a decision was made to replace water
as the cooling agent and to use in its place a commercially available
heat transfer fluid circulated through a panel coil attached to the
inside of the weir shell surrounding the downcomer. Therminol (g) 66* was
selected as the heat transfer fluid. The cooling system design called for
maintenance of a downcomer skin temperature of 123°C (25^°F). The !
testing of this downcomer design was cut short because of serious cooling
problems.
PHASE III - TESTS USING NON-JACKETED DOWNCOMER
Because of the unsatisfactory performance of the jacketed downcomer design
a decision was made to test non-jacketed burner downcomers. These
* A product of Monsanto Co., St. Louis, Missouri
16 '
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Table 2. EVAPORATOR PERFORMANCE
USING WATER-COOLED DOWTTCOMER
Parameter
Feed rate, I/sec (gpm)
Evaporation rate, I/sec (gpm)
Heat input, Kg-cal/hr
(BTU/hr)
Boiling point, C ( F)
Concentration of product, (
percent
Time to reach final
concentration, hrs.
Design
3.^7 (55)
2.80 (IA)
6.3 x 10^
(25 x 106)
88.8 (192)
15-25
Actual Average
1.70 (27)
N. D.a
6.91 x 106,
(27. h x iob)
88.2 (191)
20-25
2k
aNot determined
17
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downcomers were fabricated and installed, and the test results are
summarized in Table 3-
PHASE IV - TESTS USING INCONEL DOWNCOMER
Due to the failures of the stainless steel downcomers a decision was
made to switch to Inconel 601. It was decided that two different
downcomer designs would be tried, one jacketed for air cooling, with
the return air directed to the burner, and the other non-jacketed as
before. The results of this series of tests are summarized in Table k.
Based upon the results of these tests, two similar downcomers were
tested but with the gas nozzles on the sides omitted. The results of
these tests are summarized in Table 5.
PHASE V EVAPORATOR PERFORMANCE USING DOWNCOMER COOLED WITH DILUTION AIR
Because of the demonstrated need for a jacketed, cooled downcomer all
efforts were directed toward this area. An air-cooled downcomer with
dilution air to reduce the firebox temperature to 1203 C (2200°F) was
proposed by Thermal Research and Engineering, and this scheme was
approved by Anheuser-Busch. In order to reduce development costs it was
decided that only one burner would be fitted with the new downcomer. The
design of this downcomer is shown in Figure k. The results of this test
series are summarized in Table 6.
EFFLUENT SAMPLING PROGRAM
Numerous samples of the plant effluent were taken during the study period.
Due to the difficulties in finding a satisfactory design for the burner
downcomers, few samples were obtained while the evaporator was in opera-
tion, although numerous samples were taken with the evaporator out of
service. Sampling was suspended during the latter phases of the experi-
ment because the evaporator was being tested at 50 percent capacity, and
the results obtained during this period would not have been meaningful.
Sampling with the evaporator out of operation was suspended because of a
lack of data with the evaporator running which would have allowed some
comparison of effluent quality. The results of the effluent sampling
program are tabulated in the Appendices.
18
-------
Table 3- EVAPORATOR PERFORMANCE
USING NON-JACKETED DOWNCOMER
Parameter
Design
Actual Average
Feed rate, I/sec (gpm)
Evaporation rate, I/sec (gpm)
Heat input, kg-cal/hr
(BTU/hr)
Boiling point, C (°F)
Concentration of product,
percent
Time to reach final
concentration, hrs.
(55)
2.80
6.3 x lo
(25 x 10b)
88.8 (192)
15 - 25
2.52 (ItO)
2.21 (35)
6.05 x 106
(2k x 106)
88.2 (191)
22
30
19
-------
Table 1*. EVAPORATOR PERFORMANCE
USING INCONEL 601 DOWNCOMERS - SERIES 1
Parameter
Design
Actual Average
Feed rate, I/sec (gpm)
Evaporation rate, I/sec (gpm)
Heat input, Kg-cal/hr
(BTU/hr)
Boiling point, °C (°F)
Concentration of product,
percent
Time to reach final
concentration, hrs
(55)
2.80
6.3 x K)
(25 x 10b)
88.8 (192)
15 - 25
2.15 (3*0
1.83 (29)
h.5k x lp6
(18 x lo6)
88.2 (191)
20 - 22
20
-------
Table 5. EVAPORATOR PERFORMANCE
USING INCONEL 601 DOWNCOMERS SERIES 2
Parameter
Design
Actual Average
Feed rate, I/sec (gpm)
Evaporation rate, I/sec (gpm)
Heat input, Kg-cal/hr
(BTU/hr)
Boiling point, °C (°F)
Concentration of product,
percent
Time to reach final
concentration, hrs
3-^7 (55)
2.80 (kk)
6.3 x 10^
(25 x 10b)
88.8 (192)
15 - 25
1.58-1.70 (25-2?)
1A5 (23)
3-53-^.03 x,106
6 x 106)
88.2 (191)
21
N. D.a
aNot determined
21
-------
Figure k. FINAL DOWWCOMER DESIGN
Burner
Natural Gas and Air
Oombustioi
Chamber
Refractory
Downcomer
Dished
Head
22
-------
Table 6. EVAPORATOR PERFORMANCE
USING JACKETED DOWNCOMER COOLED WITH
DILUTION AIR
Parameter
Feed rate, I/sec (gpm)
Evaporation rate, I/sec (gpm)
Heat input, kg-cal/hr
(BTU/hr)
Boiling point, °C (°F)
Concentration of product,
percent
Time to reach final
concentration, hrs
3.
Design
1.73 (27)
l.UO (22)
3-2 x 10 ,
(12.5 x 10 )
88.8 (192)
15 - 25
f
Actual Average
1.55 (24.5)
1.32 (21)
3.2 x 10
(12.5 x 106)
88.2 (191)
20
16 - 35
.
aEvaporator operated with only one burner
23
-------
SECTION VI
DISCUSSION
PROCESS EQUIPMENT
Phase I - Tests Using Water-Cooled Downcomer
Steady state conditions were achieved during this phase which allowed
the dry recycle system to "be tested. Dried grain was successfully mixed
with pressed grain and concentrate (20 percent) and dried.
Analyses of the products of combustion from each burner using an Orsat
apparatus indicated near perfect combustion with only negligible excess
oxygen. An Orsat apparatus exposes a measured sample of exhaust gases
to reagents which absorb carbon dioxide, oxygen, and carbon monoxide;
nitrogen is determined by difference. The feed rate was considerably
less than design. The heat input required was much higher than expected
and a considerable heat loss, largely due to the downcomer cooling
system, was discovered. Inspection of the evaporator interior following
test runs revealed no build-up of solids on the downcomer jackets or
tank surfaces. Minimal charred grain was observed at the burner tip
only where the flame directly hits a baffle to divert the hot gases
upward and where the inlet feed is injected into the vessel. Small
pieces of broken refractory were found at the bottom of the evaporator
drain line. After the final test it was discovered that the deflector
plate on one downcomer had broken off and fallen to the bottom of the
vessel. No cause for this failure was immediately apparent.
Phase II - Tests Using Jacketed Downcomer and Closed Loop Cooling System
Actual tests with this system revealed that a coating of burnt liquor
built up on the weir of the downcomer within 31 hours of operation. This
coating functioned as an insulator and caused the temperature of the heat
transfer oil to reach 171°C (3^0°F) by the time the test was called off.
Inspection of the downcomer deflector plates showed that these had
partially broken off from the downcomer. At this time it was also
discovered that demister on the evaporator stack had become clogged and
a decision was made to remove the demister until a more satisfactory
location could be determined. The demister was not in place during the
latter phases of the experiment.
2k
-------
Phase III - Tests Using Non-Jacketed Downcomer
The evaporator performed under steady state conditions for 2? hours using
this downcomer configuration. Some foaming of the liquor was detected
until the 22 percent solids level was reached. During this time, the
concentrate from the evaporator was mixed with waste yeast and dried
grain and fed to the dryer.
After 57 hours of operation one downcomer failed. The test was terminated
and a visual inspection of the interior was made. Fire brick had broken
loose on both downcomers due to insufficient support, and the shell on
the one downcomer had buckled due to excessive heat.
Data analysis of the first series of tests indicated that the blower was
delivering insufficient air for complete combustion of the gas being
added, resulting in the poor thermal efficiencies noted. It was deter-
mined that an adjustment in the gas flow rate was necessary to establish
a proper fuel-air mixture with the blower output, and that a possibility
existed that air delivery capacity of the blower might be insufficient
for the rate of evaporation desired. It was also discovered that opera-
tion of the evaporator without the demister indicated higher than actual
evaporation rates, due to significant entrainment of liquor in the stack
gases.
Phase IV - Tests Using Inconel Downcomer
Two downcomer designs were evaluated in this test. The non-jacketed
downcomer failed after 6 days of operation due to a split of a circum-
ferential weld. The jacketed downcomer remained in operation for 12
days until the test was terminated. A post-test inspection revealed a
deflector plate failure on this downcomer.
Performance of the overall system in this test was excellent. All
concentrate produced was mixed with dried grain and fed to the dryer with
pressed grain and waste yeast. By reducing the firing rate by 25 percent
the smoke and odor from the evaporator stack became barely perceptible.
Efficiency checks performed after this series of tests revealed increas-
ing the air to gas ratio did not boost the evaporation rate as had
previously been thought. In fact, the evaporation rate dropped off at
high air to gas ratios.
Based upon the results of these tests, two similar downcomers were
fabricated without gas nozzles on the sides. The evaporator ran for 23
consecutive days in this series of tests. Inspection revealed that
the air-cooled downcomer had bulged out in one small area. A large
deposit of burnt liquor had formed at the bottom of the downcomer
impeding the flow of liquor up inside the weir. Several of the gas out-
let holes had started to burn open. The non-jacketed refractory-lined
25
-------
downcomer had burned upon at the lower weld of a metal band which had
been welded on to repair a split from a previous test. The deflector
plate was in good condition.
Phase V - Evaporator Performance Using Downcomer Cooled with Dilution Air
The redesigned evaporator using a jacketed, cooled downcomer was
operated for several extended periods, ranging up to 3^ days. Inspection
of the downcomer at periodic intervals revealed no build-up of solids or
any mechanical damage. At most about 0.6 cm (0.25 in) of 1Imud" was
detected on the downcomer wall and surrounding weir. This material was
not caked on and could be easily removed. The final inspection of the
evaporator revealed a break in the air piping supplying cooling air to
the downcomer.
No further testing or development work was carried out because of gas
curtailments which began in late 1972 and carried over into 1973- Gas
shortages threatened the ability of the gas supplier to the Houston
Brewery to meet its service obligations to its customers. Therefore,
the Texas Railroad Commission which regulates gas utilities in that
state, authorized the institution of a curtailment plan to assure gas
supplies to homes, hospitals, and the like. One curtailment was
experienced which lasted several days and shut down all production at
the brewery.
EFFLUENT STRENGTH REDUCTION
Initial plans called for a long term study of the brewery effluent both
with and without the benefit of the spent liquor evaporator. The deci-
sion to use only one burner and downcomer at a time during the latter
stages of the development phase restricted the amount of the spent
grain liquor which the evaporator could concentrate.
The effects, then, of having an evaporator installation sufficient to
concentrate all the spent grain liquor could not be measured. The
approximate effect, however, can be determined by deducting the pollutant
load from the spent grain liquor, using established data, from the meas-
ured pollutant load from the brewery without evaporation of the liquor.
This calculation is shown in Table 7 for the Houston Brewery. Projected
reductions in B.O.D.r, C.O.D. and suspended solids are all quite signi-
ficant, ranging from ^3-5 percent up to 60.3 percent.
ECONOMICS
Table 8 shows the estimated capital and operating costs of an evaporation
system designed for a brewery having a production capacity of 2.35 million
hectoliters (2 million barrels) per year. Three situations are illustrated,
one using low-cost fuel, assumed to be natural gas at 800 per million
Kg-cal (200 per million BTU), one using fuel at $1.60 per million KG-cal
26
-------
Table 7. PROJECTED EFFLUENT IMPROVEMENT
Parameter
Total effluent
with liquor
Spent grain liquor
Total effluent
without liquor
Percent reduction
Flow
cu m/day
(mgd)
71*00
(1-96)
300
(0.08)
7100
(1.88)
IK 08
BOD5
mg/1 Kg/day (Ibs/day)
1,760 13,060 (28,770)
18,750 5,680 (12,510)
I,0l40 7,360 (16,260)
1*0.9 **3.5
COD
mg/1 Kg/day (Ibs/day)
3,01*0 22,560 (1*9,690)
38,150 11,550 (25,1*50)
1,550 11,010 (2^,2UO)
U9.0 51.2
mg/1
850
12,550
350
58.8
S.S.
Kg/day
6,310
3,800
2,510
60.3
(Ibs/day)
(13,890)
(8,370)
(5,520)
ro
-------
Table 8. ECONOMICS OF ADDING SPENT GRAIN
LIQUOR CONCENTRATOR TO EXISTING DRYING OPERATION
Fuel Cost, $/million Kg-cal
Evaporator
Capital cost
Annual yield of additional dried grain @
$55.00/metric ton ($50.00/ton)
Incremental costs of operating
Concentrator in addition to dryer ($/yr)
Maintenance @ 5$
Labor
. Property tax and insurance
Evaporator fuel (nat. gas)
Evaporator steam
Additional fuel to dry concentrate
and screenings/ cake
R.O.I., % (assuming 15 yr. life
with no salvage value)
0.80
Submerged
Combustion
$425,000
226,800
21,300
18,000
9,500
1*3,800
25,200
15.09
Multiple-
Effect
$680,000
226,800
3^,000
18,000
15,300
28,600
25,000
8.09
1.60
Submerged
Combustion
$1*25,000
226,800
21,300
18,000
9,500
87,600
50,lKX)
2.80
Multiple-
Effect
$680,000
226,800
3U,000
18,000
15,300
1*5, too
50,1*00
2.80
3.20
Submerged
Combustion
$1*25,000
226,800
21,300
18,000
9,500
175,200
100,800
No return
on investment
Multiple-
Effect
$680,000
226,800
3^,000
18,000
15,300
78,900
100,800
No return
on investment
TO'
00
-------
per million BTU), and another using relatively high-cost fuel, such
as natural gas at $3-20 per million Kg-cal (800 per million BTU), or
No. 2 oil at k<£ per liter (160 per gallon). The value assumed for low
cost fuel is typical for those areas where natural gas has historically
been readily available and there have been few, if any, interruptions
to industrial customers. The value assumed for high cost fuel would
apply to those areas where natural gas is not available to industrial
customers on a year-round basis. This figure allows for an equivalent
amount of No. 2 oil to be burned during gas interruption or at all times
if necessary.
For each condition two cases are illustrated. The first case utilizes
a submerged combustion evaporator system as demonstrated. The second
case involves the use of a conventional multiple-effect evaporation with
solid bowl centrifuges provided to reduce the suspended solids load and
thereby minimize the fouling potential. Three systems such as these
have recently become operational in U.S. breweries.
The R.O.I. (Return on Investment) percentages calculated in Table 8
indicate that submerged combustion is the process of choice when fuel
at less than $1.60 per million Kg-cal (UO(Z$ per million BTU) is available.
At low fuel cost the return is attractive enough on the investment to
suggest its funding irrespective of pollution control consideration.
A far different situation is presented for the case of high cost fuel.
Here neither submerged combustion nor conventional evaporation can be
economically justified on the basis of product recovery alone. In
cases where some type of control system is mandatory to reduce waste
loadings, conventional evaporation would be far less costly due to its
greater efficiency.
29
-------
SECTION VII
REFERENCES
1. O'Rourke, J. T., and H. D. Tomlinson. Effects of Brewery Wastes
on Treatment. Industrial Water and Wastes. 7 (5): 119-127*
September-October 1962.
2. Stein, J. L., J. H. Dokos, T. Brodeur, and M. R. Radecki. Concen-
tration of Brewery Spent Grain Liquor Using a Submerged Combustion
Evaporator. In: Food Processing Waste Management, Proceedings
of the 1973 Cornell Agricultural Waste Management Conference.
Ithaca, Cornell University, 1973- P- 150-l6o.
3. Mulligan, T. J. Characteristics and Treatment of Brewery Wastes.
Brewers Digest, k-2: 82-88, August 1967.
k. LeSeelleur, L. A. A Perspective on Brewery Effluents. Technical
Quarterly of the Master Brewers Association of America. 8 (l):
52-62, January 1971.
5. Schwartz, H. G., Jr., and R. H. Jones. Characterization and
Treatment of Brewery Wastes. In: Proceedings Third National
Symposium on Food Processing Wastes. Corvallis, U. S. Environmental
Protection Agency, 1972. p. 371-^00.
6. McWhorter, T. R., and R. J. Zielinski. Waste Treatment for the
Pabst Brewery at Perry, Georgia. Wiedeman and Singleton Engineers.
(Presented at 26th Annual Purdue Industrial Waste Conference.
West Lafayette. May 4-6, 1971.) 1^ p.
7. Perry, R. H., C. H. Chilton, and S. D. Kirkpatrick. Chemical
Engineers Handbook. New York, McGraw-Hill, In.c, 1963. 1901 p.
8. Lowe, E., and E. L. Durkee. Salt Reclamation from Food Processing
Brines. In: Second Food Wastes Symposium Proceedings. Corvallis,
U. S. Environmental Protection Agency, 1971. p. 7^-84.
30
-------
9- Antony, A. P., and R. M. Ahlgren. Modern Handling Methods for
Grain Effluents. Aqua-Chem, Inc. (Presented at the Southeastern
Quarterly Meeting of the Master Brewers Association of America.
Fort Lauderdale. June 12, 1971.) 8 p.
10. Hernandez, R., M. R. Radecki, G. A. Eckman, M. R. Doering, P. E.
Haley, R. J. Wekeriborg, and E. W. Erker. Processing of Liquid
Brewery Wastes. Anheuser-Busch, Inc. (Presented at the Seventy-
Second National Meeting of the American Institute of Chemical
Engineers, Symposium on the Processing of Liquid Wastes in the Food
Industry. St. Louis. May 21-2^, 1972.) 18 p.
31
-------
SECTION VIII
GLOSSARY
B.O.D.c Five-day "biochemical oxygen demand. The quantity of oxygen
utilized in the "biochemical oxidation of organic matter under standard
laboratory procedure in five days at 20°C, expressed in milligrams per
liter.
Demister - A device for removing entrained liquid from a vapor stream.
Downcomer A cylindrical duct used to direct hot gases from a "burner
into a liquid from which water is to be evaporated.
Entrainment - The carrying off of a liquid as a fine mist or spray by
a vapor rising from a heat exchange surface.
Firebox - Combustion chamber.
Inconel 601 A heat and corrosion resistant nickel-chromium alloy.
Insoluble Solids - Solids removable by laboratory filtering. Suspended
solids.
Multiple-Effect Evaporator - A series of evaporative bodies so connected
that the vapor from one body is the heating medium for the next body.
Panel Coil - A heat transfer device fabricated from two embossed metal
sheets welded to form a series of passes through which a heating or
cooling media flows.
Recompression Evaporator - An evaporator in which vapors which have
been boiled off the heat exchange surface are compressed to raise the
energy level and then fed back inside the heat exchanger where they
then condense.
Solid Bowl Centrifuge - A centrifuge which utilizes a spinning cylinder
to cause particles to settle out along the wall. Frequently provided
with a screw conveyor inside the bowl in order to push collected sediment
out of the machine.
32
-------
Soluble Solids - Total solids less insoluble solids.
Suspended Solids - Insoluble solids.
SWECO (g) Screen - An eccentric-weighted horizontal disc screen as made by
SWECO, Inc.
o
Total Solids - Residue on evaporation to dryness at 103 C.
