U.S. Environmental Protection Agency Industrial Environmental Research
Office of Research and Development Laboratory
Research Triangle Park, N.C. 27711
MECHANISM AND KINETICS OF
THE FORMATION OF NOX
AND OTHER
COMBUSTION POLLUTANTS:
Phase I. Unmodified Combustion
Interagency
Energy-Environment
Research and Development
Program Report
-------
RESEARCH REPORTING SERIES
Research reports of the Office of Research and Development, U.S.
Environmental Protection Agency, have been grouped into seven series.
These seven broad categories were established to facilitate further
development and application of environmental technology. Elimination
of traditional grouping was consciously planned to foster technology
transfer and a maximum interface in related fields. The seven series
are:
1. Environmental Health Effects Research
2. Environmental Protection Technology
3. Ecological Research
4. Environmental Monitoring
5. Socioeconomic Environmental Studies
6. Scientific and Technical Assessment Reports (STAR)
7. Interagency Energy-Environment Research and Development
This report has been assigned to the INTERAGENCY ENERGY-ENVIRONMENT
RESEARCH AND DEVELOPMENT series. Reports in this series result from
the effort funded under the 17-agency Federal Energy/Environment
Research and Development Program. These studies relate to EPA's
mission to protect the public health and welfare from adverse effects
of pollutants associated with energy systems. The goal of the Program
is to assure the rapid development of domestic energy supplies in an
environmentally—compatible manner by providing the necessary
environmental data and control technology. Investigations include
analyses of the transport of energy-related pollutants and their health
and ecological effects; assessments of, and development of, control
technologies for energy systems; and integrated assessments of a wide
range of energy-related environmental issues.
REVIEW NOTICE
This report has been reviewed by the participating Federal
Agencies, and approved for publication. Approval does not
signify that the contents necessarily reflect the views and
policies of the Government, nor does mention of trade names
or commercial products constitute endorsement or recommen-
dation for use.
This document is available to the public through the National Technical
Information Service, Springfield, Virginia 22161.
-------
EPA- 600/7- 76- 009a
August 1976
MECHANISM AND KINETICS
OF THE FORMATION OF NO
X
AND OTHER COMBUSTION POLLUTANTS
PHASE I. UNMODIFIED COMBUSTION
by
V.S. Engleman and W. Bartok
Exxon Research and Engineering Company
P. O. Box 8
Linden, New Jersey 07036
Contract No. 68-02-0224
ROAPNo. 21BCC-013
Program Element No. 1AB014
EPA Project Officer: W. Steven Lanier
Industrial Environmental Research Laboratory
Office of Energy, Minerals, and Industry
Research Triangle Park, NC 27711
Prepared for
U.S. ENVIRONMENTAL PROTECTION AGENCY
Office of Research and Development
Washington, DC 20460
-------
TABLE OF CONTENTS
Page
FOREWORD i
SUMMARY 1
1. INTRODUCTION 2
2. EXPERIMENTAL PROCEDURES AND RESULTS 3
2.1 Jet-Stirred Combustor 3
2.2 The Multiburner 16
2.2.1 The Multiburner Furnace 16
2.2.2 Burner Design 18
2.2.3 Sampling and Gas Analysis 22
2.2.4 Data Reduction 22
2.2.5 Results for Premixed Flames . 27
2.2.6 Results for Diffusion Flames ,- . . . . 31
3. THEORETICAL CALCULATIONS . 37
3.1 Equilibrium Calculations on Premixed Flames . 37
3.2 Survey of Coupled NO /Combustion Kinetics 37
X
3.3 Kinetics Calculations 44
3.4 Results of Theoretical Calculations for Methane/Air .... 61
3.4.1 80% Stoichiometric Air 61
3.4.2 100% Stoichiometric Air 62
3.4.3 120% Stoichiometric Air 66
3.5 Discussion 66
3.6 Reactions of Importance at the Interface Between the
Branching Zone and the Relaxation Zone 69
3.7 Comparison of Theoretical Calculations with
Experimental Results 72
4. CONCLUSIONS 74
APPENDIX A - MASTER LIST OF REACTIONS FOR 25 ALLOWED SPECIES .... A-l
APPENDIX B - CROSS INDEX OF REACTIONS FOR 25 SPECIES B-l
APPENDIX C - KINETIC DATA ANALYSIS FOR JET-STIRRED COMBUSTOR .... C-l
APPENDIX D - NO/NO PLOTS D-l
X
APPENDIX E - CO/C02/HC/02 DATA PLOTS E-l
APPENDIX F - DATA LISTINGS F-l
-------
- 1 -
FOREWORD
This report summarizes the results of Phase I of a study on
the "Definition of the Mechanism and Kinetics of the Formation of NOX
and Other Pollutants under Normal and Combustion Modification Conditions".
This study was conducted by Exxon Research and Engineering Company under
Contract 68-02-0224 funded by the Environmental Protection Agency.
The helpful comments and suggestions of Messrs. W. S. Lanier,
G. B. Martin, and D. W. Pershing, project officers for this contract,
are gratefully acknowledged. The skillful assistance of Messrs. F. D. Remyn
and R. M. Buono in conducting the laboratory portion of this program is
also acknowledged.
-------
- 1 -
SUMMARY
The objective of this study was to investigate the mechanism
and kinetics of the formation of NOX and other pollutants in combustion.
A combined experimental and theoretical study was undertaken for this
purpose. This report covers Phase I, the study of combustion under
unmodified conditions and calculations using the best available kinetic
data from the literature.
A jet-stirred combustor was used to extend the range and accuracy
of data taken in previous studies. Since precise measurements of
concentrations and temperatures are critical to allow meaningful results
in combustion calculations for a well-stirred reactor, additional studies
on the combustion of hydrogen, carbon monoxide, methane, and propane
with air were made. These studies of coupled combustion/pollutant
formation indicated substantial heat loss from a conventional stirred
reactor and the need for the development of an adiabatic stirred combustor.
A furnace capable of studying combustion under adiabatic
conditions (called the multiburner because it was designed for multifuel
firing capability in the same combustion zone) was further refined for
these studies. This unit is an electrically-heated furnace with a
zirconia muffle tube that is capable of attaining temperatures up to
about 2500°K. Premixed flames of the flat-flame and focused-flame type
as well as laminar and turbulent diffusion flames were studies using
methane and propane as fuels. These studies included both adiabatic
and heat-loss conditions. In addition, a few runs were made with wall
temperatures above the adiabatic flame temperatures.
Both stirred reactor and plug flow calculations were made.
Stirred reactor calculations indicated the need for more detailed
kinetics in hydrocarbon-air combustion for the prediction of NOX formation.
Plug flow calculations (with kinetic data available from the literature
at the time) indicated strong coupling between combustion reactions and
NOX formation in the flame zone. However, since no reaction rate data
were available to test the direct coupling between hydrocarbon fragments
and nitrogenous species, further elucidation of the kinetics is required
to determine the importance of such reactions for NOX formation.
-------
- 2 -
1. INTRODUCTION
Under Contract No. 68-02-0224, sponsored by the Environmental
Protection Agency, Exxon Research and Engineering Company conducted a
study to relate the kinetics and mechanism of pollutant formation reactions
and those of hydrocarbon reactions. The emphasis in this program was
placed on NOX formation and destruction reactions as they relate to
hydrocarbon combustion. This program was performed in two phases. This
report covers the work in Phase I which included studies of unmodified
combustion in a non-adiabatic stirred combustor and a plug flow combustor
capable of adiabatic operation. Preliminary kinetics calculations based
on the most complete kinetic data available from the literature at the
time were also conducted in Phase I. Phase II, which is covered in a
companion report, included experimental studies of modified combustion in
a plug flow system as well as studies in a newly developed adiabatic
stirred combustor. Kinetics calculations, using updated literature
information as well as estimates for potentially important reactions not
available from the literature, were also performed.
The purpose of these studies was to provide further understanding
of the coupling between combustion reactions and pollutant formation (with
emphasis on NOX) leading to the capability to perform accurate predictive
calculations on complex combustion systems. The ultimate aim of this and
other fundamental combustion research studies being conducted for the
Combustion Research Branch of the Industrial Environmental Research
Laboratory of EPA is developed control technology for stationary sources.
Clearly, in a practical system, there will be interactions
among chemistry, fluid mechanics and heat transfer. However, without
an understanding of the basic chemistry of combustion, agreement between
theory and experiment in a particular case may be fortuitous and will not
allow application of the same theory to a new system. Thus, the theory
becomes merely an empirical correlation. These studies on the chemistry
of combustion/pollutant formation were therefore undertaken, in order to
progress towards a theory of general applicability to a wide variety of
combustion systems. These studies were oriented toward studying combustion
under idealized conditions, either controlled by chemical kinetics or
with minimum, or well-defined fluid mechanic and heat transfer interactions.
-------
- 3 -
2. EXPERIMENTAL PROCEDURES AND RESULTS
Two experimental devices were used In the experimental portion
of this study: (1) the jet-stirred combustor—non-adiabatic stirred
reactor capable of operating under kinetically-limited combustion conditions
and (2) the multiburner—plug flow reactor, with interchangeable burners,
capable of operating under adiabatic conditions. This section covers the
experimental portion of the study, while the theoretical considerations
will be discussed in the following section.
2.1 Jet-Stirred Combustor
The jet-stirred combustor used in this program is a modification
of the Longwell-Weiss reactor (2-1) with hemispherical geometry. This
device was selected because it has been used extensively in fluid mechanic
and combustion modeling and because the combustion rates are limited by
chemical kinetics as opposed to transport effects (2-2) . The apparatus
used was described in the Final Report for the preceding program (conducted
under Contract No. CPA 70-90, Reference 2-3) whose purpose was to investigate
the basic factors affecting nitric oxide formation in the combustion of
fossil fuels. The reactor (Figure 2-1) consists of an outer shell of
fire-brick shaped as two halves of a sphere three inches in diameter.
The upper hemisphere is solid with the exception of the hole through which
the reactants are brought to the injector. The lower hemisphere is
hollowed out to a reaction zone of 1.5 inch diameter. The insulating
shell has twenty-five holes of 0.125 inch diameter, through which the
burned mixture exits.
Fuel and air are metered separately through calibrated rotameters,
preheated to the desired inlet temperature and then mixed before entering
the combustor. The temperature of the fuel/air stream is measured
immediately before injection. The fuel-air mixture enters the reaction
zone through a stainless steel injector which is a hemisphere into which
are drilled forty radial holes of 0.020 inch diameter. The reactants
enter the reaction zone as small sonic jets which stir the reactor
contents and produce a mixture of essentially uniform temperature and
composition in a characteristic time which is short compared with the
average residence time. The combustion experiments were conducted at
atmospheric pressure with a range of residence times from 1-1/2 to 4
milliseconds.
2-1 Longwell, J. P. and Weiss, M. A., Ind. Eng. Chem. 47, 1634 (1955).
2-2 Hottel, H. C., Williams, G. C., and Miles, G- A., Eleventh Symposium
(International) on Combustion, p. 771, The Combustion Institute, 1967.
2-3 Bartok, W., Engleman, V. S., and del Valle, E. G., Laboratory Studies
and Mathematical Modeling of NOX Formation in Combustion Processes,
Final Report EPA Contract CPA 70-90, December 1971.
-------
- 4 -
FIGURE 2-1
SCHEMATIC OF THE JET-STIRRED COMBUSTOR
INCONEL SPHERE
FIRE BRICK
INJECTOR
THERMOCOUPLE
PRE-MIXED AIR AND
FUEL INLET
FIRE-BRICK
WATER-COOLED PROBE
-------
- 5 -
Gas temperatures were measured up to temperatures slightly in
excess of 2000°K with a Pt/Pt-10% Rh thermocouple 0.010 inches diameter.
Radiation corrections were found to be negligible because of the intense
stirring in the combustion zone (see Appendix C). Duplicate runs were
made with silica coated and uncoated thermocouples in selected cases to
check for catalytic effects on temperature measurements. No measurable
differences were found. The thermocouple was movable so that traverses
could be taken during a run. It was found that the temperatures were
quite uniform throughout the reaction zone although slightly cooler in
the immediate vicinity of the injector sphere and in the immediate
vicinity of the outer wall when the thermocouple was drawn back into its
port.
The combustion gases were sampled through a water-cooled
stainless steel probe, 0.125 inches outside diameter and 0.033 inches
inside diameter similar to that used by Longwell and Weiss (2-1). The
probe was placed through a port in the shell of the combustor. The
quenched gases were pumped through a diaphragm pump to the combustion
gas analyzers. The most important species analysis in this study was
the measurement of NOX concentrations. During the preceding program
(CPA 70-90, Reference 2-3) these analyses were performed primarily with
the Envirometrics Multigas Analyzer although cross-checks were made with
the DuPont Photometric NOX analyzer. During the present program
(68-02-0224) a Thermo Electron Chemiluminescence Analyzer was used and
the results of both programs served as cross-checks of the data. Care
had to be taken when using the Envirometrics analyzer in the presence
of CO, although since the response time to CO is slower than the response
time to NOX, CO concentrations of up to 5-10% could be handled with
minimum interference by cyclic sampling/purge techniques which took
advantage of the different response times for NOX and for CO.
The hydrogen was Linde extra dry grade with a stated minimum
purity of 99.95%, the carbon monoxide was Matheson C.P. grade with a
stated minimum purity of 99.5% and the propane was Matheson C.P. grade
with a stated minimum purity of 99.0%. The air was Baker dry grade
manufactured by mixing nitrogen and oxygen with a typical argon concentration
of 450 ppm. The oxygen concentration of each cylinder was measured and
was generally found to be 21.0%.
Precise experimental measurements of concentrations and temperature
are extremely critical for achieving meaningful results in combustion
calculations for a well-stirred reactor. To assure the precise nature
of the measurements made in the preceding program (reference 2-3) and
to extend those measurements to include those parameters necessary for
kinetic calculations for the assessment of the importance of combustion
intermediates in coupled combustion/pollutant formation, further studies
were made with the jet-stirred combustor for hydrogen, carbon monoxide,
methane, and propane.
Temperature measurements for methane/air combustion are shown
in Figures 2-2 and 2-3. Figure 2-2 shows temperature vs. mixture ratio
with the solid line being the same one indicated in reference 2-3. The
dotted line is the extension of this line to fuel-rich conditions with
the peak indicated at about 90% stoichiometric air. In reference 2-3
temperature measurements were taken only under fuel lean conditions at
these flow rates. An indication of the temperature uniformity within the
-------
- 6 -
FIGURE 2-2
TEMPERATURE AS A FUNCTION OF MIXTURE RATIO
JET-STIRRED COMBUSTOR / METHANE - AIR
H
W
W
2000
1900
1800
1700
1600
50
O
FROM REFERENCE 2-3
J L
100
PERCENT STOICHIOMETRIC AIR
150
FIGURE 2-3
TEMPERATURE PROFILES AT REPRESENTATIVE STOICHIOMETRIES
JET-STIRRED COMBUSTOR / METHANE - AIR
EH
<
tf
2000
1900
1800
1700
1600
.0--° O O
0
a
•a
.A.. A.
0.25
0.50
M
Vo,
0.75
% ST AIR
73
123
n
'[]
65
141
163
1.00
1.25
-------
- 7 -
jet-stirred combustor with methane is given in Figure 2-3. Temperature
is plotted against (r/Ro)3} a normalized volumetric parameter, indicating
the portion of the reactor volume at a given temperature. It can be
seen that the temperatures are quite uniform throughout the combustor.
Near the injector sphere the temperature apparently drops off but this
is probably caused by a combination of convective cooling by the cool
inlet jets in the vicinity of the injector sphere and radiative cooling
of the thermocouple bead by the injector sphere. The temperatures used
for kinetics calculations are indicated by the horizontal dashed lines.
The NOX emissions from the jet-stirred combustor with methane/air
are indicated in Figure 2-4. It should be noted that peak NQx formation
occurs under slightly fuel-rich conditions. These data were measured
with a Thermo-electron NO/NCx chemiluminescence analyzer and are in very
good agreement with the results obtained in reference 2-3 using Envirometrics
electrochemical analyzers and a DuPont photometric analyzer.
The oxygen results were obtained with a polarographic oxygen
analyzer. They are shown in Figure 2-5 and compare favorably with those
reported in reference 2-3 which were taken with a paramagnetic oxygen
analyzer. The results are in good agreement with calculated values of
residual oxygen in a well-stirred combustor.
