October 1976
DEVELOPMENT OF A PROTOTYPE SYSTEM FOR PYROLYSIS
OF AGRICULTURAL WASTES INTO FUELS
AND OTHER PRODUCTS
by
J. W. Tatom and A. R. Colcord
Engineering Experiment Station
Georgia Institute of Technology
Atlanta, Georgia 30332
Grant No. R 803430-01-0
Program Element No. EHE-624
EPA.Project Officer: W. W. Liberick, Jr.
Industrial Environmental Research Laboratory
Office of Energy, Minerals and Industry
Cincinnati, Ohio 45268
Prepared for
U. S. ENVIRONMENTAL PROTECTION AGENCY
Office of Research and Development
Washington, D.C. 20460

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ABSTRACT
An experimental study of the performance of the one tonne/hr pyrolytic
convertor located at the Georgia Tech Engineering Experiment Station
has been conducted. Peanut hulls were used as the feed in a series
of thirteen tests. In addition, two tests were conducted using saw-
dust. The objects of the test program were to determine the effects
of scale, feed material, mechanical agitation, air/feed and bed
depth on the product yields of the EES pyrolytic convertor. Also
investigated was the performance of an integrated mechanical agita-
tion-air supply system (AIRGITATOR) designed to improve the through-
put of the unit.
From the tests, and after comparison with earlier smaller scale
work with sawdust, it appears that changing feed and scale, and
the use of mechanical agitation have little influence on the product
yields. Bed depth, while not affecting the total potentially
available energy in the char and oil, substantially influences
relative amounts of these products. The air/feed ratio again
appears to be the dominant influencing variable and data from the
present study and earlier work are shown to correlate to a single
curve.
The influence on system performance of the integrated mechanical
agitation-air supply system, while not investigated comprehensively,
appears to be very favorable. Using this system, off-gas temper-
atures were raised, while stable operation was maintained at very
low values of air/feed.
This report is submitted in fulfillment of EES Project Number B-446
in an initial, .reporting period. The work was supported under Grant
NumbSt *R''8O34'30'-O1-O of the Environmental Protection Agency. Work
was completed in December 1975.
feUV- .Tr-V* -
ii

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CONTENTS
Page
Abstract	ii
List of Figures	iv
List of Tables	v
Nomenclature	vi
Acknowledgments	vii
Sections
I	Conclusions	1
II	Recommendations	2
III	Introduction	3
IV	Testing	8
V	Integrated Mechanical Agitation-
Air Supply System	^
VI	References	50
VII	Appendices	51
iii

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FIGURES
No.	Title	Page
\
1	EES Pyrolytic Unit Process Flow Diagram	9
2	Overall View of Advanced EES Pyrolytic	10
Converter System
3	Close-Up View of EES Pyrolytic Convertor	11
4	Close-Up View of Conveyor and Input System-	12
EES Pyrolytic Convertor
5	Close-Up View of Cyclone and Condenser Systems-	12
EES Pyrolytic Convertor
6	Close-Up View of Off-Gas Burner-EES Pyrolytic	12
Convertor
7	Schematic of EES Convertor with Rotating	16
•Agitator
8	Schematic of EES Convertor with Integrated	17
Mechanical Agitation-Air Supply System
9	Percent Available Energy in Char-Oil Mixture	34
10	Percent Available Energy in Char-Oil Mixture-	35
Composite of All Data
11	Energy Breakdown of Pyrolysis Products	37
12	Oil Yield Variation with Increasing Bed Depth	39
13	Effects of Feed Moisture on Available Energy	42
From Char-Oil Mixture
14	Heating Value of Non-Condensible Gas	43
15	Design for AIRGITAIOR	46
16	Overall View of AIRGITAIOR	47
17	AIRGITAIOR Installed on Pyrolytic Convertor	^
iv

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TABLES
No.
Title

Page
1
Test Summary

27
2
Transformed- Data

30
B-l
Laboratory Analysis, Test
1
57
B-1
Laboratory Analysis, Test
2
58
B-3
Laboratory Analysis, Test
3
59
B-4
Laboratory Analysis, Test
6
60
B-5
Laboratory Analysis, Test
7
61
B—6
Laboratory Analysis, Test
9
62
B-7
Laboratory Analysis, Test
10
63
B-8
Laboratory Analysis, Test
11
64
B-9
Laboratory Analysis, Test
12
65
B-10
Laboratory Analysis, Test
14
66
B—11
Laboratory Analysis, Test
15
67
v

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NOMENCLATURE
Symbols
h
HV
L
M
w
Subscripts
a
c
ch
f
g
h
o
n
wl
wo
xch
xf
Definition	Units
Enthalpy	kcal/gm
Heating Value	kcal/gm
Losses (see equation 2)	kcal
Mass gm
Weight Fraction	gm/gm
Air
Carbon
Char
Feed
Off-Gas
Hydrogen
Oil and Oxygen
Nitrogen
Water in Feed
Water in Off-Gas
Ash in Char
Ash in Feed
vi

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ACKNOWLEDGEMENTS
This effort was supported by the Industrial Environmental Research
I
Laboratory of the Environmental Protection Agency under Grant
R 803430-01-0. We wish to express our appreciation to Mr. Donald
A. Oberacker of MERL for his many contributions and suggestions.
And a note of thanks is offered to Ms. Beth Lanier for her
invaluable assistance in the preparation of this document.
vii

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SECTION I
CONCLUSIONS
From the results of this work the following conclusions can be
drawn:
The effects of the air/feed ratio on product energy yields
appears to be dominant; changing scale and feed material,
and the effects of mechanical agitation are of minor
importance compared with air/feed.
The available energy in the char-oil mixture appears from
the results of this and earlier work to be a single function
of air/feed; all the data correlated to a common curve.
While the total energy in the char-oil mixture is a function
only of air/feed, the relative amounts of char and oil can
be changed significantly by varying the bed depth.
The processing of peanut hulls through the convertor
presents no problems either with or without the use of
mechanical agitation.
The integrated mechanical' agitation-air supply system or
"AIR6ITAT0R", which was tested successfully, appears to
offer many advantages in increased through-put, operating
stability and off-gas temperature at very low values of
air/feed. The ability of this system to allow continuous
variation in the bed depth provides an additional, signif-
icant and attractive feature.
The overall mass, energy, and chemical balances appear to
be satisfactory; thus giving confidence to the results of
the testing.
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SECTION II
RECOMMENDATIONS
The results of the study further reinforce the attractiveness of
the mobile pyrolytic convertor concept by providing additional
operating data and basic understanding of the physical processes
at work. However, while the design, fabrication and test of the
complete mobile system can be initiated in the very near future,
several technical studies should be made before this final phase
begins. These include:
(1)	an investigation of the operating and ignition characteristics
and derating required of a modified gasoline engine operating
on the low heating value gas.
(2)	a study of the burning characteristics of the char-oil mixture
in various combinations with coal and petroleum oil.
(3)	further development and test of the integrated mechanical
• •
agitation-air supply system (AIRGITATOR) evaluated in the
current work.
When these studies have been completed, successfully, the design^^
fabrication and test of the full-scale mobile pgrol^sis^^convert^er	'
itself should be initiated. Upon successful operation of this
component the complete mobile system should be designed and con-
structed.
2

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SECTION III
INTRODUCTION
GENERAL
This report describes an experimental program designed to improve the
technology required for the development of a mobile pyrolysis system
for conversion of agricultural and forestry wastes at the site of their
production into a clean and easily transportable fuel. The program
Involves a series of tests using peanut hulls, primarily, as the feed
in the one tonne/hr Georgia Tech Engineering Experiment Station (EES)
pyrolytic convertor pilot plant and is a follow-on study to earlier
work (1,2,3,4) using wood waste as the feed material in a smaller,
227 kg/hr (500 lb/hr) EES pilot plant.
RATIONALE FOR MOBILE PYROLYSIS CONCEPT
Agricultural wastes, while representing a huge potential source of
« •
energy for the U. S., have certain'adverse characteristics which have
limited their use as fuels in the past and which must be dealt with in
any successful energy conversion system. These characteristics include
the facts that:
*	Agricultural waste (organic matter) is typically quite wet,
containing 30 to 70 percent water and therefore relatively
low in heating value per pound.
*	Since these materials would be scattered all over the country-
side, the transportation costs per kcal to large thermal
conversion plants would be very high.
*	Because of the water content of these raw materials, the use
of existing thermal conversion equipment is doubtful, at
least at its rated capacity. Most likely new or modified
facilities would be required. (The overall steam side ef-
ficiency of boilers utilizing wet organic fuels such as
bagasse and bark, is typically 60 to 65 percent. Thus there
is a serious conversion penalty using these as-received, wet
materials.)
3

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*	The particulate emissions from boilers operating on raw
organic fuels would likely require the installation of
expensive flue gas clean-up equipment.
¦ Agricultural wastes with a few exceptions are produced
seasonally, not continuously. Thus a steady supply of fuel
from these wastes is not available and also it is imprac-
tical to tie-up capital equipment that'cannot be used year
round.
*	Associated with the construction of a waste conversion
facility dependent upon an adjacent, fixed supply of wastes
over a long time period are contractual problems between
the producer of the wastes and the waste utilizer. While
initially the waste producer may be spending two to five
dollars per tonne of raw wastes for disposal, he may hesi-
tate or refuse in a long term contract to give away, or
perhaps pay a disposal charge for his wastes. And clearly,
once a facility for waste utilization has been constructed,
the waste producer, upon termination of the original
contract, has the waste utilizer in an uncomfortable economic
position.
One solution to these problems is to utilize a mobile pyrolysis system
that could be transported to the site of the waste production and there
convert the wastes into a char, an oil and a low quality gas. The gas
could be used to dry the wet feed and to operate the associated
equipment and the oil and char could be sold as fuels. The weight
reduction and the associated transportation costs thereby affected
would be very substantial. A further benefit to be derived is that
since the system is portable it would provide greater leverage for
the waste utilizer in contract negotiations with the waste producer,
since the unit could always be moved to a new.location. The porta-
bility feature would also guarantee greater equipment utilization
and through proper scheduling between seasonal agricultural wastes
and continuously available forestry wastes could provide an almost
constant supply of fuel. Finally, since the portable system could be
4

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assembled in factories, using mass production techniques it would likely
be less expensive than a comparable fixed installation.
The Engineering Experiment Station (EES) at Georgia Tech over the last
eight years has developed a simple, steady-flow, low temperature,
partial oxidation pyrolysis system which is completely self-sustaining.
In the EES design the pyrolysis occurs in a vertical porous bed.
This unit requires no special front end system, has very few moving
parts, and depends upon a relatively small blower to provide the air
supply necessary to maintain the partial oxidization of the feed.
Typically a tonne of as-received wastes would be converted, using the EES
process, to about 225 kg (495 pounds) of a powered char-oil fuel,
similar to coal, with a heating value of 6.00 to 9.00 kcal/gm
(11,000-13,000 Btu/lb.) Thus, depending upon the feed moisture
content, the energy available for use at the central thermal conversion
plant could be 75 to 80 percent of that theoretically available from
the original dry wastie; and, using a boiler conversion efficiency of
80 to 85 percent, the overalltsteam-side*efficiency of the process
could be 65 to 70 percent. Hence the percent of useable energy could
be as large and perhaps larger than that available with direct
burning but with avoidance or significant reduction of the problems
of:
•	Transporting the wastes.
•	Modification or construction of new facilities compatible
with fuels derived from organic wastes.
•	Emissions resulting from unburned fuel particles.
The powdered char-oil fuel could be burned in either suspension fired
or in stoker fired boilers with essentially no modification. It could
be blended with cheaper high sulfur coal to produce an additional
economic advantage.
Two additional elements, which make the concept even more attractive,
have recently come to light, i.e.
5

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(1)	The application of the mobile pyrolysis concept to large
barges* moving on the thousands of miles of inland and inter-
coastal waterways appears to have great promise. This would
not only permit an increase in the scale of the mobile system
but would also allow its application to the municipal waste of
smaller communities which presently cannot individually justify
or afford a large, economical waste conversion system, but
which in groups could successfully operate such a system.
(2)	The char-oil fuel produced by the mobile pyrolysis system was
considered primarily in (1) as a coal substitute which could
be used in existing suspension or stoker fired systems. It
appears now from work with coal-oil slurries at Combustion
Engineering (6) General Motors (7) and at the ERDA, Pittsburgh
Labs (8) that combinations of petroleum oil and the char-oil
mix in energy release ratios of up to 50 percent may be
practical in existing oil-fired boilers with minimum or no
modification. The low sulfur content and relatively low ash
content of the char-oil mixture make it highly desirable as a
fuel-oil extender and presently no technical obstacles pre-
venting its use are anticipated. Because so many existing
boilers are oil fired, this development may represent an
important step away from reliance on oil as a boiler fuel.
These two considerations should have relatively little influence on
the planned development program for the portable system, but
strengthen significantly the justification for the portable concept
with production of the char-oil fuel.
OBJECTIVES
The investigation, which was primarily experimental, had several
objectives, i.e.
* The barge concept was developed by Mr. Kevin Everett of the
Florida Resource Recovery Council and is described in an un-
published paper (5).
6

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To determine the effects of scale on pyrolytic convertor
performance.
To determine the effects of changing feed material on
pyrolytic convertor performance.
To determine the effects of mechanical agitation on
pyrolytic convertor performance.
To determine the performance of an integrated mechanical
agitation-process air supply system.
To determine the influence of air/feed and bed depth on
product yields.
In the following sections a description o£ the study is presented.
7