33
-------
SECTION IX
APPENDICES
A. Evaporator Tests Using Water-Cooled Downcomer -
Series 1 36
B. Evaporator Tests Using Water-Cooled Downcomer -
Series 2 14.3
C. Water-Cooled Downcomer Tests - Feed and Product
Samples from Series 1 14.0,
D. Water-Cooled Downcomer Tests - Feed and Product
Samples from Series 2 57
E. Evaporator Tests Using Water-Cooled Downcomer -
Orsat Analyses 63
F. Evaporator Tests Using Jacketed Downcomer and
Closed Loop Cooling System 6^
G. Jacketed Downcomer Tests - Feed and Product
Samples 72
H. Evaporator Tests Using Non-Jacketed Downcomer 75
I. Non-Jacketed Downcomer Tests - Feed and Product
Samples 80
J. Evaporator Tests Using Inconel 601 Downcomer -
Series 1 8^
K. Inconel 601 Downcomer Tests - Series 1 -
Feed and Product Samples 93
L. Evaporator Tests Using Inconel 601 Downcomer -
Series 2 90,
-------
Page
M. Inconel 601 Downcomer Tests - Series 2
Feed and Product Samples 10U
N. Evaporator Tests Using Jacketed Downcomer
Cooled with Dilution Air 109
0. Effluent Sampling with Evaporator Operating 113
P. Effluent Sampling with Evaporator Not Operating llU
35
-------
APPENDIX A - EVAPORATOR TESTS USING
OJ
?-.^l Lsvois V. T^r.p. CoolinK Water
Zi " r;
-'81/-J.
1:15
1 15?
:.::;
i i -.J
H55
8::>
2:1-
2::;
2:-5
*«
- 'i')
'-.r. 3J '" LI
1:
2
£ i "
I : '<.
i '/ 1 li
i >i- 1 U
1
2 l^-=
i
2 5= 13U
1
1
2 >- i^i'
a -N 92 tV'
i
i
i':. Fl«r Inlot Out Tomp.
I'K Bait Water
CF 1 2 Temp. #1 gS
92.5
93. ?
93.7-
92.5
93.
93.5
91.0
83.
87.0
91.5
TO. 5
92.5
vo.
92.5
93.0
93.0
93.0
92.5
93.0
90.0
88.
67.5
91.0
90.0
91.0
70.
130 132
132 13J
132 133
132 13't
132 13'i
132 133
135 131*
135 13U
136 137
133 13'»
133 13U
132 133
Tomp.
Out
Evap.
Moyno
121
121
122
122
10,
125
189
130
132
13U
136
137
J.ar.er
Set Pt. Set Pt.. Set Pt . Spe.'ifio f*t Pt. Air
Feed Evap. Ccno. ,-travitv ~ry Blcwer ?
FCV F^T :.;c-yr.c .:..-. ri'.'y.'le -taos 1 2
0
0
1.2
25
18
6
i)
11
0
0
8
8
7
8
0 0
0 v-
psig
111 0 C
psig
6 00
peig
0 0 C
psig
5«- o r
0
fair.
5& 0 c
psig
** 0 C
0 1/10
psig
5* 0 2/10
5
--
as
S5
35
S5
-------
;.:. :/i/O:: '',. ";::&.
~-;2. ;l. '"' '-- TT *>
Z » * ^ ^*" i >
::"-> 5 ;-": 19-
3:25 a i'>
: = :5 i SC 1*
3:-5 2 9c
::;; \ ICC 1^
1
-:2C 2 95 l%k
1::C 2 92 18U
-:;*; 2 9?
-..'. \ *'.'.. ift
s . « * j ^? i flt-
X»'^ - /. J..T
2_
'.'oolini; VA'il
F'lov; Inlet
l:-.i.r. Vnt.fr
i 2 Temp.
9?.o
03.5
90.5
92.0
92.5
93.5
90.5
91.0
92.5,
5?. 5
91.5
92.0
91.0
90.5
90.5
92.0
92.0
92.5
90.
91.0
9L5
90.0
92.5
93.0
.'r
Out
fi-
131
132
132
132
131
131
131
131
130
130
131
130
Temp.
132
133
133
133
132
132
131
132
132
132
132
132
Tomp. . SuiT.sr
Out Set PI. Sot Pt . ;Vv Pt. s'iv.-ii':.- j>o: ?-. . Air
Rvap. Fe«"d Evap. Oor..-. wraviry ?ry Blcver ?
Moyno FCV F.T ML-.V-X .V::.-. He.-. .-I? .tips 1 ^
137 P 5
138 8
10 psig
lUo 1.2 5
10
Ito 12 55
10
lltl 12 0 2/10
I'tS 9
l'*3 l» i»^
2 psig
l'(l» 'i li^ 0 5/10 65
1 hli O(I
.tt^ e,^
10 psig
lUU 8-lU 5-6
5 psig
fl
ll»5 10
lU psig
ll«6 15 5$
-------
~. " ''''<', ~' r.p.
:-^ S -i"% LI
-21 "I 1
;:-; 2 '-1 1?U
1
1
^:-5 2 10*"/-1- 1s''
1
M5 2 ir.* i?ij
i
":-; £ 1V> 1%.
1 ICO
*:15 £ IV, IV,- 15U
i
U) ?:-5 2 I":4- 13U
00
5:15 2 IV,* 151*
1
5:-> £ IV, l?:'i
i
1C:!? 2 ""CO- 1?1*
1
ii:-; = ;ii+ 3'':'.
i
11:15 2 I'/,- I':-
z.
ll:-5 £ IV. + l'-1-
Ono.lim
rr Wntrr
l-'i'.w itili-i uuL
l-it... Wal.'.-r
"? 1 2 Temp. #1
50.0
91.5
9^.0
88.5
87.0
90.
90.
92.5
V',.0
93.0
'..T-.O
Vj.O
r/',.0
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91.0
92.0
88.5
87.5
88.
88.5
92.0
9*.5
92.5
C0.0
93.0
92.0
132
131
130
132
13'»
I
133
131
130
130
129
in
12y
129
IViiip.
#2
133
132
132
133
133
133
132
131
131
130
130
130
130
Temp.
z--,-.,-
Out Ufl 1't. Jol i'l . Jc' rt . J^-.'.-i :'l _ ^\'*. i\ . (Ter.o. ' Air
I^ap. Focd Ev-.-ip. >VH.-. .iv-.v'. ty ?!-.; Blower ?"
Moyno FCV FOV Hcvnr- >r..-. Recycle A.-DS ' " '
1U6
1U7
ll»7
lU8
150
159
163
166
]'.n
171
173
)YH
375
10
11
6
6
10
10
6
7
7
8
0
2
10
10-13
10
10
3
1*
10
10-lh
13
I'j
9
10
press
54-
psig
% 3A
psig
5
psig
5
psig
5
Sl-f
psig
"i
psig
"*
psig
'i. )->. 5
psifl
'j.5
psig
5
S5
A:-P3
' 5? 125
;-: 125
?- 125
90
>V 12?
V 125
-------
VO
r .'.-I /..:): >,. 7'.r/p.
~rir.* '.^r. "" CF LI °F
is"= = i 100- i?:-
i
12:1-; s 100+ i?i:
1:15 £ 100+ 1%
1
1:1; 2 i:'_- l?i-
£:15 2 100- 151*
1
5:1? 2 100+ 151.
1
;:15 2 100+ 1^
1
;:-5 2 100+ 13k
1
1:15 2 100+ 15I»
, 1
1;-? 2 100+ 19k
1
5:15 2 100+ 19*
1
>:-5 S 100+ 19:
i
^:15 2 100- 151;
?:-5 2 10C+ 15U
I'm
Flow
hate
1 2
S--.5
90.0
92.5
92.5
93.0
93.0
93.0
93.5
93.5
93-5
92.5
93.0
93.5
S6-0
92.5
89.0
92.5
91.0
91.5
92.5
91.5
92.5
92.0
92.5
91.5
92.5
92.0
92.0
J3nr; W'if.'T
Inlet Out
Water
Terop. #1
129
130
129
129
128
128
127
127
128
127
126
126
126
126
Temp.
#2
130
131
130
130
129
129
129
128
129
129
128
128
128
128
Tr-mp.
Out
Evup.
Moyno
176
177
177
177
177
178
177
177
r.r
177
176
176
176
176
8
9
12
Ih
8
8
8
9
10
12
10
12
10
12
9
10
12
11*
31
12
10
11
10
11
10
12
10
11
Set Pt.
Feed
FCV
press
5
psig
5
psig
5
psig
5
psig
5.5
psig
5.5
psig
5.5
psig
5
psig
5
psir
5.5
5
5.5
psig
5
5
Set Pt.. jet >-.. S-os:ii'i; fe*. Pt. Air
Evap. A-IIO. Gravity ?ry Blower p
FCV Mcyno Ccr.c. Recycle flnps 1 2
90
°o
90
90
90
90
90
90
92
90
90
90
90
90
-------
7-;^' !: .*!.- >/ TW.D.
":iL :-J;-.. ~r: '-i Li '-v
-/££'" 1
-!i; & 2 io'.+ I'M
!
-;!i5 2 100+ 18U
1
5:15 2 100+ 1SU
1
?:L; 2 ;<-5&- 19U
1
5:15 2 =-53 I8fc
i
5:1-5 2 5--5? 16U
1
10:15 2 5*- 18U
1
10;!-5 2 92 18U
1
11:15 2 IOC 1?U
Tsnp.
1 100 Stack
ll:l-5% 2 ICO SO 18U 187
1 100
12:15 2 100 75 17<
1 Lr r-.ar.^ei
1:15 2 LT :-'*r.ij': 1% 127
1 0.
1:;0 2 12 1*\iu-. CiJtxvlty Try Blower ?
FCV Moyr.o CCr.c. Eecycle A=ps 1 2
90
90
85
90
91
98
93
95
Feed Air Air
20 In Burner
9 1?0 3.75 95
0 95
0 130 .6 75
5. "5 97
-------
Lf.':
~'-e. ".}
-,'".'"1 r
-
2;!-; 2
;_
;:15 2
T
2 :-; 2
_
^:15 2
T_
l:i-5 2
T_
r 5:1; S
i
5;l-x 2
1
6:15 2
2.
^ :-? 2
1
":15
'':-; 2
1
8:15 2
-":" -.-.
. - ^ ^_ . -iy .
r;;
100
100 82
"Sr
87
"5
n
"
100
I'/i 8-0
:oo
100 100+
100
100 100+
100
100 100+
100 +
100
100 100 +
'-lr '/ T'-p.p.
CF LI °F
175
185
185 80 158
185 80 157
185 81 15*,
185 81 151*
185 81 15U
185 100 153
185 100
185 90
185
1-5
18-
r,'oolinp! Wnt.er
1
y.
91.
92.
93.
92.
93.
92.
92.
88.
90.
00.
92.
90.
riuw inlul
rvil.': V/.-lt.c.T
2 Temp.
92.
91-
92.
93.5
5 93.0
0 92.5
o 92.0
0 93.0 5U
90. 58
88. 66
90.
90. 7U
91. 66
(nil
#1
119
126
126
125
123
122
123
125
129
125
IP?
127
127
'LVnip .
#2
121
127
126
125
12l>
123
12U
121*
130
127
1214
129
129
Temp.
uul.
Kvap.
Moyno
1U9
ll*7
1UU
1U3
11*2
lUl
137
160
:67
177
iflo
170
175
y«-u pi. -^i PI. Jci PI. i-p-.-.-ir;.- -' -' ;" ^ir
Fooi Ev:\p. >V:u-. CIr:u-i-..v rs-y ?lov-.>r ?
FCV FCV Moyno Ccnc. Recycle A=ps 1 2
7
10
I'l psig
16 5.5 100
10 psig
12 5i ?5
18 psig
20 6 22
11
lU 21.5 100
1"» psig o CP
16 5.5 185 100 125 F 30
21.5 137 125 2.75
oo
20
-------
:*-.*.'
VC.V'
*r
r: iVt!
T!
.«.]-. '; 7':rp.
c? LI °F
Cor.lll
i? Water
Flow Inlet Out
Hate Water
1 ?. Temp. #1
Tomp .
#2
Temp.
Out
Evap.
Moyno
B-.:rr.er
Set Pt. Set Pt. Set. Pt . Speoifio :?*- ?t. Air
Feed Evap. Cono. Gravity ?ry Blower ?
FCV FCV Moyno Cono. Recycle Anus 1 2
, . f , r/.
-'*-:, ~
5:15
10:15
11:15
:./22/71
12:15
1:15
8:15
3:15
1:15
5:15
7:15
^£0
2 1'
2
1
2
1
2
1
2
2
1
2
1
2
1
2
1
2
1
2
1
2
>0 100+
:r.'/+
100+
100+
100+
^..%
7^-75
57-50
90-92
90-92
100+
100+
195 91*
195 100
195 72-7U
185 38-1*0
195 0
185 30
185 85
185 27
185 50 172
135
165
1%
90.
90.
90.
91.5
91.0
90.0
88.5
fW.O
89.0
90.5
90. -J
Cd.o
91.
90.
90.5
90.5
90.0
90.0
89.0
88.0
88.5
90.0
90.0
IR.O
129
130
130
130
129
132
13U
135
13U
133
132
131
130
130
130
131
130
133
135
136
135
13U
133
13J
178
178
180
179
178
178
177
181
181
181
180
177
22
25
16
18
7
9
0
1
28
30
IP
20
22
2k
21
23
21
23
15
17
12
psig
6
Psig
6
psig
5
psig
3
psig
6.5
psip
6
psig
6
Psig
6+
psig
6+
psif.
b+
psig
'-> .V'i
32 c2-
30+
30+
30+
30+
2U
2,
27
28
28
29i
<0
-------
APPENDIX B - EVAPORATOR TESTS USING
WATER-COOLED DOWNCOMER - SERIES 2
Date/
Tire
5/W71
5:05 M
9:20
9:35
9:55
10:35
11:05
11:&0
5/15/71
12:15 AH
12:U5
1:20
2:00
Svap.
Fuel
Valve
tc
Open
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
0
0
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
Levels & Temp.
5vap.
LI °F
U"
13
27
W
15
56"
s
17
So
17
5T
1U.5
50
1325
Tr
17.0
16.0
51
n. 7g
"»3
1U.75
'S
Cone.
Tank
Stack
LI °F
Cooling Water
Flew Inlet Out
Rate Water
1 2 Temp, #1
Temp.
#2
n
0
0
0
0
0
0
0
0
0
0
0
0
185
190
190
190
190
189
189
190
190
92
92
92
91
89
72
91
93
92
90
90
92
95 78 F
95 136
131
96 137
95 135
93 76°F 138
95
95
95
95
93.5
9!*
95
133
135
133
135
137
136
iS6-
135
135
133
132
13j*
132
133
135
136
131
130
131
lit
ill
131
132
T3o~
Tomp. Flow Controls
Out Set Pt.
. Evap . Feed Gas
Moyno FCV #1
116
113
26
ll*3 26"
1U5
11*7
1U8
1U8
32
ll*9 30
151*
165 35
16U 3U"
37.5
167 37.5
31
170 3T
psig
U.75
psig
5.25
psig
5.75
psig
5.5
psig
5-5
11.25
12.5
12.75
12.25
12.U
12.5
12.25
11.60
11.2
No
V/ater
12.7
Gas
#2
10.70
11.90
12.20
11.75
12.00
12.1
12.0
11.9
12.1
12.0
12.0
Anns
100
107
108
105
107
108-
109
109-
110
105
10U
10U
10 U
Gas
Press
U.O
3-9
3.8-
3-9
U.O
3.9
3.9
3.95
3.93
3.9
3.0+
3-9+
Pressures
Blcwer
Out
P/T
8U-86
6U-86
83-85
83-65
83-85
83-86
117
83-85
115
83-85
115
8U-35
-liTT
8U-86
115
in
86-87
111
Burner
Air
P
1 2
22-
29
21-
23
21-
28
22-
28
22-
30
22-
29
20-
30
22-
29
22-
30
22-
23
21-
29
21-
29
21-
29
22-
23
22-
30
21-
29
20-
30
23-
29
20-
30
-------
Svap.
Levels & Temp.
Pressures
Date./
5/iVn
2:25 A:-!
3:00
3*0
U:15
5:00
5:U5
6:30
6:Uo
7:25
8:00
8:00
6:55
9:35
Valve
l^.r.
1
2
1
2
1
2
1
2
1
2
1
2
2
1
2
1
2
1
2
1
2
1
2
1
2
15
15
15
15
15
15
15
15
15
15
15
15
0
15
0
15
15
15
15
15
15
15
15
15
Cone
Tank
Evap.
LI °F LI
'-7
17
55
12
Ti22
15.0
50
IT
12.25
12-0
18.0
59
1U
15
50
0
0
0
0
0
0
#1 Burner
0
0
#1 Burner
0
0
0
. Cooling Water
Stack
°F
190
190
191
190
190
Out -
185
18U
On
191
191
191
Flow Inlet
Rate Water
1 2 Temp.
88
91
92
91
91
91
Coil
91
91
90
82
85
92
9U
9U
95
*
*
Burnt
t
95
95
92.5
86
88 76°F
Out
ill
133
1*
130
122
130
131
131
99
97
131
131
132
Temp.
#2
121
130
132
122
129
129
127
128
128
125
121*
130
130
129
Temp. Flow Controls
Out Set Pt.
Evap. Feed Gas
Moyno FCV #1
170
171
171
168
168
170
168
16U
162
161
163
$
11
31
ho
JO
$
12
33
31
ii
15
20
20
10
10
*
as.
32
psig
5.5 12.8
5.5 12.8
psig
6.0 12.9
psig
5.5 12.7
psig
5.5 12.6
5.5 12.6
psig
U.2
--
psig
U 12.7
13.2
psig
5.6 12.75
Gas
U.9
11.9
11.9
11.9
11.9
11.9
12.9
12.8
11.7
12.0
11.9
Gas
A.T.P Press
10S 3.9+
108 fs.9+
110 3.9+
108 3.9+
109 3.9+
108 3.9+
89 U.2
91 l*.2
106 3.9+
106 3.9+
106 3.9
Blower
Cut
P/T
Sfi*
85*36
112
85-36
110
%P
85-87
107
85-87
107
91-92
112
22
117
85-87
8U-85
122
8U-85
120
Burr.er
Air
P
1 2
22-
29
2U-
30
23-
3P
22-
29
22-
29
22-
28
20-
30
2U-
29
2U-
30
23-
31
2!»-
29
2U-
29
2U-
29
23-
30
20-
30
22-
29
21-
27
-------
i-.-ap.
Fuel
Valve
Iir.e C^er.
5/1U/71
10:00 A;-!
10:30
11:00
11:35
12:00 N
-
1 12:30
1:00 PM
1:30
2:00
2:?0
3s30
U:30
5:30
6:30
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
.15
15
15
15
15
15
15
15
15
15
Lsvels & Temp.
Cone.
Tank
Evap. Stack
LI °T LI °F
i
15.75
52
~W
15.75
15.0
T*o~
12.25
uo
10.75
35
10.25
33
10.75
35
11. g
?7
12.0
39
11.0
35
10.1
35
10.5
35
0
190 o
0
190 o
189 o
190 o
190 o
190 o
190 o
0
190 o
190 o
190 n
190 sf<%
191
120
155
191
190
191
192
191
191
Ipl
191
190
190
190
Flow
Rate
1 2
8U
85
8U
85
83
8U
8U
82
85
87
88
87
87
87
87
90
89
88
88
88
87
87
88
92
92
92
92
93
Cooling
Inlet
Water
Temp.
125
120
121
121
--
120
120
120
120
121
120
120
Water
Out
#1
132
132
132
132
132
128
127
127
127
125
12U
123
122
122
Temp.
#2
130
130
130
129
130
125
125
126
125
122
122
121
120
120
Temp. Flow Controls
Out Set Pt.
Evap. Feed Gas
Moyno FCV #1
163
161.
16U
165
163
160
155
152
1U9
lU7
1U2
138
153
16U
3U
If
12
33
"32^5
31
30
21
30
22
33
25
-*-*-
35
27
36"
21
36
35
3?