The effect of the water-cooled sampling probe on the temperature
of the jet-stirred combustor is dramatic if species probe traverses are
attempted. As long as the probe is outside the volume of the reactor
(up to a position flush with the wall) the temperature in the reactor
remains fairly constant. As the probe enters the reaction zone, the
temperature begins to drop, and it drops more than 100 K by the time
the probe is three fourths of the way to the center of the reactor. This
is illustrated in Figure 2-6 for which the uncooled thermocouple probe
was held in a fixed position while the cooled species sampling probe was
inserted into the reactor.
Temperature measurements for carbon monoxide/air combustion are
shown in Figures 2-7 and 2-8. Figure 2-7 shows temperature vs. mixture
ratio with the solid line being the one calculated on a theoretical
basis as indicated in the paper presented at the Fourteenth Combustion
Symposium and shown in Appendix C. The data have been extended on the
fuel rich side beyond the data available at the time of writing the
Combustion Symposium papert The temperature uniformity in the combustion
zone for carbon monoxide air is also good as indicated in Figure 2-8.
The temperatures used for kinetics calculations are indicated by the
horizontal dashed lines.
The NOX emissions for CO/air are shown in Figure 2-9 and were taken
with a chemiluminescence analyzer. The agreement with the results reported
in reference 2-3 is quite good on the lean side. There is some disagreement
under fuel rich conditions between 50 and 65% stoichiometric air but
the present results should be considered more reliable because the CO
content in the exhaust exceeds 10%. That high a concentration is difficult
to eliminate as an interference with the NOX Paristor (even with the
special cyclic sampling techniques developed (2-3)) when the NOX level
is below 50 ppm; the chemiluminescent analyzer does not have such a CO
interference.
-------
FIGURE 2-4
w
<
W
ra
§
x
O
OS
W
O
O
75
50
25
10
50
NO AS A FUNCTION OF MIXTURE RATIO
JET-lTIRRED COMBUSTOR / METHANE - AIR
O
O
O
6
50 100 150
PERCENT STOICHIOMETRIC AIR
FIGURE 2-5
OXYGEN AS A FUNCTION OF MIXTURE RATIO
JET-STIRRED COMBUSTOR / METHANE - AIR
u
O
o .o Q"°. I
1 - 1 _ 1 _ 1
100 150
PERCENT STOICHIOMETRIC AIR
-------
- 9 -
FIGURE 2-6
EFFECT OF WATER-COOLED SAMPLING PROBE POSITION
ON JET-STIRRED COMBUSTOR TEMPERATURE
o
EH
S
O
o
w
EH
W
w
H
1800
1700
1600
EXHAUST PORTS
COMBUSTOR—*-
_-o o
THERMOCOUPLE MAINTAINED
IN FIXED POSITION AT
r/fe0 = l.,00 ,
'NORMAL
[SAMPLING
POSITION
INJECTOR »
250
200
150
100
50
0
COOLED PROBE POSITION
(ARBITRARY UNITS)
-------
- 10 -
FIGURE 2-7
TEMPERATURE AS A FUNCTION OF MIXTURE RATIO
JET-STIRRED COMBUSTOR / CARBON MONOXIDE - AIR
w
EH
2100
200(_
1900
180C-
1700-
CALCULATED TEMPERA
TURE (SEE APPENDIX C)
1 1 1 1
1 1 1 1
I 1
50 100 150
PERCENT STOICHIOMETRIC AIR
FIGURE 2-8
TEMPERATURE PROFILES IN JET-STIRRED AT
REPRESENTATIVE STOICHIOMETRIES COMBUSTOR / CARBON MONOXIDE - AIR
O
O
m
tf
W
2100
2000
1900
1800
1700
si-
j
•3
A
D i
n ~
/•o--0 ° o c
o'
0'
1 1 1
PERCENT
STOICHIO-
METRIC
AIR
» 117
J 53
1^.
)^ 142
0 0.25 0.50 0.75 1.00 1.25
, ^ 3
-------
AS MEASURED
PH
&
NO
X
OXYGEN (PERCENT
co
01
o
o
-^
01
^
O
M
01
- 11 -
FIGURE 2-9
NOX AS A FUNCTION OF MIXTURE RATIO
JET-STIRRED COMBUSTOR / CARBON MONOXIDE - AIR
f
o
1
50
100 150
PERCENT STOICHIOMETRIC AIR
FIGURE 2-10
OXYGEN AS A FUNCTION OF MIXTURE RATIO
JET-STIRRED COMBUSTOR / CARBON MONOXIDE - AIR
10
- O EXPERIMENTAL
THEORETICAL (SEE APPENDIX
50
100 150
PERCENT STOICHIOMETRIC AIR
-------
- 12 -
The oxygen concentration is shown In Figure 2-10 and is in
good agreement with theoretical calculations indicated by the solid line.
Careful temperature probing of the reaction zone was accomplished
and a study of the effect of preheat on NOX formation was undertaken for
propane. Data were also taken with hydrogen fuel for better characterization
of the flame temperature vs. mixture ratio for this system in the jet-stirred
combustor, and to obtain more accurate NOX measurements under extremely lean
and extremely rich conditions.
The NOX measurements for the propane-air system are presented
in Figure 2-11. The agreement with data taken previously is good in the
case of no preheat. The NOX peak appears to occur on the slightly
fuel-rich size (at about 90% stoichiometric air).
The results for preheat in Figure 2-11 indicate only a slight
effect on NOX formation. However, temperature measurements show that
only at 150% stoichiometric air conditions did the combustion temperature
reflect fully the nominal amount of preheat. At 135% stoichiometric
air the difference in combustion temperatures was only half of the
preheat and there was no difference in combustion temperatures under fuel
rich conditions. This lack of recovery of prehat temperature in the
combustion zone is directionally consistent with adiabatic equilibrium
calculations in which higher preheat causes dissociation at high temperatures
and some of the sensible heat is converted to latent heat. At 150%
stoichiometric air the difference of about 100°C in combustion temperature
results in a NOX increase by more than a factor of two. This behavior
is in line with theoretical predictions of well-stirred reactor performance.
Temperature and oxygen measurements for the propane/air system
are shown in Figure 2-12. The difference between theoretical adiabatic
well-stirred reactor temperatures and experimentally increased temperatures
indicates a heat loss on the order of 30-40 cal./sec. over the conditions
studied. The measured oxygen concentrations match the calculated oxygen
concentrations for a well-stirred reactor operating at the measured
temperatures.
Probing of combustor temperature profiles showed that temperatures
were quite uniform in the jet-stirred combustor for propane-air. The
temperatures are plotted in Figure 2-13 against (r/Ro)3. As discussed
before, this parameter represents the fraction of total volume in a
given zone of the combustor. The temperatures were found to be quite
uniform throughout the combustor from the vicinity of the injector to
within a short distance of the wall. Temperature probing was performed
both with bare metal thermocouples and with thermocouples coated with
silica. Because of the intense stirring and the apparent lack of catalytic
effects on the thermocouples under the conditions studied, no difference
was observed between the measurements obtained with coated and uncoated
thermocouples.
Measurements were also made in the hydrogen-air system. The
measurements were made under fuel-rich conditions around 40% stoichiometric
air and under fuel lean conditions between 140% and 250% stoichiometric
air. The chemiluminescence analyzer permits more accurate analysis of
combustion gases at low NOX levels than we were able to achieve during
the previous investigation (2-3) which employed Envirometrics electro-
chemical analyzers.
-------
- 13 -
FIGURE 2-11
N<> FORMATION IN JET-STIRRED COMBUSTOR (PROPANE/AIR)
'••
X
Q
W
B
03
<
W
X
150
100
50''li.
O1,
-\Q
I- NEAR
BLOWOUT
k/
- NO PREHEAT
D - "WITH PRE-
HEAT
(SEE TEXT).
50
100
150
PERCENT STOICHIOMETRIC AIR
-------
- 14 -
FIGURE 2-12
TEMPERATURE AND OXYGEN LEVELS
PROPANE - AIR
w
E-i
W
W
H
2200 L
2100 L-
2000 I—
1900 (-
ADIABATI
WELL-ST
REACTOR
EXPERIMENTAL
100 150
PERCENT STOICHIOMETRIC AIR
-------
15 -
FIGURE 2-13
TEMPERATURE PROFILES IN JET-STIRRED COMBUSTOR
PROPANE - AIR
U
o
tt
o
H
— «-n — -D-— --Q ~ -n
j
B ^
-o
^. ••._-•_„-.•.. —
* 1 1 1
% ST AIR
nc
95
^ 120
1
60
150
0
0.25
0.50
0.75
1.00
1.25
-------
- 16 -
Calculations were performed to show that the jet-stirred
combustor operates as a well-stirred reactor for "clean" combustion
systems (hydrogen and carbon monoxide) and calculations have been performed
on propane to test a quasi-global combustion model for calculations of
NOX formation. The results (2-4) of this study are reported in Appendix C.
The calculations have been valuable to our current program to point out
critical areas for experimentation and further kinetic studies. As
discussed in detail in Appendix C, the theoretical analysis based on a
simplified quasi-global approach failed to produce predicted NOX
concentrations in agreement with the experimental results for the
propane/air system. This lack of agreement was particularly pronounced
under fuel-rich conditions. Therefore, it was concluded that the
investigation should be broadened to a detailed treatment of the kinetic
data and also, that further experimental results should be obtained under
conditions which eliminated heat loss as well as mixing limitations for
comparison in theoretical predictions.
2.2 The Multiburner
Studies in the multiburner were undertaken to allow investigation
of combustion reactions with well-controlled heat loss. The multiburner
was operated as a flow reactor for this portion of this study with both
hot and cold walls. The multiburner studies conducted indicated the
need for the development of a new combustor capable of behavior as a
well-stirred reactor under adiabatic conditions. These complementary
studies with stirred reactors and flow reactors provide data on a range
of conditions from well-mixed combustion controlled by chemical kinetics
to diffusion flames controlled by fluid mechanics.
2.2.1 The Multiburner Furnace
The multiburner (so-called because it was designed to burn gas,
oil or coal in the same idealized combustion zone) is an electrically-
heated furnace with a zirconia muffle tube that is capable of attaining
temperatures up to about 2500°K. The furnace is shown schematically in
Figure 2-14. The furnace heating zone has tungsten mesh heating elements
and molybdenum radiation shields and is purged with gettered argon to
extend furnace component lifetimes. High temperature gasketing for the
furnace is composed of zirconia felt. Temperatures inside the furnace
are monitored with tungsten-rhenium thermocouples which also serve as
the input to the temperature controller for the furnace when operating
in the automatic mode. Wall temperatures can also be monitored by optical
pyrometry through three sight ports provided in the side of the furnace.
The power supply is a 25 KVA AC unit which is also equipped with a thermal
watt converter for input to the controller in cases where it is desirable
to control power input rather than strictly the temperature of the furnace.
The controller on the power supply is also capable of operating in a
"manual" mode, in which case current input to the furnace is controlled.
2-4 Engleman, V. S., Bartok, W., Longwell, J. P., and Edelman, R. B.,
Fourteenth Symposium (International) on Combustion, p. 755, The
Combustion Institute, 1973.
-------
FIGURE" 2-14
MULTIBURNER FURNACE
SEAL
SEAL
MOLYBDENUM
RADIATION
SHIELDS
WATER-
COOLED
JACKET
TUNGSTEN-
HEATING
ELEMENT
STABILIZED
ZIRCONIA
MUFFLE TUBE
-------
- 18 -
The muffle tube in the furnace has a heated length of 15
inches and the "constant temperature section" of the heated zone is
uniform within + 10°C under combustion operation conditions. The muffle
tube is quite stable at high temperatures and can be exposed to varying
thermal environments in the temperature range above 1300°C. However,
extreme care must be exercised in heating up and cooling down the furnace
since the zirconia is most sensitive to thermal shock in the temperature
range around 900°C.
The multiburner can be operated with the combustion zone wall
temperature at any desired level and at the extremes it can either be
used to add heat to the combustion zone or, if desired, to remove heat.
Thus, the multiburner can operate- with all of the flexibility of a
laboratory combustor without the high heat loss generally found in
small scale devices. This permits the use of the multiburner under
combustion conditions that would not be possible with the typical
small scale combustor.
2.2.2 Burner Design
The burners used in this part of the study were designed to
be simple examples of the following types of burners:
• premixed flat flame
• premixed focused flame
• diffusion flame - with interchangeable fuel nozzles
The simple design of each of these burners (shown in Figures 2-15, 16
and 17) was aimed at ease of comparison with analytical calculations.
Each of the burners was readily interchangeable with the others because
they were all built into the same size water jacket, which served to
maintain constant burner temperatures during combustion experiments.
Even though the burners produced three different basic flame types,
the total burner face area, through which combustion gases pass, was
maintained constant for all three types.
The flat flame burner has a porous stainless steel disc across
its face which provides a flat velocity profile for the combustion gases
entering the furnace. The gases are mixed immediately before entering
the burner body and pass through a pair of mixing/calming plates before
exiting through the porous disc. A diagram of the flat flame burner
is given in Figure 2-15.
The premixed focused flame burner used in this study is char-
acteristic of a commercial gas furnace burner; the burner has a single
center hole and eight pilot holes to stabilize the flame. As in the
flat flame burner, the fuel and air are mixed immediately before entering
the burner body and pass through mixing plates before exiting from the
burner face. A diagram of the premixed focused flame is given in
Figure 2-16.
-------
_ 1 Q _
FIGURE 2-15
FLAT FLAME BURNER
POROUS S.S. DISC
WATER-COOLED
TUBE
FLOW STRAIGHTENERS
WATER-COOLING JACKET
GAS FLOW CHA
WATER INLET
PREMEXED
GAS INLET
WATER OUTLET
WATER INLET
-------
- 20 -
FIGURE 2-16
PREMKED FOCUSED FLAME BURNER
FLAME ARRESTOR
WATER COOLING JACKET
GAS FLOW CHANNEL
WATER INLET
FLAME ARRESTOR
PREMIXED GAS
UNIT
-------
- 21 -
FIGURE 2-17
DIFFUSION FLAME BURNER
FLOW STRAIGHTENERS
WATER COOLING JACKET
WATER INLET
AIR INLET
\
FUEL INLET
-------
— 22 —
The diffusion flame burner is of the concentric type with the
fuel flowing through the inner tube and the air flowing through the outer
one. Two types of fuel injector were tested; one with a single fuel
jet and the other with an orifice plate containing six 0.020 inch
diameter holes covering the fuel jet to produce turbulence and increase
mixing. The latter, called the "stabilized" diffusion burner was found
to give better performance. The single fuel jet burner was tested in
two different configurations; one in which the fuel jet diameter was
kept constant when changing fuels from methane to propane allowing the
velocities to change between the fuels, and one in which the fuel velocity
was kept constant for the two fuels by changing the fuel jet diameter.
A diagram of the diffusion flame burner is given in Figure 2-17.
2.2.3 Sampling and Gas Analysis
Combustion gas samples were extracted through a cooled quartz
probe drawn to a nozzle tip. The sampling probe was cooled to 65 C to
prevent water condensation in the probe. The Teflon sampling lines were
also heated to prevent water condensation before the water knockout. The
sample touched only quartz and Teflon lines until it was cooled sufficiently
to prevent further reaction at which point stainless steel lines were used.
The combustion gases were analyzed for NO and NOx with a
Thermoelectron Model 10A Chemiluminescence analyzer. The analysis for
NO is accomplished directly while the analysis for NOx is accomplished
by converting N0£ (and under certain conditions other nitrogenous
compounds) to NO and then analyzing for NO.
Analyses for CO and C02 were performed with two MSA 303 Analyzers,
both of the NDIR type. Stacked cells each with a dual range switch allowed
full scale ranges from 0.1% to 15% for CO and from 0.5% to 25% for C02-
Oxygen analysis was performed with a Beckman Model 742
polarographic oxygen analyzer with full scale ranges from 1% to 25%.
Hydrocarbon analyses were performed with a Beckman Model 400
flame ionization analyzer with full scale ranges calibrated from 50 ppm
to 5% hydrocarbon as methane.
2.2.4 Data Reduction
Experimental data as taken were coded onto computer input forms
and were reduced to measured species concentrations by a data reduction
program. The data produced in this phase of the program are presented
in the Appendix. A further subroutine can also be called to plot the
results on a printer plot. The data plots are also found in the Appendix.