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SECTION IV
TESTING
GENERAL
The experimental program was conducted in the new, one tonne/hr EES
pilot plant. Peanut hulls were used as the feed material in a series
of 13 tests and sawdust was used in 2 tests, for a total of 15 tests
in the complete study. All told, approximately 45.5 metric tons
(50 tons) of hulls were used in the program. The tests involved in-
vestigation of the influences of scale, feed, air/feed, mechanical
agitation and bed depth on product yields. In addition, the per-
formance of an integrated mechanical agitation-process air system on
product yields and process rates was studied. This section presents
a description of the test facilities, the calibration and test pro-
cedure, the laboratory procedure, the data reduction methodology and
the results of the test program.
FACILITIES
A process flow diagram of the EES pilot plant is shown in Figure 1.
Photographs of this unit showing views of the separate components
involved are presented in Figures 2 through 6.
The system operates in the following manner, the peanut hulls, (dried
at the sheller), are collected, weighed and then stored in drums.
During a test the drums are emptied into a receiving bin which
supplies a conveyor to the pyrolysis unit with input feed. The.
pyrolysis unit is 5.5 meters (18 feet) tall and is 1.8 meters (6 feet)
on each side. The inside of the unit is cylindrical, with a diameter
of 1.2 meters (4 feet) and a depth of 2.4 meters (8 feet). The feed
enters the convertor through a gate valve at the top and passes down
through the vertical bed. Process air tubes are located in the lower
portion of the bed. These water cooled tubes supply enough air to
oxidize the feed in their immediate proximity and thereby produce
3

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Totalizing
Flow Meter
EES Pyrolytlc Unit Process Flow Diagram
Figure 1

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Figure 2
Fourth EES Pyrolytic Pilot Plant.
10

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Figure 3
Close-Up View of EES Pyrolytic Converter
Figure 4
Close-Up View of Conveyer and Input System - EES Pyrolytic
Converter
11

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Figure 5	Figure 6
Close-Up view of Cyclone dnd	Close-Up View of Off-Gas Burner-
Condenser System - EES Pyrolytic	EES Pyrolytic Converter
Converter
.	-J
^|f -r'S^ri
12

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sufficient heat for pyrolysis of the remaining feed material. The
char at the bottom of the bed passes through a mechanical output
system and into a screw conveyor that transports it into receiving
drums.
The gases produced during decomposition of the feed pass upward through
the downward moving feed and leave the unit near its top. The gases
then pass through a cyclone where particulates are removed and then
to an air cooled condenser which operates at a temperature above the
dew point of the mixture. The condenser removes the higher boiling
point oils which are collected and weighed. The remainder of the un-
condensed oils, the water vapor, some condensed oil droplets and the
non-condensible gases pass through the draft fan and into the burner
which incinerates the mixture. The amount of gas production is
controlled by the bed temperature which in turn is controlled by the
air/feed ratio.
The instrumentation used in the study includes:
1)	An in situ calibrated orifice to measure process air flow rate.
2)	Scales used to weigh the dry input feed, the char and the oil
yields.
3)	A water meter to measure total cooling water flow.
4)	Dial thermometers to measure inlet and exit cooling water
temperatures.
5)	Various thermocouples to measure the pyrolysis gas temperatures
at several points in the system, internal bed temperature,
external surface temperatures, and the burner temperature.
6)	A multiple channel recorder to provide continuous read-out of
the various thermocouples.
7)	A gas sampling system for laboratory analysis of the off-gas
composition.
The system operates at a few centimeters of water below ambient; thus
any leaks present generally result in the introduction of air into
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the System. However, within the cavity between the sliding plates
of the gate valve, the displacement of the pyrolysis gas by the
input feed does result in some lost gas when the gate valve operates.
As the process rate of the unit increases, the gas production increases
and the pressure tends to rise. To control the pressure, the draft
fan speed can be varied within certain limits. The unit has pressure
relief doors which operate at about 25 centimeters (10 inches) of water.
These doors provide a safe means of relieving overpressure for any
system malfunction.
The process rate of the system is governed by the setting of the
output feed mechanism. A level indicator senses the need for addi-
tional feed and activates the gate valve and conveyor system to
provide the necessary input. Thus the gate valve cycles only upon
demand, not continuously; hence the gases lost through this valve do
not represent a significant energy loss or pollution problem.
The condenser is of a relatively simple design having a series of
air cooled vertical tubes through which the hot pyrolysis gases pass.
The condenser temperature is governed by a thermostatically operated
fan which controls the cooling air flow. .In all but the last tests
the condenser was operated at about 93°C (200°F), however, to deter-
mine the influence of condenser temperature an oil yields, the
condenser temperature was dropped to 77-82°C (170-180°F) in the last
test. It has been observed that oil droplets are frequently carried in
suspension through the off-gas system, past the draft fan and into
burner. This results in some loss of oil; however, analytical
techniques are used to correct for this loss.
In many of the tests, a simple.rotating mechanical agitation system
was utilized to enhance the flow of material through the waste
convertor and to prevent the formation of bridges or arches which
can obstruct the downward moving feed. A schematic view of the
14

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agitator used in these tests is-shown in Figure 7. The system was
operated by a high torque gear drive system. The maximum
rotation speed of the agitator was about one RPM.
In the latter phase of the testing, an integrated mechanical
agitation-process air system (AIRGITATOR) was also tested. A
schematic view of this system is shown in Figure 8. The system is
driven by the same gear drive as the simpler agitator and is described
in more detail in Section V.
It might be noted that the off-gas flow rate was not measured
directly during the tests because of the presence of droplets of
oil and moisture in the stream which make conventional instrumentation
techniques impractical. Instead, analytical techniques involving
nitrogen, carbon, hydrogen and oxygen balances were used to compute
the flows of the various constituents which make up the off-gas
stream.
CALIBRATION AND TEST PROCEDURE
Prior to the testing many elements of the system instrumentation
were carefully calibrated. The accuracy of some components such
as the thermocouples, however, was not checked since the required
precision did not demand temperature measurements of greater
accuracy than the nominal values of the manufactured wire. Also
the accuracy of the cooling water meter was taken at face value
from the name-plate data. However, careful attention was given to
calibrating the process air orifice against a laminar flow element.
This ASME sharp-edged orifice was calibrated in situ to insure
accuracy. Tares were individually determined for all the drums in
which the dried feed was stored. The procedure during the tests
was relatively straightforward: the unit, loaded with feed or
char the previous day, was heated-up by use of an electrical
resistance heating element. When the temperature was sufficiently
15

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Noncondensible
Gases
Feed
Process Air
/\ A, /\ Ak
v V V V Vi
Char
Figure 7
Schematic of EES Convertor with Rotating Agitator
16

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Air
Noncondensible
Gases
Feed
Process Air
(Start-up Only)
Char
Figure 8
Schematic of EES Convertor with Integrated
Mechanical Agitation - Air Supply System
17

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elevated the process air was introduced slowly and the element
removed. Once it was apparent that the system was operating in a
self-sustaining mode, the output system was activated and slowly
brought-up to the operating capacity chosen for the test. Likewise,
the process air feed rate was adjusted to correspond to the desired
ratio of air-to-feed for the test. The system was then allowed to
come to a steady-state condition, which required a nominal four
hours. Constant checks and adjustments were'made during this period
to insure that the actual operating conditions were those desired;
however, it was found that the ability to establish a given feed
process rate and given air-to-feed ratio was limited to a tolerance
of plus or minus about 10 percent.
Upon initiation of the test run, continuous records of time, feed
.input, char output, oil output, orifice manometer readings, and the
various temperatures were made. In addition a continuous sample of
the pyrolysis off-gasses was taken. Every effort was made to insure
that the unit remained in a steady-state operating mode by continuous
surveillance and adjustment of the various instruments measuring
and controlling the inputs of the system. "Grab samples" of the
feed from each drum were taken throughout the run. At its comple-
tion all of the char and oil produced were collected and represent-
ative samples of each obtained. The char sample was obtained by
use of a grain sampler. The oil was collected in a large drum,
mixed throughly and a sample of about one-half liter (one pint)
taken. All of the feed grab samples were mixed and cut using a
rifle splitter to obtain a composite sample of about one kilogram.
18

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LABORATORY TESTING
The laboratory played a vital role in the determination of the
feed and products characteristics and in the subsequent analysis
of the data. Thus the work was checked carefully and every pre-
caution made to insure the accuracy of the results. However,
despite these efforts there are occasional instances where incon-
sistencies did arise. While inherent errors associated with the
specific test procedures themselves clearly contributed to the
problem, it is believed that the principal explanation for these
occasional inconsistencies lies in the difficulty of sampling. .
Frequently and of necessity a few grams sampled from a run were
taken to represent the entire production of the oil or char in
some piece of sensitive, chemical analysis laboratory equipment.
Thus even though several tests were usually made, there were
some occasional problems with repeatability of results. While
these variations are predominantly less than one percent, the over-
whelming Impression is of good repeatability. The presence,
expecially in the CHNO analysis, of even small inconsistencies was
found to have a significant effect on the' test results. Thus,
while these data by ordinary standards stand up well, the sensi-
tivity of the overall test results to some of these data make close
scrutiny necessary. A review of the breadth of the laboratory work
done reveals a wide assortment of different analytical procedures.
These procedures include analysis of the :
1. Feed for:
percent moisture
percent ash
percent acid-insoluble ash
percent carbon
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percent hydrogen
percent nitrogen
percent oxygen
heating value
Char for:
percent moisture
percent ash
percent acid-insoluble ash
percent volatiles
percent carbon
percent hydrogen
percent nitrogen
percent oxygen
heating value
Oils for:
percent moisture
percent carbon
percent hydrogen
percent nitrogen
percent oxygen
The composition of the off-gas was determined by gas chromatography
and reported as:
percent
nitrogen
percent
carbon monoxide
percent
carbon dioxide
percent
hydrogen
percent
methane
percent
components
percent
components
percent
components
20

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Presented in Appendix A are brief descriptions of the laboratory
procedures followed to obtain all these data and estimates of the
accuracy limits intrinsic to the test themselves. The data itself
are presented in Appendix B.
DATA REDUCTION
General
The primary data obtained from the pilot plant testing, plus the
laboratory findings, provided a substantial body of information
and a solid basis to conduct complete energy, mass and elemental
balances for each test. In fact, a redundancy in the available
information provided the means for an even more complete
evaluation of the internal consistency of the data. Presented in
this section is a discussion of the rationale by which the data
was reduced and' additionally provided is a description of a
sensitivity analysis by which the influence on the overall
balances of small variations in the measured results is determined.
Finally, a method by which the initial data is transformed into a
generally consistent set of revised data which simultaneously
satisfies the physical conservation principles and the laboratory
findings is presented.
Data Reduction Methodology
The data from the pilot plant testing included the mass of feed
processed, the corresponding char and recovered oil and aqueous
yields and an integrated off-gas sample. Data regarding pyrolysis
f
bed and off-gas temperatures, cooling water flow and temperatures
and surface temperature completed the Information available from the
testing. The laboratory findings, as described previously, included
percent moisture, ash, carbon, hydrogen, nitrogen, oxygen, and
heating values for the feed, char, and oil. In addition, the compo-
sition of the non-condensible gas was provided. This then allowed
computation of the heating value of the gas.
21

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Using part of these data and the laws o.f energy, mass and elemental
conservation, a system of algebraic equations can be written.
These equations have been solved on the computer and the calculated
results compared with the remaining observed data to obtain a measure
of the internal consistency of the entire set of data. The effects
on internal consistency,of small variations in the values of the
original data have also been studied. It has been found that
typically variations in specific measured values of no more than a
few percent are required to put all the data into a generally con-
sistent form. Since it must be recognized that all the data is sub-
ject to some uncertainty, it has been assumed that on the average
the modified values (e.g. the original value plus the computed
variation) are likely superior to those actually measured or ini-
tially computed and therefore these modified values have been used
in the data analysis and in the presentation of the results (study
of the latter, as presented in the following section, provides
further justification for this action since the revised data is
generally consistent with earlier results (1) and shows an accep-
table degree of scatter).
Analysis
The equations used in the data analysis include
Conservation of Mass:
*M+M+M1+M=M, + M+M.	(1)
g o ch wo f a wi
Conservation of Energy:
(HV+h)M+(HV+h)M+(HV,+h,)M1+h M -
v g g g o o o	ch ch ch wo wo
(HV. + h,) M, + h M + h . M . - [conduction and cooling water
v f f f a a wi wi
losses]
*A table of Nomenclature is presented on page vi.
22

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By establishing ambient conditions as a reference, and can
be set to zero. Now generally the sensible and latent heat terms
involving h^, hQ, h^, and hwi and the heat losses are small in
comparison to the other terms. Thus it is convenient to combine
these terms into a single expression
L = h M +h M + h,M,-h.M. + [conduction and cooling
g g o o ch ch wi wi	°
water losses]
and to rewrite the energy equation as:
(HV ) M + (HV ) M + (HV ) M + h M « (HVf) Mf. - L	(2)
g g	o o	cn cti wo wo	r t
Since L is small compared with the other terms, approximate
values can be taken with little error in the resulting solution.
Conservation of Nitrogen:
w Mg + w M + w ,M,=w£M£+w, Ma	(3)
ng	no o nch ch nf f ha
Conservation of Carbon:
wM+wM+w,M»w_M,	f,\
eg g co o cch cn cf f	W
Conservation of Hydrogen:
w, tl + w, + w, , M , + w, M = w M. + w, M	(5)
hg g ho o hch ch hwo wo hf f hwi wi
Conservation of Oxygen:
(6)
w M„ + w M+w.M.+w M =w.M, + w M. + w .M.
og 8 oo o och ch owo wo of f oa a owi wi
In addition to these relations, the Dulong-Petit equation was used
to calculate the heating value of the oil:
HV » 14,500 w + 61000 w,	,7x
o	co	ho	)
The C, H, N, 0 analysis of the oil requires that:
w + w, + w +w =1
co ho no oo	(g)
23