2i
32
2£
31
i
2£
35
5.7
press
5.25
psig
5.25
psig
5.5
psig
5.75
psig
5.75
psig
6.0
psig
6.0
psig
5.75
psig
5.5
psig
5.5
psig
6.0
psig
6.0
12.90
12.75
12.70
12.75
12.7
12.8
12.8
13.0
13.0
12.7
12.7
12.5
12.6
12.5
Gas
#2
12.00
12.0
11.9
11.9
12.0
12.3
12.3
12.3
12.2
12.2
12.1
12.2
12.0
12.2
Ar.p
106
106
105
105
105
105
109
109
109
106
105
105
105
105
Gas
Press
2.99
3.95
3.98
3.95
U.o
U.O
U.O
U.O
U.o
U.O
U.o
U.O
U.O
U.c
Pressures
Blcwer
Cut
P/T
83-65
83-85
125^
83-3U
127
8U-85
127
82-83
130
82-83
130
82-8U
125
82-83
127
62-83
125
62-83
"12T
83-BU
128"
83-81*
130
62-8U
83-8U
127
Burner
Air
P
1 2
22-
28
22-
29
20-
29
22-
27
22-
27
22-
28
22-
28
22-
28
_
22-
28
22-
28
22-
28
22-
28
21-
29
22-
29
22-
28
20-
28
20-
23
21-
29
20-
29
20-
23
22-
28
22-
28
22-
28
22-
23
20-
28
-------
lir.e
5/15/71
7:30 PM
3:30
9:20
10:30
11:30
v 5/16/71
12:30 AM
1:30
2:30
3:30
U:30
5:20
6:30
7:25
8:30
Z rap .
Fuel
Valve
to
Coar.
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
Levels
Evap.
LI CF
10.5
35
10.5
35
10.5
25
10.5
25
10.5
35
10.6
35
10.5
35
10.5
35.0
10.5
35
10.5
35
10.5
35
10.5
35
10.1
35
10.5
35
190
190
190
190
190
190
190
190
190
190
190
190
190
& Temp.
Cone.
Tank
Stack
LI °F
uu$ 190
56£ 190
72* 191
82-t 191
9ki 191
~75U°F 192
51.0%
153°F 192
6?!
153 192
193
82^
150 192.5
90^
1U"8 192
98^
l55°F 192
192
100$
192
Pressures
Flow
Rate
1 2
95
95
92
90
90
90
90
91
90
85
85
86
86
89
90
90
87
85
85
86
85
86
85
90
90
90
91
9U
Cooling
Inlet
Water
Temp.
119
120
119
121
121
125
117
117
123
121
121
122
120
120
Water
Out
12U
121
121
125
125
123
112.5
123
122
121
122
119
120
118
Temp.
ife
122
120
119
122
123
122
121
122
120
120
120
120
119
116
Temp.
Out
Evap.
Moyno
166
180
175
176
--
178
166
168
16U
161
16U
166
160
168
Flow Controls
Set Pt.
Feed Gas
FCV #1
2i
35
2i
35
36
35
26
35
26
35
'1
2£
3^
$
press
6.0
psig
6.0
psig
6.0
psig
6.0
psig
6.0
psig
5.6
psig
5.7
psig
5.8
psig
5.8
psig
5.8
psig
6.0
psig
6.0
12. U
12. U
12.7
12.7
12.7
12.6
12.5
12.7
12.5
11.7
12. U
12.3
12.5
12.5
Gas
#2
12.2
12.1
12.1
12.1
11.9
11.8
11.8
11.9
11.9
12.6
11.8
11.7
H.9
11.9
Amp
105
105
105
108
108
108
108
108
108
108
108
103
108
10?
Gas
Press
U.O
U.O
U.O
U.O
U.O
U.O
U.O
U.O
U.O
U.O
U.O
3.95
3-95
?.95
Blcwer
Cut
P/T
83-8U
125
8U-35
125
8U-85
120
8U-85
020
8U-85
120
8U-B5
117.5
85.0
utr
85.0
119
85
85
tar
85. |?
86.0CF
115°F
85_.5
135°
8g
120
Burner
Air
P
1 2
22-
23
22-
28
22-
29
22-
23
22-
28
23-
28
22-
28
23-
28
23-
28
23-
28
23-
28
23-
28
23-
23
2,_
28
20-
23
20-
28
20-
23
20-
28
20-
23
28
23-
28
23-
28
27-
28
23-
28
23-
28
23-
28
23-
23
23-
23
-------
Date/
Tir.e
5/16/71
9:30 AX
10:30
11:30
1:00
1:30
"^
2:00
2:U5
2:U°
U:05
5:05
5:30
c:00
:30
Evap.
Fuel
Valve
tc
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
15
15
15
15
15
15
12
12
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
Levels &
LI
10.5
55
10J.
55
10^5
?5
10.5
33
10.5
35
2-22
32
9.50
31
9.50
21.5
'l-'2
7.5
'2
9.?5
31-32
9-6
2
9.75
:-2
9.5
'CF
190
190
190
(
192 '
192
192
192
192
102
192
192
192
Temp.
Cone.
Pressures
Cooling Water
Tank Flow Inlet
Stack Kate Water
LI F 1 2 Temp.
ioo?£ 150 85
100$ 151 85
100$ 153 86
100$ 87
100^ 90
100 88
91
92
86
132 90
92
763 91
70 90
90 120
90 120
92 130
91
95 76
93 77
96
97
90
9U
96
95
91*
Out
#1
118
119
119
120
118
119
117
117
121
119
120
120
119
Temp.
#2
117
117
118
118
116
116
116
116
119
117
117.5
118.0
121
Temp. Flow Controls
Out Set Pt.
Evap. Feed Gas Gas
Moyno FCV #1 &
167
168
168
172
170
178
172
173
173
173
173
17U
36 press
3& 5.7 12.5
36 psig
3? 5.8 12.5
36 psig
3~6" 5.U 12.6
35.5
36 10.5
35^5
36 12.75
35.5 psig
36 5.5 13-0
35.5
36 12.9
35^1
3T^ 13.1
37-5
3ET" 13.1
37.5
38" 12.9
17 psig
38 6.0 12.9
3J.
39 13-0
4
35 12.9
11-9
11.9
11.8
11.9
12.0
12.1
11.9
12.1
12.0
12.1
12.2
12.2
12.1
Ar.p
106
107
105
105
105
107
108
105
105
107
106
103
109
Gas
Press
3.95
3-95
3-95
li.OO
3-95
U.o
3.95
3-95
3.95
3.95
3-95
3. 70
'.70
Blcwer
Out
P/T
eu.5_
12U
8U
127
83.5
130
83.0
82.0
132
83.0
132
82.0
132
63.0
131
83.0
159
82.0
139
63
131
83
125
§?
Burner
Air
P
1 2
22-
28
22-
28
22-
28
22-
28
22-
29
2k-
28
23-
28
23-
28
23-
28
22-
29
22-
28
23-
20
22-
28
22-
28
22-
23
22-
28
22-
28
2U-
28
2*-
28
22-
28
22-
28
22-
29
19-
29
20-
28
-------
Date/
Tine
5/16/71
7:00 PM
9:00
fr
CD 10:10
11:00
12:00
Mid.
Svap.
Fuel
Valve
tc
Open
1
2
1
2
1
2
1
2
1
2
15
15
15
15
15
15
15
15
15
15
Levels
& Temp.
Pressures
Cone. Cooling Water Temp.
Evap.
LI °F
-1
9.5 190
CHANGED
35
10.5 191
21.
10.5
22
10.5 191
32_
10.5
Tank Flow Inlet Out
Stack Rate Water
LI °F 1 2 Tenro. #1
62 192 91 95 121
LEVEL CONTROLLER TO
81* 191 91 95 122
192 91 95 122
192 93 90 120 121
119
Temp. Out
Evap,
jfe Moyno
119 173
10.5 AT
120 165
120 170
120 165
122
Flow Controls
Set Pt.
Feed Gas Gas Gas
FCV #1 #2 Amps Press
3J3 press
37 6.0 12.9 12.1 108 3.90
8:U5 p. m.
38 psig
37 6.0 12.7 12.0 10° 3.9+
fpsig
6 12.7 12.0 110 3.9+
fpsig
6.0 12.7 12.2 110 U.O
U2
T»2 115
Blcver
Out
P/T
_§a
125
8»t-85
120
8U-85
117
8U-35
"TlT
80-81
Burner
Air
P
1 2
29-
29
2U-
29
2U-
29
2U-
29
22-
28
2U-
28
2U-
28
20-
28
-------
APPENDIX C - WATER-COOLED DOWNCOMER TESTS
FEED AM) PRODUCT SAMPLES FROM SERIES 1
Date
U/15/71
V15/71
U/15/71
V15/71
V15/71
V15/71
V15/71
V15/71
V15/71
V15/71
V15/71
V15/71
U/15/71
U/16/71
V16/71
Vie/71
Vi6/7i
Vie/Ti
Vie/Ti
Vi6/7i
Vie/71
Sample
No.
1
2
3
If
5
6
7
8
9
10
12
ii
13
i
2
3
U
5
6
7
8
Sample Description
Composite Sample to Link Belt Screen
Composite Sample to Link Belt Screen
Composite Sample to Link Belt Screen
Composite Sample to Link Belt Screen
Evaporator Feed. - Sweco Liq.
(Screen Only) 3:30 PM
Evaporator Feed Sweco Liq.
(Screen Only) 3:30 PM
#1 Press Output to Dryer
#2. Press Output to Dryer
#3 Press Output to Dryer
Evaporator Feed Sweco Liq.
(Screen & 3 Presses) 6:23 PM
Evaporator Feed - Sweco Liq.
(Screen & 3 Presses) 6:23 PM
Sample of Initial Liq. in Evap.
Taken at Bottom 6:30 PM
Sample of Initial Liq. in Evap.
Taken at Bottom 6:30 PM
f
Composite Sample to Link Belt Screen
Composite Sample to Link Belt Screen
Composite Sample to Link Belt Screen
Composite Sample to Link Belt Screen
Sample of Initial Idq. in Evap.
Taken at Bottom
Sample of Initial Liq. in Evap.
Taken at Bottom
Dust Slurry from Brewhouse
Dust Slurry from Brewhouse
% %
T.S. S.S.
8.70
8.61 Avg.
8.92
8.82
2.32
5.26
35.2
37.9
U2.8
3.09
1.6U
^. 31
1.76
9.02
8.28 Avg.
9.22
8.U8
U.86
1.60
1.77
.U7
Ratio
SS/IS
8.76
79
1.13
.69
8.75
.U9
.362
-------
Date
V16/71
U/16/71
V16/71
V16/71
V16/71
V16/71
V16/71
V16/71
V16/71
V16/71
V17/71
V17/71
V17/71
V17/71
U/17/71
U/17/71
V17/71
U/17/71
V17/71
U/17/71
U/17/71
V18/71
V18/71
V18/71
V18/71
Sample
No.
9
10
11
12
It
17
15
16
13
18
1
2
3
t
5
6
7
8
9
10
11
1
2
C-l
C-2
Sample Description
Composite Sample to Link Belt Screen
Composite Sample to Line Belt Screen
Composite Sample to Link Belt Screen
Composite Sample to Link Belt Screen
Sample from Bottom of Evap. 7:00 PM
Sample from Bottom of Evap. 7:00 PM
Sample from Suction Side of Evap. Feed Pump
7:00 PM
Sample from Suction Side of Evap. Feed Pump
7:00 PM
Sample of Leakage around Burners
Sample of Leakage around Burners
Sample from Bottom of Evap. Pre Start-Up
(11:00 AM)
Sample from Bottom of Evap. Pre Start-Up
(11:00 AM)
#1 Press - Output to Dryer
#2 Press Output to Dryer
#3 Press - Output to Dryer
Dust Slurry from Brewhouse
Dust Slurry from Brewhouse
Composite to Link Belt Screen
Composite to Link Belt Screen
Composite to Link Belt Screen
Composite to Link Belt Screen
Thick Material on Floor from Evap.
Thick Material on Floor from Evap.
Thick Material on Floor from Evap.
Thick Material on Floor from Evap.
T.S. S.S.
8.5U
8.87
Avg.
9.15
9.02
3-10
1.65
2.90
1.-5
3-06
1.31 1.75
6.15
1.60
1»0.9
t2.3
U2.9
1.78
.UU
10.2
10.2
Avg.
10.8
10.6
13.7
13.7
13-7
13.6
Ratio
SS/IS
8.89
1.00
1.335
.178
V19/71
Thick Material on Floor from Evap.
50
2.07
-------
Date
U/19/71
U/19/71
U/19/71
U/19/71
U/19/71
U/19/71
U/19/71
U/19/71
U/19/71
U/19/71
U/19/71
U/19/71
U/19/71
U/19/71
U/19/71
U/19/71
U/19/71
U/19/71
U/19/71
U/19/71
U/19/71
U/19/71
U/19/71
U/19/71
U/19/71
U/19/71
Sample
No.
2
3
U
5
27
28
6
7
8
9
10
n
12
13
1U
15
16
17
18
19
20
2U
21
22
23
25
26
Sample Description
Composite
Composite
Composite
Composite
to Link Belt Screen
to Link Belt Screen
to Link Belt Screen
to Link Belt Screen
Dust Slurry from Brewhouse
Dust Slurry from Brewhouse
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
to
to
to
to
to
to
to
to
to
to
to
to
to
to
to
to
to
to
to
to
to
Link
Link
Link
Link
Link
Link
Link
Link
Link
Link
Link
Link
Link
Link
Link
Link
Link
Link
Link
Link
Link
Belt
Belt
Belt
Belt
Belt
Belt
Belt
Belt
Belt
Belt
Belt
Belt
Belt
Belt
Belt
Belt
Belt
Belt
Belt
Belt
Belt
Screen
Screen
Screen
Screen
Screen
Screen
Screen -
Screen
Screen -
Screen
Screen -
Screen -
Screen
Screen -
Screen
Screen
Screen
Screen
Screen -
Screen
Screen -
Time
Time
Time
Time
Time
Time
Time
Time
Time
Time
Time
Time
Time
Time
Time
Time
Time
Time
Time
Time
Time
2
2
2
2
2
2
2
2
2
:18
:23
:28
:33
:38
:U3
:U8
:53
:58
- 3:03
3:08
3
:13
- 3:18
- 3
3
3
- 3
- 3
- 3
- 3
3
:23
:28
:33
:38
:U3
:U8
:53
:58
T.
7.
7.
7.
8.
1.
11.
11.
8.
10.
n.
10.
10.
n.
11.
n.
n.
11.
12.
n.
11.
12.
n.
11.
12.
12.
12.
% Ratio
S. S.S. SS/IS
69
73
Avg. 7.83
89
00
71
.30
395
90
36
5U
90
52
93
95
81
55
20
Avg. 11.53
U5
87
07
65
80
13
78
90
35
25
22
-------
Date
V21/71
V21/71
U/21/71
U/21/71
V21/71
U/21/71
U/21/71
U/21/71
U/21/71
V21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
Sample
No.
1
2
3
U
5
6
7
8
9
10
11
12
13
1U
15
16
17
18
19
20
21
22
23
2U
29
30
31
32
33
Sample Description
Liquor to Sewer Brew $6
Liquor to Sewer - Brew #6
Liquor to Sewer Brew #7
Liquor to Sewer Brew #7
Evaporator Feed Tank - 9:50 AM
Evaporator Feed Tank 9=50 AM
Liquor to Sewer - Brew #U -
Liquor
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
Sample
to
to
to
to
to
to
to
to
to
to
to
to
to
to
to
to
to
to
to
to
to
to
0
J
T
1
1
3
Sewer Brew #U
Link-Belt
Link-Belt
Link-Belt
Link-Belt
Link-Belt
Link-Belt
Link-Belt
Link-Belt
Link-Belt
Link-Belt
Link-Belt
Link-Belt
Link-Belt
Link-Belt
Link-Belt
Link-Belt
Link-Belt
Link-Belt
Link-Belt
Link-Belt
Link-Belt
Screen
Screen
Screen
'Screen
Screen
Screen
Screen
Screen
Screen
Screen
Screen
Screen
Screen
Screen
Screen
Screen
Screen
Screen
Screen
Screen
Screen
Time
Time
- Time
Time
- Time
- Time
Time
- Time
- Time
- Time
Time
- Time
Time
- Time
- Time
- Time
- Time
- Time
- Time
- Time
- Time
- 9:30 AM
9:35
9:UO
- 9:U5
9:50
- 9:55
- 10:00
10:05
10:10
10:15
- 10:20
- 10:25
- 10:30
10:35
- 10:Uo
- 10:U5
- 10:50
10:55
- 11:00
- 11:05
11:10"
12
7
lU
6
9
9
10
11
10
9
.9
10
n
10
12
12
12
12
13
12
i % Ratio
.S. S.S. SS/IS
.59
.856
.29
.713
.Uo
.975
1.68
.032U
.0188
9
.06
.28
.7
9U
.25
.78
.15
.00
.Uo
.70
.8
.6
.1
.9
.2
.6
.5
.3
.1
.7
-------
Sample
Date No .
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
U/21/71
27
28
37
38
39
Uo
3U
36
25
5U
58
26
U2
U7
35
UU
U3
U8
Ul
U5
U6
50
U9
51
53
56
52
57
Sample Description
Liquor to Sewer B.H. D.W. Screen
Liquor to Sewer B.H. D.W. Screen
Liquor to Sewer B.H. D.W. Screen
Liquor to Sewer B.H. D.W. Screen
Liquor to. Sewer B.H. D.W. Screen
Liquor to Sewer B.H. D.W. Screen
Evap. Feed 2:00 PM
Evap. Feed - 2:00 PM
Concentrate 2:00 PM
Condensate 2:00 PM
Condensate 2:00 PM
Cone. 3:00 PM
Evap. Feed - U:00 PM
Evap. Feed - U:00 PM
Cone. - U:00 PM
Cone. - U:00 PM
Evap. Feed - 6:00 PM
Evap. Feed 6:00 PM
Cone. 6:00 PM
Cone. - 6:00 PM
Cone. 7:00 PM
Cone. - 7:00 PM
Cone. - 8:00 PM
Cone. - 8:00 PM
Evap. Feed - 9:00 PM
Evap. Feed - 9:00 PM
Cone. - 9:00 PM
Cone. - 9:00 PM
$ % Ratio
T.S. S.S. SS/IS
2.95
l.Ul
3-93
2.29
3.86
2.0U
3-73
.735
1.38
3.02
1.5U
1.07
.795
5.22
3.12
1.30
1.79
U.85
1.87
3.50
1.07
1.81
5.83
2.05
8.05
2.09
7-30
2.8U
3.51
1.1U
1.87
9.U
53
-------
Date
4/21/71
4/21/71
4/21/71
4/21/71
4/21/71
4/21/71
4/21/71
4/21/71
4/21/71
4/21/71
4/22/71
4/22/71
4/22/71
4/22/71
4/22/71
4/22/71
4/22/71
4/22/71
4/22/71
4/22/71
4/22/71
4/22/71
4/22/71
4/22/71
4/22/71
4/22/71
4/22/71
4/22/71
4/22/71
Sample
No.
55
59
60
64
62
67
61
65
63
66
68
69
1
3
2
4
5
7
6
8
9
10
11
13
12
14
15
16
17
Condensate
Condensate
Concentrate
Concentrate
Evap. Feed
Evap. Feed
Concentrate
Concentrate
Concentrate
Concentrate
Evap. Feed
Evap. Feed
Concentrate
Concentrate
Concentrate
Concentrate
Evap. Feed
Evap. Feed
Concentrate
Concentrate
Concentrate
Concentrate
Evap. Feed
Evap. Feed
Concentrate
Concentrate
Concentrate
Condensate
Condensate
Sample Description
- 9:OO PM
- 9:00 PM
- 10:00 PM
- 10:00 PM
- 11:00 PM
- 11:00 PM
11:00 PM
11:00 PM
- 12:00 MN
- 12:00 MN
- 1:00 AM
- 1:00 AM
- 1:00 AM
- 1:00 AM
2:00 AM
- 2:00 AM
- 3:00 AM
- 3:00 AM
- 3:00 AM
3:00 AM
- 4:00 AM
- 4:00 AM
- 5:00 AM
- 5:00 AM
- 5:00 AM
- 5:00 AM
- 6:00 AM
- 6:40 AM
- 6:40 AM
% % Ratio
T.S. S.S. SS/IS
.39
1.73
.247
9-23
4.18
1.78
10.9
4.75
11.42
5.2
3.47
.875
1.62
12.8
5-37
13.6
5.62
3.42
.78
1.50
13.4
.189
15-5
5.78
3.49
.75
1.50
13.5
6.75
14.4
2.99
1.64
-------
Date
U/22/71
V22/71
U/22/71
It/22/71
U/22/71
V22/71
U/22/71
U/22/71
U/22/71
U/22/71
U/22/71
U/22/71
U/22/71
U/22/71
U/22/71
U/22/71
U/22/71
U/22/71
U/22/71
U/22/71
U/22/71
U/22/71
U/22/71
U/22/71
V23/71
V23/71
U/23/71
V23/71
U/23/71
Sample
No.