A summary of runs completed in this phase is presented as
Table 2-1. The table is divided into three sections; section A covers
the cold wall tests, section B the hot wall tests on premixed flames,
and section C the hot wall tests on diffusion flames. For each of the
runs in the table fuel type, burner type, firing rate, mixture ratio,
and type of probing are given. Wall temperature is shown for the hot
wall tests. The experimental findings on premixed flames are discussed
in Section 2.2.5 and the findings on diffusion flames are discussed in
Section 2.2.6.
-------
TABLE 2-1
A. Cold
Run No.
101
102
103
104
105
106
107
108
109
110
111
112
113
114
116
119
141
* I/O =
AX =
RD =
Wall Tests
Fuel Type
Propane
Propane
Propane
Propane
Methane
Methane
Methane
Methane
Methane
Methane
Methane
Methane
Methane
Methane
Methane
Propane
Methane
Input/Output
Axial
Radial
SUMMARY OF RUNS
Burner Type
Flat Flame
Flat Flame
Flat Flame
Flat Flame
S. Diff**
S. Diff
S. Diff
S. Diff
S. Diff
S. Diff
Flat Flame
Focused Flame
Focused Flame
Focused Flame
Flat Flame
Flat Flame***
Flat Flame
MADE WITH MULTIBURNER (PHASE I)
Firing Rate
SCFM Air
0.854
0.546
0.546
0.546
2.172
2.172
2.172
2.172
0.264
0.264
0.546
2.067
2.067
2.067
0.481
2.094
0.481
Mixture Ratio
% Stoich Air
83
98
120
101
106
103
122
94
83
101
101
120
120
107
128
145
86
104
96
115
76
119
80
110
132
88
101
Probing*
I/O
I/O
I/O
AX
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
RD
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
** Stabilized Diffusion
*** High
Velocity Flame
(Lifted)
1-0
OJ
-------
TABLE 2-1 (CONTINUED)
SUMMARY OF RUNS MADE WITH MULTIBURNER (PHASE I)
B. Hot Wall Tests - Premixed Flames
Run No. Fuel Type Burner Type Firing Rate Mixture Ratio
SCFM Air % Stolen Air
115 Methane Flat Flame 0.481 161
141
60
117 Methane Flat Flame 0.481 161
119
80
118 Propane Flat Flame 0.481 161
61
120 Propane Focused Flame 0.481 156
121 Propane Focused Flame 0.481 125
101
101
82
117
78
95
117
95
78
101
130 Methane Flat Flame 0.481 140
131 Methane Flat Flame 0.481 120
78
111
101
Probing
RD
RD
RD
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
I/O
I/O
I/O
I/O
I/O
I/O
I/O
I/O
I/O
I/O
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
Wall
Temp.
°C
1703
1853
1783
1703
1703
2098
1723
1838
1768
2068
2068
2138
2138
2068
2068
2068
2138
2138
2138
2138
1858
2043
2043
2138
2218
I
N3
-C-
-------
TABLE 2-1 (CONTINUED)
SUMMARY OF RUNS MADE WITH MULTIBURNER (PHASE I)
B. Hot Wall
Run No.
131(cont)
132
133
134
135
136
137
138
139
140
Tests - Premixed Flames (cont'd)
Fuel Type
Me thane
Methane
Methane
Me thane
Propane
Propane
Propane
Propane
Methane
Me thane
Burner Type
Flat Flame
Focused Flame
Focused Flame
Focused Flame
Focused Flame
Focused Flame
Focused Flame
Focused Flame
Focused Flame
Focused Flame
Firing Rate
SCFM Air
0.481
0.481
2.094
0.481
0.481
2.094
2.094
0.481
0.481
2.094
Mixture Ratio
% Stolen Air
111
120
131
140
151
91
80
160
160
140
140
65
139
141
121
121
120
120
Probing
I/O
I/O
I/O
I/O
I/O
I/O
I/O
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
AX/RD
Wall
Temp.
°C
2218
2218
2218
2218
2218
2218
2218
1713
1713
1863
1858
1873
1898
1883
2068
2068
2043
2048
-------
TABLE 2-1 (CONTINUED)
SUMMARY OF RUNS MADE WITH MULTIBURNER (PHASE I)
C. Hot Wall Tests - Diffusion Flames
Run No.
122
123
124
125
126
127
128
129
Fuel Type
Methane
Methane
Me thane
Propane
Propane
Propane
Methane
Methane
Burner Type
S.
s.
S.
s.
s.
s.
Large
S.
Diff
Diff
Diff
Diff
Diff
Diff
Single Hole
Diff
Firing Rate
SCFM Air
2
2
2
2
2
2
2
2
.094
.094
.094
.094
.094
.094
.094
.094
Mixture Ratio Probing
% Stoich Air
160
140
120
80
160
140
120
100
80
100
160
141
114
80
160
140
140
AX/RD
AX/RD
AX/RD
AX/RD
I/O
I/O
I/O
I/O
I/O
AX
AX/RD
AX/RD
AX/RD
AX
AX/RD
AX/RD
RD
Wall
Temp.
°C
1723
1863
2048
2098
2228
2228
2228
2228
2228
2228
1698
1883
2143
2143
1713
1863
1863
I
N>
-------
- 27 -
2-2.5 Results for Premixed Flames
Species profiles have been obtained for premixed flames of
methane-air and propane-air in the multiburner with hot and cold walls.
Two types of premixed flames were studied: (1) the flat flame in which
the flame zone is flat across the burner face and the flame is essentially
one-dimensional, and (2) the shaped flame which is more representative of
premixed furnace burners although much more complex than the flat flame
in a fluid mechanical sense. The cold-wall runs are listed in Table 2-1(B).
The data listings for these runs are presented in Appendix F. The NOX
plots for the individual runs are presented in Appendix D and the plots
for CO/C02/HC/02 are presented in Appendix E. A summary of the types of
data obtained on premixed flames will be presented in this section while
the comparisons with theoretical calculations will be discussed in
Section 3.
Centerline species profiles (CO, C02, 02, NO and NOX) for a -
premixed flat flame of methane/air at 104% stoichiometric air are presented
in Figure 2-18. While the hydrocarbons are not plotted in this figure,
about 20,000 ppm were measured within 0.05 inches of the burner face,
but the concentration had dropped off to 70 ppm at 0.10 inches, and to
essentially zero at 0.50 inches. The oxygen profile drops rapidly from
about 7% within 0.05 inches to about 2.4% at 0.10 inches, and to 1.5% at
1 inch, settling at about 0.8% at greater distances. It was not possible
to probe close enough to the burner face to permit observation of the
increasing portion of the CO profile, but the decreasing portion is
plotted from a distance of 0.1 inches outward with only minor concentrations
of CO measurable after 5 inches. The C02 concentration increases rapidly,
reaching 90% of its ultimate value within 0.5 inches of the burner face.
The NOx plot exhibits substantial curvature in the region up to about
two inches from the burner face and increases only gradually thereafter.
It is interesting to note that the NO measurements are only
about 2/3 of the NOX measurements up to one inch and about 3/4 of the NOX
measurements up to two inches. At 10 inches the NO is about 90% of the
NOX= There are a number of possible interpretations for this early N02
peak.* One possible interpretation is that during the quenching process
in the probe, a portion of the oxygen atoms combine with the NO to form
N02- Calculations indicate that, with instantaneous quenching to 300°K
and assuming no heterogeneous reactions, 100 ppm of NO and 1000 ppm of
oxygen atoms react to form 38 ppm of N02 and 62 ppm of NO (allowing all
possible reactions between species containing nitrogen and oxygen but
ignoring species containing carbon or hydrogen). Such a calculation,
while oversimplified by the idealized quenching and limitation of species,
should still be somewhat conservative because of the probable underestimation
of oxygen atom concentration in the flame zone.
Cernansky, N. P., and Sawyer, R. F., "NO and N02 Formation in a Turbulent
Hydrocarbon/Air Diffusion Flame", Fifteenth Symposium (International)
on Combustion, The Combustion Institute, Pittsburgh, 1974; Merryman, E. L.
and Levy, A., "Nitrogen Oxide Formation in Flames: The Roles of N0£ and
Fuel Nitrogen", Fifteenth Symposium; Fenimore, C. P., "Ratio of Nitrogen
Dioxide to Nitric Oxide in Fuel-Lean Flames", Combustion & Flame,
volume 1, page 85, 1975.
-------
FIGURE 2-18
PREMDCED FLAT FLAME (METHANE / Am)
104% STOICHIOMETRIC AIR
W
u
tf
w
-------
- 29 -
To give an idea of the results of NO probing at other
stoichiometries, premixed flat flame data for methane/air are plotted
in Figure 2-19. At each stoichiometry on this plot, curvature can be
observed in the first inch or so from the burner face. As the stoichiometry
changes from 111% stoichiometric air to 160% stoichiometric air, the
temperature drop is sufficient to decrease post-flame NOX formation
despite increasing oxygen concentrations. This factor is accentuated
by the unheated walls. At 104% stoichiometric air, NOX is formed more
rapidly near the burner face, but the concentration flattens out after
about two inches so that the concentration at seven inches from the
burner face is lower than that for 111% stoichiometric air. The
combination of lower oxygen concentration in the post-flame zone and the
temperature drop caused by heat losses result in this lower post-flame
concentration.
-------
- 30 -
FIGURE 2-19
PREMISED FLAT FLAME (METHANE/AIR)
250 r
111% STOIC H. AIR
0
0 5 10
DISTANCE FROM BURNER (IN)
-------
- 31 -
Heated walls change the post-flame picture, as would be expected.
With the walls maintained at the adiabatic flame temperature at each
stoichiometry, peak NOX concentrations at 500-msec residence time are
observed at 100% stoichiometric air as shown in Figure 2-20. NOX concentra-
tions appear to approach zero at about 70% and at 150% stoichiometric air
when the walls are maintained adiabatic. However, if the walls are
maintained at a constant temperature of 2220°K, only minor differences
are noted on the fuel rich side (very little post-flame NOX formation) while
major differences appear under fuel lean conditions. Because of the sub-
stantial concentrations of oxygen present under fuel lean conditions, the
high temperature encourages the formation of post-flame NOX and rather than
dropping off, the NO levels increase on the fuel lean side, approaching
2000 ppm at 1507o stoichiometric air and 500 msec residence time. This
indicates that if substantial air preheat were used, high NO levels would
result on the fuel lean side. However, high preheat on the fuel rich side
does not have the same effect in a premixed flame. With interstage heat
removal to allow burnout at lower temperatures, after a fuel-rich first
stage, the NO levels resulting from high-temperature, high-oxygen operation
would be avoided.
2.2.6 Results for Diffusion Flames
Limited data were taken with diffusion flames to investigate
their behavior under a variety of heat loss conditions. Some investigations
were also made into the effect of fuel jet velocity on NOX formation.
The detailed data and centerline species plots are presented
in the Appendix. Only illustrative highlights will be covered in this
section. Under adiabatic wall conditions (wall temperature maintained
at the adiabatic flame temperature) the NO concentrations as a function
of stoichiometry are similar to those for premixed flames far downstream
of the burner face. In Figure 2-21 it can be seen that methane/air exhibits
a peak NO level of 1000 ppm at 100% stoichiometric air for 150 msec residence
time for adiabatic wall condition. Adiabatic flame temperatures vary with
stoichiometry. At 100% stoichiometric air, the adiabatic flame temperature
is about 2220°K, while at 60% stoichiometric air it is 1784°K and at 160%
stoichiometric air it is 1709°K for methane/air combustion. With the walls
heated to 2220K, the higher oxygen level at higher excess air causes more
rapid post-flame NO formation at a constant temperature. For a residence
time of 150 msec, peak NOX is shifted from 100% stoichiometric air to 1201
stoichiometric air when the walls are maintained at 2200K. As the residence
time is increased further towards the 500 msec residence time used with the
flat flame (with walls at 2220°K), the peak would shift toward leaner
mixtures, and the diffusion flame NO curve in Figure 2-21 would look more
and more like the flat-flame NO curve in Figure 2-20.
A comparison between the NOX levels for turbulent diffusion
flames of methane/air and propane/air with adiabatic walls is illustrated
in Figure 2-22. The NOX levels for propane/air are somewhat higher which
could be attributed in part to the higher adiabatic equilibrium temperature
for propane/air and in part to differences in flame chemistry. The curves
are similar in shape and behavior.
-------
- 32 -
FIGURE 2-20
PREMIXED FLAT FLAME (METHANE/AIR)
2500
2000
Q
W
CQ
H
1500
CM
1000
500
ADIABATIC
_OR 2220°K
WALL TE
Q
ADIABATIC WALL
60 80 100 120 140" 160
PERCENT STOICHOMETRIC AIR
180
-------
- 33 -
FIGURE 2-21
TURBULENT DIFFUSION FLAME (METHANE/AIR)
1500
g 1000
CQ
<
W
PH
Q 500
0
WALL = 2220°K
ADIABATIC
WALL
60 80 100 120 140 160
PERCENT STOICHIOMETRIC AIR
180
-------
- 34 -
FIGURE 2-22
TURBULENT DIFFUSION FLAME
1500
0
80 100 120 140 160
PERCENT STOICHIOMETRIC AIR
180
-------
- 35 -
A comparison of results for different fuel jet velocity and
induced turbulence yields some interesting results. Three types of fuel
jets were used in the same basic burner, All fuel jets had strictly
axial injection with no induced swirl. The fuel jet of the stabilized
burner had a 0.250 inch inside diameter which was covered with an end-plate
with six 0.020 inch holes drilled in a circular pattern. The fuel jet
of the large single hole burner had a 0.250 inch inside diameter fuel
jet with no end plate and the small single hole burner had 0.156 inch
inside diameter fuel jet with no end plate. The latter two fuel jets
were sized so that the velocity of the methane from the large jet matched
the velocity of the propane from the small jet at the same stoichiometry.
Table 2-2 shows that for methane/air under excess air conditions
the stabilized jet yields lower NO results than either the large single
hole or small single hole burners and the results drop off more rapidly as
the excess air level is increased. This is probably caused by the rapid
breakup of the multiple individual jets, resulting in behavior similar to
that found in a premixed flame. For the small single hole fuel nozzle the
measured NOX levels are essentially independent of excess air levels on an
"as measured" basis. This behavior seems to indicate that the fuel jet from
this burner maintains its integrity for a long distance downstream so that
stoichiometry plays a smaller role in NO level.
X
Propane/air gives higher NOX levels than methane/air for the
stabilized jet and for the small single hole, as expected from the higher
flame temperature. But the large single hole burner gives much lower NO
levels than either of the other two burners. This fuel/jet combination
gives the lowest jet velocity and may provide an explanation for the
results since in this case, the fuel velocity is smaller than the air
velocity. The low velocity fuel jet would cause lack of penetration of
the fuel into the air stream and recirculation of the surrounding air jet
to mix with the fuel stream near the burner face. This could cause
locally fuel rich combustion to yield results similar to that of staged
combustion. This subject was not pursued extensively at this time since
the major objective of this study was the understanding of the chemistry
rather than the fluid mechanics. However, it is noted as a possible area
for future investigation.
-------
TABLE 2-2
DIFFUSION FLAME NO/NO MEASUREMENTS
NO/NOX, ppm
Methane Propane
Percent Stoichlometric Air Percent Stoichiometric Air
Burner 120 130 140 110 125 150
Stabilized 30/35 16/18 5/10 55/60 25/30
(6 Hole)
Large 40/45 25/30 15/20 35/37 10/15
Single Hole
Small 45/55 45/50 40/45 68 60/65 48/50
i
u>
ON
Measurements taken after 100 msec residence time. ,
Velocity of methane from large single hole burner matches velocity of propane
small single hole burner at same stoichiometry. Air velocity constant.
-------
- 37 -
3. THEORETICAL CALCULATIONS
Theoretical calculations have been undertaken to obtain com-
parisons between experimental data obtained under well-defined conditions
and detailed chemical kinetics calculations. In addition, consideration
has been given to the significance of chemical reactions for which data
are available and the potential significance of reactions for which data
are not available. This section contains a discussion of the thermochemical
and kinetic calculations that have been performed thus far.