-------
Likewise the C, H, N, 0 analysis of the char and feed requires
that:
wu+wlu + wv+w T.-1	ra\
cch hch nch och = 1 - w ,	(9)
xch
w . + w, . + w . + w .
cf hf n£ 1 of - I - wx£	(10)
Correspondingly, a computed C, H, N, 0 composition of the off-gas
from the gas chromatographic results requires that:
w + w, + w +W =1
eg hg ng og
These 11 equations represent a complete description of the
applicable conservation principles for the data, and upon simul-
taneous solution and comparison with the laboratory data, provide
a redundant body of information with which to check the internal
consistency of the results.
The procedure, therfore, followed in the data reduction has been
to simultaneously solve the first eight equations for the values, of:
It has been assumed that the 26 terms:
Mf, Mch, Ma, Mwi, HVg, HVo, HVch, hwo, HVf, L, wng, w^, w^,
Wna' Wcg' Wcch' Wcf' Whg» Whch' Whw» Whf» Wog' Woch»' Wow' Wof'
and w are known to within a certain precision; generally less
oa
than 10 percent (based on previous pilot plant and laboratory
experience).
*These three values could not be determined simply from the test
results, while Mf, Mch, and and Mwi, could be measured directly.
**The C, H, N, 0 composition of the oil and its heating value have
been chosen as "unknowns" because it is believed there is greater
uncertainty in the measured oil composition and heating value than
for the feed, char or gas (which could have just as easily been
used) due to the presence of water.
24

-------
Once values of the eight "unknowns' are determined, a sensitivity
analysis by which the effect on the computed values of the "un-
knowns" of individual variations in each of the 26 "known" co-
efficients is conducted. Those coefficients, which have a major
influence on the solution, are thereby identified. Since the
final object is to obtain as internally consistent a set of data
as possible, the next step is a least squares procedure by which
variations between the measured and computed values of w , w, ,
co ho
w , and w , are minimized. This is accomplished by introduction
no	oo
of combinations of up to four of the major influencing coefficients
and by allowing the values to vary simultaneously about their
"known" value, usually within bounds of + 10%. A least squares
program then selects that combination of the major influencing
coefficients while minimizes the sum of the squares of the
difference between the computed and measured data. This
generally results in a complete set of transformed data which is
very nearly consistent internally and which represents an exact
solution to the first eight.equations.
In one case, Test 14, variations in the "known" coefficients of
considerably more than.10% were required to bring the system of
equations in a proper balance. This occurred both with the char
and the #feed carbon content which was adjusted significantly.
However, since the modified data for this case (as seen in the
next section) plots up well with all the other results, it is
believed that whatever the cause of this anomaly, the applied
correction is made apparently in the proper term and to the
required extent.
Presented in Appendix C are listings of the computer programs for
the sensitivity analysis (SENSAN) and the least squares procedure
(1TERAT) developed from the analysis. Also presented are sample
calculations for Test 1 (Run 4) to illustrate the output of these
two programs.
25

-------
TEST RESULTS
Overview of Test Conditions
The experimental program involved a series of 15 tests; 13 with
peanut hulls and two with sawdust. In addition, there were
several unreported tests at the beginning of the program to check
out the procedures with peanut hulls and the basic agitator used in
the first part of the study. Of the 15 reported tests, two were
checkouts of the first generation integrated mechanical agitation-
process air supply system or "AIRGITATOR", for which no quantitative
data was recorded. Besides these two tests, two more were found
to have dtlective off-gas compositions, apparently due to an air
leak somewhere in the system. Thus while some data for these
latter two tests were obtained, the primary basis for the results
presented in this section is the 11 remaining tests.'
Of the 11, ten were conducted using the hulls, and one with saw-
dust. There was one extended run of 12 hours using hulls (Test 7),
but normally the runs lasted two to three hours, sometimes slightly
more or less. In addition, two of the 11 were conducted using the
"AIRGITATOR". In the 9 basic tests, the influence of mechanical
agitation, changing feed material, changing bed depth and the
air/feed ratio was studied. In the last two tests, the
performance of the "AIRGITATOR" was evaluated at a fixed bed
depth.
Table 1 presents a summary of the test conditions, along with some
of the observed data from the pilot plant tests. Study of the
table shows that basic agitation was involved in eight of the 15
tests conducted, while three were completed without any form of
agitation. Four tests were made with the "AIRGITATOR".
26

-------
TABLE I
TEST SUMMARY




Oil &










Char
Aqueous
Off-Gas


Average





Feed
Yield
Yield
Yield


Maximum Measured



Test

Rate
kg/kg
kg/kg
kg/kg

Off-Gas
Bed Temperatures
Bed (cm)


Number
1
kg/hr dry feed
dry feed dry feed
Air/Feed
Temp. 3CO
rc)5
Depth
Aftltstlon
AlrRltatlon
1
Peanut Hulls
572
.217
.039
1.108
.364
96
649
132
No
No
2
Peanut Hulls
390
.239
".085
.941
.265
93
732
132
No
No
3
Pine Sawdust
676
.266
.057
.849
.172
113
760
132
No
No
4
Pine Sawdust
464
.249
.070
.932
.251
140
732
132
Yes
No
S
Peanut Hulls
494
.288
.079
.86
.227
86
649
132
Yes
No
6
Peanut Hulls
481
.321
.072
00
CO
.277
85
716
132
Yes
No
7
Peanut Hulls
476
.229
.047
.994
.270
88
704
132
Yes
No
8




*
CHECK OUT "AIRGITATOR"


No
Yes
9
Peanut Hulls
408
.400
.161
.897
.458
78
960
89
Yes
No
10
Peanut Hulls
501
.249
.0453
1.17
.464
88
560
89
Yes
No
11
Peanut Hulls
570
.270
.234
1.035
.539
87
682
89
Yes
No
12
Peanut Hulls
471
.284
.178
1.151
.613
83
787
89
Yes
No
13




CHECK
OUT MODIFIED
"AIRGITATOR"


No
Yes
14
Peanut Hulls
490
.414
.035
.691
.140
174
471
127
No
Yes
15
Peanut Hulls
324
.283
.262
.645
.190
226
471
127
No
Yes
TOTAL FEED PROCESSED - 43,400 kg
TOTAL OPERATING TIME - 119.5 hours
1	Test runs were of two to'three hours duration, except number 7, which was a 12-hour run.
2	The "off-gas yield" (Including moisture of cosituation uncondensed oil, oil in suspension and noncondensible gas) Is determined by differ-
ence.
3	The "off-gas temperature" is that measured as the gas exits from the pyrolyt'lc converter.
** The indicated temperatures correspond to the average maximum measured by the thermocouples In the lower bed of the convertor. Since the
temperature of the bed varies three-dloenslonally in space and also varies in time (due to variations In the environment near the sensing
element), the quantitative significance of the specific indicated temperatures Is doubtful. However, they are presented for completeness
and to Indicate the range of temperatures encountered. Study of the data does indicate a general, trend of increasing temperature with
increasing air/feed; however, there is considerable scatter.

-------
Further, it is seen that testing was conducted at two bed depths, i.e.
127-132 cm (50-52 inches) and 89 cm (35 inches). The air/feed varied
from 0.14 to 0.613; a range within which most operations Would be
found. Study of the off-gas temperatures indicates they were generally
in the range of 77 to 88°C, except the two tests with sawdust
which ran somewhat hotter. While not reported, the condenser thermo-
stat temperature was usually set in the range of 93 to 99°C
except in the last test where it was set at 99°C to determine
the influence of condenser temperature on oil recovered.
Additional study of the table shows that the dry feed rates varied
from slightly over 300 kg/hr (700 lb/hr) to nearly 700 kg/hr (1,5000
lb/hr). Oue puzzling result is the wide variation in the recovered
oil and aqueous phases from the condenser. Reference to Appendix
reveals that sometimes the water content is quite.significant, and
other times it is small. Apparently minor variations in the off-
gas and condenser temperatures can produce significant changes in the
oil yield exists, it is believed, in the form of more volatile
hydrocarbons, the recovered yields (on a dry basis), with the ex-
ception of Test 15, are generally much smaller than the computed
yields, as discussed in the following section.
In the course of the testing, almost 42,000 kgm (100,000 pounds) of
feed were consumed and the unit was operated for a total of 119.5
hours.
Analysis of the Data
Besides the data shown in Table 1, the laboratory analysis of the
feed, char, oil and non-condensible off-gas are presented in
Appendix A. The data from these tables was transformed in the
manner described in the previous section to produce a generally
28

-------
consistent set of results which is believed to be, on the average,
more accurate than the original raw data. This transformed data
is presented in Table 2 and is the basis for all further discussion
of the testing. Shown also in the table, in parentheses, are
the amounts the transformed data was changed from the original.
Inspection reveals that only a minor part of the data has been
modified and the changes are generally small.
While many of the modifications appear to be random, there is a
rough pattern to some of the changes. For example, there appear
to be relatively frequent reductions of the order of 8 percent on
the off-gas nitrogen composition and in the char carbon content
required to make the data more consistent. Likewise, there appear
to be several cases where the carbon content of the feed and the
heating value of the feed must be increased about 6 percent to
make the results internally consistent. An explanation for the.
need for nitrogen reduction is the possibility that some air may
have leaked into the system. At present, no plausible explana-
tions can be offered regarding the-three remaining changes.
An area of concern, at first glance, are the considerable
variations present in the computed oil heating values and also in
the measured values tabulated in Appendix B. Comparison shows
frequent, substantial variations between individual values of these
two sets of numbers. These differences require some explanation:
Concerning the calculated values; since the computed oil CHNO
analysis is often somewhat different than the measured, which in
turn varies considerably, it is not surprising that the calculated
heating value, via the Dulong-Petit equation, varies also. Perhaps,
therefore, a more meaningful value would be an average which is
7.408 kcal/gm (13,335 Btu/lb). Regarding the laboratory reported
29

-------
Table 2
Summary of Transformed Data
1
Data Unlta Teat 1 ¦ Teat 2 Teat 3 Test 6 Teat 7 Teat 9 Teat 10
(Caa)
H2
gm/ gin
.485
.530
(-8X)
.382
(-8Z)
.442
.434
.517
(-8Z)
.574
C
gm/gm
.191
.199
.258
(-2Z)
.194
.201
.199
.163
«2
gra/ga
.021
.021
.027
.028
.028
.017
.019
°2
gra/go
.303
.289
.364
.336
.338
.306
.244
HV kcal/gm
1.5
1.488
1.966
1.528
1.528
1.333
1.317
(Char)








n2
gm/gm
.025
.021
.011
.029
.027
.027
.008
c
gm/gm
.721
(4Z)
.829
.844
.724
.795
(-8Z)
.677
(8Z)
.808
(-8Z)
«2
gm/gm
.026
.018
.017
.017
.016
(5.5Z)
.018
.015
°2
gm/gm
.089
.032
.064
.165
.121
.121
.103
HV *kcal/gm
6.111
7.111
7.333
6.778
(10Z)
7.000
(2Z)
6.722
6.611
(Feed)








N2
gm/gm
.017
.021
.001
.012
.012
.012
.012
C
gm/gm
.457
(6Z)
.462
(2X)
.450
(2Z)
.445
(6X)
.473
.444
(8Z)
.464
(4Z)
«2
gm/gm
.061
.058
.054
.057
.057
.059
.059
°2
gm/gm
.437
.452
.488
.457
.458
.446
.446
IIV kcal/gm
4.650
4.400
4.294
(6X)
4.539
4.628
(-2Z)
4.778
(2Z)
4.583
(6Z)
*Not aah free;on dry basla
Teat 11
Teat 12
Test 14
Teat 15
.478
.189
.017
.314
1.283
.008
.809
(-4Z)
.013
.031
6.833
.012
.444
(81)
.059
.446
4.389
(10Z)
.510
(-8X)
.199
.016
.314
1.406
(-8Z)
.011
.773
.009
.089
6.389
.012
.483
.059
.446
4.778
(2Z)
.396
.216
.018
.369
.1.322
.011
.393
(-50Z)
.018
.115
6.944
.007
.304
(40Z)
.061
.427
4.728
.351
.218
.011
.422
.856
.007
.818
(-4Z)
.014
.091
6.889
.007
.466
(8Z)
.061
.427
4.728

-------
Table 2 - Continued
Data
Units .
Teat-1
Teat 2
Teat 3
Teat 6
Teat 7
Teat 9
Teat 10
Teat 11
Teat 12
Teat 14
Teat
HEIGHT
ERACTIONS
OF
ELEMENTS
IN OIL











n2
gm/ga
.040
.047
.016
.029
.078
.014
.015
.315
.017
.012
.012
C
gm/gm
.657
.831
.758
.732
.687
.737
.725
.722
.712
.703
.694
H2
gm/gm
.071
.059
.067
.080 '
.081
.080
.084
.080
.075
.077
.077
°2
gm/gn
.242
.064
.145
.158
.155
.168
.176
.182
.197
.203
.217
n2
«
gn/gn
.034
1
.039
.024
.046
.078
.056
.028
.008
.043
.0B7
.111
C
gm/gm
.650
.813
.670
.723
.723
.582
.743
.691
.679
.660
.676