19
20
18
21
23
2U
22
0-3
C-U
0-5
25
26
c-6
27
28
C-7
C-8
29
30
C-9
C-10
C-ll
C-13
c-iU
C-15
c-i6
C-17
31
32
Sample Description
Evap. Feed
Evap. Feed
Concentrate
Concentrate
Evap. Feed -
Evap. Feed
Concentrate
Concentrate
Concentrate
Concentrate
Evap. Feed
Evap. Feed
Concentrate
Evap. Feed -
Evap. Feed -
Concentrate
Concentrate
7:00 AM
7:00 AM
7:00 AM
8:00 AM
9:00 AM
9:00 AM
9:00 AM
- 10:00 AM
- 11:00 AM
12:00 PM
1:00 PM
1:00 PM
1:00 PM
3:00 PM
3:00 PM
3:00 PM
- U:00 PM
Evap. Feed - 5:00 FM
Evap. Feed - 5:00 PM
Concentrate
Concentrate
Concentrate
Concentrate
Concentrate
Concentrate
Concentrate
Concentrate
Evap. Feed -
Evap. Feed -
5:00 PM
- 6:00 PM
- 7:00 PM
- 8:00 PM
10:00 PM
- 12:15 AM
2:00 AM
- U:00 AM
6:00 AM
6:00 AM
# %
T.S. S.S.
3.U5
1.U7
15.0
15-7
3.73
1-59
16.5
16.9
17.2
17-9
3.89
1.90
1U.5
U.18
1.90
17.3
17. U
3.19
1.80
17.0
19.8
21.7
17.0
1U.8
13.8
1U.6
13-7
3.35
1.87
Ratio
SS/IS
7U
-7U
95
.83
1.39
1.26
55
-------
Sample % $ Ratio
Date No. Sample Description T.S. S.S. SS/IS
V23/Y1 C-12 Concentrate 6:00 AM 13.1
lf/23/71 C-18 Concentrate 8:00 AM 13.25
-------
APPENDIX D WATER-COOLED DOWNCOMER TESTS
FEED AND PRODUCT SAMPLES FROM SERIES 2
Date
5AV71
5AV71
5/lVTl
5/1V71
5/lVTl
5AV71
5AV71
5/lVtl
5/lU/Tl
5/lVTl
5AV71
5/1V71
5/1V71
5/1U/71
5/1V71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
Time
5:00 PM
5:00
5:30
5:30
5:30
5:30
7:30
8:30
9:30
9:30
9:30
10:30
11:30
11:30
11:30
1:30 AM
1:30
1:30
2:30
2:30
3:30
3:30
3:30
U:30
5:30
Sample
No.
1
2
3
U
5
6
7
8
9
10
11
12
15
13
1U
16
18
19
20
21.
22
23
21*
25
28
29
Sample Description
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Stack
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Feed Tank Bottoms
Feed Tank Bottoms
Bottom Prior to Startup
Bottom Prior to Startup
Feed
Feed
Concentrate
Concentrate
Concentrate
Feed
Feed
Concentrate
Concentrate
Feed
Feed
Feed
Feed
Condensate
Concentrate
Concentrate - Cenco
Feed
Feed
Concentrate
Concentrate
Feed
Feed
57
H> T.S. $ S.S.
3
5
3
k
k
k
3
5
5
3
3
10
10
3
11
11
3
.71
1.96
30
2.07
71
1.85
.17
55
.76
.68
.13
.70
.68
1.95
.60
1.81*
,2ll*
.29
99
.56
1.81
.10
.62
.69
Ratio
SS/IS
1.12
.6U
1.02
1.11
1.13
1.05
1.035
.995
-------
Date
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
Time
5:30 AM
6:15
:15
7:30
7:30
7:30
.7:30
8:30
9:30
9:30
9:30
9:30
10:30
11:30
11:30
11:30
12:00 PM
12:30
1:30
1:30
1:30
2:30
2:30
3:30
U:00
3:30
3:30
Sample
No.
30
31
27
33
35
3*
32
36
friQ
JlT
37
39
38
16
UU
hp
ll/T
50
51
U9
U8
1.6
1
52
3
Sample Description
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Stack
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Concentrate
Concentrate
Concentrate
Feed
Feed
Concentrate
Concentrate Cenco
Concentrate
Feed
Feed
Concentrate
Condensate
Concentrate
Concentrate
Feed
Feed
Concentrate - Cenco
Concentrate
Feed
Feed
Concentrate
Concentrate
Concentrate - Cenco
Concentrate
Concentrate - Cenco
Feed
Feed
% T.S. % S.S.
12
Ik
13
3
13
11
lit
3
11*
16
16
3
17
16
3
16
19
.75
.92
.00
2.05
.62
.65
.15
.71
1.96
.90
.10^3
.60
.3
.52
1.90
9
.8
1.91
.7
.1
Ratio
SS/IS
l.M*
1.12
1.17
1.17
16.15
16.6
17
3
.6
3U
1.83
1.21
-------
Date
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/15/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
*
u
5
5
6
6
7
7
7
7
8
Time
:15 PM
:30
:30
:30
:30
:30
:30
:30
:30
:30
:30
8:30
9
9
:30
:30
10:30
10:30
10
10
:30
:30
11:30
11
12
12
1
1
:30
:30 AM
:30
:30
:30
1:30
1
:30
Sample
No.
5
2
6
7
8
9
10
11
12
13
16
15
18
17
19
22
20
21
23
2U
25
26
27
30
28
29
Sample Description
Stack
Evap,
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Condensate
Concentrate
Concentrate
Feed
Feed
Concentrate
Concentrate Cenco
Feed
Feed
Concentrate
Concentrate Cenco
Concentrate
Concentrate Cenco
Concentrate
Concentrate - Cenco
Feed
Feed
Concentrate
Concentrate Cenco
Concentrate
Concentrate - Cenco
Concentrate
Concentrate - Cenco
Feed
Feed
Concentrate
Concentrate - Cenco
Ratio
$ T.S. % S.S. SS/IS
16
16
3
19
19
3
23
19
21
22
20
18
.3
20
19
23
22
20
21
2
2k
22
.173
.6
.7
.26
1.31
1.85
.7
.2
.27
1.335
1.87
.2
.5
.2
.3
.2
.8
.07
1.275
1.72
.0
.7
.0
.3
.8
.h
.99
1.135
1?59
.0
.0
59
-------
Date
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5Vl6/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
Time
2
2
3
3
:30 AM
:30
:30
:30
4:30
4:30
4
:30
4:30
5
5
6
6
7
7
7
7
8
9
10
10
10
11
1
1
1
2
3
:30
:30
:30
:30
:30
:30
:30
:30
:30
:30
:30
:30
:30
:30
:30 PM
=30
:30
:30
:30
Sample
'No. Sample Description
31
32
33
34
37
38
35
36
39
40
41
42
43
44
46
45
47
49
50
51
52
53
54
56
58
55
59
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Stack
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Evap.
Concentrate
Concentrate - Cenco
Concentrate
Concentrate Cenco
Feed
Feed
Concentrate
Concentrate - Cenco
Concentrate
Concentrate Cenco
Concentrate
Concentrate Cenco
Feed
Feed
Concentrate
Condensate
Concentrate
Concentrate
Feed
Feed
Concentrate
Concentrate
Concentrate
Feed
Feed
Concentrate
Concentrate
Ratio
i T.S. $ S.S. SS/IS
20.
22.
22.
21.
3.
21.
22.
24.
22.
21.
22.
3.
23-
.
24.
24.
3-
25.
24.
28.
3.
27.
9
3
0
4
47
1.27
1.94
8
0
8
8
8
8
58
1.22
1.97
1
343
8
6
75
2.15
2.56
0
9
2
94
1.77
2.52
9
28.2
60
-------
Date
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/16/71
5/17/71
5/17/71
5/17/71
5/17/71
5/17/71
5/17/71
Time
K
Ji
Ji
K
5
6
6
7
7
7
:00 PM
:30
:30
:30
:30
:30
:30
:30
:30
:30
7:30
8
8
9
9
10
10
10
10
11
11
12
12
1
1
1
1
:30
:30
:30
:30
:30
:30
:30
:30
:30
:30
:30 AM
:30
:30
:30
:30
:30
Sample
No.
57
62
61
60
63
2
3
6k
1
k
5
6
7
8
9
10
13
11
12
llf
15
16
17
19
18 '
20
21
Evap
Evap
Evap
Evap
Evap
Evap
Evap
Evap
Evap
Evap
Evap
Evap
Evap
Evap
Evap
Evap
Evp.
Evap
Evap
Evap
Evap
Evp.
Evap
Evap
Evap
Evap
Evap
Sample Description
. Concentrate Cenco
. Feed
. Feed
. Concentrate
. Concentrate
. Concentrate
. Concentrate Cenco
. Feed
. Feed
. Concentrate
. Concentrate Cenco
. Concentrate
. Concentrate Cenco
. Concentrate
. Concentrate Cenco
. Feed
Feed
. Concentrate
. Concentrate Cenco
. Concentrate
. Concentrate - Cenco
Concentrate
. Concentrate - Cenco
. Concentrate
. Concentrate Cenco
. Feed
. Feed
^T
26
k
28
27
26
27
3
26
26
Ratio
.S. $ S.S. SS/IS
.9
.20
1.36
2.U2
.2
.8
.0
3
.71
1.73
2.35
.7
.8
2k. 6
23
26
26
3
25
21
25
26
25
27
26
25
3
.2
A
.2
.69
1.31
2.09
.5
.5
.2
.8
.3
.8
.1
.9
.58
1.31
2.03
61
-------
Date
Time
Sample
No.
Sample Description
% T.S.
S.S.
Ratio
SS/IS
5/17/71 2:30 AM 22
5/17/71 2:30 23
5/17/71 3:30 2k
5/17/71 3:30 25
Evap. Concentrate 2k.6
Evap. Concentrate Cenco 25.6
Evap. Concentrate 22.8
Evap. Concentrate Cenco 22.0
62
-------
APPENDIX E EVAPORATOR TESTS USING
WATER-COOLED DOWNCOMER ORSAT ANALYSES
Date
5/11/71
5/H/71
5/11/71
5/H/71
5/12/71
5/13/71
5/13/71
5/13/71
5/13/71
5/13/71
5/15/71
5/15/71
5/15/71
Time
U:30 PM
8:30 PM
9:^5 PM
10:30 PM
U:l;5 PM
1:30 PM
2:30 p.m.
3:00 PM
U:00 PM
1±:30 PM
12:30 AM
1:15 AM
1:^5 AM
Sample
Point
Stack
Stack
Stack
Stack
Stack
Burner #2
Burner #1
Burner #1
5 ft. Into
Stack
3 ft. Into
Stack
Burner #1
Burner $2
Stack
* CO.
5.U
7.0
6A
6.6
7.0
10. U
8.8
9A
7.8
8.3
10.0
10.8
5.9
*0f>
6.7
3.U
2A
U.2
3.2
0.0
0.2
0.2
1.2
.9
O.U
0.2
2.5
i CO
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
% Diff .
(1o No) + (°lo Other)
87.9
89.6
91.2
89.2
89.2
89.6
91.0
go.k
91.0
90.8
89.6
89.0
91.6
63
-------
APPENDIX F - EVAPORATOR TESTS USING
JACKETED DOWNCOMER AND CLOSED LOOP
COOLING SYSTEM
Burners
Temp. Gas ~ Blov.-er
Valve Levels fc Temp. Therminol Out OrificeAP C-as Burner Cutput
Date/ tc Evap. Therminol In Temp. Out Temp. Stack Evap. AP AP Press AirAP Flew Unit
7i;r.e Cper. II CF LI Psig #1 #2 #1 #2 Temp. Moyno #1 #2 Psig #1 fe Amps Feed Press Drex Press
9/2/71 11 2U
11:15 A 2 1 7.5 122 150 170 122 2.3 2.2 U.2 6U 0 88
16 U5 7.5
11:30 2 15 123 11 775 230 165 2U5 220 186 123 5.6 5.1 U.I 10-15 5-25 9U 8U.25
1 9 U_3_ 8.0
11:^5 2 9 13 12 775 230 2l»0 265 2UO 192 122 9.25 9-30 U.05 15-25 20-30 110 78
1 9 37
12:00 JJ 2 9 11.5 122 265 2U5 122 9.140 9-70 U.OO 110 Uo 76.5
19 33 7.7
12:15 2 9 12.0 176 12.0 775 235 2U? 270 2l*5 192 176 11.80 9-50 3.95 15-20 15-30 109 50 77.0
1 9 U7
12:30 2 9 1575 270 250 183 11.50 9-10 ^.05 108 78.0
1 9-0 57 7.8
1:00 P 2 9.2 17.5 191 12.0 576" 2U5 2Uo 270 250 193 191 10.6 8.8 U.OO 15-20 15-30 10U 39 78.0
1 9.0 70
1:15 2 9.2 21.5 275 250 10.25 8.3 U.05 102 38 79.5
1 8.9 6U 8.0
1:30 2 9-1 19.5 192 575 2U5 235 275 250 191* 192 10.75 8.7 U.05 13-20 18-20 10U 39 79.0
1 8.8 60
1:U? 2 9.1 193 275 193 10.8 9.1 U.O 106 U2 79.0
1 9.0 59 8.0 Ul
2:00 2 9.2 16 192 12+ HI) 2U5 235 275 250 193 192 11.9 8.8 U.05 15-22 20-30 107 5? 80
-------
Svap. Burners
FMS! Tenp. Gas 31cv."r
Valve Levels ?> 7or.p. Therminol Out OrificeAP Gas Burner
Date/ *c Evap, Therminol In Temp. Out Temp. Stack Evap. Ap AP Press Air A P Flvw Unit
Tlr.» C?er. LI F LI Pslg #1 #2 #1 jfe Temp. Moyno #1 /fe Pslg #1 fe Ar.ps F^ed Press Drex Press
9/2/71 1 ?.o 57
2:1= P 2 9.1 17 192 275 192 10.75 8.9 U.OO 10S 79.5
1 o U; 6.2
2:U5 29 V< 168 57U" 2U5 230 270 250 192 168 11.5 9-6 U.O 15-25 15-35 112 60 77
1 9 '-2 6.3
U:15 2 9 1273 170 lU 778 2U5 232 273 250 192 170 11.35 10.0 U.O 15-25 15-35 106 60 78
1 9-25 5Z M
U:U5 2 9.75 ItTTf 179 I1* 7-9 2Ug 232 275 252 193 179 11.3 9.6 U.O lU-25 15-32 108 50 78.5
1 9.25 53 8.U
5:15 2 9.75 1572 188 lU 576" 250 23U 278 252 193 188 11.1 9-1* b-0 10-20 15-35 10U 50 78.5
1 U.o 60
5:U5 2 9.75 15 189 lU 8.0 235 250 187 189 10.3 U.2 15-UO 96 2U 8U
57
C-:15 2 9.75 17.5 182 10.5 7.2 235 250 186 182 10.U U.2 15-35 88 28 %
1 9.0 6U 7.5
6:U5 2 9.3 20 186 5.5 2U? 230 275 250 19U 186 10.5 9-U U.O 15-20 20-25 10U 1*5 80
1 9.0 69 9.0
":15 2 0.2 10.5 185 ll.o 9.0 250 230 275 250 19!* 185 10.25 8.5 U.O 15-20 20-30 10U U5 80
1 9.0 (.6
7:U5 2 9.2 20.5 187 9-0 250 230 275 250 19U 187 10.35 8.U U.05 15-20 20-25 103 U7 Bl
1 9.0 81
8:15 2 9.U 25.5 190 275 250 190 9-75 8.U U.05 102 39 82
1 9.0 87 9.2
8:U5 2 9.U 23.5 191 9.0 250 235 275 250 19U 189 9.90 9.0 U.OO 15-20 50-25 102 39 81.75
1 o.o 86
9:15 2 9.U 2T 190 275 250 160 9.5 8.6 U.O 100 37 82.5
-------
Evap . _ Burners _
"".el Temp. Gas Blcv:«r
Velvs Leva-Is ;. Temp. Therminol Out Orifice^,? Gas B';rr.sr Cutout
Sate/ tc Evap. Thermincl In Temp. Out Temp. Stack Evap. AP AP Press AirAP Flew Ur.lt
Tir.e C-per. LI F LI PsiK #1 #S //I #2 Temp. Moyno #1 |2 Psig ll -'--2 Ar.ps Feed Press Dre.x Press
9/2/-1 1 9.0 77 9.2
9:1*5 ? 2 5.1; 23 191 12" 9.0 250 230 275 250 19U 191 9-9 9.0 U.I 15-20 15-25 103> 1*2 81.5
1 9.0 79
10:15 2 9.5 23.5 188 275 250 188 9.8 8.8 U.O 102 Us Sl.O
1 9-0 79 2il
10:^5 2 o.f 2U 187 12" 9-0 250 232 280 255 19U 187 9-7 8.8 U.O 10-20 10-30 100 ho, 82
1 o.o 75
11:15 2 9.6 23 187 280 255 18? 9-9 9.0 1».0 102 Ul 8l.5
1 9-0 73 9.2
ll:U5 2 9.6 22.5 185 I1*" 9-3 255 235 280 255 191* 185 9.9 8.7v U.O 12-20 15-30 loU U2 82.0
12ll5 A 2 o.o 23 18U 280 258 18U 9.8 8.8 U.O 100 U2 81.5
1 9.0 75 9.2
12:U? 2 9,6 23 183 8T9 250 235 280 258 19U . 183 9.65 8.6 U.O 13-20 20-25 100 U2 81.5
1 9.0 75
1:15 A 2 9.6 23 183 280 258 183 9.7 8.6 U.O 100 U2 31.5
1 9.0
1;1»5 2 9.6
1 9.0 78 2ii
2:15 2 9.6 IT 182 9.0 260 238 282 260 195 188 9.3 8.5 U.O 15-20 18-25 102 U2 31.5
i.2
1 o.o ^OQ 9.2
3:15 2 9.6 21*.75 182 875 260 2^0 288 26l 195 182 9.15 8.3 U.05 13-21 17-2U 100 la 32
1 o.p ?i 0.3
^:15 2 9.6 2TT75 l8l 9.1 270 2»»2 292 265 195 181 9.0 8.2 U.05 15-20 16-2U 9? Uo 82.5
5:15 2 I'.l 1^75 131 975 270 2U3 290 265 195 181 9-0 8.15 U.05 15-20 20-25 100 ^0 ?2.0
-------
ON
Date/
9/3/71
t. :15 A
9:15
9;U5
10:15
11:15
12:15 ?
1:15
2:15
3:15
3:^5
!»:15
~-:--.-o.
F-;ei
Valve
tc
C-or:p.
1 9.0
2 9.^
1 9.0
2 CF?
1 9.0
1 9-L5
1 9.0
2 o.U
1 92
2 °2
1 9.1
2 o.l
2 oil
l 9.1
2 9.1
1 9-1
2 0.3
1 o.o
2 9.1
1 9.0
2 o.i
l 9.0
2 9-3
Levels & Temp.
5vap.
LI °F
77
2?. 5 176
55
li: .'75 171
Z7_
CU? 173
77
23.5
77
25.5
77
23.5
7a
23-5 179
7"
23.5
7 a
2?. 5
72
21.5
2;. 25
1 '
23.25 is"
7-7
Tlierminol
LI Pr.ic
«*
0^5
8.8
o ^7R
O.U
P.j
F75
a.o
F3
8.0
8.00
10" 8~725
8.0
Therminol
In Temp.