3.1 Equilibrium Calculations on Premixed Flames
Equilibrium calculations have been performed using the NASA
CEC71 computer program with the thermochemical information from the
JANAF Thermochemical Tables, Second edition (NSRDS-NBS 37). Equilibrium
compositions for the adiabatic flame temperature at one atmosphere for fuel/
air compositions with initial conditions of 298°K at one atmosphere have been
calculated for methane/air, propane/air, hydrogen/air, and carbon monoxide/
air. The information is presented in Tables 3-1 through 3-4. Only species
for which concentrations exceeded 5 ppm are included in the tables; species
considered in the calculations that did not exceed 5 ppm are listed at the
bottom of the table. Input air is considered to be dry and to contain
appropriate percentages of argon and carbon dioxide.
3.2 Survey of Coupled N0x/Combustion Kinetics
A survey of kinetic data for methane/air combustion was initiated
during this phase of the study. The status of the study at the end of this
phase is described below. An updated version of the survey will be found in
Reference 3-1.
The 25 species considered along with those species eliminated from
primary consideration are listed in Table 3-5 along with the factors that
went into making the species selections. The reactions included in this
portion of the study were those involving the 25 primary species for which
experimental or theoretical information was available in the literature.
A prescreening of the literature indicated that such information existed for
142 reactions. Thus, these reactions were numbered from 1 to 142* on an
interim basis. During the detailed reaction data accumulation it was
determined that there was not sufficient information in the literature to
yield a numerical estimate for some of these reactions (although the informa-
tion on some of them was sufficient to ascertain that the rates were slow).
It was also decided not to maintain separate headings for unimolecular
reactions of differing order. Thus, numerical data were available only on
127 of the 142 reactions of the interim list.
3-1 Engleman, V. S., Survey and Evaluation of Kinetic Data on Reactions
in Methane/Air Combustion, EPA-600/2-76-003, January, 1976.
* This interim numbering differs from the final numbering system in
Reference 3-1 which runs from 1 to 322. A cross-reference will be
found in Appendix A.
-------
TABLE 3-1
EQUILIBRIUM COMPOSITION OF PRODUCTS IN METHANE/AIR COMBUSTION
P=l ATM
INITIAL TEMP. = 298°K
PCT STOICH AIR
TEMP, DEC K
60
1784
80
2097
100
2226
120
2045
140
1861
160
1709
PRODUCTS
AR
CO
C02
H
H2
H20
NO
N02
N2
0
OH
02
PRODUCT MOLE FRACTIONS
0.00709
0.09824
0.03488
0.00011
0.11459
0.15114
0.00000
0.00000
0.59395
0.00000
0.00001
0.00000
0.00787
0.05328
0.05757
0.00057
0.03529
0.18548
0.00006
0.00000
0.65948
0.00000
0.00036
0.00001
0.00837
0.00898
0.08541
0.00039
0.00364
0.18296
0.00197
0.00000
0.70061
0.00021
0.00286
0.00459
0.00856
0.00086
0.07955
0.00004
0.00037
0.15890
0.00333
0.00000
0.71569
0.00016
0.00197
0.03057
0.00867
0.00011
0.06969
0.00000
0.00006
0.13859
0.00264
0.00000
0.72502
0.00005
0.00082
0.05434
0.00875
0.00002
0.06165
0.00000
0.00001
0.12261
0.00183
0.00000
0.73195
0.00001
0.00033
0.07285
MOLE FRACTION LESS THAN 0.000005
CN
CN2 C2
C(S) C CH CH2 CH20 CH3 CH4
C2H C2H2 C2H4 C2N C2N2 C20 C3 C302 C4 C5
HCM HCO HNO H02 H20(S) H20(L) H202 N NH NH2
NH3
N2C N2H4 N20 N204
U)
00
-------
TABLE 3-2
EQUILIBRIUM COMPOSITION OF PRODUCTS IN PROPANE/AIR COMBUSTION
P=l ATM
INITIAL TEMP. = 298°K
PCT STOICH AIR
TEMP DEC K
60
1822
80
2140
100
2254
120
2076
140
1888
160
1732
PRODUCTS
AR
CO
C02
H
H2
H20
NO
N02
N2
0
OH
02
PRODUCT MOLE FRACTIONS
0.00728
0.12308
0.04098
0.00013
0.09554
0.12281
0.00000
0.00000
0.61016
0.00000
0.00001
0.00000
0.00805
0.06366
0.07233
0.00065
0.02699
0.15342
0.00010
0.00000
0.67431
0.00001
0.00047
0.00002
0.00852
0.01183
0.10341
0.00042
0.00316
0.14841
0.00232
0.00000
0.71307
0.00028
0.00301
0.00555
0.00870
0.00132
0.09667
0.00005
0.00037
0.12285
0.00366
0.00000
0.72702
0.00020
0.00205
0.03111
0.00879
0.00017
0.08471
0.00001
0.00037
0.11232
0.00291
0 .00000
0.73510
0.00006
0.00086
0.05501
0.00886
0.00003
0.07484
0.00000
0.00001
0.09926
0.00201
0.00000
0.74096
0.00002
0.00034
0.07367
MOLE FRACTION LESS THAN 0.000005
CN
CN2 C2
C(S) C CH CH2 CH20 CH3 CH4
C2H C2H2 C2H4 C2N C2N2 C20 C3 C302 C4 C5
HCN HCO HNO H02 H20(S) H20(L) H202 N NH NH2
NH3 N2C N2H4 N20 N204
-------
TABLE 3-3
EQUILIBRIUM COMPOSITION OF PRODUCTS IN HYDROGEN/AIR COMBUSTION
P=l ATM
INITIAL TEMP. = 298°K
PCT STOICH AIR
TEMP, DEC K
60
2183
80
2349
100
2383
120
2216
140
2037
160
1884
PRODUCTS
AR
CO
C02
H
H2
H20
NO
N02
N2
0
OH
02
MOLE
C(S)
C2
C5
NH2
0.00625
0.00016
0.00005
0.00219
0.1866,
0.28061
0.00004
0.00000
0.52359
0.00000
0.00045
0.00000
FRACTIONS LESS THAN 0.000005
C CH CH2 CH20 CH3
C2H C2H2 C2H4 C2N C2N2
HCN HCO HNO H02 H20(S)
NH3 N2C N2H4 N20 N204
PRODUCT MOLE
0.00707
0.00013
0.00009
0.00349
0.07954
0.31478
0.00038
0.00000
0.59194
0.00007
0.00239
0.00012
CH4 CN
C20 C3
H20(L) H202
FRACTIONS
0.00762
0.00005
0.00019
0.00181
0.01534
0.32991
0.00260
0.00000
0.63717
0.00055
0.00687
0.00483
CN2 CO
C302 C4
N NH
0.00792
0.00001
0.00024
0.00029
0.00223
0.29115
0.00453
0.00000
0.66067
0.00049
0.00539
0.02707
0.00810
0.00000
0.00026
0.00004
0.00044
0.25801
0.00404
0.00000
0.67661
0.00020
0.00272
0.04957
0.00824
0.00000
0.00026
0.00001
0.00010
0.23054
0.00308
0.00000
0.68872
0.00007
0.00127
0.06770
o
I
-------
TABLE 3-4
EQUILIBRIUM COMPOSITION OF PRODUCTS IN CARBON MONOXIDE/AIR COMBUSTION
P=l ATM
INITIAL TEMP. = 298°K
PCT STOICH AIR
TEMP, DEC K
PRODUCTS
AR
CO
C02
NO
N02
N2
0
02
60
2306
0.00626
0.18884
0.28016
0.00052
0.00000
0.52382
0.00009
0.00031
80
2417
PRODUCT MOLE
0.00704
0.09379
0.30186
0.00292
0.00000
0.58815
0.00070
0.00555
100
2384
FRACTIONS
0.00754
0.04226
0.29690
0.00511
0.00000
0.62909
0.00106
0.01804
120
2285
0.00787
0.01582
0.27914
0.00589
0.00000
0 . 65 637
0.00083
0.03407
140
2151
0.00809
0.00472
0.25497
0.00545
0.00000
0.67485
0.00044
0.05148
160
2009
0.00824
0.00124
0.23023
0.00442
0.00000
0.68785
0.00018
0.06785
MOLE FRACTION LESS THAN 0.000005
C(S) C CN CN2 C2 C2N C2N2 C20 C3 C302
C4 C5 N N2C N20 N204
-------
- 42 -
TABLE 3-5
SPECIES CONSIDERED FOR KINETICS SURVEY ON METHANE/AIR COMBUSTION
SPECIES
C
CH
CHN
CHO
CH2
CH20
CH3
CH30
CH4
CN
CNO
CO
C02
C2
C2H
C2H2
C2H3
C2H4
C2H5
C2H6
C20
C4
C5
PRIMARY
X
X
X
X
X
X
X
X
X
X
X
SECONDARY
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
LOG K
AT 2000
-10
-10
-2
+3
-8
+1
-5
-3
-6
+7
+10
-12
-6
-3
-5
-1
-10
-15
-14
FACTORS INCLUDED IN
CONSIDERATION
possible role in soot formation
hydrocarbon radical
possible role in prompt NO
stable radical
hydrocarbon radical
combustion intermediate
hydrocarbon radical
possible role in ignition
starting material
possible role in prompt NO
possible role in NO/HC interaction
combustion product
combustion product
possible role in soot formation
C2 intermediates possibly
important for
fuel rich combustion of
methane or higher
hydrocarbons
J
difficult to form from CO
"^possible role in soot formation
/more likely from higher
J hydrocarbons
-------
- 43 -
TABLE 3-5 (CONTINUED)
SPECIES
H
HN
HNO
HO
H02
H2
H2N
H2N2
H20
H202
H3N
H3N2
H4N2
N
NO
N02
N03
N2
N20
N204
N205
0
02
Oq
PRIMARY
X
X
X
X
X
X
X
X
X
X
X
X
X
X
SECONDARY
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
LOG K
AT 2000K
-3
-8
-5
0
-3
0
-6
-12
44
-5
-14
-9
-2
-4
-10
0
-6
-15
-18
-3
0
-7
FACTORS INCLUDED IN
CONSIDERATION
combustion intermediate
possible role in prompt NO
possible role in prompt NO
combustion intermediate
combustion intermediate
combustion product
possible intermediate
not likely for methane/air
combustion product
possible role in ignition
possible role fuel rich
not likely for methane/air
not likely for methane/air
important role NO formation
of prime interest
oxidation of NO
higher oxidation state of NO
starting material
possible role in prompt NO
not likely for methane/air
not likely for methane/air
combustion intermediate
starting material
possible role in ignition
-------
- 44 -
The interim recommended rates for the reactions used in this
portion of the study are included here as Table 3-6. More up-to-date
recommendations will be found in Reference 3-1. All reactions included
in the table are covered by rate constants and/or comments. The rates
are also calculated for temperatures of 300°, 1500°, and 2500°K in the
direction indicated (F for forward and R for reverse). Where five asterisks
appear in the comments section, only limited estimates are available and
should be regarded with caution. It should be realized that recommended
rates are evolutionary. As further kinetic and thermochemical data become
available, recommendations require updating. Thus, any recommended rates
should be considered as subject to further evaluation.
Additional reactions can be written involving these species in
unimolecular and bimolecular reactions, some of which could prove to be
significant in the mechanism of methane combustion with pollutant
formation. Thus, a listing has been made of all the possible unimolecular
and bimolecular reactions among 25 species in the methane/air combustion
system. The listing (Appendix A) contains notations indicating the type of
reaction for those included in the survey. An evaluation of the potential
importance of each of these reactions in methane combustion will be found
in Reference 3-1. The 322 reactions in this "master list" are numbered
both with their interim reaction numbers, where applicable, and sequentially,
with "X" numbers which cross-reference this list to the complete survey in
Reference 3-1.
3.3 Kinetics Calculations
Kinetics calculations during this phase of the program were
performed using the version of the CKAP* program modified for use on an
IBM 370 computer. Difficulties were encountered in attempting to
prevent negative concentrations in plug-flow cases. The rate of disappearance
of hydrocarbons is so rapid as their concentrations approach zero that
concentrations of these substances frequently go negative instead of
leveling off near zero. By taking special care with step size control and
relative error criterion, the problem could be alleviated in most cases.
The initial set of calculations for reaction screening and data
comparisons have been run under isothermal conditions at the adiabatic flame
temperature in the region between 80 and 120% stoichiometric air at atmo-
spheric pressure. The isothermal approach offers a number of advantages:
computer time is shortened, screening is facilitated since the rate para-
meters are held constant, and ignition is easily accomplished. Additional
runs have been made for the case of adiabatic ignition.** These runs
indicate the same qualitative behavior as the isothermal runs and basically
similar proportions of reaction intermediates are computed, even though the
absolute concentrations are not identical for the two cases.
* Supplied by EPA for use in this program. Developed for detailed kinetic
analysis by Ultrasystems under EPA contract 68-02-0220.
** Such runs were accomplished by allowing a small amount of initial
reaction to occur at high temperature. After a temperature rise of
about 200°K, the system was dropped back to the lower temperature
(initial temperature + temperature rise) and ignition was allowed to
proceed.
-------
RECOMMENDED RATES
REACTION
IF. CH + CRN = CH2 + CN
2F. CH + CHO = CH2 + CO
3Ft CH + CH20 = CH2 + CHO
4F. CH + CH3 * CH2 + CH2
5F. CH + CH4 - CH2 + CH3
6F. CH + C02 = CHO + CO
7F. CH + H = CH2
8F. CH + H + M = CH2 + M
9R. CH2 + N a CH + HN
10F. CH + HN = CN + H2
11F. CH + HNO = CH2 + NO
TABLE 3-6
INTERIM RECOMMENDED RATES
1500-2500K. 9/30/73
C COMMENTS
8. #**** NOTE B.
BASED ON Tl (J-P)
1. ***** NOTE B.
BASED ON Tl (J-P)
4. ***** NOTE B.
BASED ON Tl (J-P)
5. ***** NOTE B.
BASED ON Tl (J-P)
6, ***** NOTE 8.
BASED ON Tl (J-PI
6. ***** NOTE A*
BASED ON Tl (EST)
0. BASED ON Tl (EST)
USE THIRD ORDER
SEE 8F.
NO DATA
WILL ESTIMATE
11.8 0.67 4.0.5 ***** NOTE A.
BASED ON MS (J-P)
NO DATA
PROBABLY SLOW
9R FASTER THAN 10F
31R FASTER THAN 10R
LOG A B
11.5 0.6
10.5 0.7
11.0 0.7
11.1 0.7
11.4 0.7
10.0 0.5
11.7 0.5
11.8 0.5
***** NOTE A.
BASED ON Tl (EST)
TEMP* KELVIN
300 1500 2000 2500
LOG K
7.2 12.2 12.6 12.8
11.5 12.6 12.7 12.8
9.8 12.6 12.9 13.0
9.2 12.6 12.9 13.0
8.8 12.7 13.1 13.3
6.9 10.7 11.0 11.2
12.9 13.3 13.4 13.4
-16.0 8.0 9.6 10.5
13.0 13.4 13.5 13.5
Ln
I
NOTE A - BEST ESTIMATE AVAILABLE, USE WITH CAUTION
NOTE B - ONLY ESTIMATE AVAILABLE, USE WITH CAUTION
NOTE C - LIMITED EXPERIMENTAL DATA AVAILABLE, USE WITH CAUTION
-------
RECOMMENDED RATES
REACTION LOG A
12F. CH -t- HO = CHO + H 11.7
13R. CH2 + 0 = CH + HO
14F. CH + HO = CO + H2
15F. CH + H02 = CHO + HO 11.7
16F. CH + H02 = CH2 + 02 10.0
17R. CH2 + H = CH + H2
18R. CH2 + HO = CH + H20
19F. CH + N = CN + H
20F. CH -t- NO = CHO + N
21F. CH -i- N2 = CHN + N
22F. CH + 0 = CO + H 11.7
23F. CH + 0 + M « CHO + M 16.
TABLE 3-6 (CONTINUED)
1500-2500K 9/30/73
B C COMMENTS
0.5 10. ***** NOTE A.
BASED ON Tl (EST)
11.3 0.7 26.
***** NOTE B.
BASED ON M8 (J-P)
NO DATA
PROBABLY SLOW
13R FASTER THAN 14F
14R UNFAVORABLE
0.5 6. ***** NOTE A.
BASED ON Tl !EST)
0.5 15. ***** NOTE B.
BASED ON Tl (EST)
11.5 0.7 26,
11.7 0.5
***** NOTE B.
BASED ON M8»T1 (J-P)
***** NOTE A.
BASED ON Tl (EST)
NO DATA
WILL ESTIMATE
NO DATA
PROBABLY SLOW
NO DATA
SPIN FORBIDDEN
0.5 4. ***** NOTE A.