3m/gm
.043
.004
.001
.021
.024
.093
.013
.090
.097
.102
.106
°2
gm/gn
.269
.144
.306
.210
.175
.270
.215
.212
.181
.152
.107
UV kcal/ga
6.722
6.722
5.422
6.667
6.500
7.833 •
(.444
8.611
8.778
8.778
9.056

-------
Data Units Teat 1
Teat 2
Teat 3
Table 2 - Continued
Teat 6 Teat 7 Teat 9
MASSES
CHAR gm/100
gm dry
Feed
FEED 100 ga
dry
AIR gm/100
gm dry
Feed
MOISTURE(IN)
gm/100
gm dry
Feed
OFF- gm/100
GAS gm dry
Feed
OIL gm/100
gm dry
Feed
MOISTURE(OUT)
gm/100
gm dry
Feed
ENERGY LOSSES
kcal/100
gm dry
Feed
21.7	23.9
100	100
36.4	26.5
4.6	4.5
57.7	39.5
29.1	22.8
32.5	44.9
30	30
26.6	32.1
100	100
17.2	27.7
5.3	4.8
33.3	44.2
20.7	27.9
42.0	36.7
30	30
22.9	40.0
100	100
27	45.8.
4.8	28.7
47.8	68.2
14.0	6.49
36.1	59.8
30	30
Teat 10
24.9
100
46.4
28.7
63.4
21.4
65.4
30
Teat 11
27.0
100
53.9
28.7
88.6
8.45
58.5
30
Teat 12
28.4
100
61.3
28.7
94.0
11.3
56.4
30
Teat 14
41.4
100
14.0
6.5
27.5
12.4
39.2
15
Teat 15
28.3
100
19.0
6.5
42.4
20.9
33.9
30

-------
heating values which are for the indicated moisture contents, again
an average of the dry heating values is probably a more accurate
value (in passing it should be noted that the uncertainity in the
moisture percentage can be significant and thus the corrected heating
value is also uncertain). However, upon adjusting the indicated
numbers to a dry basis and after computing an average value, the
result obtained is 7.906 kcal/gm which is 6.7% greater than the
average of the computed results. It is believed that the justifica-
tion for working with these average values is adequate, and that
these two values are sufficiently in agreement to satisfy the
accuracy requirements of the study.
Using the results presented in Table 2, several informative graphs
can be drawn. This is done in the next six figures which
correlate closely with corresponding figure in (1).
Graphical Data Presentations
Perhaps the most important results of the entire program are those
plotted in Figure 9 which presents the percent available energy
of the char and oil (related to the feed) as a function of the
air/feed ratio. The figure shows that for'all .the tests, at
various bed depths, with-and without agitation and with both sawdust
and°peanut hulls, the data correlates to a single line. This line
is identical to that reported in (1) using sawdust in a unit 1/2
the geometric scale of the present unit. In fact, when the data
from the present program and that from the earlier study are
combined the agreement is striking. This is illustrated in Figure
10 for which the best fit straight line is again identical to both
that in Figure 9 and that from (1).
This suggests therefore, that to an acceptable engineering precision
the available energy fraction of the feed in the char-oil miv is
independent of unit scale, feed material, bed depth and the presence
of mechanical agitation; and is a linear function only of the air/
• feed ratio.		
" _
i
33
)

-------
90-
15
80-
E
14
~
at
Sj
C
w
.c
«
4
a)
3
H
03
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00
c
X
o
o
70.
60.
50—1
«
4)
S
lJ

-------
>N
a>
60
3
W

41

e
>
w
60

C
•H
"H
0
1
¦U
aj
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u
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at
<
fe
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o
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90-
80 _1
70-
601
50
40 -
30"
20 -
10 -
SYMBOL NOMENCLATURE
PREVIOUS STUDY (1)
All data ^
PRESENT STUDY
Bed
Depth
(cm)
Agitation Airgitation Neither
89
O

9
127
~
ffl
¦
132
A
A
A
—i	1	1	r-
0.1 0.2 0.3 0.4
Air/Feed
0.5
l
0.6
"7
0.7
Figure 10
•Percent Available Energy in Char-Oil
Mixture- Composite of all Data
35

-------
Figure 11 presents an energy breakdown of the pyrolysis products
as a function of the air/feed ratio. Examination of the figure
reveals the relative consistency of the data and, as in Figure 9,
suggests that the dominant influencing variable is the air/feed
ratio. Comparison of similar results from (1) shows generally
good agreement with the total of the sensible energy in the oil
and water in the off-gas and heat lost by conduction and to the
cooling water. Likewise, the energy in the off-gas is almost
identical with the results from (1). And finally the combined
energy in the char-oil agrees very well with the results from (1).
However, there is a significant difference in the way in which
the separate energies in the oil and char vary from those presented
in (1). An explanation for this difference may shed considerable
light on the physical processes at work, and provide a means of
varying the relative amounts of oil and char produced at a given,
fixed*air/feed ratio:
In (1), the char yields linearly decreased and the oil yields
linearly increased with increasing air/feed while in the present
study the char yields remain practically constant and independent
of air/feed, whereas the oil yields decrease with increasing air/feed.
However, in (1) the pyrolysis off-gas temperatures were always in
the range of 150-175°C while in the present study the off-gas temp-
eratures using peanut hulls"1" and with the exception of Test 14 and
++
15 , were in the range of 75-95°C. This difference in the off-gas
+ The off-gas temperatures with the sawdust were somewhat higher,
but still low in comparison with the tests in (1) using sawdust.
++• Test 14 and 15 were conducted using the integrated mechanical
agitation-air supply system and for reasons presently not completely
understood produced relatively high off-gas temperatures at very
low air/feed ratios.
36

-------
90
80
70
60
50
40
20
10
O
Air/Feed
Figure 11
Energy Breakdown of Pyrolysis Products
37

-------
temperature is very significant because in the latter case the higher
boiling point oils are condensing in the bed. Laboratory experience
has taught that when pyrolytic oils are heated, a significant degree
of carbonization occurs along with evaporation. Hence, in the current
study, once the oils condensed and were reheated in the downward
moving feed only a part of the original oil evaporated, while a con-
siderable portion was converted into solid carbon. The result was
the almost constant char yield and a diminishing oil yield with
increasing air/feed.
The reason why the off-gas temperatures in the present study were
generally so low compared with the results from (1) is because the
bed depth was generally near the maximum. The results from (1),
at a smaller scale, had suggested that for maximum oil yields a
larger bed depth was desirable and therefore, in the present study
the larger bed depths had been deliberately chosen to obtain the
greatest amounts of oil. It appears, however, that the bed depths
selected were considerably greater than'the optimum for oil produc-
tion.
Physical reasoning suggests that for a given feed, for fixed values
of process air and feed rate, and for a very shallow bed depth, the
off-gas temperature approaches the temperature in the combustion
zone and there is little or no pyrolytic conversion of the feed.
Under these conditions a breakdown of the oily products occurs to
produce more gaseous constituents. For increasing bed depth,
pyrolytic conversion of the feed begins to occur and the oil yields
grow as the off-gas temperature decreases. However, as the bed
depth increases beyond some optimum point, significant amounts of
condensation occur in the bed and the oil yields are diminished.
Clearly at some critical bed depth, moisture condensation occurs
and above this point the process become unstable. All this beha-
vior is illustrated graphically in Figure 12 which also shows the
surmised operating zones for the present study and that for (1).
38

-------
Operating
zone in
(1)
Operating
zone in pre-
sent study
Forbidden operation
due to moisture
condensation
A
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i\NS\NS\\WS\\'\
VV\S\\\\\\\\\\\
s\\V\s\\ss\\\\
sssssNwssss \\S
.sssssssvssss ws
SSSSSSSSSSSN \SS
SSSSSSSSSSSV.SSS
SSSSSSSSSSSSSNS
sssssssssssssss
SSSSSSSSSSSSSNS
'11
VsW
SSSSSSSS
>*yssssss
S\vS^SS N
NNSSV\S^.
ssssssss'
ssssssss
ssssssss
ssssssssss
ssssssssss
' " ' v
sssss ss
sssssss
SSSSNNN
NNSSSSS
Sssssss
sssssss
SSSNNSS
sssssss
sssssss
Maximun
bed
practical
depth
~
it
b
3
4J
(0
0)
a.
e
0)
H
a>
at
u
I
M-4
Off-gas
dew point
Increasing Bed Depth
Figure 12
Oil Yield Variation with Increasing Bed Depth
39

-------
Taken together, this all suggests that while the sum of the energy
in .the char and oil is basically dependent on the air/feed ratio,
the distribution of the energy between the oil and the char is a
function of both the bed depth and the air/feed. Thus a means to
independently vary the relative amounts of oil and char in the py-
\
rolysis products for a fixed air/feed exists. Conveniently, over
a range of bed depths the off-gas yields appear to be relatively
*
independent of the bed depth and only a function of air/feed.
In more specific terms, to maximize char yields, the pyrolysis unit
should be operated at the greatest allowable bed depth. Conversely,
to optimize oil yields the corresponding optimum bed depth should
be determined and the unit operated near this point. It should
be recognized that when the char yields are maximized, a very
large portion of the oil produced is likely to be unrecoverable
because its boiling point lies below the dew point of the off-gas
mixture. Thus while .the available energy in tjie char-oil mixture
is approximately constant (at a given air/feed), it may be more
desirable in many situations to avoid a deep bed in order to
actually recover a maximum percentage of the oil in a useable form.
Therefore it appears that for maximum recovery of both the char and
the oil, operation near the point of maximum oil production is
indicated.+
*This indicates that in this image the carbonization of the oil results
in a minor amount of oil gasification, and therefore that the oils are
broken down into the more volatile fractions. Since the condenser
temperature, in the testing was limited by moisture condensation
considerations this would explain why the recovered oil yields were
generally so small.
+Thus one of the important advantages of the AIRGITATOR system is
its ability to continuously vary the bed depth, therefore pro-
viding the capability to vary the relative oil and char yields over
a wide range.
40

-------
It should be noted that the presence of water in the feed acts
effectively to increase the bed depth, since greater amounts of
energy are required to pyrolyze the feed and thus the off-gas
temperature tends to be reduced. Therefore, if a maximum of both
char and recoverable oil is desired, it would be best to operate
with as dry a feed as possible.
Figure 13 is a crossplot of computed data from (1) and experimental
data from the present study. The figure provides a convenient means
for determining the required air/feed ratio for a given feed
moisture percentage and further allows computation of the available
energy in the char-oil mixture. The computation assumptions regarding
the energy requirements to operate the portable unit are taken from
(1). To illustrate the use of the figure, at a feed moisture per-
centage of 20 percent, the required energy for drying and processing
is .444 kcal/gm (800 Btu/lb) dry feed. Correspondingly, at an
air/feed value of 0.16 the available energy in the gas is .444
kcal/gm (800 Btu/lb) dry feed and that available in the char-oil
is 3.611 kcal/gm (6,500 Btu/lb); thus establishing the relation
between the moisture content and the air/feed. Finally for conven-
ience the figure allows computation of the energy available in the
char-oil mixture, as shown earlier in Figure 9.
Figure 14 presents a plot of the heating value of the non-
condensibl.e component of the off-gas in kcal/cubic meters
as a function of air/feed. As before, and as in (1), there is a
correlation with this parameter, although the data scatter is
greater than desired. The curve drawn through the data lies within
5 to 10 percent of the corresponding curve from (1) and thus
again establishes the close correlation of the d&ta from the two
studies.
41

-------
i—i—i—i—r
,7 .6 .5 .4 .3 .2
Air/Feed
1.0
M
O
JS
u
§ B
M 00
<4-<

<
- 2.0
E
o
u
>«
Xi
3.0
«
U
4.0
t i r
10 20 30 40 50 60 70 80 90
Feed Percent Moisture
- 1000
"O
« ~1
©
fa
«
§
H
pa
700({
2000
3000
4000
5000
-6000
Assumptions:
1)	Gross heat energy
required to process one
one pound dry feed =
91 kcal (360 Btu)
2)	378 kcal required in
drier to evaporate
one pound of water
Figure 13
Effects of Feed Moisture on Available
Energy from Char-Oil Mixture.
42

-------
3000
~
3
m
15
SYMBOL NOMENCLATURE
Bed
Depth
Cinches)
35
50
52
Agitation Airgitation Neither
o
~
A
©
E
A
- 2500
I
-I 2000
" 1500
-j 1000
!
500
0.1
~	i	r
0.2 0.3 0.4
Air/Feed
0.5
0.6
Figure 14
Heating Value of Non-Condensible Gas
43