4l #2
280
295
295
300
300
300
300
290
300
255
185
250
255
255
255
260
260
260
Out
#1
302
311
315
320
320
320
320
315
315
2UO
315
320
Temp.
268
165
268
270
270
270
270
270
270
275
275
275
Stack
Ttmp.
195
185
195
195
195
195
195
195
195
Temp .
Out
Evap.
Moyno
176
171
173
177
179
178
179
181
183
176
178
180
Gas
Orif iceA P
AP AP
//I //2
9.0
10.6
9.0
9.0
9-3
9-25
9-50
9.50
9.60
9.70
9-5
9-5
0.1
8.0
8.1
8.0
8.0
8.1
8.6
8.8
8.7
8.U
8.6
Burners
Gas Burner
Press AlrAP
PsiB i'l &
U.05 13-23 18-26
U.2 20-25 206
U.O
U.I 10-20 15-25
U.I
U.O 10-20 15-25
U.05 10-20 15-25
U.05 10-20 15-25
U.05 10-20 15-25
U.I 12-18 15-25
A-l
U.I 15-20 15-20
Ar.ps
98
97
97
98
100
102
100
100
100
100
Blcv.-er
Output
Flrw
F-=ed
20.5
uu
U7
50
50
50
U7
L8
US
Unit
Press Drex Press
92
57
83
82
32
82
91.25
81
91
91.5
81.5
. .
5:15 2 9.; 23.50 16" BTo 300 260 320 275 195 181 9.U 8.5 U.05 10-18 15-25 100 U? 9i.o
-------
Svap. Burners
F«l Temp. Gas Blcver
Valve Levels & Temp. Thermlnol Out Orifice A P Gas Burner Cutput
Cats/ -tc Svap. Therminol In Temp. Out Temp. Stack Evap.
-------
Date/
*"*" C.
9/e/7i
11:50 P
9/9/71
12:50 A
1:20
1:50
ON 2:50
VO
3:50
1*:50
5:50
6:50
7:50
9:50
9s50
10:50
Ivap.
Fuel
Valve
tc
Coer.
1 9.25
2 9-7
1 9.1*
2 9-75
1 9.3
2 9.75
1 9.1*
2 9^
!£.!*
2 9-75
1 9-5
2 9.8
1 9.5
2 10.1
1 0
2 9.0
1 0
2 9.0
1 0
2 9.0
l 9.0
2 9.0
1 9.9
2 10.1
1 9.1
2 9-9
Burners
Levels & Temp.
Therminol
Svap. Therminol In Temp.
LI °F LI Psig #1 #2
2C.O
3T~
21*. 5
77
25
5i
27
21*
59
26
S£
23.5
97
20.5
35~
21
£93
25.5
W~
,0+
100+
30+
100+
18
59
2U
2U+
2U+
2U+
2k+
2k+
2k-
23-
23-
2.1»
21*
2l*
8.6
9.0 235
3.3
O, 255
8T2 258
8.1 ~
8~72 260
8.2
B7o 260
8.2
B7o 260
7.8
57o 230
7.6
570 200
7 A
elo 190
9.2
8"7o 260
8.2
BTo 270
8.2
7.9 275
218
219
219
220
220
220
218
215
215
220
230
235
Out
#1
272
272
282
272
275
279
260
190
189
188
282
288
298
Temp.
ffe
259
259
260
261
262
262
265
260
260
262
265
273
278
Stack
Temp.
190
192
193
193
192
192
190
187
187
192
192
192
Evap. Gas
Cjt OrificeAP
E\ap. /IP Ap
Moyno #1 #2
190 9-7
191 9.8
192 9-6
191 9.1*
190 9-3
189 8,9
187 8.7
181*
180
180
180 8.6
182 7.9
180 10.0
8.7
8.8
8.8
8.6
8.5
8.6
8.6
9-0
8.9
8.6
7.7
8.0
9.6
Gas
Press
Psig
U.05
1*.05
1*.05
1*.05
1*.05
U.O
U.15
U.15
U.15
1*.2
1*.05
1*.05
U.O
Burner
AirAP
#1 ^
10-20
12-20
12-20
15-25
15-25
15-25
20-30
20-30
20-30
10-20
15-20
15-20
15-25
15-30
10-25
10-20
10-20
10-20
0-10
0-10
0-10
20-30
20-30
20-?0
Blcver
Output
Flew
Amps Feed
IQl* 39
101 UO
102 1*0
100 39
100 38
100 UO
100 39
31* 2U
81* 22
?U 21
0
:5
51
Press
81.5
81.5
82
82
82
82
82
39
90
?9.5
6!*
37
80.5
Unit
Drex Press
88 13+
91 10.0
91
92 10.0
93 12.0
9k
95
88
90
90
9U
ou
92
-------
Burners
_
7-;s Temp. Gas Elc-.:er
Valve Levels & Temp. _ Therminol _ Out Orifice:! P Gas Burner _ Cv.tput _
Date/ to Evap. Therminol In Temp. Out Temp. Stack Evap. Ap AP Press AlrAp Flew Unit
Tlr.' Oper. LI °F LI Prig #1 fe #1 fe Temp. Moyno #1 #2. Psig #1 ?2 tops Feed Press Drex Press
9/9/71 1 10.3 30+ 8.0
11:50 A 2 10.25 100+ 23 TB 270 2l*0 290 280 193 183 9-3 9-1* "*.0 10-20 15-25 ho 35 95
1 10.1 21 9.0
12:50 A 2 10.2 f? 23 5.5 255 2l*0 2l*0 282 192 183 9-8 9.0 4.05 15-20 l«-22 10U !il* 62 73
1 OFF 18.25 515
1:50 2 10.25 eo" 16.25 7-7 220 2Uo 190 280 188 179 0 10.6 U.2 0 0 86 28 89 55
1 10.30 90 7.6
2:50 2 11 27.5 12.00 7.0 260 2l*0 300 290 192 183 9.1* 9.3 1*.05 15-20 18-23 96 1*0 SI* 86
1 10.2 23.5 8.8
3:50 2 11 93 12 BT5 285 2U5 305 28? 193 183 9-2 9-2 U.OO 15-20 18-23 96 to 83.5 93
1 11.6 26.5 8.
. . . ,
2 11.1* 9!* 12.25 875 285 255 305 290 192 182 9-9 9.6 U.OO 15-20 18-23 96 Uo 8U 86
1 11.7 28.5 8.6
5:50 2 11.6 93 12.00 O 290 260 310 295 192 181 10.1 9.7 >*.0 15-20 20-22 91* ho 8U 68
1 11.8 28.5 8.5
6:50 2 11.7 95"~ 11.75 B7$ 295 260 313 278 192 178 10.1 9-5 U.O 15-22 20-22 95 ho 85 68
1 11.7 28.5 8.2
7:50 2 11.8 W 11.25-575 300 267 315 302 192 179 9-9 9-6 'If. 05 15-25 20-22 $k ho 85.5 72
1 11.7 28.5 8.5
8:50 2 11.8 93 11.00 B75" 300 2?2 320 307 -192 179 10.2 9.1* U.05 15-25 20-22 9!* ho 86 69
I 11.6 28 8.5
9:50 2 11,75 93 11" O 280 322 312 192 178 9.9 9.6 1*.0 15-25 18-25 91* to 85 72
1 11.6 28.5 8.7
10:50 2 11.75 93~ 11" 9.0 312 288 327 318 192 178 9-9 9-8 1*.0 15-22 15-25 95 ^0 8^.5 69 3.5
-------
Evap. Burners
?-si Temp. Gas Blcv.-sr
Valve Levels & Temp. Therminol Out Orifice A P Gas Burner Cutpv.t
I«te/ t( Evap. Thorminol In Temp. Out Temp. Stack Evap. Ap Ap Press AirAP Flew Unit
Tire Op*r. LI F LI Pr.ig //I jfe #1 #2. Temp. Mbyno ffl #2 Psig #L ^2 Amps Feed Pi-ess Dre.x Press
9/9/71 1 11.6 29.5 8.U
11:50 P 2 11.75 W 11" H77 319 291 331 322 192 178 10.0 9-9 >».0 15-23 18-25 95 ^0 8U.5 70.5 2.3
9/10/71 1 11.6 28.25 8.3
12:50 A 2 11.75 "94 10" ETf 318 293 331 330 192 177 10.7 10.0 U.05 12-22 18-22 95 >*> 8U.5 67 2.3
1 11.6 28.5 8.U
1:50 2 11.75 ~95~ 9.5" IT? 321 297 336 330 191 177 9.8 9-9 "+-05 16-2?, 18-25 9^ ^0 85 69 1.9
1 11.6 23.5 8.2
2:50 2 11.75 93 9.0" 575 326 300 337 331* 192 180 10.0 10.0 U.O 15-23 15-25 91* te SU 79 2.7
1 11.6 26.5 8.2
3:50 2 11.75 93 8.5" BT5 328 300 339 339 191 180 10.1 10.1 U.o 17-23 15-23 91* ^ 83.5 93 3-3
-------
APPENDIX G- JACKETED DOWNCOMER TESTS
FEED AND PRODUCT SAMPLES
Date Time
9/2/71 9:30 AM
11:25
1:20 PM
3:45
6:45
7:45
10:45
9/3/71 1:45 AM
4:45
7:45
10:45
1:45 PM
2:45
3:45
4:45
4:45
5:45
6:45
9/8/71 6:30 AM
7:00
5:50 PM
6:50
7:50
8:50
8:50
Sample
No.
10 & 11
12 & 13
16 & 18
24 & 25
28 & 29
32 & 33
36 & 37
42 & 43
47 & 48
52 & 53
57 & 58
5 & 6
7
8
9
10 & 11
12
13
1 & 2
3 & 4
5 Se 6
7
8
10
11 & 12
Sample
Description
Feed
Feed
Feed
Feed
Feed
Feed
Feed
Feed
Feed
Feed
Feed
Feed
Cone.
Cone.
Cone.
Feed
Cone.
Cone.
Feed
Feed
Feed
Cone.
Cone.
Cone.
Feed
72
j> TS
3.08
3-47
2.90
2.32
2.31
2.98
3.28
3.26
3.19
2.97
2.76
3.18
18.15
17.43
18.16
3.41
18.06
16.55
2.29
2.73
2.65
4.23
5.12
6.53
2.94
j SS
1.67
2.26
1.44
1.24
1.26
1.72
1.94
1.97
1.74
1.57
1.50
1.58
2.26
1.40
1.42
1.52
1.48
SS/IS
1.18
1.87 Start-Up
0.99
1.15
1.22
1.37
1.45
1.53
1.20
1.12
1.19
0.99
1.96
1.75
Fill
1.08
1.34 Start-Up
1.01
-------
Sample Sample
j SS SS/IS
Date Time
9/8/71 9:50 PM
10:50
11:50
9/9/71 12:50 AM
1:50
1:50
2:50
3:50
t:50
t:50
5:50
6:50
7:50
7:50
8:50
9:50
10:50
10:50
11:50
12:50 PM
1:50
1:50
2:50
3:50
t:50
t:50
5:50
6:50
No.
13
It
15
18
19
20 & 21
22
23
27
25 & 26
28
29
32
30 & 31
3t
35
38
36 & 37
39
tl
t2
t3 & tt
t7
t8
3
t & 5
6
7
Description
Cone.
Cone.
Cone.
Cone.
Cone.
Feed
Cone.
Cone.
Cone.
Feed
Cone.
Cone.
Cone.
Feed
Cone.
Cone.
Cone.
Feed
Cone.
Cone.
Cone.
Feed
Cone.
Cone.
Cone.
Feed
Cone.
Cone.
73
1* TS
7-30
7.79
8.56
8.96
9.62
3.03
10.95
11.65
12.38
2.88
13-31
13.26
It. 15
3-Ot
lt.55
15.60
17.05
2.92
17.05
18.20
18.35
2.7t
18.33
18.67
19.72
2.86
19.58
19.72
1.U8 0.96
1.05
1.58 1.08
1.61 1.23
1.55 1.30
1.53
-------
Date
9/9/71
-
9/10/71
Time
7:50 FM
8:50
9:20
9:50
10:50
11:50
12:20 AM
12:50
1:50
2:50
3:20
3:50
Sample
No.
8
9
10 & 11
12
13
3A
15 & 16
17
18
19
20 & 21
22
Sample
Description
Cone.
Cone.
Feed
Cone.
Cone.
Cone.
Feed
Cone.
Cone.
Cone.
Feed
Cone.
% TS
19-75
20.00
2.90
19.98
20.30
20.30
2.22
20.57
20.28
19.75
2.0k
19-55
% SS SS/IS
1.55 1.15
1.18 1.13
0.98 0.925
Stack Condensate
Date
9/3/71
9/8/71
9/9/71
Time
Noon
7:50 PM
^:15 AM
8:00
Noon
2:00 PM
1*:00
Sample
No.
1 & 2
9
2k
33
1*0
U5 &k6
1 & 2
Sample
Description
Cone.
Cone.
Cone.
Cone.
Cone.
Cone.
Cone.
fo TS
O.U8
3.99
2.97
0.10
3.67
0.095
0.68
# SS SS/IS
0.03
0.092 30.6
Q.3k 2.00
-------
APPENDIX H - EVAPORATOR TESTS USING
NON-JACKETED DCWNCOMER
Date/
10/5/71
12:30 P
1:00
2:00
3:00
L.-OO
5:00
6:00
7:00
8:00
9:00
11:00
E'/ap.
Fuel
Valve
£,-
pper.
I
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
15
Levels & Temp. Temp.
Evap.
Board
LI LIC
Ul
U3
1*1*
62
63
65
52
81
50
100+
1*8
12
13
13
18
16.5
ll*.0
25.0
16.0
30+
9
lU.O
Therminol Out
Drex Stack Evap.
LI PSIG Gas Meter Temp. Moyno
1*581*733
32 2300-2350 186 111*
27 29 2l*,500 192 186
25 21* 193 192
1*59860!*
68 23500-21*000 193 192
65 192 192
63 22500-21*000 191 191
61 19!* 190
U617630
59 2150-2250 19!* 190
61
:10 BURNERS OFF 9:55
192 163
Burners
Gas
OrificeAP Gas Burner
AP .\P Press AirAP
#1 #2 PSIG #1 #2
6.7
7.5
7.5
7.1
6.9
7.2
6.1*
6.7
5.2
BUR
5.5
6.6 1*.0 15-25 15-30
7.1* U.05 18-2U 15-25
7.6 lt.05 18-2U 15-28
6.9 U.10 15-25 15-25
6.6 U.10 15-25 15-25
6.8 U.I 15-22 15-25
6.2 U.I 13-23 10-25
6.7 U.I 13-22 8-25
5.U U.15
N E R S ON
5.6 U.15 5-16 0-22
Blcwer Output
Amps
92
92
10U
98
96
9U
98
92
93
78
Temp.
Feed
Tank
9U
9U
80
70
91
9U
88
93
92
U6
Feed
Rate
20-UO
30
30-UO
30
0
30
0
100
30
0
.22
0
30_
100
1
30
1*0
Cone.
0
0
0
0
0
0
0
0
0
0
-------
Date/
Iir.e
10/6/71
1:00 A
2:CO
3:00
U:00
5:00
-
-------
Date/
Tir.e
10 '6/71
2:00 P
3:00
U:00
5:00
6:00
7:00
8:00
9:00
10:00
11:00
12:00 M
10/7/71
1:00 A
2:00
ivap.
Fuel
Valve
tc
Cper.
1 15
2 15
1 15
2 15
1 15
2 15
1 15
2 15
1 15
2 15
1 15
2 15
1 15
2 15
1 15
2 15
1 15
2 15
1 15
2 15
1 15
Z 15
1 15
2 15
1 15
2 15
Burners
Levels &
Evap.
Board
LI LIC
30
ao
71
73
71
77
7U
67
59
56
56
1*6
U8
2U.O
2U. 0
21.5
21.0
21.0
23.0
21.5
20.5
18.0
17.0
17.0
1U.O
1U.5
Terr.p.
Therminol
Drex
LI PSIG Gas Meter
62
63
63
60
U2
52
58
U2
Ul
20
21
22,000-23,000
U695556
22,000-23,000
U70U287
2200-2300
U712359
2200
U721999
2100-2200
U730739
2150-2200
U7395U9
Stack
Temp.
192.0
193
192
192
192
193
192
192
192
191
192
191
192
Temp.
Out
Evap.
Moyno
185
186
187
186
185
182
186
177
182
179
181
177
185
Gas
Orifice... P Gas
P <;1P Press
#1 #2 PSIG
6.5
6.5
6.75
6.6
7.2
7.1
6.5
6.6
5-9
5.9
5.9
5.2
5.8 U.io
6.0 l*. lo
6.0 U.15
6.1 U.15
6.0 U.I
5.9 U.I
6.0 U.15
6.1 U.15
6.2 U.I
6.3 U.15
6.2 U.15
6.3 U.15
6.6 U.15
Burner
AirAP
#1 #2
15-22
15-22
15-20
17-22
15-20
17-22
13-23
15-23
15-23
20
lU-23
15-25
16-20
10-20
10-20
8-18
10-22
10-22
10-25
8-25
10-25
10-23
10-25
10-25
10-25
12-18
Blcwer Output
Amps
102
98
102
100
102
95
92
96
100
80
92
102
92
Tenp.
Feed
Tank
66
76
82
90
89
90
90
80
75
90
90
92
90
Feed
Rate
""0
0
$
1
i
I
to
30
3_0
79
-4
0^6
I?.
32
U2
T*I
U2
Oonc.
32
16
28
U3
0
0
0
0
8
0
0
0
0
-------
Burners Blcwer (Mtput
Date/
Tir.5
10/7/-1
3:00 A
U;00
5:00
6:00
7:00
8:00
_j
00 9:00
10:00
11:00
12:00 11
1:00 P
2:00
3:00
F-uei
Valve
tc
CUer.
1 15
2 1U.75
1 lU. 3
2 lli. 3
1 1U.8
2 lU.8
1 1U.8
2 lU.8
1 1U.3
2 1U.8
1 lU.8
2 lU.3
1 lU.8
2 lU.8
1 lU.8
2 1U.8
1 1U.3
2 lU.8
1 lU.8
2 lU.8
1 lU.8
2 1U.8
1 lU.8
2 lU.8
1 lU.8
2 lU.8
I.
.'.vels & Temp.
Evap.
Beard
LI LIC
UU
U6
U7
U2
U2
U6
1*6
1*6
U6
U6
U6
U6
U6
13-5
lU.O
lU.O
13.0
12.8
lU.O
lU.O
lU.O
lU.O
lU.O
lU.O
lU.O
lU
Drex
LI PSI
23
2U
26
27
27
29
29
31
33
33
3U
3U
33
Therrainol
G Gas Meter
2300-2UOO
U7U8627
23.2(U75713U)
23.0(U?66lOO)
23.2(U775762)
23.0(U785232)
23500-22500
U79U022
23500-sUoOO
U80U217
Stack
Temp.
193
193
193
193
193
193
193
193
193
193
193
193
193
Temp.
Out
Evap.
Moyno
ie-j
180
170
167
166
173
17U
1?U
176
176
176
176
171
Gas
Orifice A P
NP ^P
#1 fe
7.3
7.2
6.9
6.9
6.9
6.8
7.0
6.9
6.9
6.9
6.8
7.2
7.7
7.0
6.9
6.9
7.0
6.9
6.9
6.9
6.9
6.9
7.0
7.0
7.0
6.9
Gas
Press
PSIG
U.l
U.l
U.l
U.l
U.l
U.l
U.l
U.l
U.l
U.l
U.15
U.10
U.l
Burner
AirA P
#1 #2
8-20
15-20
16-20
15-20
15-20
16-21
17-22
15-20
15-19
15-19
17-16
17-18
19-20
13-20
13-20
13-20
13-22
lU-23
17-23
15-22
13-20
13-20
15-20
13-18
12-18
13-17
Amps
86
91
8U
88
85
86
85
81
96
95
98
98
98
Feed
Tank
92
9U
95
95
95
95
95
95
91
90
82
68
50
Feed
Fate
38
IB
22.
to
31
35
26
37
37
15
UO
Til
1*0
51
38
Uo
3J
W
3i_
39-5
3§
39
38
39-5
Cone.