BASED ON Tl (EST)
•0.5 0. ***** NOTE A.
BASED ON Tl (EST)
TEMPt KELVIN
300 1500 2000 2500
LOG K
5.7 11.8 12.3 12.5
-5.9 9.7 10.8 11.4
8.6 12.4 12.7 12.9
0.3 9.4 10.0 10.4
•5.7 9.9 11.0 11.6
8.6 12.4 12.7 12.9
10.0 12.7 12.9 13.0
14.8 14.4 14.3 14.3
i
j^
-------
28Rt CH3 + CN = CHN + CH2
29R. CH4 + CN = CHN + CH3
30R. CHO + CN = CHN + CO
31F. CHN + H = CN + H2
32F. CHN + HO = CN + H20
33R. CN + HN = CHN + N
34R. CN + HNO = CHN + NO
LOG A B C
11.7 0.5 6.
RECOMMENDED RATES
REACTION
24F. -CH + 02 = CHO + 0
25F. CH + 02 = CO + HO
26R. CN + H + M = CHN + M 16.5 -0.5
27R. CH20 + CN = CHN + CHO 11.1 0.7
TABLE 3-6 (CONTINUED)
1500-2500K 9/30/73
11.0 0.7
11.5 0.7
11.3 0.5
0.7 18.
11.3 0.6
11.0 0.5
11.6 0.5
COMMENTS
***** NOTE A.
BASED ON Tl (EST)
NO DATA
PROBABLY SLOW
***** NOTE A.
BASED ON Tl (EST)
***** NOTE A.
BASED ON Tl U-P)
***** NOTE A.
BASED ON Tl (J-P)
*****
BASED ON Tl (J-P)
XPT 100X J-P 300K
REQUIRE A=13.5 OR
REQUIRE E=0.
***** NOTE A.
BASED ON Tl (EST)
***** NOTE B.
BASED ON Tl (J-P)
***** NOTE A.
BASED ON Tl (J-P)
***** NOTE A.
BASED ON Tl (EST!
***** NOTE A.
BASED ON Tl (EST)
TEMP* KELVIN
300 1500 2000 2500
LOG K
8.6 12.4 12.7 12.9
15.3 14.9 14.8 14.8
10.6 12.9 13.1 13.2
10.5 12.8 13.0 13.1
9.6 13.0 13.3 13.4
12.5 12.9 13.0 13.0
0.0 11.0 11.7 12.2
9.1 12.5 12.7 12.9
10.8 12.3 12.4 12.5
12.8 13.2 13.3 13.3
-j
i
-------
TABLE 3-6 (CONTINUED)
RECOMMENDED RATES
REACTION
35F. CHN + 0 = CN + HO
LOG A
11.5
38F. CHO + CH2 = CH3 + CO
40F. CHO + CH3 = CH4 + CO
42R. CH2 + 0 = CHO + H
B
0.7
36F. CHO +M=CO+H+M 20.4 -1.5
37F. CHO + CHO = CH20 + CO 11.2 0.5
10.5 0.7
39F. CHO + CH3 = CH2 + CH20 11.2 0.7
11.5 0.5
41F. CHO + CH4 = CH20 + CH3 11.9
11.7
0.6
0.5
1500-2500K 9/30/73
C COMMENTS
17. ***** NOTE B.
BASED ON Tl (J-P)
16.8 SRI ESTIMATE 4/11/73
BASED ON HINSHELWOOO
-LINDEMANN THEORY
XPTL REF B65 GIVES
A=12.3»B=0.5»E=29.
NOT SENSITIVE XPT
0. ***** NOTE A«
BASED ON Tl (EST)
1. ***** NOTE A.
BASED ON Tl (J-P)
A, ***** NOTE B.
BASED ON Tl (J-P)
0. ***** NOTE A.
BASED ON Tl (EST)
9. ***** NOTE B.
BASED ON Tl (J-P)
44F. CHO + H = CO + H2
10.5 1.
4t
43R. CH20 + M = CHO + H + M 33.9 -4.5 87.
***** NOTE A.
BASED ON Tl (EST)
SRI ESTIMATE 4/11/73
BASED ON HINSHELWOOD
-LINDEMANN THEORY
SRI ESTIMATE 4/6/73
REF Tl ESTIMATES
A=12.2»B=0.5»E=0.
TEMPt KELVIN
300 1500 2000 2500
LOG K
0.8 11.2 12.0 12«4
4.4 13.2 13.6 13.8
12.4 12.8 12.9 12.9
11.5 12.6 12.7 12,
10.0 12.8 13.1 13.2
12.7 13.1 13.2 13.2
6.8 12.5 12.9 13.2
10.0 12.7 12.9 13.0
-40.6 6.9 9.5 11.0
13.0 13.7 13.8 13.9
00
I
-------
RECOMMENDED RATES
REACTION LOG A
45F. CHO + NO = CH20 + NO 11.5
46R. CH20 + 0 = CHO + HO
TABLE 3-6 (CONTINUED)
1500-2500K 9/30/73
C COMMENTS
0. ***** NOTE A.
BASED ON Tl (EST)
47F. CHO + HO « CO + H20
48R. CH20 + H = CHO + H2
49R. CH20 + HO = CHO + H20
50F. CHO + N = CO + HN
51F. CHO + NO = CO -f HNO
52F. CHO + 0 = CO + HO
53F. CH2 + CH4 = CHS + CH3 12.1 0.7
54F. CH2 + HNO = CH3 + NO
11.3 1. 4.4 BASED ON D22»N7»M27
USING B = 1
FIT MODIF ARRHENIUS
D22 BEST HI T
N7 & M27 BEST LO T
10.5 1. 0. SRI ESTIMATE 4/6/73
XPT 14. AT 2000K
OTHER ESTS 12.5
AT 2000K
10.1 1. 3.2 BASED ON W32
USING 8=1
NO DATA ABOVE 1000K
9.5 1. 1. SRI ESTIMATE 4/6/73
AGREES WITH REF Tl
11.3 0.5 2. ***** NOTE A.
BASED ON Tl (EST)
11.3 0.5 2. ***** NOTE A.
BASED ON Tl (EST)
11.5 1. 0.5 SRI ESTIMATE 3/28/73
OTHER ESTS 12.8
20. ***** NOTE A.
BASED ON Tl (J-P)
11.8 0.5 0. ***** NOTE A.
BASED ON Tl (EST)
TEMP, KELVIN
300 1500 2000 2500
LOG K
12.7 13.1 13.2 13.2
10.6 13.8 14.1 14.3
13.0 13.7 13.8 13.9
10.2 12.8 13.1 13.2
11.2 12.5 12.7 12.8
11.1 12.6 12.7 12.8
11.1 12.6 12.7 12.8
13.6 14.6 14.7 14.9
-0.7 11.4 12.2 12.7
13.0 13.4 13.5 13.5
-------
TABLE 3-6 (CONTINUED)
RECOMMENDED RATES
REACTION
55F. CH2 + HO = CH3 + 0
56R« CH3 + H = CH2 + H2
57R. CH3 + HO = CH2 + H20
58F. CH2 + 02 = CH20 + 0
59R. CH3 + 0 = CH20 + H
LOG
A
1500-2500K 9/30/73
B C COMMENTS
300
TEMP.
1500
KELVIN
2000
2500
LOG K
11.
11.
10.
11.
7
3
8
7
0.5
0.7
0.7
0.5
6.
3.
2.
7.
*****
BASED ON
*****
BASED ON
*****
BASED ON
*****
NOTE A.
Tl (EST)
NOTE B.
Tl (J-P)
NOTE B.
Tl (J-P)
NOTE A.
8
10
11
7
.6
.8
.1
.8
12
13
12
12
.4
.1
.7
• 3
12.7
13.3
12.9
12.6
12.9
13.4
13.0
12.8
12.3 0.5
991R. CH30 + M a CH20 + H + M 40.6 -7.5
BASED ON Tl (EST)
-0.3 BASED ON M25»D22
USING B - 0.5
M25 LO T» 022 HI T
22.6 SRI ESTIMATE 4/11/73
BASED ON HINSHELWOOD
-LINDEMANN THEORY
NOTE A.
60R. CH3 + 02 = CH20 + HO
13.5
30,
BASED ON D22
SRI RECOMMENDS
C = 30
D22 GIVES C=10
FOUR CENTER
13.8 13.9 14.0 14.0
5.6 13.5 13.4 13.1
-8.4 9.1 10.2 10.9
61R. CH4 + M = CHS + H + M 15.
17.3
0.
0.
104
62F. CH3 + HNO = CH4 + NO
11.7 0.5
BASED ON H32
FIRST ORDER
87.5 BASED ON H32
SECOND ORDER
RECENT XPT
0. ***** NOTE A.
BASED ON Tl (EST)
•60.8 -0.2 3.6 5.9
-46.4 4.6 7.7 9.7
12.9 13.3 13.4 13.4
Ol
o
-------
RECOMMENDED RATES
REACTION
63R. CH4 + 0 = CH3 + HO
TABLE 3-6 (CONTINUED)
1500-25QOK 9/30/73
LOG A B C COMMENTS
10. 1. 8. BASED ON W25»H25
USING B = 1.
64F. CHS + H02 = CH4 + 02 11.0 0.5
65R. CH4 + H = CH3 * H2 10.7 1.
66R. CH4 + HO = CH3 + H20 13.5 0.
992F. CHS + 02 = CH30 + 0 9.4 1,
67F. CN + NO = CO + N2 11.5 0.
993F. CN + 0 = CO + N 12. 0,
68F. CN + 02 = CO + NO 11.5 0.
69F. CO + HNO = C02 + HN 11.0 0.5
70F. CO + HO = C02 + H 9.6 0.5
6. ***** NOTE A.
BASED ON Tl (EST)
10. BASED ON W30
USING B = 1.
AGREES W/ OTHER
XPT AND EVAL
5. BASED ON W31
EVAL 300-2000K
AGREES G18» 300-500K,
28.5 SRI ESTIMATE 4/11/73
BASED ON EARLIER EST
USING B = 1.
0. ***** NOTE C.
BASED ON B78 (XPT)
0. BASED ON B78» R5
ASSUME C = 0
DATA 300-700K
0. ***** NOTE C.
BASED ON B86 (XPT)
UPPER LIMIT
7. ***** NOTE A.
BASED ON Tl (EST)
0. BASED ON TRANS STATE
PARAMETERS H = -1»
S = -30» CP = -3
LOG K = 11. AT 300K
BETTER FIT TO DATA
WITH A=5.9fB=2.»C=-l
TEMP* KELVIN
300 1500 2000 2500
LOG K
6.6 12.0 12.4 12.7
7.9 11.7 12.0 12.2
5.9 12.4 12.9 13.2
9.9 12.8 13.0 13.1
-8.9 8.4 9.6 10.3
11.5 11.5 11.5 11.5
12.0 12.0 12.0 12.0
11.5 11.5 11.5 11.5
7.1 11.6 11.9 12.1
10.8 11.2 11.3 11.3
Ol
I-1
-------
TABLE 3-6 (CONTINUED)
RECOMMENDED RATES
REACTION
71F. CO + H02 = C02 + HO
72R. C02 + H2 = CO + H20
73R. C02 + N = CO + NO
74F. CO -f N02 = C02 + NO
75F. CO + N20 = C02 + N2
76R. C02 = CO + 0
77R. C02 +M=CO+0+M
78F. CO + 02 = C02 + 0
79R. H2+M=H+H+M
80F. H + HN = H2 + N
LOG A
11.
9.0
11.3
12.5
11.0
1500-2500K. 9/30/73
B C COMMENTS 300
0. 10.5 SRI ESTIMATE 9/11/73 3.4
REF Lll RECOMMENDS
A=12. »B=0.»C=16.5
0.5 15. ***** NOTE A. -0.7
BASED ON Tl (EST)
0.5 25. BASED ON Tl -5.7
WITH HIGHER C
PROBABLY SLOW
SPIN FORBIDDEN
0. 30. BASED ON B47» J6 -9.4
LIMITED OLD DATA
0. 23. ***** NOTE C. -5.8
TEMP» KELVIN
1500 2000 2500
LOG K,
9.5 9.9 10,1
8.4 9.0 9.4
9.2 10.2 10.8
8.1 9.2 9.9
Ul
7.6 8.5 9.0 i
BASED ON L9 (XPT)
USE THIRD BODY
SEE 77R.
15. 0. 100. BASED ON C26» 01
COMPLEX REACTION
SLOW DISSOCIATION
RECENT DATA
13. 0. 60. BASED ON D22
MINIMUM E=50
HI T DATA FAIR AGRMT
14.3 0. 96. BASED ON B88
M = AR
BEST RECENT EVAL
11.8 0.5 8. SRI ESTIMATE
QPR NO. 2. 2/15/73
BASED ON TRANS STATE
PARAMETERS H = 7.
S = -22» CP = -3
-57.9 0.4 4.1 6.3
-30.7 4.3 6.4 7.8
-55.6 0.3 3.8 5.9
7.2 12.2 12.6 12.8
-------
TABLE 3-6 (CONTINUED)
RECOMMENDED RATES
REACTION
81F. H + HNO = HN + HO
82F. H + HNO = H2 + NO
83F. H + HO = H2 + 0
84R. H20 +M=HO+H+M
85F. H + H02 = HO + HO
86F. H + H02 = H2 + 02
87F. H + H02 = H20 + 0
88R. HO + H2 = H + H20
89F.H+N+M=HN+M
90R. HN + 0 = H + NO
LOG A
11.3
13.
9.9
15.5
14.4
13.4
13.0
B
0.5
0*
0.
0.
1500-2500K 9/30/73
C COMMENTS
13. ***** NOTE A.
BASED ON Tl (EST)
2.5 BASED ON H3 1
FIT DATA 200-2000K
7. BASED ON B88
CRIT EVAL 400-2000K
105. BASED ON B88
M = N2
CRIT EVAL 2000-6000K
DIFFICULT TO STUDY
1.9 BASED ON B88
CRIT EVAL 290-800K
0.7 BASED ON 888
CRIT EVAL 290-800K
13.4 0.
1. BASED ON Lll
EVAL 300-1000K.
LOWER THAN REC B88
12.9 AT 293K
5.2 BASED ON B88
EVAL, AGREES XPT
16.5 -0.5 0. ***** NOTE A.
BASED ON Tl
-------
RECOMMENDED RATES
REACTION
91R. HO + N = H + NO
92F.H+NO+M= HNO + M
93R. HNO + 0 = H + N02
94F. H + N02 = HO + NO
95R. HN + N * H + N2
96F. H + N20 = HN + NO
97R. HNO + N = H + N20
TABLE 3-6 (CONTINUED)
1500-2500K 9/30/73
LOG A B
11.8 0.5
16.3 Oi
10.7 0.5
14.5 0.
11.8 0.5
11.0 0.5
10.7 0.5
C COMMENTS
8. SRI ESTIMATE
QPR NO. 2» 2/15/73
BASED ON TRANS STATE
PARAMETERS H = 7
S = -22» CP = -3
K = 13.5 AT 320K
BASED ON REF C8
WOULD REQUIRE C = 0
ALSO USE C=0 FOR SCR
GIVES 13.45 AT 2000K
0. BASED ON C20. HlO
AT 300K
USING B = 0» C * 0
M = H2
DATA 200-700K INDIC
SLIGHT NEGATIVE E
0. ***** NOTE A.
BASED ON Tl (EST)
1.5 BASED ON B90
300-600K
NO DATA ON REVERSE
0. SRI ESTIMATE
QPR NO. 2* 2/15/73
BASED ON TRANS STATE
PARAMETERS H = -1
S = -22» CP = -3
30. ***** NOTE A.
BASED ON Tl (EST)
3. ***** NOTE A.
BASED ON Tl (EST)
TEMP. KELVIN
300 1500 2000 2500
LOG K
7.2 12.2 12.6 12.8
16.3 16.3 16.3 16.3
11.9 12.3 12.4 12.4
13.4 14.3 14.3 14.4
13.0 13.4 13.5 13.5
-9.6 8.2 9.4 10.1
9.8 11.9 12.0 12.1
Ul
I
-------
TABLE 3-6 (CONTINUED)
RECOMMENDED RATES
REACTION LOG A B
98F. H + N20 = HO + N2 13.9 0.
99F. H+0+M=HO+M 15.9 0.
100R. HO + 0 - H + 02 13.4 0.