-------
SECTION V
INTEGRATED MECHANICAL AGITATION-AIR SUPPLY SYSTEM
GENERAL"
The present concept of the EES waste converter system operation
involves the addition of process air near the bottom of the vertical,
gravity-fed porous bed. This air allows combustion of a small
fraction of the feed material and thus provides the heat required
for pyrolysis. The air is added by means of several fixed, water
cooled air tubes. The presence of these air tubes represents a
hindrance to flow of the feed material and is thus partially
responsible for the need for a mechanical agitation system to
enhance feed throughput. There is also the fact that since the
system throughput is limited to a large extent by gravity,
»
residence times are far greater than required to pyrolyze the feed.
Thus there appears to be considerable advantage in the use of an
integrated mechanical agitation-process air system, especially
if the mechanical agitation system is a requirement in any
case, to process bulky wastes. By so doing, the principal
hindrance to flow through the converter is changed into a means
for facilitating the flow. Such a system also possibly allows the
processing of somewhat wetter feed than the present EES waste
converter permits. This section, then, presents a description of
a "first generation" integrated mechanical agitation-process air
supply system or "AIRGITATOR" and a discussion of the initial
tests conducted with it.
44

-------
SYSTEM DESIGN
There are conceptually a large number of possible configurations
that the system might have taken. However, it was decided at the
outset that the simplest configuration possible was to be selected.
This was done in order to minimize fabrication problems and to avoid,
as much as practical, the possiblity of failure and the opportunity
for leaks, by minimizing the number of welds. Thus an "L" shaped
system was chosen.
The system is presented schematically in Figure 8 and the design is
shown in Figure 15. The tubes are made of 4130 alloy steel and are
typically .318 cm (1/8 inch) thick. The air delivery ports are .159 cm
(1/16 inch) in diameter and located 1.26 cm (1/2 inches) apart. From
the metal types and gages, it should be apparent that the system
was designed to withstand a hugh torque in a relatively hostile en-
vironment. A photograph of the unit, fabricated in the EES shop, is
presented in Figure 16.
A commercially available rotating coupling, which was compatible
with the water and air flows required, was found; thus avoiding the
necessity for designing and fabricating this component at the EES.
This coupling, along with the final drive mechanism and the copper
tube connections for the process air and cooling water are shown
in Figur^ 17 which depicts the "AIRGITATOR" installed on top of
the converter. The installed system, as can be seen, is not complex,
and involved a drive system, the coupling and the "L" shaped
"AIRGITATOR".
In the initial design, the horizontal portion of the unit extended
to within one inch of the inside walls of the convertor and the ends
were cut off squarely. A later modification involved the removal
of one inch from this horizontal portion and the beveling of the
45

-------
^ Passage Union
H:
n
00
§
¦ 1
"r
v.«>v|
i
n
L
v...
i./"
r
ilH
8

-I
7vn
n
\
/
/
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CT«:r::r-~:—:-a
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11
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	8 !
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r T
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		 |	it
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._	:-y?-)6 nfi--
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Ve«-fctu\	,| !•¦--¦
. - - < . . 1 " '• '
I «0' t»'~- * —	
	i 		 ;••• * ;
/
.^OriZfKifol £*«-• -,t		
II
Poll Mo. IJ».
Daeeripficii
Material
ENGINEERING Er.fEIUMEN? STATION
TliCHflOLOGY APPLICATIONS GUOO?
Til!r
Design for AIRGITATOR
III
1
a?p.
Orit- • rtov.
p.//..
i
¦j


Dwff. Ma
©--• -r'r- ^ >•
.i.-t-i-T	ri
^ 1 : . :, l. -1
'
-------
Figure 16
Overall View of AIRGITATOR
Figure 17
AIRGITATOR Installed on
Pyrolytic Converter
||}|g - t-v:
	- ~rjr - ~- j
"¦ \


47

-------
end so that the end surface formed a sharp edge which cut through
the char. These modifications were made to avoid binding of the
feed between the walls and the end of the unit, in situations
where due to irregularities in the inner surface, the end
approached the wall too closely.
SYSTEM TESTING
About midway through the main test program, the first checkout
tests of the "AIRGITATOR" were conducted. The results of these
first tests were almost disastrous; the main bearings supporting
the unit failed after several hours of testing, apparently due
to very large torques that occasionally were required to rotate
the system. It was concluded that binding, as described above,
had occurred and the indicated modifications were made. Additionally,
the complete drive system.was strengthened substantially.
The modified unit was then tested and no problems were encountered.
Apparently the improvements made were sufficient to overcome the
difficulty. One important feature in these latter tests was the
use of two wall mounted air tubes in the start-up of the unit and
also occasionally to stabilize the hot char bed during normal
operation. The extra depth to the hot char bed provided by these
two tubes, not only enabled a stable hot char zone to be
established initially, but provided a cushion against "losing the
char bed" in anomalous circumstances where the instantaneous feed
rate exceeded the charring rate and threatened the loss of the hot
char which sustains the bed operation.
Perhaps the most interesting feature of the latter tests were the
relatively high off-gas temperatures achieved at very low air/feed
ratios. The ease with which the system operated, the high quality
48

-------
of the char and the clear ability of the system to operate at a
much greater throughput than tested, taken together demonstrated
that the potential of the "AIRGITATOR" is at least as great as has
initially been forecast and is perhaps even greater. In addition,
the ability of the system to vary the bed depth continuously
provides an important capability with which to tailor the oil
and char yields to meet a wide range of requirements.
49

-------
SECTION VI
REFERENCES
1.	Tatom, J.W., Colcord, A.R., Knight, J.A., Ells ton, J..W., and
Har-oz, P.H. "Utilization of Agricultural Forestry and Survival
Waste for the Production of Clean Fuels" Final Report under EPA
Contract 68-02-1485, Engineering Experiment Station, Georgia
Tech, Atlanta, Georgia, September, 1976.
2.	Tatom, J.W., Colcord, A.R., Knight, J.A., Ellston, L.W.,
and Har-oz, P.H. "A Mobile Pyrolytic System - Agricultural
and Forestry Wastes into Clean Fuels" Proceedings 1975
Agricultural Waste Management Conference published as Energy
Agriculture and Waste Management, Ann Arbor Science Publishers,
Inc.v Ann Arbor, Michigan.
3.	Tatom, J.W., Colcord, A.R., Knight, J.A., Ellston, L.W., and
Har-oz, P.H., "Parametric Study for a Pyrolytic System for
Production of Clean Fuels from Agricultural and Forestry
Wastes" Proceedings Tenth Intersociety Energy Conversion
Engineering Conference, published by Institute -of Electrical
and Electronics, Inc., New York, N.Y.
4.	Tatom, J.W., Colcord, A.R., Knight, J.A., Ellston, L.W., and
Har-oz, P.H., "Clean Fuels from Agricultural and Forestry
Wastes - The Mobile Pyrolysis Concept, 1975 A.S.M.E. Winter
Annual Meeting, paper no. 75 - WA/HT - 47.
5.	Everett, Kevin, "Playing Ball with the Big Boys"; Has Mobile
Pyrolysis Come of Age?" unpublished paper, Florida Resource
Recovery Council, December 1975.
6.	Long, J.R.M., "Coal-in-Oil Fuel Study", Final Report, January
2, 1964, Combustion Engineering, Inc.
7.	Private Communication, Mr. Andrew Brown, General Motors.
8.	Private Communication, Mr. Joe Demeter of the E.R.D.A.
Pittsburgh Laboratory.
50

-------
SECTION VII
APPENDICES
Laboratory Procedure
Laboratory Test Results
Data Analysis Computer Program
51

-------
APPENDIX A-LABORATORY PROCEDURE
The following procedures were followed in the laboratory analysis of
the input feed and the pyrolysis products:
Solid Samples
Sample Preparation—The solid samples examined consisted of the
dried peanut hulls, used as feed material for the waste convertor,
and chars produced by the convertor. The sample size received in
the laboratory ranged from one to eight liters for the peanut hull
feeds and from one to two liters for the char products. The samples
were thoroughly mixed and divided by quartering or by a rifle
splitter trt produce a representative one liter sample, which was
passed through a Wiley Model 4 mill using a six millimeter screen.
The ground sample was again mixed and divided into approximately
equal parts. One part was again passed through the Model 4 Wiley
mill using a two millimeter screen. This material was then mixed
0
and reduced by quartering to approximately 100 grams. . The 100
gram sample was then passed through a Wiley intermediate mill using
40 mesh screen, remixed, and quartered. The larger portion of the
-40 mesh sample was stored in a tightly closed glass bottle for use
in laboratory analysis. The remaining quarter of the material was
again passed through the Wiley intermediate mill using an 80 mesh
screen, remixed, and stored in a tightly capped vial for elemental
analysis.
Analytical Procedures—1. Percent Moisture in Peanut Hull Feeds:
Duplicate 1.000 gram samples were placed in aluminum dishes and
dried for one hour at 40.5°C in a forced air oven. The dried
samples were coded in a desiccator and weighed. The estimated
error is + 0.6 percent (absolute).
52

-------
2.	Percent Moisture and Percent Volatiles in Chars: These
analyses were performed by ASTM Method D-271. The estimated error
is + 0.3 percent (absolute).
3.	Percent Ash and Percent Acid-Insoluble Ash in Feeds and Chars:
Duplicate 1.000 gram samples of the feed or char were weighed into
tared porcelain crucibles, ignited to constant weight in a muffle
furnace at 600°C, cooled in a desiccator, and reweighed. The ash
was digested in a 1:3 mixture of hydrochloric acid and nitric acid
for 30 minutes. The mixture was then diluted to approximately
100 ml. and filtered through a Whatman No. 40 paper. After thorough
washing with distilled water, the filter paper and undissolved ash
were returned to the crucible used for the original ash determina-
tions, ignited to constant weight at 600°C, cooled in a desiccator
and weighed. The estimated error is + 0.2 percent (absolute).
4.	Heating Values: The heating values of the feeds and chars were
determined in a Parr Plain (Isothermal Jacket) oxygen bomb
calorimeter. Following the procedures described in pp. 33-38 of
Oxygen Bomb Calorimeter and Combustion Methods, Technical Manual
No. 130, Parr Instrument Company, Moline Illinois (1960). Agree-
ment among replicate samples was better than 2.5 percent (absolute)
for the feeds and 3.5 percent (absolute) for the chars.
5.	Elemental Analysis: Carbon, hydrogen and nitrogen were
determined using a Perkin Elmer Model 240 Elemental Analyzer.
(Oxygen was determined by difference.) The manufacturer claims a
precision of + one percent (relative) for pure, crystalline
materials. Because of the heterogeneous nature of the samples,
loss of volatiles form the chars in the purge fraction of the
analytical cycle, and the difficulty of selecting a representative
53

-------
three milligram sample, occasional variations as high as 15 percent
(absolute)' have been observed in the carbon and oxygen determination
on char samples. In most cases however, the agreement was better
than six percent (absolute) for carbon and oxygen in the feeds and
chars. Agreement among replicate hydrogen or nitrogen determinations
was better than one percent.
Oil Samples
Sample Preparation— The oil samples received in the laboratory
were stored in tightly closed glass bottles and stirred before
each analysis.
Analytical Procedure—1. Percent moisture in Oil: The percent
moisture in the oil was determined by the method of Dean and Stark.
The error is believed to be + five percent (relative), although the
oil is known to begin to decompose partially with liberation of
additional water at the temperature of the toluene-water azeotrope,
and that acetone and other water soluble compounds have been
detected in the head space over stored oil samples.
Non-Condensible Gas Samples
Sample Preparation—Gas samples were drawn continuously from the
head space in the waste convertor or from the upstream end of the
condensers. The sample stream was passed through a series of water
cooled condensers, a glass wool demister, an ice cooled trap,
a chemical drying tube, and a dry test meter to a tee in the
sampling line. From the tee the major portion of the sample was
exhausted to the atmosphere through a vane type pump. A smaller
portion of the stream was led from the tee through a tubing pump
and a wet test meter into a 96 liter "Saran" gas collection bag.
54

-------
The flow rate in the gas streams was held constant throughout the
sampling periods. At the end of the test the waters and oils from
the condenser train were measured and the gas collection bag was
closed and returned to the laboratory for analysis.
Analysis of Non-Cpndensible Gas Samples—The gases were mixed by
kneading the sample collection bag and their concentrations were
determined by gas chromatography. Oxygen and nitrogen were
determined using a Perkin Elmer Model 990 Gas Chromatograph using
helium carrier gas, a Molecular Sieve 5A column, and a thermal
conductivity detector. Hydrogen was determined in a similar manner
using argon as the carrier gas. Carbon monoxide, methane, and
carbon dioxide were determined in the same instrument using helium
carrier gas and an activated carbon column. Hydrocarbons con-
taining two or more, carbon atoms were determined in a Perkin Elmer
Model 154 instrument using helium carrier gas, a Perkin Elmer "R"
column, and a flame ionization detector. The estimated error wa!s
+ five percent (relative).
55

-------
APPENDIX B-LABORATORY DATA
Listed In the following pages are the results of the laboratory
analysis described in Section IV for the feed, char, oil and off-
gases from the test program. It should be noted that the CHNO
analysis and the heating values for the oils are for the indicated
moisture content. Thus, the results for dry oil in Table 2, have
been corrected for this moisture. The CHNO analysis and heating
values for the feed and char are on a dry basis.
56