0
0
0
0
0
0
0
1U
30
U6
62
65
76
-------
Date/
Tire
ic/-/-i
1*:00 P
f :CO
6:00
7:00
3:00
9:00
Evap.
Fuel
Valve
tc
Cper.
1 iL ^
2 1U.6
1 1L.9
2 l-.S
1 lit. 8
2 1U.3
1 11*. 8
2 lU.S
1 1U.3
2 lli. 3
1 1U.8
2 1U.9
Burners
Levels &
2vap.
Board
'LI LIC
36
29
?1
29
30
30
11
8.5
9.0
9.0
9.0
9.0
Temp.
Therminol
Drex
LI PSIG Gas Meter
30
27
28
30
32
32
2UOOO
1*812001*
21*000-21*500
1*822611*
21*000-21*500
>*833005
Stack
Temp.
193
193
193
192.5
193
193
Temp.
Out
Evap.
Moyno
180
178
176
177
178
Gas
Orifi.ce/-.P Gas
AP AP Press
#1 #2 PSIG
8.0 7.0 U.05
7.6 7.1* 1*.10
7.50 7.3 't.lO
7.70 7.30 1*.10
7.70 7.30 !*.15
8.10 7.1*0 U.05
Burner
Air,:.P
#1 #2
22
23-2U
22-2U
23-25
2l*-25
27.5
12-18
15-20
15-20
15-20
15-20
15-20
Blcwer Cutput
Tenp.
Feed
Amps Tank
100 58
106 70
106 81*
102 87
IQl* 88
106 88
Feed
Rate
28
39
33
39.5
1*2
TO
1*2
T*3
1*1*
55
l+i*
^*5
Cone.
76
71
1*5
38
3*
36
10:15 SHUTDOWN
-------
AFPEMDIX I - NON JACKETED DOWWCOMER TESTS
FEED AND PRODUCT SAMPLES
Date
10/U/71
10/V71
10/5/71
10/5/71
10/5/71
10/5/71
10/5/71
10/5/71
10/5/71
10/5/71
10/5/71
10/5/71
10/5/71
10/5/71
10/5/71
10/5/71
10/6/71
10/6/71
10/6/71
10/6/71
10/6/71
Time
U:00 PM
6:00 PM
12:20 PM
12:35 PM
2:00 PM
3:00 PM
3:00 PM
1^:00 PM
5:00 PM
6:00 PM
6:00 PM
7:00 PM
8:00 PM
9:00 PM
9:00 PM
11:00 PM
12:15 AM
1:00 AM
1:15 AM
2:00 AM
3:00 AM
Sample
No.
1
3
l
2
5
6
7
9
10
11
12
lU
15
16
17
19
20
22
23
2h
25
Sample
Description
Feed
Feed
Feed
Feed
Cone.
Cone.
Feed
Cone.
Cone.
Cone.
Feed
Cone.
Cone.
Cone.
Feed
Cone .
Feed
Cone.
Sight Glass
Foam
Cone.
Cone.
% T.S. % S.S.
1.56 .7^5
1.505 .69
1.97 1.025
2.08 1.01
3-2
U:5
2.10 1.02
U.79
5.32
5.96
2.13 1.07
6.83
7.21
7.79
2.1+0 1.39
8.33
2.66 i.Ul
8,60
8.97
9-1
10.05
80
-------
Date
10/6/71
10/6/71
10/6/71
10/6/71
10/6/71
10/6/71
10/6/71
10/6/71
10/6/71
10/6/71
10/6/71
10/6/71
10/6/71
10/6/71
10/6/71
10/6/71
10/6/71
10/6/71
10/6/71
10/6/71
10/6/71
10/6/71
10/6/71
10/6/71
Time
3:15 AM
U:00 AM
5:00 AM
5:15 AM
6:00 AM
6:15 AM
7:00 AM
8:00 AM
9:00 AM
9:15 AM
10:00 AM
11:00 AM
12:00 K
12:00 N
1:00 PM
2:00 PM
3:00 PM
U:00 PM
5:00 PM
6:00 PM
6:00 PM
7:00 PM
8:00 PM
9:00 PM
Sample
No.
26
28
29
30
32
33
35
36
37
38
ho
hi
h2
h3
±5
U6
hi
h9
50
1
2
h
5
6
Sample
Description
Feed
Cone.
Cone.
Stack
Condensate
Cone.
Feed
Cone.
Cone.
Cone.
Feed
Cone.
Cone.
Cone.
Feed
Cone.
Cone.
Feed
Cone.
Cone.
Cone.
Feed
Cone.
Cone.
Cone.
i T.S. % S.S.
2.35 1.11
11.0
11.6
1.08 .65
11.90
2.22 .965
12. k
13-1
1U.6
2. hO 1.12
lh.7
15.3
16.0
2.59 1.19
17.27
2.23 1.06
15.06
19.07
19.36
2.59 1.30
20.02
19.83
19.58
81
-------
Date
10/6/71
10/6/71
10/6/71
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
Time
9:00 PM
10:00 PM
11:00 PM
12:00 M
12:00 M
1:00 AM
2:00 AM
3:00 AM
3:15 AM
1+:00 AM
5:00 AM
6:00 AM
6:15 AM
7:00 AM
8:00 AM
8:30 AM
9:00 AM
9:15 AM
10:00 AM
11:00 AM
12:00 N
11:1+5 AM
1:00 PM
2:00 PM
Sample
No.
7
9
10
11
12
lU
15
16
17
19
20
21
22
2U
25
26
28
29
31
32
33
3^
36
37
Sample
Description
Feed
Cone.
Cone.
Cone.
Feed
Cone.
Cone.
Cone.
Feed
Cone.
Cone.
Cone.
Feed
Cone.
Cone.
Stack
Condensate
Cone.
Feed
Cone.
Cone.
Cone.
Feed
Cone.
Cone .
% T.S. i S.S.
2.59 1-3^
18.32
18.70
17.83
2.75 1.50
18.60
16.12
16.93
2.70 1.53
15.62
15.00
19.52
2.90 1.63
20.2
20.1
.73 .37
20.25
2.52 1.39
20.75
20.75
20.75
'2.36 1.30
20.00
20.22
82
-------
Date
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
10/7/71
10/8/71
10/8/71
10/8/71
Time
2:53 PM
3:00 PM
U:00 PM
5:00 PM
6:00 PM
6:00 PM
7:00 PM
8:00 PM
9:00 PM
9:00 PM
1:00 PM
Sample
No.
38
Uo
1*2
^3
1*1*
^5
1
2
3
1*
6
7
8
Sample
Description
Feed
Cone.
Cone.
Cone.
Cone.
Feed
Cone.
Cone.
Cone.
Feed
Sweco
Overflow
Sweco
Overflow
Sweco
Overflow
1o T.S. io S.S.
2.17 l.lU
22.00
21.02
21.68
22.22
2.U2 1.21*
22.30
23.12
22.55
2.89 1.50
6.69
6.36
6.65
83
-------
APPENDIX J - fiVAPCRATOR TESTS USIKC
INCONEL 601 DCWNOOMERS - SERIES 1
Temp.
Out Gas Orifice Gas Burner Feed Cone. Cone.
Eate/
Tire
12/2/71
5:15 A
5:^5
6:U5
12/U/71
8:30 A
9:00
10:00
11:00
12:00 N
1:00 P
2:00
3:30
U:30
=1 Panel -Fox Drexel Gas Rec
=2 LI LIC Brook Flow
START-UP
6.0
15.0 60.0 18.0 58
1U.3
15.0 67.0 20.5 56
0
U883882
£4
cT? 63 19.25 100+
9.8
O 6U 19.5 100+
9.7 13,000
o77 65 20 100+ U893U66
9.7
63 6U 19.75 100+
9.e 13,000
oTE 65 19.75 100+ UgooUio
&H* 63 19.00 100+
OPENED UP & DRA
LOWERED LEVEL I
Stack
Temp.
192
190.5
192.5
191.5
189
189
188
I N E D
N EVA
of
Moyno
18U
STAR
120
187
187
183
181
183
C 0 N D
P 0 R A
AP
#1 #2
M
3.5
T -
U.I
3.5
2.2
2.1
2.0
2.0
E N
T 0
,
2.7
0 P
U.I
3.6
2.U
2.3
2.2
2-3/8
SATE
R P
Press AirAp
PsiR #1 #2
U.2
U.2 13-lU 6-7
U.15 13-15 10-20
U.2 10-11 12-15
U.2 1) 10-20
U.2 1-3 0-10
U.2 1-3 0-10
U.O
U.2 2-8 0-10
STACK
ERFORMANCE
Blower Tank Feed Tank $ Tank Blower
Amps Level Rate Level T.S. Press Output
70 92 30-Uo 0
89-90 78 U-7 1JX) 3.3
83 85 30-Uo 100
60 86 16 0 3.8
53 82 6 0
5U 78 10 0 U.5
5U psig 6.75
U6 2.0 6.50
75 Amps
65
INCREASED
-------
KIC
Temp.
Out Gas Orifice Gas Burner Feed Ccnc. Cone.
Eate/
12/L/71
5:00 ?
f:00
7:00
3:00
9:00
10:00
00
\J1 11:00
12/5/71
12:00 M
1:00 A
2:00
3:00
1*:00
5:00
6:00
S5
8
10.2
C *
10.1
10.1
10.1
10.1
10.1
10.1
10.1
10.1
10.1
10.1
10.1
10.1
Panel Fox
LI LI"
5'*
5~
56
56
55
56
58
60
6U
61*
69
63
56
61
17.00
17.50
17.0
17
17.5
17.75
18.0
18.5
19.0
19.5
17.0
18.5
16.5
20.0
Drexel
Brook
100+
100+
86-
100+
80-90
70-80
70-80
50-60
50-66
1*0
--
56
Gas Eec.
Flow
19-17000
!, 01 5003
17-20,000
U92U232
18-19,500
1*929912
38-19,500
1*929912
18-20,000
1*935753
18-20,000
1*91*3190
18-20,000
1*950938
19,500
1*959075
Stack
Temp.
192
192
193
191.5
192.0
192.0
193.5
193
193
193
191
193
190
192
of
Moyno
187
190
191
190
190
190
189
187
187
186
181*
183
183
182
AP Press
#1 #2 Psig
3.75 3.75
3.90 U.25
I*. 10 U-3/8
U.I U-3/8
U.3 U-5/8
U.3 U-5/8
i*.25 U-7/16
U.io i*-5/8
U.2 U.6
U.2 U.7
U.U U.9
U.3 U.9
U.3 U.9
U.15 U.8
U.2
U.2
U.2
U.2
U.2
U.I
U.2
U.2
U.15
U.15
U.15
U.15
U.15
U.15
#1
15
15
lU-16
15
13-15
12 -1U
13-15
13-15
1U
1U
1U
1U
lU
13
''#>
15
16
27
17
26
18-19
29
17-18
29
16-19
31
15-20
30
18
37
18
30
18
25
20
26
20
30
18
11
Blcver
Amps
86
88
88-90
90
93
92
91
91
91
92
91
92
92
92
Tank Feed
Level Rate
30-Uo
18-26
Full 26-30
Full 0
92 o
83 o
82 0
Full 0
Full 0
Full 0
Full 100+
Full 0
96 0
Tar.k £
Ls^el T.S.
0
5.2
26
20 6.2
16 8.00
1U
2U 9.9
19
16 10. U
16
28 11.9
36 12.8
U3 lU.o
Tank Blcwer
Press Cutout
.7
.7
.U
0
0
0
0
0
0
0
0
0
0
0
7-1/8
7-1/3
7-1/8
7-1/16
7-1/16
7-1/16
7-1/8
7-1/8
7.1
7.05
7.05
7.0
7.0
7.0
-------
Temp.
Out Gas Orifice Gas
tire
12/5/71
?:00 A
3:00
9:00
10:00
11:00
12:00 II
1:00 P
3:00
U:00
5:00
6:00
7:00
8:00
9:00
^1 Par.el Fox
? II LIC
10.1
Sr
10.1
10.2
10.2
10.1
10.1
10.2
10.1
10.1
10.1
10.1
10.1
10.1
55
60
63
60
57
60
69
56
57
56
57
56
55
55
18.5
17.5
19.5
17.5
18.5
18
17.75
17.25
17.25
17.25
17.50
17.0
17.0
17.0
Drexel Gas Rfic.
Brock Flow
18-20,500
U967037
19,000
U975035
~
18,500
1*9875911
18,500
5003160
«
17500-19000.
5011090
__
Stack
Temp.
191
192
193
193
192.5
192
192
192
192
192
192
192
192
192
of
Moyno
180
178
177
176
17U
173
171
171
170
169
170
17U
17U
#1 '
U.2
U.2
U.2
U.2
U.2
U.2
U.I
U.2
U.I
U.I
U.2
U.I
U.I
U.l
ff Press
#2 PsiK
U.8
U.9
U.8
U.7
U.6
U.7
U.7
U.I
U.2
U.I
U.o
U-l/16
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
Air
#1
13
12-13
13
10-15
10-12
13-15
15
12-15
10-12
10-13
10-12
10-13
10-12
10-13
AP
#2
35
18-19
33
17-19
30
17-19
15-20
15-20
15-20
15-20
15-20
13-19
15-20
15-20
15-20
15-20
15-20
Blower Tank
Amps Level
93
92
91
92
91
92
90
91
90
90
90
91
92
92
98
96
97
92
8U
71
59
71
61
52 '
68
8U
92
82
Feed
Kate
0
100+
100+
0
100+
0
0
30
28- 3U
28-3U
Uo
35
35
35
Tank *-
Level T.S.
50
58
6U 15.7
70 17.3
69 17. U
69 17.8
69
56 19.2
U3
3U 20.0
32 20.2
UO 21.0
55 20.0
65 20.5
Tank
Press
0
0
0
0
0
0
0
0
0
0
0
0
0
0
Blower
Output
7.0
7.0
7.0
6.9
6.9
6.9
6.9
6.9
6.9
6.9
7.0
7.0
7.1
7.1
-------
rate/
Tir.e
12/5/71
10:00 ?
il:GO
12/6/71
12 :oo:-:
1:00 A
2:00
3:00
U:00
.5:00
7:00
8:00
9:00
10:00
11:00
12:00 ::
1
10.1
10.1
10. 1
10 .j.
10.1
log
10.1
6.0
FTT
10. 1
10.1
10.1
10.1
10. 1
10.2-
vlr1
56
56
56
56
55
56
56
56
56
56
56
56
56
LI?
17.0
17.0
17.0
17.0
17.0
16.5
16.5
17.'0
17.0
17.0
17.0
17.0
17.0
17.0
Drixel Otic Rec.
Brook Flew
17500-19000
5026110
18?00- 17500
5029950
--
18500-18000
5038076
19-17,000
50U536
--
18,000
5052919
18-19,000
5060770
18-19,500
5068762
18-19,500
5076669
Stack
Temp.
192
192
192
192
192
192.
192
192
192
192
192
192
192
192
Temp.
Out
of
Moyno
175
175
176
176
176
17U
173
175
173
173
172
172
173
172
Gas Orifice
AP
#1 fc
U.I
U.I
U.I
U.I
3.8
3.8
3.8
U.I
U.I
U.I
U.I
U.I
U.O
U.15
3.75
3.80
3.85
3.85
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
Gas
Press
Ps if?
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
Burner
AirA.P
#1 #>
10-12 15-20
10-12 15-22
10-12 12-20
10-12 15-20
10-12 15-20
10-12 15-20
10-12 15-20
12 18
12 17-19
12 17-19
12 17-19
10-11 17-19
10-11 17-19
10-11 15-20
Feed
Blcver Tank
A::.TJS Level
92
90
91
91
91
90
90
90
90
92
91
91
91
90
76
92
9U
9U
9U
9U
95
93
95
9U
85
90
96
9U
Feed
Fate
35.5
35.5
35.5
35.5
35.5
35.5
35.5
35.5
35.5
35.5
35.5
3U
3U
3U
Icnc. Cone.
Tank ?>
Level T.3.
78 21.0
88 20. U
96 19.7
100+ 19.0
100+ 20. U
100+ 20. U
100+ 18.5
100+ 18.5
100+ 19.1
100+ 19.1
100+ 19.0
100+ 20.00
91 19-5
76 18.9
Tank Elcwer
Press Cutput
0 7.0
0 7.0
0 7.0
0 7-0
0 7.0
0 7.0
0 7.0
0 7.0
0 7.0
0 7.0
0 7.0
0 7.0
0 7.05
0 7.0
-------
~Tir.e
12/6/71
1:CO ?
2:00
3:00
5:00
6:00
7:00
8:00
9:00
10:00
11:00
12/7/71
16:00 M
1:00 A
2:00
3:00
=1
10.2
10.2
10.2
10.1
10.2
57T
10.1
10.1
10.1
10.1
5~r
10.1
6.9
10,. 1
10.1
10.1
Panel Fox Drcxel Gas Rec.
LI LIC Brook Flow
56
56
55
55
55
55
56
56
56
56
56
55
56
56
16.5
17.0
16.75
16.75
16.75
17.0
17.0
17.0
17.0
17.0
17.0
17.0
17.0
17.0
18,000
5091UOO
19,000
51060U2
18,500
51116UO
18,500
5H9U37
17000-18500
5126880
18,000
Stack
Temp.
192
192
192
192
192
195
192
192
192
192
192
192
192
192
Temp.
Out
of
Moyno
172
172
172
173
172
172
172
170
172
172
172
172
172
172
Gas Orifice
#1 '' #2
U.I
U.I
U.O
U.O
U.O
U.O
U.O
3.9
3-95
3.90
U.O
U.05
U.oo
U.oo
3.75
3.7
U.2
U.15
U.2
U.15
U.I
U.I
U.I
U.O
U.O
U.I
U.I
U.I
Gas
Press
PsiK
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
Burner
AirAP
#1 #2
10-12
10-11
10-12
10-12
10-12
10-13
10-12
10-12
10-12
10-12
10-12
10-12
9-11
9-11
15-20
16-19
15-20
15-20
15-20
lU-19
15-20
15-22
15-20
13-21
13-20
10-25
10-25
10-25
Feed
Blower Tank
Amps Level
91
90
91
91
90
91
90
91
91
91
91
91
91
92
9U
95
96
97
97
6U
70
72
8U
90
96
96
96
Feed
Rate
33
33
33
33
33
33
33
33
33
33
3U
3U
3U
35
Cone.
Tank
Level
5U
36
27
29
32
32
31
33
32
3U
Uo
50
62
75
Cone.
T.S.
18.7
18.2
18.3
19-7
19.6
19-7
20.2
20.0
21.0
21.5
20.8
21.8
22.0
22.0
Tank Blcver
Press Output
0
0
0
0
0
0
0
0
0
0
0
0
0
0
7.0
7.0
7.0
7.0
7.0
7.0
7.1
7.1
7.1
7.1
7.15
7.15
7.20
7.20
-------
Temp.
Out Gas Orifice Gas Burner Feed
Ccnc. Oonc.
.rate/
7ir.*
12/7/71
-:00 A
5:00
6:00
7:00
3:00
CO 9:00
VO
10:00
11:00
12:00 B
1:00 P
2:00
3:00
U:00
5:00
-I
=>
10.1
6.9
10.1
6.9
10.1
^9~
10.1
?79~
10.1
10.1
10.1
*T
10.0
5T
10.0
5T
10.0
ST
10.0
^9"
10.0
S7T
10.0
?X
10.0
TT"
Par.sl
LI
56
56
56
56
55
57
56
56
56
55
55
56
56
55
Fox Drexel Gas Rec.
LIO Brook Flow
17.0
17.0
17.0
17.0
16.5
17.5
17.0
17.0
17.0
16.5
17.0
17.0
17.0
17.0
18,000
51U2000
17-18,500
51U9772
18,000
5157525
5161*707
17-18.500
5172U69
17-18,500
5176020
17-19,000
5180188
18000-19000
5187917
Stack
Temp.