1500-2500K
9/30/73
10IF. H + 02 + M - H02 + M 15.2 0,
102F. HN -i- HN a H2 + N2
103F. HN + HO = H2 + NO
104F. HN + HO = H20 •*• N 11.7 0.5
105R. HNO + N = HN + NO 11.0 0.5
106F. HN + N02 = HNO + NO 11.3 0.5
107F. HN + N20 = HNO + N2 11.0 0.5
C COMMENTS
15. BASED ON 890
CRIT EVAL 700-2500K
0. BASED ON S30
LIMITED DATA
REF B88 GIVES NO REC
0. BASED ON B88» W31
NOTE REF 688 REC'S
FOR 100F. A= 14.4.
B = 0.» C = 16.8
CRIT EVAL 300-2000K
1. BASED ON B88
M = AR
FOUR CENTER
PROBABLY SLOW
D8 GIVES 14 AT 2000K,
BAHN CITES 13 FROM
REF M8 (ERROR)
FOUR CENTER
PROBABLY SLOW
2. ***** NOTE A.
BASED ON Tl (EST)
2. ***** NOTE A.
BASED ON Tl (EST)
5. **** NOTE A.
BASED ON Tl (EST)
3. ***** NOTE A*
BASED ON Tl (EST)
TEMP* KELVIN
300 1500 2000 2500
LOG K
3.0 11.7 12.3 12.6
15.9 15.9 15.9 15.9
13.4 13.4 13.4 13.4
14.5 15.1 15.1 15.1
11.5 13.0 13.1 13.2
10.8 12.3 12.4 12.5
8.9 12.2 12.4 12.6
10.1 12.2 12.3 12.4
Ul
Ui
-------
RECOMMENDED RATES
TABLE 3-6 (CONTINUED)
1500-2500K 9/30/73
REACTION
108F. HN + 0 = HO + N
109F. HN + 0 + M = HNO + M
110R. HNO + 0 = HN + 02
111R. H02 + N = HN + 02
113F. HNO + HO = H20 + NO
114F. HNO + NO = HO + N20
115F. HNO + 0 = HO + NO
ll6Rt H2 + 02 = HO + HO
LOG A B
11.8 0.5
16.0 -0.5
11.0 0.5
11,
Oi
112R. HO + N + M = HNO + M 15.0 -0.5
14.0
12.
0.
0.
c
8.
0.
1.
12.3 0. 26<
11.7 0.5 0,
12.4 0. 39.
COMMENTS
SRI ESTIMATE
QPR NO. 2, 2/15/73
BASED ON TRANS STATE
PARAMETERS H = 7»
S = -22» CP * -3
***** NOTE A.
BASED ON Tl (EST)
***** NOTE A.
BASED ON Tl (EST)
***** NOTE C.
BASED ON K25 (XPT)
LOWER LIMIT
***** NOTE A.
BASED ON Tl (EST)
BASED ON H31
SRI ESTIMATE 3/28/73
BASED ON W23
REEXAMINATION OF
EXISTING H2-NO DATA
1000-1300K
***** NOTE A.
BASED ON Tl (EST)
BASED ON R2
1400-2500K
REF B88 INDICATES
R2 PROBABLY VALID
BUT MAKES NO REC
TEMP, KELVIN
300 1500 2000 2500
LOG K,
7.2 12.2 12.6 12.8
14.8 14.4 14.3 14.3
7.1 11,6 11.9 12.1
11.0 11.0 11.0 11.0
13.8 13.4 13.3 13.3
14.0 14.0 14.0 14.0
11.3 11,9 11.9 11.9
-6.6 8.5 9.5 10.0
12.9 13.3 13.4 13.4
-16.0 6.7 8.1 9.0
I
Ul
-------
RECOMMENDED RATES
REACTION
117F. HO + HO = H20 + 0
118F. HO + H02 = H20 + 02
119F. HO + NO = H02 + N
120R. H02 + NO = HO + N02
121R. H02 + M = HO + 0 + M
122R. H02 + 0 = HO + 02
123F. H2 + N02 = H20 + NO
124R. N2+M=N+N+M
125F. N + NO = N2 + 0
TABLE 3-6 (CONTINUED)
1500-2500K 9/30/73
LOG A B C
12.8 0. 1.
13. 0. 1.
12,
15.6 -1.5 64.
13.7 0,
21.6 -1.6 225,
13.2 0.
11.8 0.5
0.
0.
COMMENTS 300
BASED ON B88 12.1
EVALUATION 300-2000K
BASED ON Lll
H37 INDIC 14 AT 300K
B88 SUGGESTS 12.8 AS
LOWER LIMIT AT 300K
NO DATA
WILL ESTIMATE
SRI ESTIMATE 3/28/73
LOWER THAN J12.N6
WITHIN LIMITS Lll
SRI ESTIMATE 4/6/73
NO VALID DATA (888)
BASED ON Lll
300-1000K
LIMITED INFO
SLOW
K=3.5 AT 700K
BASED ON B90
M = N2
TEMP* KELVIN
1500 2000 2500
LOG K
12.7 12.7 12.7
12.3 12.9 12.9 12.9
9.8 11.6 11.7 11.7
-34.7 1.5 3.7 4.9
13.0 13.6 13.6 13.6
-146.3 -16.3 -8.3 -3.5
BASED ON B90 13.2
CRITICAL EVALUATION
SRI ESTIMATE 13.0
QPR NO. 2» 2/15/73
BASED ON TRANS STATE
PARAMETERS H = -1»
S = -22« CP = -3
13.2 13.2 13.2
13.4 13.5 13.5
I
Ul
-------
TABLE 3-6 (CONTINUED)
RECOMMENDED RATES
REACTION
126Ft N 4- NO 4- M = N20 + M
127F. N 4- N02 = NO + NO
1500-2500K
128F. N 4- N02 = N2 4- 0 + 0
129F. N 4- N02 = N2 + 02
130F. N 4- N02 = N20 + 0
131F. N 4- N20 «= NO + N2
132R
133F. N 4- 02 = NO 4- 0
LOG A
12.6
12.2
12.0
12.7
8.7
10.
20.6 -Ii5 150.
148,
9/30/73
COMMENTS
NOT LIKELY
GOES TO
STABILIZ
PROBABLY
N2 4- 0
S30-NO EVIDENCE
BASED ON P10
USING B = 0» C =
B90 INDICATES
P10 UPPER LIMIT
PROB 2.5X LOWER
BASED ON P10
USING B = 0» C *(
UPPER LIMIT
BASED ON P10
USING B - 0» C
PROBABLY UPPER
= 0
LIMIT
BASED
USING
ON
B
P10
= 0»
9*8
11.8
1.
0.5
6.3
8.
*#*##
BASED ON B19 (SEL)
BASED ON B90
M = AR» N2» 02
CAUTION RECOMMENDED
RASED ON M26» M « AR
(0) FORMATION MEAS.
BASED ON B90
EVALUATION 300-3000K
SRI ESTIMATE
QPR NO. 2» 2/15/73
BASED ON TRANS STATE
PARAMETERS H = 7,
S = -22. CP * -3
TEMP* KELVIN
300 1500 2000 2500
LOG K,
12.6 12.6 12.6 12.6
12.2 12.2 12.2 12»2
12.0 12.0 12.0 12.0
12.7 12.7 12.7 12.7
1.4 7.2 7.6
7.8
-92.4 -6.0 -0.7 2.4
-93.7 -7.5 -2.1 1.2
7.7 12.1 12.4 12.6
7.2 12.2 12.6 12.8
i
00
-------
TABLE 3-6 (CONTINUED)
RECOMMENDED RATES
REACTION
134F. NO + NO = N2 + 02
135R. N20 + 0 * NO + NO
136F. NO + N02 = N20 + 02
137F. NO + N20 = N02 + N2
138R. N02 +M=NO+0+M
139R. N02 + 0 = NO + 02
140R. N20
141R. N20 + 0 * N2 + 02
142Rt 02+M=0+0+M
LOG A B
14.0 0*
12.0
12.3
16.0
13.
14.
14.
18.4
19.4
0*
0.
0*
-1.
-1.
1500-2500K 9/30/73
C COMMENTS
SPIN FORBIDDEN
PROBABLY SLOW
OLD DATA DID NOT
MEASURE THIS RX
ACTUALLY MEAS 135F
28. BASED ON B90
EVAL 1200-2000K
SAME RATE AS 141R
NO TRANSITION STATE
NO EXPTL EVIDENCE
60. BASED ON B19 (EST)
40. BASED ON K30
USING A = 12.3
NO RECENT DATA
65. BASED ON B90» T4
M = AR* 02
1400-2400K
1. BASED ON B53
CRIT EVAL 300-600K
NO HI T DATA
50. APPROXIMATE
COVERS LIMITED DATA
IN 1500-2500K RANGE
28. BASED ON B90
REC 1200-2000K
SAME RATE AS 135R
118.7 BASED ON J4» M = AR
118.7 BASED ON J4i M = 02
CRITICAL EVALUATION
WIDE TEMP RANGE
1000-8000K FOR 02
300-15000K FOR AR
TEMP» KELVIN
300 1500 2000 2500
LOG K
-6.4 9.9 10.9 11.6
-31»7 3.3 5.4 6.8
-16.8 6.5 7.9 8.8
-31.4 6.5 8.9 10.3
12.3 12.9 12.9 12.9
-22.4 6.7 8.5 9.6
-6.4
-70.6
-69.6
9.9
•2.1
-1.1
10.9
2.1
3.1
11.6
4.6
5.6
I
Ul
-------
- 60 -
In the screening studies, reactions could be eliminated for one
of three reasons:
1. The reaction itself is too slow to play a major
role for any species.
2. The reaction is part of a loop which merely returns
its starting material.
3. A species involved in the reaction is of no
importance in either combustion or pollutant
formation.
These practical considerations must be handled with some caution since
reaction elimination based on species could vary with the goals of the
screening procedure. For example, calculations oriented primarily toward
heat release and combustion efficiency could easily ignore NO forming
reactions since these reactions play a very small role in that respect.
At peak NO formation rate, the NO forming reactions are involved in only
about 0.017= of the 0 atom appearance or disappearance reactions. Since NO is
of prime interest in these calculations, such reactions must be carefully
retained. On the other hand, since soot is not likely to form in methane/air
combustion unless substantial concentrations of hydrocarbons remain at the
end of the combustion zone, reactions precursor to soot formation can probably
be ignored with a fair degree of safety as long as calculations are restricted
to the region of 807o-1207o stoichiometric air at atmospheric pressure.
While progress toward the definition of a "minimum reaction set"
is an ultimate goal it is more important initially to appreciate the chemistry
of the coupled reactions. With 322 possible unimolecular and bimolecular
reactions which can be written for the 25 species in the kinetics survey,
it is entirely possible that some reaction beyond those 142 reactions for
which rate information was reported in the literature might be of importance.
While many of the reactions not reported in the literature are not elementary
reactions an evaluation of the potential importance of each of the remaining
reactions will be undertaken as a step towards the complete evaluation of
the combustion/pollutant formation mechanism for the 25 species considered.
-------
- 61 -
3.4 Results of Theoretical Calculations for Methane/Air
Screening calculations have been performed, using the interim
(September 1973) recommended rates for the kinetics survey, to gain insight
into the major reaction paths and major reactions in the coupled combustion/
pollutant formation for methane/air. The interim rates have since been
superseded by the recommended rates given in Reference 3-1 but the results
obtained from these calculations are instructive for the overall features
uncovered. However, the reader should be aware that the quantitative details
would be different if the revised rates were used and that the reaction set
used for these calculations was not complete. Therefore potentially impor-
tant paths for NO formation have been omitted from these calculations.
x
Most of the calculations were accomplished under isothermal con-
ditions at the adiabatic flame temperature as discussed earlier. These iso-
thermal calculations result in temperatures and reaction rates in the early
combustion zone which are higher than those observed experimentally. There-
fore, the calculations indicate a hydrocarbon burnout rate which is more
rapid than for the case of an adiabatic flame. However, the essential
features of the combustion are preserved as indicated by comparison with
calculations of adiabatic ignition from room temperature. The concentrations
calculated for the intermediates remain basically the same. The concentra-
tion levels are sufficiently close for screening purposes although the over-
shoots tend to reach higher concentrations (but for shorter times) in the
isothermal case.
Concentrations of selected species as a function of time for plug
flow reaction at stoichiometries of 80%, 100% and 120% stoichiometric air
are given in Tables 3-7, 3-8 and 3-9 respectively. It should be emphasized
that these are only preliminary calculations based on the limited number
of reactions reported in the literature. Such calculations are highly
informative but must be followed by more complete calculations for further
elucidation. The reaction times selected for these tables are illustrative
of some of the zone divisions to be discussed in Section 3.5. At this point
a discussion of the species concentrations themselves will be presented.
3.4.1 80% Stoichiometric Air
In Table 3-7 for 80% stoichiometric air, the first column of
concentrations indicates the initial conditions corresponding to zero time.
After 35 psec (assuming no ignition delay) the methane is essentially gone.
The CO has built up to essentially its maximum concentration and some of
the CO has already reacted to form C02. Before CO reaches its peak,
substantial concentrations of hydrocarbon intermediates as well as CHO and
CH20 are observed but these have dropped off by the time CO has peaked.
Concentrations of the radical intermediates H, HO, and 0 reach their peaks
at about the same time as CO, with H being 1.2 mole %, HO being 1.1% and
0 being 0.4%. Molecular hydrogen has also reached a high level (2.3%)
although water is much higher at 18.0%. NO has not yet formed to a
substantial extent, being on the order of 0.2 ppm but its rate of formation,
-------
- 62 -
as indicated in Table 3-7, is quite high. Two species (N and N02) present
in very low concentrations have quite different orders of importance.
Atomic nitrogen plays a major role in NO formation* through N + 02 and
N + OH and it is formed almost exclusively by the reaction N2 + 0 —> NO + N.
Thus N concentration is essentially determined by the 0 concentration.
On the other hand, N02 never builds up to any substantial extent in the
combustion zone and, almost as quickly as it is formed, it returns to NO.
After 600 psec CO and C02 have almost reached their ultimate
concentrations. Species H, HO and 0, while having decreased in concentration,
are still substantially above their equilibrium values. The concentrations
of H2 and H20 have essentially leveled off while NO is still increasing
but at a much slower rate.
After 4.6 msec, species concentrations remain fairly constant,
and although 0 and N atom concentrations are still somewhat above equilibrium,
they are not high enough to cause substantial incremental NO formation.
3.4.2 100% Stoichiometric Air
Table 3-8 summarizes the kinetics calculations for 100%
Stoichiometric air. After 12 psec (no ignition delay) methane has
disappeared and CO has reached its peak. Some of the CO has already reacted
to C02- Concentration of H2 has reached 2% and H20 has reached 13.6%.
Atomic nitrogen is over 0.1 ppm, a high mole fraction for this intermediate,
while NO has just started to form, being slightly in excess of 1 ppm.
Molecular oxygen has dropped from its initial concentration of 19% to
about 4% on its way to 0.5%. The rate of NO formation, at this point, is
extremely high (320,000 ppm/sec) but is dropping off quite rapidly as the
concentration of oxygen atom decreases. By the time 300 ysec have elapsed
the rate of NO formation has dropped to 90,000 ppm/sec and about 50 ppm of
NO has formed.
After 10 msec, CO and C02 concentrations have leveled off at
about 1% and 8% respectively. The concentrations of radical intermediates
have dropped off to within 150% to 200% of their equilibrated values and
the NO formation rate has dropped off to 7,000 ppm/sec. The calculated
concentration of 200 ppm represents an average formation rate of 20,000
ppm/sec, compared to an average formation rate of 150,000 ppm/sec up to
0.3 msec, and an average formation rate of 5,500 ppm/sec up to 100 msec.
At the 100 msec point the instantaneous formation rate has dropped to less
than 4,000 ppm/sec. The rapid initial formation of NO, even though probably
overpredicted because of the high initxai temperature, bears many resemblances
to what might be called "prompt NO" (3-2) .
* It should be noted that recommended rates were not available at the
time of these calculations for additional reactions, which are potentially
important for NO formation. Therefore, the inferences made here should
be regarded as preliminary and subject to further refinement.
(3^2) Fenimore, C. P., 13th Symposium (International) on Combustion,
p. 373, The Combustion Institute, 1971.