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WATER
ASH
ACID
INSOLUBLE
ASH
CARBON
HYDROGEN
NITROGEN
OXYGEN
UNITS
Percent
Percent
Percent
Percent
Percent
Percent
Percent
TABLE B-l
LABORATORY ANALYSIS
TEST 1
FEED
4.4
3.4
48.6
6.0
1.7
43.7
CHAI?
8.3
10.9
li.l
2.6
2.5
8.9
OFF - GAS
NON-	PER-
CONDENSIBLE CENT COM-
OIL
11.9
COMPONENTS POSITION
57.0
t
7.6
3.5
31.9
n2
CO
CO,
H,
CH4
C2H6
C2H4
C3H8
C3H6
44.37
16.88
15.78
16.17
4.60
0.52
0.72
0.13
0.24
HEATING
VALUE
kcal/gm 4.651
6.083
6.960
		i
1.	The CHNO analysis and heating values are based on oil with the
Indicated mositure content.
2.	The volatile component of the char probably contains very little
water and is primarily gaseous hydrocarbons.
3.	Note, this is the volume, not the weight composition.
57

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TABLE B-2
LABORATORY ANALYSIS
TEST 2
OFF- GAS
NON-
PER-
CONDENSIBLE CENT COM-

UNITS
FEED
CHAR
OIL COMPONENTS
POSITION
WATER
Percent
4.3
'0.3
33.2
n2
47.1
ASH
Percent
2.3
10.0
-
CO
14.5
ACID
INSOLUBLE
ASH
Percent
- .
-
-
co2
H2
19.9
11.1
«




ch4
5.52
CARBON
Percent
47.0
82.9
55.5
C2H6
0.63
I
HYDROGEN
Percent
5.8
1.8
7.6
C2H4
0.90
NITROGEN
Percent
2.03
2.1
3.11
C3H8
0.14
OXYGEN
Percent
45.17
3.2
33.79
C3H6
0,27
HEATING
VALUE
kcal/gm
4.397
7.111
5.299


1.	The CHNO analysis and heating value-are based on oil with the
Indicated moisture content.
2.	The volatile component of the char probably contains very little
water and is primarily gaseous hydrocarbons.
3.	Note, this is the volume, not the weight composition.
58

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WATER
ASH
ACID
INSOLUBLE
ASH
CARBON
HYDROGEN
UNITS
Percent
Percent
Percent
Percent
Percent
-NITROGEN Percent
TABLE B-3
LABORATORY ANALYSIS
TEST 3
FEED
5.0
1.2
OXYGEN
Percent
45.8
5.4
0.1
48.8+.1
CHAR
4.6
6.5
84.4
1.7
1.1
6.4
OFF " GAS
NON-
PER-"
OIL
21.1
CONDENSIBLE CENT COMr
COMPONENTS POSITION
60.6
7.7
1.3
30.4
n2
CO
C02
*2
cha
C2H6
C2H4
C3H8
°3H6
33.8
18.2
24.0
12.5
9.5
0.6
0.9
0.1
0.3
HEATING
VALUE
kcal/gm 4.569
7.345
5.728
1.	The CHNO analysis and heating value are based on oil with the
indicated moisture content.
2.	The volatile component of the char probably contains very little
water and is primarily gaseous hydrocarbons.
3.	Note, this is the volume, not the weight composition.
59

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WATER
ASH
ACID
INSOLUBLE
ASH
CARBON
HYDROGEN
NITROGEN
OXYGEN
UNITS
Percent
Percent
Percent
Percent
Percent
Percent
Percent
TABLE B-4
LABORATORY ANALYSIS
TEST 6
FEED
4.6
2.3
47.3
5.7
1.2
45.8
CHAR
2.7
6.5
72.4
1.7
2.9
16.5
OFF - GAS
NON-	PER-3
I CONDENSIBLE CENT COM-
OIL COMPONENTS POSITION
17.9
60.1
8.6
2.4
28.9
N,
CO
co2
=2
ch4
C2H6
C2H4
C3H8
C3H6
41.1
9.8
22.4
18.7
6.7
0.6
0.6
HEATING
VALUE
kcal/gm 4.539
7.550
No Fire
1. The CHNO analysis and heating value are based on oil with the
indicated moisture content.
'2. The volatile component of the char probably contains very little
water and is primarily gaseous hydrocarbons.
3. Note, this is the volume, not the weight composition.
60

-------
WATER
ASH
ACID
INSOLUBLE
ASH
CARBON
HYDROGEN
NITROGEN
OXYGEN
UNITS
Percent
Percent
Percent
Percent
Percent
Percent
Percent
TABLE B-5
LABORATORY ANALYSIS
TEST 7
FEED
4.6
2.3
47.3
5.7
1.2
45.8
CHAR
0.6
9.8
73.6
1.8
2.7
12.1
OFF - GAS
NON-
PER-"
I CONDENSIBLE CENT COM-
OIL COMPONENTS POSITION
16.1
57.6
8.6
6.5
27.3
N2 41.9
CO 24.51
CO--
CH,.
c2h6
<¥4
C3*S
C3H6
8.14
15.07
8.91
0.65
0.78
HEATING
VALUE
kcal/gm 4.539
7.127
5.978
1.	The CHNO analysis and heating value are based on oil with the
Indicated moisture content.
2.	The volatile component of the char probably contains very little
water and is primarily gaseous hydrocarbons.
3.	Note, this is the volume, not the weight composition.
61

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UNITS
WATER	Percent
ASH	Percent
ACID
INSOLUBLE
ASH	Percent
CARBON	Percent
HYDROGEN	Percent
NITROGEN	Percent
OXYGEN	Percent
TABLE B-6
LABORATORY ANALYSIS
TEST 9
FEED
22.3
4.6
1.4
48.3
5.9
1.2
44.6
2
CHAR
0.6
9.8
73.6
1.8
2.7
12.1
OIL
20.3
OFF - GAS
NON-	PER-3
CONDENSIBLE CENT COM-
COMPONENTS POSITION
56.9
8.7
1.1
33.3
N2
CO
co2
H2
CHa
C2H6
C H
2 4
C3fi8
C3H6
45.32
19.89
15.36
6.14
5.67
0.66
0.52
0.13
0.20
HEATING
VALUE
kcal/gm
4.874
6.702
6.582
1.	The CHNO analysis and heating value are based on oil with the
Indicated moisture content.
2.	The volatile component of the char probably contains very little
water and is primarily gaseous hydrocarbons.
3.	Note, this is the volume, not the weight composition.
62

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WATER
ASH
ACID
INSOLUBLE
UNITS
Percent
Percent
TABLE B-7
LABORATORY ANALYSIS
TEST 10
FEED
22.3
4.6
CHAR
1.5
13.6
OFF - GAS
NON-	PER-3
1 CONDENSIBLE CENT COM-
OIL COMPONENTS POSITION
26.1
ASH
Percent
1.4
4.4

co2
h2
ch4
11.31
12.84
4.40
CARBON*
Percent
48.3
74.8
53.6 *
C2H6
0.41
HYDROGEN
Percent
5.9
1.5
9.1
c2h4
0.50
NITROGEN
Percent
1.2
0.8
1.1
C3H8
0.09
OXYGEN
Percent
44.6
10.3
36.2
C3H6
0.18
HEATING
VALUE
kcal/gm
4.873
6.636
6.258


Nr
CO
53.26
17.03
1.	The CHNO analysis and heating value are based on oil having the
Indicated moisture content.
2.	The volatile component of the char probably contains very little
water and is primarily gaseous hydrocarbons.
3.	Note, this is the volume, not the weight composition.
63

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TABLE B-8
LABORATORY ANALYSIS
TEST 11
OFF -GAS
NON-
PER-*
UNITS
FEED
2
CHAR
, CONDENSIBLE CENT COM-
OIL COMPONENTS POSITION
WATER
Percent
22.3
3.2
28.6
N 2
46.98
ASH
Percent
4.6
17.0
-
CO
17.91
ACID
INSOLUBLE
ASH
Percent
1.4


C02
18.18
CARBON
Percent
48.4
77.8
51.5
h2
CH4
C2H6
11.13
4.63
0.41
HYDROGEN
Percent
5.9
1.3
8.9
C H
2 4
0.53
NITROGEN
Percent
1.2
0.8
1.1
c3%
0.09
OXYGEN
Percent
44.6
3.1
38.5
C3H6
0.16
HEATING
VALUE
kcal/gm
4.873
6.596
5.818
tr


1.	The CHNO analysis and heating value are based on oil having the
indicated moisture content.
2.	The volatile component of the char probably contains very little
water and is primarily gaseous hydrocarbons.
3.	Note, this is the volume, not the weight composition.
64

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TABLE B-9
LABORATORY ANALYSIS
TEST 12
OFF " GAS
NON-	PER-3
2	i CONDENSIBLE CENT COM-
UNITS	FEED	CHAR OIL COMPONENTS POSITION
WATER
Percent
22.3
1.2
34.0
n2
46.88
ASH
Percent
4.6
20.1
-
CO
21.86
ACID
INSOLUBLE
ASH
Percent
1.4
-
-
co2
*2
CH4
16.36
8.72
4.84
CARBON
Percent
48.3
77.3 '
47.0
C2H6
0.43
HYDROGEN
Percent
5.9
0.9
8.7
C2H4
0.63
NITROGEN
Percent
1.2
1.1
1.1
C3H8
0.09
OXYGEN .
Percent
44.6
8.9
43.2
C3H6
0.19
HEATING
VALUE
kcal/gm
4.773
6.027
6.117


1. The CHNO analysis and heating value are based on oil having the
indicated moisture content.
2.	The volatile component of the char probably contains very little
water and is primarily gaseous hydrocarbons.
3.	Note, this is the volume, not the weight composition.
65

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TABLE B-10
LABORATORY ANALYSIS
TEST 14
OFF - GAS
NON-

UNITS
FEED
2
CHAR
1 1
OIL
WATER
Percent
6.1
1.2
14.7
ASH
Percent
2.8
7.1
-
ACID
INSOLUBLE
ASH
Percent
0.5
1.0

VOLATILES

-
12.2
-
CARBON
Percent
50.6
78.5
60.0
HYDROGEN
Percent
6.1
1.8
8.2
NITROGEN
Percent
0.7
1.1
1.0
OXYGEN
Percent
42.7
11.5
30.8
HEATING
VALUE
kcal/gm
4.727
6.959
6.281
1. The CHNO analysis and heating value
Indicated moisture content.
are based
n2
CO
COo
H2
CH,,
• C2H6
C2H4
C3H8
C3H6
PER-"
40.3
23.2
19.3
9.84
6.03
1.0
0.1
0.1
2. The volatile component of the char probably contains very little
water and is primarily gaseous hydrocarbons.
Note, this is the volume, not the weight composition.
66

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TABLE B-ll
LABORATORY ANALYSIS
TEST 15
OFF - GAS
NON-
PER-
UNITS
FEED
2
CHAR
1 CONDENSIBLE CENT COM-
OIL
COMPONENTS POSITION
WATER
Percent
6.1
0.9
18.1
n2
47.0
ASH
Percent
2.8
10.2
-
CO
11.1
ACID
INSOLUBLE
ASH
Percent
0.5
3.0

co2
26.1
VOLATILES

-
11.0
-
**2
CH,
4
0.5
3.33
CARBON
Percent
50.6
78.7
56.8 *
C2H6
0.99
HYDROGEN
Percent
6.1
1.4
6.29
c2h4
-
NITROGEN
Percent
0.7
0.7
1.0

0.20
OXYGEN
Percent
42.7
9.1
35.91
C3H6
0.13
HEATING
VALUE
kcal/gm
4.727
6.911
5.817


1.	The CHNO analysis and heating value are based era oil having Che
Indicated moisture content.
2.	The volatile component of the char probably contains very little
water and is primarily gaseous hydrocarbons.
3.	Note, this is the volume, not the weight composition.
67

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APPENDIX C-LISTING OF" DATA REDUCTION
COMPUTER PROGRAM
Presented In this section are listings and sample calculations
illustrating the use of the data analysis computer program.*
To demonstrate the sample computer output; in run number 4 (test 1)
the nominal laboratory CHNO and heating values for the input feed and
products (see Table B-l) are listed below

N2
C
H2
°2
HV
Gas
.485
.191
.021
.303
2704
Char
.025
.751
.026
.089
10950
Feed
.017
.486
.061
.437
8372
Water
.770
0
0
.230
0
From the testing the char yield is 21.7 kg, per 100 kg feed; the
measured amount of air per 100 kg feed is 36.4 kg and the amount of
the moisture is 4.6 kg per 100 kg feed. The energy losses (L) are
estimated at 13,608 kcal (54,000 Btu) for each 45.36 kg (100 lb)
feed (or about 7 percent).
In the computation procedure, which involves an iterative approacn,
initial values for wqo and HVq are chosen and equations 1-8 are solved^
approximately.
Then variations of plus and minus 10 percent of each of the
coefficients in the eight equations are made and the resulting
Note: All calculations within these two programs were made using
the English system of units and conversion to metric units was made
during report preparation.
68

-------
values of each of the eight unknowns are determined. Using these
results the measured versus the computed values of the oil composition
can be compared. The results of- this procedure are presented as part
of the SENSAN OUTPUT.
Comparison of the computed versus the measured oil composition shows
the following results:
Percent	Percent
Element Measured	Computed	Percent Dif.
C .657 .837	+ 27.4
H .071 .0344	- 51.5
0 .242 .185	- 23.6
N	.04	- .056
Not only is the difference between the values for C, H and 0 substan-
tial, but the computed value for N is physically impossible. Clearly,
significant inconsistencies between the measured and the computed
results are present using the nominal values of the coefficients.
From a study of the effect of variations in the values of the co-
efficients on the deviation between the measured and computed oil
composition, it was determined that the carbon content of the char
and the carbon content of the feed have a major influence on the
results. Thus the least squares program made a search for that
combination of Wc^ arid W within bounds of ± 10 percent of the
nominal values, which minimizes the square root of the sum of the
squares of the difference between the computed and measured values of
W . W . W, and W.
co oo no	no
The results of this computation are presented in the ITERAT OUTPUT.
Study of the table shows that the measured versus the computed values
of C, H, N, and 0 for the oil are as follows:
69

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Percent	Percent
Element Measured	Computed	Percent Dif.
C .657	.654	+ .45
H .071	.043	_ 39
0 .242	.268	+ 10.7
N .04 .034	- 15
Thus with the slightly modified values of (+ 6%) and W ^ (+ 4%)
all the results are put into a much better overall agreement than is
possible from the direct computation of the first eight equations
and with only minor variations ia H , M , M , and HV.
3	g' o' w*
70

-------
SENSAN OUTPUT
RUN NIIM°E® i.