191.5
191.5
192
191.5
192
192
192
192
192
192
192
192
192
192
of
Moyno
172
171
169
169
170
173
173
173
173
176
171*
17l*
17!*
17!;
AP
#1 #2
U.oo
U.05
U.05
U.oo
U.oo
U.05
U.05
U.05
U.I
U.I
U.I
U.I
U.I
U.I
U.05
U.io
U.io
U.IO
U.15
U.IO
U.IO
U.I
U.25
U.25
U.30
U.3
>i.35
U.35
Press
Psig
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.2
AirAP
#1 #2
9-11
9-11
9-11
9-11
9-11
8-10
8-10
7-10
7-10
7-9
6-9
7-9
7-9
6-9
10-25
10-25
10-25
15-25
15-25
15-25
15-22
15-22
15-23
15-20
lU-19
15-20
lU-19
lU-19
Blower
Amps
92
93
93
91
91
91
91
90
90
90
SO
90
91
91
Tank Feed
Level Rate
96
96
96
oU
9U
9^
92
92
86
61
66
75
80
83
35
35
35
35
35
35
35
35
35
35
35
3U
3U
3U
Tank
Level
86
95
95
92
88
86
86
92
92
88
78
66
66
58
rt
T.S.
22.0
20.0
20.7
21.0
21.0
21.0
20.8
18.8
19.6
19.2
19-3
18.7
18.9
18.0
Tank Blcwer
Press Output
0
0
0
0
0
0
0
0
0
0
0
0
0
0
7.20
7.25
7.20
7.25
7.25
7.20
7.0
7.0
6.95
7.0
6.9
6.9
6.9
6.9
-------
Temp.
KI7 Out Gas Orifice Gas Burner Feed Cone. Cone. x
^1 Pans! Fo>: Drexel Gas Rec. Stack of AP Press AirAP Blower Tank Feed Tank 3 Tank Blcver
Tir.e "2 LI LIC Brook Flow Temp. Moyno #1 fe Psig #1 #2 Amps Level Rate Level T.S. Press Output
12/7/71
c:00 P
~:00
5:00
9:00
10:00
11:00
12/6/71
12:00 M
1:00 A
2:00
3:00
U:00
5:00
6:00
7:00
0.3
7.1
7\i
23.
10.1
7.0
10.1
7.0
10.0
7.0
10.0
7.0
10.0
7.0
10.0
7.0
10.0
7.0
10.0
7.0
10.0
7.0
2il
7.0
7)0
5U
56
5U
55
55
56
56
56
56
56
56
5U
56-
55
16.75
17.0
16.75
16.75
16.25
17.0
17.0
17.0
17.0
17.0
17
16.25
16.75
16.75
17500-19000
51957U2
17500-19000
17500-19000
5210972
17500-19000
5219165
17500-19000
5226863-
17500-19000
523U725
18750-17250
52U2617
192
192
192
192
192
192
192
192
192
192
192
192
192
192
173
170
169
170
171
170
170
171
172
r/U
173
17U
171
U.I
U.I
U.l
U.l
U.I
U.l
U.l
U.l
U.l
U.O
3.95
U.O
3.90
3.85
U.U
U.35
U.35
U.35
U.35
U.35
U.35
U.30
U.3
U.25
U.30
U.30
U.30
U.30
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
7-9
7-9
8-10
8-10
7-10
8-10
7-9
7-9
7-9
7-9
7-9
7-9
7-9
7-9
15-20
lU-19
16-20
15-20
15-20
lU-19
15-20
15-22
13-22
13-22
13-22
18-22
37
19-22
91.5
91
91
91
91
91
90.5
92
92
91
91
91
91
91
90
95
97
96
95
93
93
93
93
93
92
92
92
91
32.5
33.5
33
33
33
33
33
33
33
33
33
33
33
33
U5
26
lU
15
16
15
15
22
2U
2U
2U
26
19
16
18.5
18.8
19.2
19.6
20.7
20.7
20.9
20.8
20.2
21. U
21.7
21.7
0
0
0
0
0
0
0
0
0
0
0
0
0
0
6.9
6.9
6.9
6.9
6.9
6.9
6.9
6.95
6.95
6.95
6.95
6.95
6.95
6.95
-------
Temp.
HIC Out Gas Orifice Gas Burner Feed Cone. Cone.
Bate/ --1 Panel Fcx Drexel Gas Rec. Stack of AP Press AirAP Blower Tank Feed Tank 3 Tank Blcver
"ir.e --g LI LIC Br ook_ Flow Temp. Moyno #L #2 Pslg #1 #2 Amps Level Rate Level T.S. Press Output
12/8/71
8:00
9:00
10:00
11:00
12:00 11
1:00 P
£ 2!°°
3:00
U:00
5:00
6:00
7:00
8:00
9:00
ill
7.0
7.0
2^
-.0
7.0
2i2
7.0
o.o
tlo
*?
T"~O
10.0
7.0
10.0
7.0
10.0
7.0
10.0
7.0
10.0
7.0
10.0
57
56
56
56
56
56
56
55
56
56
55
56
56
56
17.25
17.00
17.0
17.0
17.0
17.0
17.0
17.0
17.0
17.0
16.75
17.0
17.0
17.0
19000-16750
5250981
19,250-16250
5258896
17000-13500
52669UO
19000-16250
527U118
16000-19000
5285773
17000-19000
5302U80
192
192
192
192
192
192
192
192
192
192
192
192
192
192
173
>*
171
172
172
173
173
173
173
173
172
169
169
169
173
3.95
3.75
3.95
U.o
U.O
U.O
3.95
U.05
U.05
U.o
U.o
3.9
3.9
3.9
U.20
U.20
U.15
U.20
U.20
U.20
U.20
U.20
U.25
U.2
U.25
U.25
U.25
U.2
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.15
7-9
7-8
7-8
7-10
6-8
6-8
6-8
6-9
6-7
7-9
7-9
7-9
8-10
7-9
17-25
10-25
15-20
15-23
10-25
10-25
10-25
10-25
10-25
15-20
15-20
15-20
15-20
15-20
91
90
88
88
88
88
89
88
89
89
89
89
89
89
91
92
92
89
93
U6
56
67
82
92
93
92
80
66
33
33
33
33
33
33
33
33
33
33
33.5
33.5
33-5
33.5
19
17
39
60
80
80
77
75
66
62
63
56
50
Uo
21.7
21.0
21.0
21.3
21.1
21.2
21.1
20.8
20.9
20.5
20.8
20.9
20.2
0
0
0
0
0
0
0
0
0
0
0
0
0
0
6.95
6.90
6.90
6.90
6.80
6.80
6.80
6.80
6.8
6.8
6.8
6.35
6.8
6.8
-------
Temp.
HI~ Out Gas Orifice Gas Burner Fs?i 'cr.:. ?cnc.
Date/ ^i Panel Fox Drexel Gas Rec. Stack of t.? Press AirAP Blower Tank Feed Tank "! TarJt Slcver
-a LI LIC Brook Flow Temp. Moyno #1 jfe Psig #1 #2 Amps Lovel Rate L°Vel T.S. Press Output
vo
12 '?'"!
10:00 ?
11:00
12/9/71
12:00 .X
1:00 A
2:00
3:00
U:00
5:00
6:00
7:00
8:00
9:00
C.T
T'°
ill
P.;
7.0
1C.O
7.0
10.0
7.0
10.0
7.0
10.0
".0
10.0
7.0
10.0
7.0
10.0
7'.0
10.0
7.0
5f
55
56
55
56
55
5c
56
56
56
56
55
17.0
16.75
16.75
16.75
17.0
17.0
17.0
17.0
17.0
17
17
17
192
192
192
17500-18500
531UU20 192
192
17000-18500
5323160 192
192
17000-19000
5333055 192
192
192
17000-18750
53U5U86 192
192
173
173
172
17U
17U
17U
176
176
177
176
176
1-7U
3.9
3.9
3.9
3.9
3.9
3.95
U.lO
U.15
U.15
U.20
U.I
U.15
U.25
U.25
U.25
U.25
U.25
U.25
U.30
U.30
U.30
U.30
U.3
U.3
U.15
U.15
U.15
U.15
U.15
U.15
U.15
U.20
U.20
U.20
U.15
U.20
7-9
6-10
7-9
7-9
7-9
7-9
6-8
7-8
6-8
6-8
1U-18
1U-18
15-20
16-19
15-20
15-20
15-20
15-20
15-18
lU-20
15-18
15-18
6-8
6-8
88
88
88
87.5
87.5
87.5
87
88
88
88
88.
89
72
77
85
93
88
88
83
38
89
33
83
88
33-5
33.5
33-5
33.5
33.5
33.5
33.0
33
33
33
33
33
l
29
22
20
23
17
19
2U
39
1-2
U2
52
19.3 0
19.7 0
0
19-9 0
0
20.0 0
19-5 0
0
0
0
20.3 o
15.6 0
6.3
6.8
6.8
6.8
6.8
6.8
6.75
6.70
6.70
6.70
6.75
6.65
-------
APPENDIX K - INCONEL 601 DOWNCOMER
* TESTS - SERIES 1
FEED AND PRODUCT SAMPLES
Sample Ratio
Date Time No. Sample Description jo T.S jo S.S SS/IS
12/2 5;ll5 AM #1 Evaporator Bottoms 2.72
#2 Midnight 1.22 .82
12/2 6:15 AM #3 Evap. Feed 2.56
#i .81? .U68
12/2 Noon #k Evap. Feed 2.60
#5 , 1.125 .75
Second Startup After Repairs
12/k 7:^5 AM #7 Evap. Feed During 2.53 -975
Startup
#8 1.25
12A 11:30 AM #9 Feed 2.36 .905
#10 1.12
12/H 5:30 PM #11 Feed 2.53
#12 1.25 .98
12A 8:30 PM #13 Feed 2.78
#ll* 1.U2 .96
12A 11:30 PM #15 Feed 2.80
#16 I-1* -^
12/5 2:.30 AM #17 Feed 2.87
#18 I-1*0 -95
12/5 5:30 AM #19 Feed 2.67
93
-------
Sample Ratio
Date Time No. Sample Description <%> T.S j, S.S SS/IS
12/5 5:30 AM #20 Feed 1.22 .84
12/5 7:30 AM #21 2.63
#22 1.19 -82
12/5 11:30 AM #23 2.31
#24 1.06 .85
12/5 4:30 PM #25 Cone. 21.4
12/5 5:20 PM #26 Cone. 21.8
12/5 5:45 PM #2? 2.60 1.20 .85
#28
12/5 8:30 PM #29 Feed 2.73
#30 Feed 1.35 .98
12/5 9:30 PM #31 Cone. 20.5
12/6 3:00 AM #32 Feed 2.57
#33 Feed 1.29 1.02
12/6 7:30 AM #34 Cone. 19-72
12/6 7:45 AM #35 Feed 2.29
#36 Feed 1.11 .94
12/6 10:30 AM #37 Cone. 18.88
12/6 10:45 AM #38 Feed 2.38 1.05
#39 Feed 1.22
12/6 5:30 PM #40 Feed 3-00
#41 Feed 1.59 1.13
12/6 9:45 PM #42 Feed 3-^0
#43 1.70 1.00
94
-------
Date
12/7
12/7
12/7
12/7
12/7
12/7
12/8
12/8
12/8
12/8
12/8
12/8
12/8
12/8
Time
2:U5 AM
8:U5 AM
,
12:^5 PM
2:35 PM
5:00 PM
10:00 PM
2:00 AM
5:^5 AM
5:^5 AM
5:^5 AM
5:U5 AM
6:30 AM
7:50 AM
10:UO AM
Sample
No.
#1
#2
#3
.fr
#5
&
#7
#8
#9
#10
#11
#12
#13
#1^
#15
#16
#17
#18
#19
#20
#21
#22
#23
#2^
Sample Description
*
Feed
Feed
Feed
Feed
Cone.
Feed
Feed
Feed
Cone, to Recycle
Press Output
Recycle to Dryer
Dry Grain to Recycle
Feed
Recycle
Cone, to Recycle
Dry Grain
Press Grain
Feed
jo T.S "lo S.S
3A5
1.88
3.35
1.8^
3-9^
1.81
20.31
2.97
l.lOf
3.22
l.6l
3.32
1.75
20.0
30.3
51.8
83.8
3>2
1.73
61.0
19-3
91-5
3^.8
3.20
Ratio
SS/IS
1.20
1.22
.85
.9^
1.00
1.12
1.02
95
-------
Date
12/8
12/8
12/8
12/8
12/8
12/8
12/8
12/8
12/8
12/8
12/8
12/8
12/8
12/8
12/8
12/8
12/9
10
u
5
5
5
5
6
7
8
9
10
10
10
10
10
11
1
Time
:1*0 AM
:35
:15
:15
:15
:15
:20
:50
*5
:U5
:30
:30
:30
:30
:30
:1*0
:35
PM
PM
PM
PM
PM
PM
PM
PM
PM
PM
PM
PM
PM
PM
PM
AM
Sample
No.
#25
#27
#28
#29
#30
#31
#32
#33
#3^
#35
#36
#37
#38
#39
#UO
#^1
#U2
Sample Description ^_
Brewhouse D
Cone.
Press
.W.
q a TT n
o. rtpU
to Recycle
Grain
2
Presses
Recycle to Dryer
Dry Grain
Brewhouse D
Brewhouse D
6 Min.
Feed
12
Brewhouse D
6 Min.
Press
Press
- 11
#1
#2
.W.
.W.
S.
S.
2
23
U3
55
90
2
1
£1
S
.06
.0
.5
.0
« T*
.73
.95
Min. Total
.W.
S.
3
2
.13
.00
Min. Total
#^3 Recycle to Dryer
1*1
41
55
.8
.8
.7
#M*- Dry Grain 89.1*
#1*5
Cone.
to Recycle
#1*6 Brewhouse D
#^7
#^8
#^9
1* Min.
- 10
Brewhouse D
U Min.
.W.
S.
20
1
.8
-56
Min. Total
.W.
- 9 Min
S.
. Total
1
.72
Ratio
S.S SS/IS
Dewatering Screen
1.63
.96
.85
1.05
.73
.82
.87
1.51 1.23
.77
.85
.91
96
-------
Date
12/9
12/9
12/9
12/9
12/9
12/9
12/9
12/9
Time
2:30 AM
3:35 AM
3:UO AM
3:UO AM
3:^0 AM
3:UO AM
3:hO AM
6:15 AM
7: to AM
12:^5 PM
12:^5 PM
12:^5 PM
l:to PM
l:to PM
3:UO PM
Sample
No.
#50
#51
#52
#53
#1
#2
#3
#^
#5
#6
#7
#8
#9
#10
#11
#12
#13
#&
#15
#16
#17
#18
#19
#20
Sample Description
Feed
Brewhouse D.W.S.
U Min. - 10 Min. Total
Recycle to Dryer
Dry Grain
Cone, to Recycle
Press 1
Press 2
Feed
Cone, to Recycle
Recycle to Dryer
Dry Grain
Press #1
Press #2
Recycle to Dryer
Press Grain
Dry Grain
Brewhouse D.W.S.#1
Brewhouse D.W.S. #2
Brewhouse D.W.S.
jo T.S
3-22
1.32
63. U
90.5
19.6
39.3
38.7
3.12
20.2
62.0
89-8
to.U
to.l
60.0
U2.7
91.5
2.01
1.7^
2.43
% S.E
1.50
.63
1.55
99
1.08
Ratio
S.S SS/IS
.875
915
.99
97
-------
Date
12/9
Time
3:UO PM
3:to PM
Sample
No.
#2
#3
Sample Description
Comp. #1 7-lU Min.
Brewhouse D.W.S.
Comp. #2 1^-15 Min.
S.S
.63
Ratio
SS/IS
1.05
-------
APPENDIX L- EVAPORATOR TESTS USING
INCONEL 601 DOWNCOMERS - SERIES 2
Temp.
HZ7 Out Gas Orifice Gas Burner Feed Ccr.c.
ra-e'' =1 Panel Fcx Drexel Gas Rec. Stack of .'.P ;*ess Air<".P Blower Tank Feed Tank Air Blcwer Tank
Tir.% --^2 LI LIC Brook Flow Temp. Moyno #1 #2 Psig #1 #2 tops Level Rate Level Temp. P/T Press
1C:TO A
10/U/72
5:CO P
.U
2.9
6:00 11
7:20
1/5/72
8:30 A
10:30
11:30
1:00 P
2:00
3:00
li;00
6:30
11
c *
₯
2.2
TB~
£i
£71
10.0
10.1
loT
10.0
£7I~
10.0
O~
10.0
16,000
6261)250 186
15,500
6322600 190
V A P . FULL 10:50 a . m
39 11.5 38
Ul 12.0 Ul
1*0 12.0 37
52 16.5 30
1*2 12.5 32
60 18.0 I*
61 18.0
61 18.0
60 18.5 100+
60 18.75 100+
READY FOR START UP
188 lllf 1.1 1.6 3.9 U.O 8.0
179 3.0 3.20 3.9 10-15 17
186 182 3.1 3.20 3.9 10-15 17
150 2.85 2.00 3.9 17-21 7.0
168 1.35 2.10 lt.0 8.0 8.0
192
lU.OOO
6335123 187 151 2.10 2.00 3-95 15.0 9.0
13,750
63UU952 187.5 156 2.50 2.00 3-95 15-20 9.0
188 l6lt 2.55 1.90 3.95 15-20 9.0
190 169 2.60 2.50 3.95 15-20 9-0
190 173 2.60 2.55 3-95 15-20 9.0
lU,500
60 18.5 100+ 6361075 190 166 2.55 2.50 3.95 15-20 9.0
68
99
99
86
66
90
88
87
87
88
86
39
7.1
39
7.1
39
32
7.60
30
7. 'to
"
7.25
W
7.
0
0
0
0
0
0
0
0
0
LI
-------
Sate/
1/5/,2
8Kx> P
1s':-'r.
9*5
11:00
11*5
H 1:15 P
O
O
3:30
1»*5
5:50
6*5
1/7/72
8*5
9*5
10*5
11*5
-l
10.0
ETF
10.0
L i
10.0
H T
c 5
tTo1
10.0
2.95
9.75
3.50
. 3
..
9.5
3.75
£75
Oo
10.00
U-25
10.15
"*-25
10.20
u-2°
OQ
^Ki5
Panel Fox
L: Lie
60
cO
62
62
62
62
59
61*
62
62
62
62
61
63
18.0
la
13.75
18.50
18.75
18.50
17.75
19.75
19.0
19.25
18.75
19.0
19.0
19.5
Drexel
Brock
100+
0
0
0
0
0
0
0
0
0
100+
100+
100+
100+
Gas Rec.
Flow
1U.500
61*15630
1U.500
6U2W36
1U.500
61*32116
lU.500
6l*l*7331»
lit, 500
61*51*1*1*0
lU,500
6506062
ll*,500
6513599
Stack
Temp.
190
189
189
190
190
190.5
189
190
190
190
189.5
189.5
190
190
Temp.
Out
of
Moyno
168
112
136
138
96
lUy
161
170
169
170
171
172
167
Gas Orifice
AP
#1 #2
2.55
2.60
2.6o
2.60
2.60
2.55
2.65
2.55
2.50
2.55
2.55
2.60
2.60
2.50
2.50
2.50
2.50
2.55
2.55
2.1»0
2.55
2.55
2.55
2.55
2.60
2.70
2.70
2.55
Gas
Press
PsiR
3.95
3.95
3.95
3-95
3.95
IK 00
U.oo
3.95
3.95
3.95
1*.00
i*.oo
IKOO
IKO
Burner
Air.'.P
#1 #2
17-21
17-22
17-22
18-23
l8-2lt
18-21*
18-21*
18-21*
18-21*
18-21*
20-27
20-25
20-26
20-26
9.0
9.0
10.0
9.0
9.0
7-10
8.0
8.5
8.0
8.0
10-11
9-10
9-10
8.0
Food
Blower Tank
Amps Level
87
89
89
88
87
85
88
87
86
88
91
90
90
87
100
100
100
100
100
100
91*
100
100
100
100
100+
100
Feed
Rate
28
25.5
255
2U.O
2U.O
28.0
26.5
25.0
25.0
28
28
28
28
Cone. j
Tank Air
Level Ter.t>.