-------
- 63 -
TABLE 3-7
KINETIC CALCULATIONS FOR PLUG FLOW CH./AIR COMBUSTION AT 807» STOICH AIR
—4
T = 2097°K
Species
CH4
CO
C02
H
HO
H2
H20
N
NO
N02
0
°2
d(NO)
dt
Branching Zone
t = 0
11.6%
—
—
—
—
—
—
—
—
--
—
18.6%
—
35 y sec
14 ppm
9.4%
1.3%
1.2%
1.1%
2.3%
18.0%
_2
2.7 x 10 ppm
0.2 ppm
-4
10 ppm
0.4%
1.4%
32,000 ppm/sec
Relaxation Zone
600 \i sec
—
5.4%
5.7%
0.4%
0.2%
3.5%
18.3%
_2
1.0 x 10 ppm
4 . 8 ppm
10 ppm
0.02%
0.04%
1,600 ppm/sec
4.6 msec
—
5.3%
5.8%
0.07%
0.05%
3.5%
18.6%
1.6 x 10 ppm
5 . 7 ppm
10 ppm
0.0007%
0.002%
59 ppm/sec
Post-Flame Zone
10 msec
—
5.3%
5.8%
0.06%
0.04%
3.5%
18.6%
1.2 x 10 ppm
5 . 9 ppm
5 x 10 ppm
0.0004%
0.001%
36 ppm/sec
Note: See Section 3-5 for discussion of "zones".
-------
- 64 -
TABLE 3-8
KINETIC CALCULATIONS FOR PLUG FLOW CH./AIR COMBUSTION AT 100% STOICH AIR
T = 2222°K
Species
CH4
CO
C°2
H
HO
H2
H20
N
NO
N02
0
°2
d(NO)
dt
Branching Zone
t = 0
9.5%
—
—
—
—
—
—
—
—
—
—
19.0%
—
12 y sec
5 x 10~ ppm
7.7%
1.1%
2.0%
2.0%
2.0%
13.6%
0 . 11 ppm
1 . 4 ppm
0.0004 ppm
1.4%
4.1%
320,000 ppm/sec
Relaxation Zone
300 y sec
—
3.1%
6.1%
0.7%
1.1%
1.4%
16.1%
0.06 ppm
49 ppm
0.02 ppm
0.4%
1.9%
90,000 ppm/sec
.10 msec
—
1.0%
8.4%
0.06%
0.4%
0.4%
18.2%
0.02 ppm
200 ppm
0.04 ppm
0.03%
0.6%
7,000 ppm/sec
Post-Flame Zone
100 msec
—
0.8%
8.6%
0.04%
0.3%
0.3%
18.4%
0.01 ppm
550 ppm
0.09 ppm
0.02%
0.5%
3,700 ppm/sec
Note: See Section 3.5 for discussion of "zones".
-------
- 65 -
TABLE 3-9
KINETIC CALCULATIONS FOR PLUG FLOW CH,/AIR COMBUSTION AT 1207, STOICH AIR
—— — 4
T = 2044°K
Species
CH4
CO
co2
H
HO
H2
H20
N
NO
N02
0
°2
d(NO)
dt
Branching Zone
t = 0
8.0%
—
—
—
—
—
—
—
—
—
—
19.3%
—
12 y sec
8 ppm
6.7%
0.8%
1.6%
1.6%
1.3%
12.2%
0.02 ppm
0 . 3 ppm
—
1.5%
6.3%
85,000 ppm/sec
Relaxation Zone
900 u sec
. —
0.9%
7.1%
0.2%
0.7%
0.4%
15.1%
0.008 ppm
22 ppm
—
0.2%
3.6%
12,000 ppm/sec
40 msec
—
0.09%
7.9%
0.004%
0.2%
0.04%
15.9%
0.0009 ppm
86 ppm
—
0.02%
3.2%
1,000 ppm/sec
Post-Flame Zone
500 msec
—
0.08%
7.9%
0.004%
0.2%
0.04%
15.9%
0.0009
483 ppm
—
0.02%
3.2%
900 ppm/sec
Note: See Section 3.5 for discussion of "zones".
-------
- 66 -
3.4.3 120% Stoichiometric Air
At 120% Stoichiometric air (Table 3-9) the basic features of
the concentration profiles are the same as with lower air supply, except
that the N atom concentrations are lower and NO is produced more slowly.
At the 12 ysec point it can be seen that the concentrations of H, HO, and 0
are almost the same as in the 100% Stoichiometric air case, yet the N atom
concentration is lower by a factor of 5. As will be discussed later,
N atoms are produced primarily by the reaction N£ + 0 ^ NO + N which
has a 75 kcal activation energy and, therefore, proceeds more slowly at
2044°K than it does at 2222°K. By the same token, NO is produced more
slowly, and again its concentration is lower by a factor of 4 to 5 throughout.
If the temperature were increased to 2222°K, one might expect more rapid NO
formation at 120% Stoichiometric air than at 100% Stoichiometric air.
Indeed, this is observed experimentally (see Section 3.5).
3.5 Discussion
Theoretical calculations based on the recommended rates from
the kinetics survey of methane combustion indicate that, at all mixture
ratios studied, the combustion process under plug flow conditions can be
divided into three zones. For identification and convenience, these zones
will be called the branching zone, the relaxation zone and the post-flame
zone. The basic charapteristics of each zone are as follows: (it should
be noted that the reaction times, provided for reference would vary with the
temperature profile. The features discussed are valid for the general
combustion case.)
(1) The Branching Zone (10-100 ysec duration following ignition
delay, if any):
- is the zone in which the hydrocarbon is consumed.
- the hydrocarbon goes primarily to CO and H20 although some
C02 and H2 are formed in this zone.
- the most important feature of this zone is that the radical
intermediates such as 0, H, HO, etc., build up to extremely
high concentrations and N atoms are substantially in excess
of equilibrium although at low absolute concentrations.
- the individual intermediates do not appear to reach maximum
concentrations at precisely the same time, but the point at
which methane concentration has reached a low level (on the
order of 1 ppm) coincides roughly with the peak concentrations
of the intermediates.
- because of the short times involved, the NO concentration at
the end of the branching zone is quite low (on the order of
1 ppm) but the rate of NO formation is at its peak because
of the high concentrations of the intermediates.
- while very little NO is produced in this zone, it is the high
concentrations of intermediates which set the stage for rapid
NO formation and, therefore, the kinetic details of this zone
are extremely important.
-------
- 67 -
(2) The Relaxation Zone (5-50 msec duration):
- is the zone in which the concentrations of intermediates
approach their ultimate values at the specified temperature.
- the end of this zone is more difficult to define because the
approach to equilibrium is asymptotic. However, the precise
definition is not critical since it is an arbitrary
separation to distinguish this zone from the post-flame
zone in which intermediates have essentially reached
equilibrium. One possible definition of the end of the
zone is the point at which intermediate concentrations
(0, OH, H, N) have reached, e.g., 200% (or 150% or 110%)
of their equilibrium values. Another definition might
involve the rate of change of concentration of these
intermediates .
- in this zone, the rapid formation of NO takes place.
However, the stage has already been set by the high
concentrations of intermediates produced in the branching
zone.
the primary NO forming reactions in this zone, using the
preliminary rate survey, appear to be N£ + 0, N + 02 and
N + HO. However, the concentrations of these species
are not yet equilibrated in this zone. Thus, the rate of
formation of NO can be substantially higher than that
predicted by classical Zeldovich kinetics.
- even without "prompt NO" reactions, which may involve
nitrogeneous species other than atomic and molecular
nitrogen, the high concentrations of intermediates do
result in very rapid or "prompt" NO formation.
- it is still worth searching for "prompt NO" reactions.
The master set of 322 reactions includes several reactions
for which rate data are currently unavailable. An evaluation
of the potential importance of each of the 322 reactions would
provide a starting point for a further screening effort.
With reasonable estimates for the resulting set, the screening
framework would provide a basis for the evaluation of reactions
of importance.
- the formation of N atoms in these calculation is found to
result almost exclusively from the reaction N2 + 0 = NO + N.
The destruction of N atoms is primarily through NO forming
reactions N + 02 = NO + 0 and N + HO = NO + H. Other N-forming
reactions should be sought in the extension of this kinetics
survey.
- the formation of 0 atoms is found to result almost exclusively
from the reaction H + 02 = HO + 0.
-------
- 68 -
the formation of H atoms is found to result, in good part,
from the reaction CO + HO = C02 + H. The destruction of H
atoms occurs, in good part, through the reaction H + 02 =
HO + 0.
- HO is formed in the H + 0? reaction and destroyed in CO + HO
(although not exclusively).
- to summarize the nature of the rapid NO formation observed
in kinetic calculations using the preliminary rate survey:
+ the NO formed depends primarily on the concentrations of
N and 0 atoms.
4- N atom formation depends on the 0 atom concentration
through N£ + 0 = NO + N. N atom destruction depends
on HO + N = NO + H and N + 02 = NO + 0.
+ 0 atom formation depends on the H atom concentration
through H + 02 = HO + 0. 0 atom destruction is
primarily through reaction with CHO at the branching/
equilibration interface and through reaction with
^0 at the equilibration/post flame interface.
+ the H atom formation depends on the CO and HO concen-
trations through CO + HO = CO, + H. Destruction of
H atoms occurs through recombination with HO and CHO
and by the H + C>2 reaction.
+ the initial concentrations of CO, HO, H and 0 in the
equilibration zone are determined by reactions occurring
in the branching zone.
(3) The Post-Flame Zone (50 usec and beyond):
- the concentrations of intermediates are either equilibrated,
or nearly so, and the modified Zeldovich treatment (including
steady state assumptions) is a good approximation of the
behavior in this zone.
The above observations lead one back to questions about a quasi-
global approach in which the hydrocarbon can partially oxidize in one step
and the intermediates can burn out in a detailed manner. The behavior of
the hydrocarbon in the branching zone, at first glance, appears to be
quasi-global in nature. Hydrocarbon reacts very rapidly to produce CO and
H20 before a substantial concentration of NO is produced. However, in
addition to CO and ^0, the hydrocarbon disappearance results in the
appearance of high concentrations of other reactive intermediates.
In the Fourteenth Symposium (International) on Combustion, a
paper by Engleman _et_ al. (3-3) demonstrated that while CO and H2 combustion
in a jet-stirred combustor could be modeled by detailed kinetics, a
quasi-global model for propane was not adequate to predict NO formation.
The global hydrocarbon step in that mechanism was
3-3 V. S. Engleman, W. Bartok, J. P. Longwell, and R. B. Edelman,
Fourteenth Symposium (International) on Combustion, p. 755,
The Combustion Institute (1973).
-------
- 69 -
(I) HC + 02 > CO + H2
The CO and H2 were then allowed to complete combustion by a detailed mech-
anxsm It appears from detailed modeling that the global hydrocarbon step
is actually
(II) HC + 02 > CO + H20 + (reactive intermediates)
(H, HO, H2, 0)
In global step I an approximation to the true picture is made by assuming
all the hydrogen in the hydrocarbon goes through H2, a species which can
participate actively in branching reactions.
Thus, the quasi-global mechanism for hydrocarbon combustion
achieves an approximation of the overshoot of equilibrium by making the
assumption that the hydrocarbon is converted in one step to CO and H£
(see Appendix C). The H2 then participates in branching reactions which
produce high concentrations of intermediates similar to those found in
detailed calculations. However, detailed calculations indicate that the
actual mechanism produces high concentrations of active intermediates
while the hydrocarbon is converted to CO and ^0 (see Tables 3-7, 3-8,
and 3-9 for species concentrations at the end of the branching zone).
These calculations indicate that the quasi-global mechanism does not
adequately predict the overshoot.
3.6 Reactions of Importance at the Interface
Between the Branching Zone and the Relaxation Zone
The interface between the branching zone and the relaxation
zone is an extremely important region from the standpoint of rapid formation
of NO in the flame zone. This interface has been defined in a previous
section as the location where certain combustion intermediates have reached
their peak concentrations. Reactions of importance for formation and
destruction of these intermediates and for NO will be discussed in this
section. It should be reiterated here (and will be discussed further in
the next section) that the events which occur within the branching zone
are very important for the establishment of the high concentrations of
intermediates. The screening that has been done thus far has been more
concerned with determining controlling reactions and less concerned with
the absolute magnitude of rate constants or the concentrations predicted
by the calculations. However, the balance among the reactants, intermediates,
products has been of major concern, since the relative concentrations help
determine the magnitude and direction of the individual reactions.
At the end of the branching zone, NO is just barely starting
to form in ppm level concentrations. At this point the concentrations
of intermediates are high and the rate of NO formation is at its peak.
It is instructive to consider some of the important reactions at this point.
It should be emphasized that while the comments in this section are based
on detailed calculation using a large number of reactions, not all possible
reactions have been included because rate information was unavailable in
-------
- 70 -
some cases. The inclusion of "prompt NO" reactions in these calculations
could result in changes in the NO mechanism under specific conditions.*
Most of the observations discussed below, however, are expected to be valid.
At the point where carbon monoxide starts to be destroyed more
rapidly than it is being produced, the primary destruction reaction is
CO + HO > C02 + H
which accounts for 70-80% of its destruction. This reaction also produces
most of the H at this point although within the branching zone most of the
H comes from hydrocarbon fragments.
The H atoms, at this point, are being destroyed by the reaction
H + 0 • » HO + 0
which accounts for 40-50% of its destruction and also produces essentially
all of the 0 atoms. H is also being destroyed (25-30%) by
CO + H + M *• CHO + M
and (10-15%) by
H + H20 —>• HO +
The 0 atoms, as indicated above are formed entirely* * by
H + 02 - » HO + 0
at the interface, and are destroyed (45-50%) by
CHO + 0 •*•••> CO + HO
and (25-35%) by***
KLO + 0 —*- HO -1- HO
* "Prompt NO" reactions, in this context, are those involving hydrocarbon
fragments which result in production of N atoms; e.g. CH + N~ ->N.
** In the branching zone itself, some 0 atoms are formed by HO + HO ->H-0 4- 0.
*** In part of the branching zone this reaction is a producer of oxygen atoms.
-------
- 71 -
Based on calculations which do not consider the role of hydrocarbon
fragments in the production of N atoms, the following observations are noted.
While 0 atoms are extremely important for the production of NO, the NO
reactions are relatively unimportant in determining 0 atom concentrations.
NO reactions account for less than 1% of the total 0 atom production and
destruction. The main NO-producing reaction at the interface is
N2 + 0 •- >- NO + N
which produces about half of the NO and essentially all of the N atoms.
The reaction
N + 0 >• NO + 0
produces 25-30% of the NO and the reaction
HO + N -—». H + NO
produces about 20% of the NO at the interface. It will be noted that all
of the NO reactions also involve N atoms. In fact the N atoms are pro-
duced and destroyed by these reactions almost exclusively. More than 99%
of the N atoms are produced by
N2 + 0 = N + NO
while about 60% of the N is destroyed by
N + 02 ——^ NO + 0
and 40% is destroyed by
HO + N "' »• H + NO
Using only the reactions for which rate data are available, at one point
within the branching zone as much as 25% of N atoms are destroyed by
reactions with hydrocarbon fragments to produce CRN and CN. These species
do not react directly to produce NO, but produce either N atoms or N2
molecules through subsequent reactions. However, the main N atom reactions
for production and destruction in these calculations were those involving NO.
-------
- 72 -
3.7 Comparison of Theoretical Calculations
with Experimental Results
The comparisons between theoretical calculations discussed
in Section 3.4 and the experimental results discussed in Section 3 are
encouraging. As expected, because of the artificial constraints placed
on the temperature in the theoretical calculations, the NO levels for
the plug-flow simulation of the flat flame are somewhat overpredicted.
However, at this point it is not certain whether the overpredictions are
more a result of the high temperatures early in the calculations or because
the rate constants used for NO formation reactions may be too high. The
latter interpretation is favored by the fact that the theoretical
overprediction continues to be observed in the post-flame zone. The
temperature profile used for reaction screening may have a less dramatic
effect than initially expected because the major portion of the reactions
involving heat release are completed before substantial NO has formed.
The theoretical-experimental comparisons under stoichiometric or
excess air conditions are the closest. Under fuel rich conditions, NO con-
centrations are underpredicted. These underpredictions could be caused by
the lack of reactions between hydrocarbon fragments and molecular nitrogen,
or the high rate of disappearance of active oxygen-containing intermediates.