N2
C
H2
02
HV
GAS
.ua«;
.111
. C21
.303
2m
CHAR
.325
.7«51
.026
.099
10450
MATER
1
0
.110
. A99
11<»G
FEED
• 017
.<.86
.0«>i
.t»3 7
8372
AIR
• 77G
G
0
• 230
0
OIL INITIAL VALt'tSl
Wf o s
. J<« 1
HtfO a 13713

TOTAL
WEIGHT!
CUA° =
21.7
FESOs 100



AH =
36. <~
MOISTURE® fc.6



ENCPGY
LOSSES5 51*000


HV=H£ATINr, V4U'Jt
HVO=HFATING VALl'C OF THc OIL
KNOsWT. FRAC. OF N2 IS CIL
NOMINAL W( 1 )= .1.85
~ 10'/. OF NCI U( 1 )= .5315
HI* 52. 706 135 26.0201 "W = <.0 .5739 HVO= 1?<.97.7
WCC= .35<»517 WHO = .C1313«. WOO = 8.27837E-2 WNO = V.4<»951E-2
-10r OF N01 U 1 > = .'~365
MG = 6<..557 10' 2<».;<*59 MWs 30.1971 WVO = 15119.W
MCO- .813616 WMC= 5.55865E-2 sOO = .317711 WNO=-.14699U
NOMINAL W< 2 )= .191
~ 107. OF NO.l At 2 J = .>101
MG= 53.0327 10= 25. 3575 .1W = 35.9093 HVO = 13599.9
MCO= .7930-K* WHO2 . G	WOO= .1*<»997 HNO=-l.25098E-2
-10*. OF NOM At Z ) - .1719	•
MG = Si..' 327 MO= 25. "575	= 35.509S HV3 = 1«»867.5
HCO= .330503 UHO= . 0 3<<<«2'i	WOO* .11<»997 WN0=-9.9933&E-2
NOMINAL W( 3 ) = .021
~ 10* OF N01 VI( 3 1 = .0231
MG = 53.C327 11= 25.337" nw = 35.S09A 1V3 = 139<»0.5
WCO= .336796 A'iC = .029b23 AQO- ,12<.9-»7 WNO=-5. 1<»157E-2
-10* Or riOM At 3 >= .Ol«»J
MG = 51.C327 10= 2S.3575 1H = T5.S09S nvo = 1<»525.9
HCO= .136796 WHO= .039235 WGO"= .16<»9'V MNO=-6.lQ277f-2
NOMINAL W ( i, > = .303
~ 1 OX -IF NOM W( c, ) = .3333
MG= 59.0327 10= 25.3575 1W= 35.9098 WVO= 1«.233.7
WCO= .136796 1HO = .DS<*t*29 WOO = .115653 WNO = 1.31222E-2
-10X OP NO.i nt u )= .2727
MG = 51.0327 11= 25.3575 »trf = 35.9091 1V0 = 1U233.7
HCO= • 136796 WHO3 . 0 ikuZl WOO= .25«.3U1 HNO=-. 125566
NOMINAL W( 5 1= 27CU
~ 10X OF NOM W{ 5 >= 2?7«».k
MRs 5A.1393 10= 2*.0938 HM= 37.0667 HVO= 1<.6U0.1
HCO= .179137 *HO= 3.0*h0l£-2 lidO = .15QS2U WNO=-6.13207E-2
-10* OF NC.1 W( = ) = 21.3 J. b
MG= 57.9262 1*3= 26.6165 .1H= 3<». 7572 HVO= 13167.2
MCO= .797977 WHO= 3.7fc<«7at-2 HOO= .2159SS WNO=-5.16229E-2
71

-------
NOMINAL WC * >3 .025
~ lO^C OF 'HM w{ & )' .0275
Hfia 57.9i9u 103 25.3*16 MW* I6.03M HVO3 1<»217.7
HCO3 .337133 WHO8 3.(»07i»JE-2 »00= .142772 MNO = -5.*»029&E-2
-10r OF ?1GM W( 6 1= .32?5
MG3 5t.l'»57 10 3 25.H^= 35.8108 HVO3	7
HCO3 .336<.D* UHC3 .03<»7 8«» WOO* .1372?<, WN03-5. 8<»l6"2E-2
NCMIUAL W( 7 >=• .751
~lOr l)F N31 W( 7 >= . *?%1
HG= 51.0327 .IT- 25.3575 HW» 35.SCJ* HV0= 13301.8
HCO3 .7725^3 WHO3 .03^2'i W00 = .iai.9'37 WNO3 8.0<»603e-3
-10X OF MOM W( 7 )= .6751
MG3 58.0327 MO3 25.3575 MW3 :»5.5Q98 HVO3 15165.6
WCO3 .90lQ6<» WHO3 .03i»U?9 WOO3 .131.917 WNO3-. 12C<»'89
NOMINAL W( 8 >= .026
~iO"1: of mom w( a >3 .02*6
HG® 51.0327 .10= 25.3575 MW = 35.5058 HVO = 1<»093.
HCO3 .336796 WHO3 .0322(K WOO3 .181.997 WM03-5.39967E-2
-10?. OF MOM W( 8 »3 .C23<»
MG3 58.0327 HO3 25.3575 MW3 35.e09d.WVO3 1<»369.<»
WCO3 .136796 WHO3 3.665I9E-2 WOO3 .13«.9<:7 WN03-5.3<.<»67E-2
NCMINAL W ( 9 »3 .0.89
~ 10* OF N0.1 Ut 9 > = .0979
MG3 53.3327 103 25.3575 MW= 35.5i.9P HVG-s 11.233.7
HCO3 • 336796 WHO3 .0.3<«i.29 WOO3 .1>733 WN03-<». 3605<»£-2
-10% OF IIOM W( 9 > = .3801
MG3 53.0327 M33 25.3575 MW3 35.5098 HVO3 K.233.7
HCO3 .836790 WHO3 .03
-------
NOMINAL <«» 13 > = .11
~102 OP MCM w( 13 >= .121
MG= 58.0327 ins 25.3575 MW= 3i.eC98 WVOs 13*05.2
HCO3 .83f>7Jb «H0S 2.0 ltij'JC-2 ^U03 .18*9«7 WN03-*.2&3?6£-2
-102 OF NOP rf( 13 >3 .0«{»
MG = 51.0327 10s 25.257*; MM2 35.3 1G?6
MG= 54.0051 MO= 25.6838 MW = 35.6111 HVO3 1*135.3
HCO3 .82637 rfHO3 3.52935E-2 HCO3 .19?323 WN03-5.U9865E-2
NOMINAL Ml 15 )= .017
~ 102 OF NCM W( 16 ) 3 .0187
KG3 58.3863 MO3 25.313* MVt« 25.5997 HVO3 1*28*.
HCO3 .33558	3.55<»c"C-2 WCO3 .1*198* WNO3-6.3l068E-2
-10"? OF NOM W< 16 ) 3 .0153
MG= S7.67 MO- 25.<*016 MWs 36.22 HVO3 1U183.6
HCO3 .838008 WHO: 3.331S9&-2 WOO3 .17fl03* UNO3-*.93606E-2
NOMINAL W( 17 I: .*36
~ m OF NOM M( 17 )= .5%6
MG= 58.0327 MO3 25.3575 UH» 35.9098 HVO3 17012.8
HCO3 1.02**6 N*Os .0 3*t<~ 2WOO3 .18*997 UNO3-.2*7381
-10?. OF NOM W ( 17 ) 3 .*37*
MG= 58.C327 103 2S.357S MW= 35.5098 HVO3 U-»5*. 7
HCO3 .6= .0671
MG- 58.0327 MO* 25.3575 MW= 35.5098 HVO3 15701.1
HCO3 .336796 WHO3 .05»fc85 HOOs .13*997 WN03-8.02777E-2
-10* OF NOM H( 18 J3 .05*9
MG= 58.0327 HOs 25.3575 MW* 35.5098 HVO* 12766.3
HCO3 .836796 WHO3 .010373 WOO- .18*997 WN03-3.21657F-2
NCPINAL W( 19 )= .*17
~102 OF NOM W{ 19 )® .*807
MG3 58.0327 MO3 25.3575 MW3 35.5098 HVO= 1*233.7
UCOs .836 796 WO3 .03**?9 WOO= .357332 WNO=-.228557
-1C/C OF NOM W< 19 ) 3 .3933
MG= 58.0327 MO= 25.3575 1rf= 35.5098 HVO3 1*233.7
HCO3 .836706 WHO3 ,0J««*2') WOO3 1.26611E-2 WNO= ,11611<»
73

-------
NCMINAL W( 20 >= ^372
~ 10'/. OF MOM rf( 2u > = 9209.2
MG = 5 7.U6 3 8 10 = .51.0-17 «W = 29.7<«92 HVO= I2o08.6
WCO= • 66<*<3-*<* WHC- =~. 1/DO"5C-2 wOO= . 322<»«»7 vno=-3.583!9E-2
-10v. OF NOi W( 20 > = 75l4.il
HG= 58.6C15 10= IS . ?»2 S Vrf = (*2 .0 70 <• HVO* 17032.9
HCO= 1.1332b WHC= 9.eUbk1±-Z WOO=-5 . 176 33E-2 rfN0=-9.13i»36E
NOMINAL W< 21 ) = .77
~ 10^ OF NGM Wf 21 ) = .81.7
MG = 63.673 19 = 2u.6?l MW = 30./96 HVO= 15086.2
MCO= .116189 WHO5 5. 330 32C-c HCO= .3333«9 WNO=-.172831
-1CX OF NOM W( ?i »= .6^3
MG= 52.1923 10= 26.0^ *W= U1.3237 HV3 = 13«»23.7
WCO= .856255 HHC= 1.66061£-2 V>00= 7.31996F-2 WNO=. .053939
NCMINAL W ( 22 1=0
*10" = 0
MG= 58.0327 n = 25.3575 1W = 35.5098 HVO = 1<»233.7
HCO= .836796 WHO = .03«,t»29 WOO = .13<»997 WN0=-5.62217E-2
-10X OF MOM W( 22 )= 0
MG= 58.0"*27 10= 25.3375 MW = 35.909* HVO = 11.233.7
WCO= .336796 WHO= .0 3«t<»?9 WOO = .18*.997 WNO=-5.62217E-2
NOMINAL WC 23 ) = 0
~ 10* OF NOM W( 23 >= 0
MG= 53.0327 MO = 25.3575 MW= 35.909P HVO= H»2»33.7
WCO= .33079& WH3 = .03<»t»29 WOC = .1SI»997 H'JQ = -5.62217E-2
-lO'* OF NOM W( 23 >= 0
MG= 58.U327 >10 = 25.3575 1W = 35.5098 HVO = 1<.233.7
WCO= .83679a WHO= .&3<»U29 HOO= .18«.997 UNO=-5.62217E-2
NCMINAL W( 2h )= .23
~ 10Z OP HOM M( 2<4 )= .253
MG= 58.0327 10 = 25.3575 HW= 35.Su9'i HVO = li»233.7
WCO= .336796 MHU= .03i.<.29 WOO= .21S013 WNO=-8.92376E-2
-10X OF NCK W( 2k > = .207
MG= 58. 0327 10= 25.3575 1W = 35.939" HVO= lt.233.7
HCO= .836796 WHO= .03<»= 0
HG = 58.0327 10= 25.3575 MW= 35.«C9« 4V0= 1<»233.7
WCO= .336796 WHO= .031.U29 HOO= .l?i»997 WNO=-5.62217E-2
-10*/J OF HCM W( 25 >= 0
MG= 58.0327 10= 25.757S MW= 35."=098 HVO= 1W233.7
WCO= .936796 WHO= .03'.<»2q WOO= .1B<»997 WNO=-5.62217E-2
NCMINAL H( 26 >= .0<«1
+ 10*< OF NOH w( Je > = .0U51
MG= 57. 8158 10= 25. ?8<»5 MW= 36.0997 HVO = 1U203.
HCO= .837539 WHO= 3. 3 7<»"
-------
~10*. of ncm wt Z7 > = io3ah.:
Hr,s 51.2«.55 MO= ?2.?39" MWs J*.?l<.6 HVO = 1508/. 1 •
WCO= .9272=>3 WMO= 2.6 C2"iȣ-t wOO = .1127 = 7 WN0=-6. 69311E-2
-10*. OF NCM U( 27 > = 1? IhI . 7
HG= 57.7671 13= Hi.utfA M»i 10 = 23.660<» M^= 35.<.052 HVO = 1<»2«»8.1
WCOa .1276-13 HMO3 3.61315E-2 <00= .20f6»7 WN03-7.31918E-2
-10X OF NOM W< 2? )3 19.53
HG = 53.Qui! 10= 27.05<«6 = 36.<»tHVO = 14221.1
HCO3 .1«»<»76o HHOs 3.2327i£-2 WCO3 .18<.2!7 WNO=-<*.13a36E-2
NOMINAL K( 20 > = 100
~ 10*. OF MOM W< 29 ) = 110
HG= 57.8955 10= 31.1266 MW = 1.0.2779 MVO = 1<»131.2
WCO3 .134681 WH3= 3.23011E-2 «00= .1675«t2 WN03-3.85237E-2
— 10*4 OF MOM rtl ?9 l« 9C
MG = 51.1*9* 10= n.SJd<» MMS 31.51.17 «. r)VO*= 1<*265.6
WCO= .8i»56<»8 WHO= 3.2	*00 = .173825 WNO3-5.23205E-2
NCMINAL W ( 31 ) = <».6
~ 10*. OF NOM *( *1 )= 5.06
MG= 51.0362 .10= 25.315W HW= 36.<.01<« HVO3 lu»«»5.6
WCO3 .138163 WMOa 3 . <«3157£-2 *003 .113905 WNO=-5.63 136E-2
— 10X OF NOM W( *1 ) = it. t +
MG= 51.0291 -10= 25.3997 M-J= 35.1.112 HVO= 14220.9
WCO3 .13543<. WHO= 3.f»5<»Uc-2 HOO= .H608<« WN0=-5.6060!»E-2
NOMINAL W( 32 1 = SuOOC
~ 10*. OF MOM W( 32 )= 591.00
HG = 5 8.069* 10 = 2<.. 923*. MMs 36.3372 4VO= 11.361.7
WC0 = •151049 WHO3 3.32U2HE-2 WOO3 .173513 WNO=-5.79149E-2
-10Z OF NOM W I 32 >= i»1gja
MG3 57.996 10= 25. 7916 "W= 35.5125 HVO= 1<»103.3
HCO3 .822985 H40= 3.557«»2c-2 WC0= .196026 WN0=-5.<»S855E-2
75