100+
100
100
89
66 1*25
100 335
100
100 1*10
100
7U 375
71 375
70 385
72 3&0
Blcver
P/T
7.U
₯
j
W*
7.1*0
7. 3g
1*3
^
7.20
52^0
7.25
51.0
7.25
T^~
fe*
7.1*0
i7ft
7 *^0
1*6
7.20
50
7.20
5T"
Tank
Press
0
0
0
0
0
0
0
0
0
0
0
0
0
-------
Temp.
?:i: Out Gas Orifice G*s Burner Feed ~cnc.
late/ =1 Panel Fox Drexel Gas Rec. Stack of Ap Press AirAP Blower Tank Feed Tank Air Blower Tank
LI LIC Brock Flow Temp. Moyno #1 #2 Psig #1 #2 Amps Level Rate Level Temp. P/T Press
1/7/72
2:^5
3*5
U:U5
5:^5
6:U5
1/8/72
9:00 A
10:00
11:00
12:00 :;
1:00 P
2:00
3:00
-:00
10.0
10.25
rtr
10.20
10^25
HIT
10.25
L~20
10.25
E~20~
10.10
L>15
10.20
L.20
10.00
L.20
10.00
L-20
10.00
i-,20
10.15
UT20"
10.20
"*-20
fcB
62
62
62
62
63
63
63
63
63
63
63
63
6?
,,
19.0
19.0
19.0
19.25
19.0
19.0
19.25
19.0
19.25
19.00
19.25
19.25
19-25
19.25
1U.500
100+ 6521*605 190
100+ 190
100+ 190
15250-1U750
100+ 6535638 190
100+ 190
100+ 190
15500-13500
loo+ 6596U56 190
100+ 190.25
100+ 190.25
o 190.25
1U500-1UOOO
o 6611550 190.25
190
190
190
173
172
168
168
167
169
172
172
172
173
172
172
173
173
2.55
2.6o
2.60
2.55
2.6o
2.6o
2.55
2.55
2.55
2.55
2.55
2.60
2.55
2.55
2.55
2.55
2.60
2.60
2.60
2.65
.265
2.60
2.65
2.70
2.70
2.70
2.70
2.70
U.O
U.O
U.O
U.O
U.O
u.o
U.O
3.95
U.OO
U.OO
U.oo
U.oo
3.95
U.oo
19-25
20-25
19-25
19-25
19-26
19-27
19-2U
18-27
19-2U
18-25
18-2U
18-25
17-23
17-2U
8.5
8-9
8-10
8.5
8.5
8.5
9.0
7-10
8.5
8.5
7-9
8-10
7-9
8-9
87
87
87
88
88
88
88
86
85
85
85
86
85
85
96
as
68
86
90
92
9U
9U
93
86
7U
7U
6U
28
28
28
27*
27
27
27
27
27
27
27
27
27
72
72
71
66
60
66
6U
62
62
62
60
56
56
295
UDO
uoo
Uoo
395
390
U05
Uio
Uio
Uio
U15
UIO
UIO
UIO
7.10
56
7.10
57
7.10
56
7.15
56
7.20
52
7.20
50
7.10
IB"
7.00
52
6.05
6TT"
6.03
6T~
6.90
6T~
6.90
5T~
6 go
W~
w1
0
0
0
0
0
0
0
0
0
0
0
0
0
0
-------
Temp.
HI" Out Gas Orifice Gas Burner Fc-:d '"cnc.
Date/ =1 Panel Fox Drexel Gas Rec. Stack of AF Press AlrAP Blower Tank Feed Tank Air Blower Tank
Tir.e -2 LI LIC Brook Flew Temp. Moyno #1 #2 Psig #1 & Amps Level Rate Level Tecp. P/T Press
1/5/72
5:00 P
1/9/-2
9:00 A
10:00
11:00
12:00 ::
1:00 P
2:00
3:00
L:CO
5:00
1/10/72
5:20 A
$:00
10:00
11:00
Mf
10.10
-.20
10.10
10.10
^TIT
10.10
10.10
FTIT
10.10
10.10
1720"
trlf
10.15
U.26
cj[2
C.7Q
£715
10.00
It. 20
16.00
T720-
63
?3
63
63
63
63
63
63
«3
63
63
63
63
63
19.0
19.25
f9.0o
19.25
19.25
19.25
19.0
19-25
19.0
19-25
19.25
19.0
19.25
19.25
ll*000-l'*500
6627028 190
13250-15000
6692530 190.25
190.5
190.5
190.5
190.5
13750-lUsoo
6717196 190.5
190.5
190.5
190.5
1U750-13000
6797715 190.5
190.5
190.5
190.5
172
173
176
177
177
176
177
177
177
175
175
17U
173
2.55
2.55
2.55
2.60
2.55
2.60
2.60
2.55
2.60
2.55
2.55
2.50
2.55
2.60
2.70
2.70
2.65
2.70
2.65
2.65
2.65
2.65
2.65
2.65
2.65
2.65
2.65
2.65
u.o
u.o
3.95
U.oo
U.OO
U.oo
U.OO
3.95
U.OO
U.OO
U.OO
U.OO
U.OO
17-2U
lU-21
15-22
lU-22
15-21
lU-21
lU-21
lU-21
lU-21
lU-21
lU-21
lU-22
lU-22
lU-20
7.5-9
7-9
7-10
7-8
6.5-7.5
6-9
6-9
6-9
6-9
7-8
7-9
6-9
7-10
7-9
8U
85
8U
8U
8U
8U
83
8U
82
82
8U
8U
85
85
68
B3
90
87
90
68
89
88
88
83
88
88
90
27
26
26
25
25
25
26
26
26
26
27
27
26.5
62
69
60
52
U2
32
30
26
2U
22
66
66
f-8
U25
U38
1*30
U30
U35
U35
U35
U35
U35
U30
U37
U35
U32
lij*
6.80
70
6.80
71
6.75
7U
6.75
7o^
6.75
77
6.70
76~
6.70
6.70
7T-
fr2
6.80
70
6.80
70
6.80
72
6.50
72~
0
0
0
0
0
0
0
0
0
0
0
0
0
0
-------
ETC
gl Panel Fox Drexel Gas Rec.
Ti-.s "2 LI LIC Brook Flow
Temp.
Out Gas Orifice Gas ' Burner Feed Tcr.o.
Stack of dp Press AirAP Blower Tank Feed Tank Air Blcver Tank
Temp. Moyno #1 #2 Psig #1 fe Amps Lave-1 Rate Level TCT.P. P/T Press
1/10/72 10.0
12:00 !1 L7T5 63 19-25
10.00
1:00 f L.15 £3 19.25
10.00
2:00 L.15 63 19.00
10. CO
3:00 L.15 63 19.00
10.00
U:00 L.15 63 19.00
fe
190.5 2.60 2.65 4.00 14-20 6-8 84 1»30
190 17l* 2.60 2.65 4.00 lU-20 7-9 84 S8 27 76 429
190 175 2.60 2.65 4.00 13-18 6-8 84 90 27 64 1*25
190 175 2.60 2.65 4.00 13-20 6-8 85 88 27 64 420
190 173 2.60 2.65 4.00 14-18 7-8 85 90 27 72 420
6.80
73 0
^
7^
6^75
72
6.80
70
-------
APPENDIX M - INCONEL 601 DOWNCOMER TESTS
SERIES 2
FEED AND PRODUCT SAMPLES
Date
[1972 )
lA
lA
lA
1/5
1/5
1/5
1/6
1/6
1/6
1/7
Sample
Time No .
10:10 AM 1
2
10:50 AM 3
k
7:30 PM 5
6
9:00 AM 7
8
1:00 PM 9
10
6:30 PM 11
12
9:00 AM 13
Ik
11:30 PM 15
16
5:00 PM 17
18
9:00 AM 19
20
Sample Description
Feed
Feed
Feed
Feed
Feed
Feed
Feed
Feed
Feed
Feed
Feed
Feed
Feed
Feed
Feed
Feed
Feed
Feed
Feed
Feed
Ratio
io T.S. i S.S. SS/IS
3.87
1.85 .905
3.83
.1.99 1.07
k.15
1.85 .805
3-89
1.90 .95
^.00
2.13 1.15
3.75
2.01 1.16
3.1*6
1.72 .99
3.36
i
1.8k l.Ui
3.25
1.50 .85
3.38
1.7k 1.13
-------
Date
1/7
1/7
1/7
1/7
1/7
1/8
Sample
Time No .
11:25 AM
11:25 AM
11:25 AM
11:25 AM
11:25 AM
11:25 AM
1:1*0 PM 28
29
3:00 PM 32
31
30
33
3^
35
5:30 PM 36
37
7:00 PM 3
2
*
1
5
6
9:00 AM 7
Sample Description
Press #1
Press $2
Recycle
Dry Grain
Cone.
Yeast
Feed
Feed
Press #1
Press #2
Recycle
Dry Grain
Cone.
Yeast
Feed
Feed
Press #1
Press #2
Recycle
Dry Grain
Cone.
Yeast
Yeast
105
% .S °lo S.£
1*0.3
in A
66.0
90.0
23.1
15.6
2.32
2.79
1.1*2
1*1.1*
1*1.1
68.5
88.0
21.6
15.1
2.91
1.29
1*2.9
1*3.1
67.25
88.0
19.95
15.10
3.56
Ratio
S.S SS/IS
1.037
.797
-------
Date
1/8
1/8
1/8
1/8
Sample
Time No .
9:00 AM 8
9
9:30 AM 111-
11
10
12
13
14
1:00 PM 16
17
1:30 PM 23
20
22
21
19
18
5:00 PM 30
5:00 PM 31
5:00 PM 26
28
29
27
25
Sample Description
Feed
Feed
Press #1
Press #2
Recycle
Dry Grain
Cone.
Yeast
Feed
Press #1
Press #2.
Recycle
Dry Grain
Cone.
Yeast
Feed
Feed
Press #1
Press #2.
Recycle
Dry Grain
Cone.
Yeast
_106
% T.S. % S.S.
3-32
1.68
34.5
to. 7
61.8
90.0
22.3
3-73
2.54
1.28
38.1
39-8
69.0
91.5
22.5
2.91
" 2.1*3
1.14
to. 8
38.3
74.25
92.3
19.95
Ratio
1.02
1.015
.885
-------
Date
1/9
1/9
1/9
1/9
1/10
Sample
Time No .
9:00 AM 3k
33
35
32
9:00 AM 36
37
1:00 PM k2
k3
39
38
to
in
5:00 PM 5
6
2
3
1
k
9:00 AM 13
lU
7
8
10
11
Sample Description
Press //I
Recycle
Dry Grain
Cone.
Feed
Feed
Press #1
Re cycle
Dry Grain
Cone.
Feed
Press #1
Re cycle
Dry Grain
Cone.
Feed
Feed
Press #1
Press #2.
Recycle
Cone.
107
% T.S.
in.8
75.0
91.25
19.6
2.83
2.1*6
Uo.3
75.5
89.2
19.05
2.75
Uo.3
73.75
90-5
19.50
3.37
36.1
35.75
68.^
21.2
Ratio
i s.s. ss/is
1.29 .837
1.11 .82
1.25 .83
1.72 1.0^
-------
Date
1/10
1/10
Sample
Time No .
9:00 AM 12
1:00 PM 21
22
16
18
15
17
20
19
Sample Description
Yeast
Feed
Press #1
Press $2
Recycle
Dry Grain
Cone.
Yeast
i T.S. i s.s.
12.5
2.76
1.51
U3.0
33.6
67.2
90.5
17.25
Eatio
1.20
108
-------
APPENDIX N - EVAPORATOR TESTS
USING JACKETED DOWNCOMER COOLED
WITH DILUTION AIR
Flow Rates
Evap . Cone .
Time & Feed Pump
Date (GPM) (Set)
10/19/72
12:00 M
1:00 AM
2:00 AM
3:00 AM
1^:00 AM
5:00 AM
6:00 AM
7:00 AM
8:00 AM
9:00 AM
10:00 AM
11:00 AM
12:00 N
1:00 PM
2:00 PM
3:00 PM
N.
k:00 PM 16
5:00 PM 0
6:00 PM 0
Stack
Firing Rate Temp. Concentrate
(Million BTU/Hr.) °F (% T.S.)
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
i
12.3
12.3
12.3
12.3
12.3
12.3 9-0
12.3 10.0
12.3
109
-------
Time &
Date
10/19/72
7:00 PM
8:00 EM
9:00 PM
10:00 PM
11:00 PM
10/20/72
12:00 M
1:00 AM
2:00 AM
3:00 AM
k:00 AM
5:00 AM
6:00 AM
7:00 AM
8:00 AM
9:00 AM
10:00 AM
11:00 AM
12:00 N
1:00 PM
2:00 PM
3:00 PM
1+:00 PM
Flow Rates
Evap . Cone .
Feed Pump
(GPM) (Set)
50
0
0
0
26
26
26
27
27
27
27
27
27
26
26 k.O
Firing Rate
(Million BTU/Hr.)
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
110
Stack
Temp . Con c entrat e
°F d T.S.)
11. i*
1^
16. k
16.8
17.6
18. U
20.0
20.0
21 A
21.2
20.2
19 :k
20.0
20.k
19. h
17.0
17.0
17.0
-------
Flow Rates
Time &
Date
10/20/72
5:00 PM
6:00 PM
7:00 PM
8:00 PM
9:00 PM
10:00 PM
11:00 PM
10/21/72
12:00 M
1:00 AM
2:00 AM
3:00 AM
k:00 AM
5:00 AM
6:00 AM
7:00 AM *
8:00 AM
9:00 AM
10:00 AM
11:00 AM
12:00 N
1:00 PM
2:00 PM
Evap.
Feed
(GPM)
25
2k
23
2k
2k
2k
2k
2k
2k
2k
2k
2k
2k
2k
2k
2k
2k
2k
2k
2k
2k
2k
Cone . Stack
Pump, Firing Rate Temp. Concentrate
(Set) (Million BTU/Hr.) °F d T.S.)
k.5
k.5
k.5
U.5
k.5
^.5
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
k.O
3.0
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
12.3
111
17. k
17.0
17.0
18.0
--
17.9
18.2
18.6
18.U
18.6
18.6
18.2
18. If-
19.0
19.2
19.0
20.
20.0
20 .k
19.8
18.0
-------
Flow Rates
Evap. Cone. Stack
Time & Feed Pump Firing Rate Temp. Concentrate
Date (GPM) (Set) (Million BTU/Hr. ) °F (
-------
APPENDIX 0
EFFLUENT SAMPLING WITH EVAPORATOR
OPERATING
12/8/71 12/9/71, 12/13/71* 12/1V71*
NA
6,120
835
800
3,268
NA
NA
NA
NA
860
3,100
800
7^0
1,89^
63.0
0.01
OA3
0.16
876
1,950
852
708
2,560
12.1
0.08
0.20
0.00
NA
2,320
676
600
1,800
NA
NA
NA
NA
NA = No Analysis
* One burner in service
113
-------
APPENDIX P
EFFLUENT SAMPLING WITH EVAPORATOR NOT OPERATING
Date of
Sample
10/11/71
10/13/71
10/19/71
10/20/71
10/25/71
H 10/26/71
11/9/71
11/10/71
11/17/71
11/18/71
11/19/71
11/20/71
11/21/71
BODc,
IDE/l
1,53**
1,566
1,870
NA
1,590
NA
1,580
NA
NA
2,1^0
1.060
NA
1,270
COD,
mK/1
NA
NA
1,750
c,910
2,160
1,920
2,160
2,070
2,570
2,720
3.7^0
1*,580
3,510
Total
Suspended
Solids
ms/1
716
808
1,300
9^0
860
1,160
9^0
980
860
810
1,3^
1,960
1,160
Volatile
Suspended
Solids
mK/1
NA
NA
1,2^0
912
81+0
1,120
932
928
8Mt
790
1,280
l',890
1,010
Total
Solids
niE/1
1,660
1,990
1,660
1,850
1,820
1,620
910
1,770
2,010
1,870
2,300
3,160
2,850
Total
Kjeldahl
Nitrogen,
mK/1
NA
NA
97.3
NA
88.0
NA
1^ .
NA
NA
1*K
16.
NA
18.
Nitrite
ffiR/l
NA
NA
LT 0101
NA
LT 0.01
NA
LT 0.01
NA
NA
LT OiOl
LT 0.01
NA
0.33
Nitrate,
mK/1
NA
NA
o.Uo.
NA
0.62
NA
0.10
NA
NA
0.08
0.10
NA
0.06
Total
Phosphorus ,
mK/1
NA
NA
5.2
NA
5-2
NA
0.05
NA
NA
3-5
0.92
NA
6.0
-------
Total Volatile Total
Suspended Suspended Total Kjeldahl Total
Date of
Sample
11/22/71
11/30/71
12/1/71
12/18/71
12/19/71
12/20/71
12/21/71
J.2/29/71
12/30/71
BODc,
raff/1
NA
NA
UlO
1,2ft
NA
1,992
NA
NA
1,752
COD,
mff/1
,28Uo
2,600
2,110
1,173
1,1*0
2,860
3,169
1,5^3
1,6U6
Solids
mg/1
900
535
560
612
1^36
1,160
1,012
680
7»*
Solids
mK/1
836
505
510
536
208
1,120
932
582
70^
Solids
mg/1
2,000
1,66U
1,876
1,266
1,^96
2,l8o
2,320
1,350
1,^
Nitrogen,
mff/1
NA
NA
13-3
3-9
NA
5-9
NA
NA
5.1
Nitrite
NA
NA
0.01
LT .1
NA
LT .1
NA
NA
ND
Nitrate,
mg/1
NA
NA
0.32
0.18
NA
0.18
NA
NA
ND
Phosphorus ,
mg/1
NA
NA
0.20
3-8
NA
2.0
NA
NA
0.5
NA = No Analysis
ND = Not Detectable
LT = Less Than
-------
SELECTED WATER
RESOURCES ABSTRACTS
INPUT TRANSACTION FORM
w
4. Title
SUBMERGED COMBUSTION EVAPORATOR FOR CONCENTRATION
OF BREWERY SPENT GRAIN LIQUOR
7. Auihor(s)
Stein, J. L.
9.
Anheuser-Busch, Inc., St. Louis, Missouri,
Engineering Department
5, R
6.
j. 8. Per fotrain 7 Organization
Report No.
10. Project No.
12060 HCW
U. Ceztrsci/Grant ?,'o.
13. Type c: Repor and
Period Covered
?_12. :' Sponsoring Organization
^^.jwiS-jfi^', ' - ' _
!r-. Supplementary No:.*:;
Environmental Protection Agency report number, EPA-660/2-7^-059, June
In. Abstract
A major waste stream in many breweries is the liquor resulting from spent grains de-
watering prior to drying. This liquor may account for a third or more of the B.O.D.c
and suspended solids generated "by a typical brewery.
Initial studies of the spent grain liquor problem indicated that recovery rather than
treatment was the best approach. A number of evaporators were evaluated to determine
which design was most satisfactory for concentrating the liquor. A submerged combus-
tion evaporator was selected on the basis of engineering analyses and pilot scale tests
A full scale unit was installed at the Houston Brewery of Anheuser-Busch, Inc., in
1970. This evaporator was modified several times to overcome failures of the burner
downcomers brought about by high temperatures. Before a final solution to these
problems could be demonstrated, the project was terminated. Fuel costs above $1.60 per
million kg-cal (U00 per million BTU) coupled with thermal efficiencies approximately
3.5 times better for conventional four-effect evaporators indicated that a conventional
evaporator would be more economical at these fuel price levels.
17a. Descriptors
*Evaporators, -^Industrial Wastes, Water Pollution Control, Water Pollution Sources,
Waste Disposal, Wastes
17b. Identifiers
^Submerged Combustion Evaporators, *Spent Grain, ^Brewing Wastes, Beer, Food
Processing, Multiple-Effect Evaporators, Resource Recovery
17c. COWRR Field £ Group
05E, 05D
18. A'-ailabiliry
19s Security Class:
(Report)
20. Security Class.
tl. fla.of
Pages
22. Pfice
Send To:
WATER RESOURCES SCIENTIFIC INFORMATION CENTER
U.S. DEPARTMENT OF THE INTERIOR
WASHINGTON. D. C. 2O24O
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