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RUN NUMHER <~
HERAT OUTPUT

N2
Q
H2
02
HV
GAS
.<~15
.191
.021-
. 3C 3
27CU
CHAR
.025
.751
.02b
.089
1095?
WATER
0
0
.110
.890
11<»0
FEE3
.017
.U16
• 051
.i»37
<»372
AIR
.770
0
3
.250
0
OIL INITIAL VALUES!
TOTAL WEIGHT!
HEIGHT FRACTIONS OF
ELEMENTS IN OIL:
WNC = .Qi»l	"VO = 13713
C H A 3- ?1.7	FE£0= 100
AIR = 36. 
-------
SENS All LISTING
9	FILE lls-SENSAH"
10	FILE	«^>="Pl;n5••.*fcs,,«U^•6M..110 = ,•RUN10•,.»^'l=,,R|JNll,•
11	PILE	=	=	n7=~RUM7"
12	FILE »19s"?usn"
20 OI*i w(T2>.A(3,3).0(3,3).£(3>.C(3>«R(6>.E(.H((t>.L('.>.i(<»>,HlU)
25	°RINT "VUN #"
26	INPUT N
30 MAT incur #N.K
<~0 PRINT "INITIAL RUN"
50 GOSUB 500
60 print •*mg=,,!P(1) ."ko=":r(2) ,"*w=":r(3) ,"hvo=":h
70 print ••wco=":*m :"who=":m5>,"woo=";r(&),"wno=";w
ao °rint "run?"
90 infut c
100 IF C»0 THiN 999
102	RESTORE JN
103	HAT INPUT HH.kl
105
PRINT
•It".
i"


110
P"INT
#1."
PUN MUHOER-JN

111
PRINT
91


«
112
PRINT
91



113
PRINT
U,"

N2
C H2 02 HV§
11<«
PRINT
#1



115
PRINT
#l.M
GAS
5"
"5w(a»:tt ";m(3i;"
116
PRINT
#1."
CHAP
M: w (&);"
'•:m7>:" -jwtai;" -; w c <3 j: '
117
PRINT
#1."
WATS*
0
s .110 .ago ii<.i
118
PRINT
»1."
FEED
"fw(16>
";w(i7>:" "imiat:'
119
PRINT
«1."
AI-»
.770
0 0 .230 0"
120
PRINT
#1."
OIL INITIAL VALUES 1
UNO =";wt26>5" HVO =":w(27)
121
PRINT
#1."
TOTAL
WE IGHT»
CHAR = ,*;M(28) >"¦ FEE3S" J W(29)
122
PRINT
»1."


AIR =";w<3d> MO IST'JRts" J M { 311
123
ORINT
n,"


ENERGY LOSSES=":W(32»
125
PRINT
91



130
PRINT
~ 1."
HV-MEATING VALUE"."
»
131
PRINT
*1,"
HVUsHEATING VAUU£ OF
THE OIL"
132
PRINT
#1."
HNOaWT
. FRAC. JF N2
IN OIL"
133
PRINT
#1



134
PRINT
11



150
PRINT
"input


160
INJUT
p



170 Ps»*.01
190 FOR I*i TO 32
195 PRINT tfl," NOMINAL Vtt" J 15 ") ='* ;w JI)
200 RESTORE »N
210 MAT IN°'JT *N,M
220 W(11= W{I»fP»W(I)
225 ppint «i," +10% of kom w(";i:")=";wm
230 GOSUB 500
235 GOSUB 300
2<»0 RESTORE JN
2<»5 HAT INPUT «K,W
250	wm=WU! -P*W(I>
251	PRINT #1," -102 OF KOM wCtlS"J s":w(l>
253 GOSUB 503
255	GOSUe 303
256	PR INT
257	PRINT *1
260 NEXT I
265 GO TO 25
i>00 FOR J = 1 TO 10
<~30 GOSUQ 500
(*«t0 W(27»=H
(*50 NEXT J
i»60 RETURN
77

-------
500	A=*(16)*K(21)+w(2i)*«(30>-W(8)»M<28)
eoo c(2) = «<(2n) ~w{.'0)-w(2u mtjn
610 C<3)=W(20>*w<29)-W<32>-W«w(2q)-H(2)*3(i>-H(7)*W(23))/R(2>
670 P.(5)= (X<18) *W(29) ~WU3> *W!31) -W(7)*0( «.) -W
685	W = L-R t e*>-«t:
686	H = { 1<.500«RU) *6Id00»R<5)>
650 RETURN
aoo print «i,~ mg=";r(d;"mo=";r<2);"mw="{R(3);"hvo=";h
810 PrtiNT #i," kco=":s(i») ;"whc = ":p(5) ;"woo=";i<-(6) ;"wno=":h
820 RETURN
999 ENJ
78

-------
ITERAT LISTING
9	file ^is-FrraLur"
10	FILE 9w="9UN|*'*» *5 = "Sti'lv" . *esM3UNb** • # lfl = ":?,JK»10'*» »ll3,"sVJNll", #12-M
11	FILE H 3=HRU'iU"i Uiis'^UMV »*153"'?U^15,*»^15='*PUN^^,,
12	FlLi
20 Oil W(3.E(<»>.H(<.>tLU>t'<(<»).Hl(<»>
25	PRINT "*UN *"
26	INPUT h
27	RESTORc #N
30 Mfl T INrJT »r<,H
<~0 HIT INPUT *N,E
<.1 COSU" 100
<~5 V*l0030uQ
50 <=0
55 PRINT "ENTER I"
60 INPUT S
65 M(KU)=W(SJ
70 W(SJ=.1*W(S)
75 H(K+1>=S
60 PRINJ "M0R£ CHANGES?"
05 INFUT C
90 IF C=0 THEN 105
95 K=K*l
100 GO TO 55
105 (.(1)310
110 L(2)=l0
115 L(3J=10
120 IU>=10
125 FOR L=K*2 TO it
130 L(U=1'
132 HCU=11
135 NEXT L
1U0 FO* L = 1 TO (.(<~>
1<»5 FOR M=1 TO L(3)
150 FOR N=1 TO L(2)
155 FOR 0=1 TO L(1J
160 GOSUS <400
165	IF P(1KJ THEN 2X5
166	IF R<2)<3 THEM 215
167	IF R(i><0 THC.N 215
170	IF RUKO THEN 215
171	IF R15X0 THEN 215
172	IF R(6XC THEN 2i5
173	IF M<0 THEN 215
18 0 Z<»s(Kt<»l-£{l))**2*(R(5l"£(2))**2*(R(6t -£ C 31 » »~ 2 »(W-E *i» 1 ) »*2
185 IF Ztf>V THEN 215
190 tf = Z«»
195 Hi(1J =W (H(l))
200 HI(2)=W (H(2 I)
205 H1(3)=W(H{3)I
210 H1(«.)=W(H(<.)>
215 HtHtl)ISW (H < 1)I*oD2*N(l)
220 NEXT O
225 w(H(li)=.q»f(i)
230 W (H (2))=W(H(2)I~.32*M(2)
235 NEXT N
2«i0 W(H(2)» =.q»M(2J
2<»5 H(H (31 ) =W(H<3> ) *.02«M(3)
250 NEXT M
255 W(H(3)) =.[)»M(?)
260 X(H(I»I ) =H(H(<»M ~ .02*N(<«)
265 NEXT L
270	H (H (<») )
271	T=H1(1) ~Ml<2) »rtl(3) WLUI
272	IF T >0 THEN 2'J5
79

-------
275 PPINT «1." NtGATIVf WEIGHT FRACTION"
280 GO TO 25
295 PRINT #1," INGICES="»"N£K VALUES="
299	FOR 1=1 TO u
300	PR I NT #1,H(	(I)
301	NEXT I
305 W (H (11> =41(1)
310 W(H(2J)=M1(2>
315 M(H(3>I-H1(3)
320 W(H(4>)
325 GOiJUP <*00
330 GO3U0 aiiO
335 GO TO 25
400 FOR J = l TO 10
<•30 G03UB 500
<•<~0 H (2 7) -H
450 N£x T J
<*60 RETUWN
500 A (1. 1 i =W (1)
510 A(1,2»=VH26)
520 A(1.3)=W(111
530 A(2,1)=i
540 A12,2>=1
550 A(2,3»=l
560 A(3,l>-wr 5)
570 A<3,2>=W<27>
580 A(3.3>= >M15>
590 CCl>=W(lo)',W(29) ~W(21) *W(30>-W(6> »W(2 9J
600 C(2)sM(29»fW(J0)-w(28)+W(3l)
610 C( J)=W(20)*W(2<))-H(T2) -W{10)*W(2a)
620 KHT Q=INV(A»
630 MAT B=Q*C
6s2(2>
642
650 X=W(19)*W(29J*W(i4>»W(3l)
660 «{«.)s(H(17) »rf(29) -W(2)	-W (7) •W(2») ) /R(2)
670 R(5)=(W(H)»W(2?) fW<13) *U(31) -W ( 3) »R (1)-W ( 3) *W (2 9) -W )/9(2)
660 R(o)3(X*M(2<») »ri(30) -W(<*><»fl(l) -U(9) •W(2a)-rf(14) *Rm >/R<2)
685 W=i-R(4)-R(5J-R(5)
6*6 H=< 1<»50C*9(4> vol000*R(5>)
690
RETURN



800
PR TNT
31,"
masses:
GAS ="
;r(1) ,"«oisTiJRi=":R (3)
802
PRINT
91,"

OIL ="
;r(2)."hsating value in cil=":h
804
PRINT
#1."
WilGHT FRACTIONS
M

805
PRINT
01."
OF ELEMENTS IN OlL« CAR30N
=";R(4),"HY0R0GEN=";R(5>
806
PRINT
»1."

OXYGEN
=";r(6»,"nitrogen=":w
820
RETURN



900
PRINT
»1,"1
tl


901
PRINT
fll."
RUN NUK9ERJ";s


902
PRINT
«1



907
PRINT
ffl



910
PRINT
#1."
N2
C
H2 02 HV"
911
PRINT
91



912
PRIHT
n,"
GA3 "tWd):"
••:w(2)
":w(3>:" ~; w 11»»; ":w
913
PRINT
n."
char -;w t ej ;"
"sum
-;w(8):" ";w
914
PRINT
U,"
WATER 0
0
.110 .890 1140"
915
PRINT
*i,"
FEED MJW(16):"
";w
M:wci8);" ":n(i9»;"
916
PRINT
#i,"
AIR .770
0
0 .230 0"
917
PRINT
01



918
PRINT
«1,"
OIL INITIAL 1/ALUESt
HNO ="?W(26>;" MVO =":W<27>
920
PRINT
#1."
TOTAL MCIGHTt
CHAR=";w(28) FEE0=";w(29)
922
PRINT
SI,"

air =-;w{jo»:" koisture=m:h(3u
923
PRINT
«1»"

ENERGY L0S5ES=":m(32)
80

-------
925	PRIM
926	°RINT
92« PRINT
930- PRINT
932 PRINT
93«. PRIM
9<»0 RETURN
999ENO
WEIGHT FRACTIONS OF"
¦ ELEMENTS lb. CILI CflRSON = ";e (U 5"	HY C*OGt N = " !Z 12)
oxrGtK="; = (3);"	mtrogen=":e ii»>
CALCULATEO VALUES ARE AS FOLLOWS! "
81

-------