The high rate of disappearance of both hydrocarbon species and oxygen-
containing intermediates would be caused by the use of isothermal conditions
in the combustion zone where experimentally the temperature is increasing
from room temperature to flame temperature.
Under stoichiometric air conditions, plug flow calculations
overpredict experimentally measured concentrations of NO in the post-flame
zone by about a factor of two. Theoretical calculations indicate 700 ppm
at 150 msec while only 350 ppm are measured; 1200 ppm are calculated at
300 msec while 600 ppm are measured. In the post-flame zone the rate of
NO formation between 200 and 500 msec is measured to be 1500 ppm/sec while
the calculated rate is about 3000 ppm/sec. The comparison between theory
and experiment, on a preliminary basis, indicate that a reduction of the
NO formation rate constants by a factor of two could bring theory in line
with experiment. However, additional theoretical analysis is required
before such reductions may be considered permissible.
A similar picture is obtained at 120 percent stoichiometric air.
Experimental measurements at 40 msec indicate concentrations in the 40-50
ppm range while calculations indicate about 90 ppm. Measurements indicate
concentrations of about 170 ppm at 500 msec while calculations indicate
about 480 ppm. The rate of NO formation is measured to be about 400 ppm/sec
between 300 and 500 msec while calculations indicate about 900 ppm/sec.
Under fuel rich conditions experimental measurements indicate
a very rapid formation of NO in the flame zone and essentially a zero
net formation rate thereafter. Calculations indicate a similar behavior,
with essentially all the NO formed in the relaxation zone, and little or
none in the branching or post-flame zones. However, the levels of NO formed
experimentally are much higher than those calculated in the screening
-------
- 73 -
studies. This is likely to be caused, in part, by the overly rapid calculated
depletion of methane and oxygen in the branching zone because of the high
temperature assumed. However, another possible explanation is because of
the lack of reactions involving hydrocarbons in NO formation in these
calculations. This possibility will be pursued further in Phase II of this
study. Measured NO formation in the flame zone is on the order of 60 ppm,
while the calculated value is on the order of 6 ppm.
-------
- 74 -
4. CONCLUSIONS
1. The survey of 142 reactions appearing in the literature for 25
species in the Clfy/air system resulted in recommended rates for
127 reactions to be used for reaction screening. Since 322 reactions
could be postulated for these 25 species, additional attention is
needed to determine if any of these additional reactions could be
important.
2. Reaction screening using only these 127 reactions or smaller subsets
indicates that between 80% and 120% stoichiometric air for methane
combustion:
- NO formation rate is controlled primarily by oxygen atom
concentration.
- Oxygen atom concentrations are substantially above equilibrium
in the branching zone before significant NO has formed.
- Oxygen atom concentrations have peaked before significant NO
has formed.
- Oxygen atom concentration controls formation of N atoms which
participate in NO reactions. N atom destruction results in NO
formation by N + OH and N + 0 .
- While reaction screening for the 127 reaction set has not uncovered
reactions other than N£ + 0 which might produce N atoms in the
branching zone, it is still worth pursuing the search for other
N-forming reactions that might occur in the branching zone. Such
reactions might produce more substantial overshoots of N atom
concentrations which could provide more rapid NO formation early
in the flame zone.
3. Reaction screening from the 127 reaction set has resulted in narrowing
down the number of reactions that need be considered for NO formation
under the conditions studied. Caution must be exercised not to
extrapolate these conclusions outside the range studied without
rechecking the calculations under the new conditions. Further
screening will be required when other reactions from the 322 reaction
set (25 species) are tested for importance.
4. As additional reactions are studied or estimated the minimum set
of reactions may change:
- The new reaction may be added to the set by itself if it
provides a new path between two important intermediates
(can affect any zone).
- The new reaction may result in the rapid destruction of an
intermediate as it is formed, preventing overshoot from occurring.
In that case the minimum set would be reduced by eliminating
reactions of that intermediate (branching zone).
The new reaction may result in rapid production of an intermediate
in the branching zone and corresponding overshoot in its concentration.
Thus, a new intermediate may play a role in NO formation - possibly
HN, CHN or CN (branching zone).
-------
75 -
5. Premixed flat and focused flames as well as laminar and turbulent
diffusion flames have been studied in the multiburner under both
cold-and hot-wall conditons:
- The burners appeared to behave as idealized examples of the
types they represented. Concentrations and temperature profiles
have been measured in these flames.
- Under certain conditions the curvature in NO formation
(non-linear extrapolation back to the origin) could be measured.
6. Comparisons of isothermal plug-flow calculations at the adiabatic
flame temperature with experimental data indicate:
- NO formation is overpredicted by a factor of two in both the
flame zone and post-flame zone for fuel-lean combustion and in
the post-flame zone for stoichiometric air conditions. NO formation
is underpredicted for fuel rich combustion by an order of magnitude.
+ Overprediction in the post flame zone under fuel lean conditions,
where intermediates other than NO have reached essentially
equilibrium concentrations, indicate that the controlling NO
formation rate, N£ + 0 = NO + N, should be reduced by a factor
of two. (This reaction has a high activation energy and
therefore temperature uncertainty must be taken into account.)
+ The possible interaction between hydrocarbon species and
nitrog'e'rious species should be investigated to determine their
possible role under fuel-rich conditions.
- Extremely high concentration gradients are predicted by the plug
flow calculations which do not include diffusion effects. In a
real system, such concentration gradients would be smoothed
somewhat by diffusion.
- For the purpose of the present study that concerns itself with the
chemistry of combustion and pollutant formation reactions, it would
be desirable to eliminate diffusion effects from the experimental
system. To achieve that goal, the development of an adiabatic
sti-rr«d-combust-or is indicated. Development of this combustor type
which incorporates the principles of mixing in the jet-stirred
combustor and adiabatic operation in the multiburner will be
discussed in the report on Phase II of this contract study.
-------
A-l
APPENDIX A
1.
2*
3.
•
4.
5.
6.
8.
9l
10.
.
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A *
A 11.
A .
A .
A 12.
A 13.
A .
A 14.
A 15.
A 16.
A .
A .
A .
A 17.
A .
A
A
A
A
A
A
A 19.
A .
A 20.
A
A
A
A
A
A
A
A 21.
A .
A .
A .
A .
A 23.
A 22.
.
18.
.
.
.
.
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
4-
4-
4-
4-
4-
4-
+
4-
•f
4-
+
4-
+
4-
•f
+
+
+
+
+
•f
+
•«•
4-
+
-t-
+
4-
-f
4-
4-
+
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
+
+
4-
4-
4-
4-
4-
4-
4-
CHN
CHO
CH20
CH20
CH3
CH30
CH30
CH30
CH4
C02
H
HN
HN
HN
HNO
HNO
HNO
HNO
HNO
HO
HO
HO
HO
H02
H02
H02
H02
H02
H2
H2
H20
H20
H20
H20
H20
N
N
NO
NO
NO
NO
N02
N02
N02
N02
NO?
N2
N2
N20
N20
N20
0
0
4- M
4- M
4- M
4- M
4- M
4- M
REACTIONS FOR 2!
CH2
CH2
CHO
CH3
CH2
CHO
CH2
CH4
CH2
CHO
CH2
CHN
CH2
CN
CHN
CHO
CH2
CH20
CN
CHO
CH2
CH20
CO
CHO
CH2
CH20
CO
C02
CH2
CH3
CHO
CH2
CH20
CH3
CH30
CHN
CN
CHN
CHO
CN
CO
CHN
CHO
CN
CO
C02
CHN
CN
CHN
CHO
CN
CHO
CO
4-
+
4-
4-
•f
•f
4-
+
+
"f
4-
4-
•f
4-
4-
•f
4-
4-
+
•f
4-
4-
4-
-f
4-
4-
4-
4-
+
4-
4-
4-
4-
•f
4-
-f
4-
4-
4-
•f
4-
4-
4-
4-
+
4-
+
CN
CO
CH2
CO
CH2
CH3
CH20
CO
CH3
CO
H
N
H2
HO
HN
NO
N
H20
H
0
H2
HO
02
0
H20
H2
H
H2
HO
H
0
H
0
N
HO
HN
02
NO
H02
HNO
HN
N
HN
NO
N2
HNO
H
+ M
+ M
•f M
-t- M
+ M
4- M
H-0 EXCHANGE
0 TRANSFER
H TRANSFER
H-0 EXCHANGE
N TRANSFER
N TRANSFER
0 TRANSFER
(HO) TRANSFER
H-N EXCHANGE
(HO) ADDITION
(HO) TRANSFER
H-0 EXCHANGE
C-H EXCHANGE
(H2) ADDITION
0 TRANSFER
(HO) TRANSFER
(H2) TRANSFER
(H20) ADDITION
N ADDITION
N TRANSFER
H-N EXCHANGE
H-0 EXCHANGE
N TRANSFER
0 TRANSFER
H-N EXCHANGE
H-0 EXCHANGE
C-N EXCHANGE
H-N EXCHANGE
N TRANSFER
0 TRANSFER
H-N EXCHANGE
X
X
X
X
X
X
X
X
X
1
2
3
4
5
6
7
8
9
X 10
X 11
X 12
X 13
X 14
X 15
X 16
X 17
X 18
X 19
X 20
X 21
X 22
X 23
X 24
X 25
X 26
X 27
X 28
X 29
X 30
X 31
X 32
X 33
X 34
X 35
X 36
X 37
X 38
X 39
X 40
X 41
X 42
X 43
X 44
X 45
X 46
X 47
X 48
X 49
X 50
X 51
X 52
X 53
-------
A-2
MASTER LIST OF REACTIONS FOR 25 ALLOWED SPECIES
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
24.
25.
.
26.
27.
28.
.
29.
30.
.
31.
.
.
,
.
,
.
32.
.
.
*
.
.
.
.
»
.
33.
.
34.
.
.
35.
.
.
.
.
»
36.
,
37.
38.
.
.
39.
40.
.
.
.
41.
42.
43.
44.
CH
CH
CH
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHN
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
+ 02
+ 02
-t- 02
+ CHO
+ CH2
+ CH20
+ CH3
+ CO
+ H
+ H
+ HN
+ HNO
+ HNO
+ HO
+ HO
+ HO
+ HO
+ H02
+ H02
+ H02
+ H2
+ H2
+ H20
-»• H20
+ H20
+ H20
+ N
+ NO
+ NO
"»- N02
+ 0
4- 0
+ 0
+ 02
+ 02
+ 02
4- 02
-t- CHO
+ CHO
+ CH2
+ CH20
+ CH20
+ CH3
+ CH3
+ CH30
+ CH30
+ CH4
+ CH4
+ H
+ H
+ H
+ M
M
=
=
3
=
=
=
S
E
=
=
=
=
=
=
=
3
=
S
=
=
=
=
=
£
=
=
=
s
=
=
=
=
s
=
=
=
=
=
=
=
=
=
s
=
=
=
=
s
=
s
=
=
=
CHO
CO
C02
CN
CH20
CH3
CH30
CH4
CHO
CH2
CN
CH2
CH2
CH20
CHO
CH2
CH20
CN
CHO
CH2
CH20
CH2
CH3
CH2
CH20
CH3
CH30
CN
CHO
CN
CHO
CHO
CN
CO
CHO
CN
CO
C02
CO
CH2
CH20
CH3
CH3
CH30
CH2
CH4
CH20
CH4
CH2
CH20
CH2
CH20
CO
4- 0
+ HO
+ H
+ H
+ CN
+ CN
+ CN
+ CN
+ CN
4- N
+ H2
-t-. ,\2
+ N20
+ N2
+ HN
+ NO
4- N
4- H20
+ HNO
4- N02
+ NO
+ HN
4- N
+ HNO
4- HN
+ NO
4- N
+ HN
+ N2
+ HNO
+ N20
•f N
+ HO
+ HN
+ NO
4- H02
+ HNO
-t- HN
+ H
+ C02
+ CO
+ CO
+ C02
+ CO
4- CH20
+ CO
+ CH20
4- C02
+ CH30
+ CH3
-t- 0
-t- H2
4- M
+ M
C TRANSFER
H TRANSFER
H-N EXCHANGE
H-N EXCHANGE
H-N EXCHANGE
N-(HO) EXCHANGE
N-0 EXCHANGE
H-N EXCHANGE
N-(HO) EXCHANGE
N-0 EXCHANGE
H-N EXCHANGE
N-(HO) EXCHANGE
H-N EXCHANGE
N-(H2) EXCHANGE
H-N EXCHANGE
N-(HO) EXCHANGE
N-(H2) EXCHANGE
CH TRANSFER
N-0 EXCHANGE
N-0 EXCHANGE
N-0 EXCHANGE
O-(HN) EXCHANGE
N-0 EXCHANGE
H TRANSFER
O-(HN) EXCHANGE
C TRANSFER
H-0 EXCHANGE
H-0 EXCHANGE
H TRANSFER
H TRANSFER
H-0 EXCHANGE
H-0 EXCHANGE
4- M
X 54
X 55
X 56
X 57
X 58
X 59
X 60
X 61
X 62
X 63
X 64
X 65
X 66
X 67
X 68
X 69
X 70
X 71
X 72
X 73
X 74
X 75
X 76
X 77
X 78
X 79
X 80
X 81
X 82
X 83
X 84
X 85
X 86
X 87
X 88
X 89
X 90
X 91
X 92
X 93
X 94
X 95
X 96
X 97
X 98
X 99
X100
X101
X102
X103
X104
X105
X106
-------
A-3
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
*
*
*
*
45.
•
46*
47.
.
.
.
.
48.
.
.
*
49.
*
.
.
50.
.
51.
•
.
*
52.
.
.
.
.
.
53.
.
.
.
.
54.
.
.
55.
.
.
.
.
56.
.
.
57.
.
.
.
*
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CH2
CH2
CH2
CH2
CH2
CH2
CH2
CH2
CH2
CH2
CH2
CH2
CH2
CH2
CH2
CH2
CH2
CH2
CH2
CH2
CH2
CH2
CH2
+
+
+
+
•f
+
•+•
+
•*•
+
+
+
+
•f
+
+
•f
+
+
+
•f
+
+
+
+
•f
•f
+
+
4-
+
•f
•f
+
+
•f
•f
•f
+
+
+
•f
+
•f
+
•f
•f
+
•f
+
+
•f
•f
HN
HN
HN
HNO
HNO
HO
HO
HO
HO
H02
H02
H2
H2
H2
H2
H20
H20
H20
H20
N
N
NO
NO
NO
N02
N2
0
0
02
02
CH20
CH30
CH4
C02
H
HN
HNO
HNO
HNO
HO
HO
HO
H02
H02
H02
H2
H2
H20
H20
H20
H20
NO
N
MASTER LIST OF REACTIONS FOR 25 ALLOWED SPECIES
H-0 EXCHANGE
H TRANSFER
N-(HO) EXCHANGE
H-O EXCHANGE
H-0 EXCHANGE
H-O EXCHANGE
H TRANSFER
H-0 EXCHANGE
H-0 EXCHANGE
+ M
+ M
M
M
=
=
s
=
=
s:
a
=
E
S
=
r
=
=
s
=
s
ss
=
=
=
=
=
=
s
=
sz
=
=
=
s
=
=
=
X
s
=
s
=
=
=
s
=
=
S5
s
s
r
=
s
c
3
=
CH?
CH20
CN
CH2
CH20
CH2
CH20
CO
C02
CH20
C02
CH2
CH20
CHS
CH30
CH2
CH20
CH3
CH30
CN
CO
CN
CO
C02
C02
CN
CO
C02
CO
C02
CH4
CH20
CH3
CH20
CHS
CHS
CH20
CHS
CH30
CH20
CHS
CH30
CH20
CHS
CH30
CH3
CH4
CH20
CH3
CH30
CH4
CH20
CN
+ NO
+ N
+ H20
+ N02
+ NO
+ 02
+ 0
+ H20
+ H2
+ 02
+ H20
+ HO
+ H
+ 0
+ H02
+ HO
+ 02
+ 0
+ HO
+ HN
+ H02
+ HNO
+ HN
+ HNO
+ HNO
+ HO
+ H
+ H02
+ HO
+ CO
+ CHS
+ CHS
+ CO
+ N
+ HN
+ NO
+ N
+ H
+ 0
+ HO
+ 02
+ 0
+ H
+ H2
+ HO
+ H
+ 0
+ N
+ H2
+ M
0-(H2) EXCHANGE
(H2) ADDITION
H-0 EXCHANGE
0-(H2) EXCHANGE
(H2) TRANSFER
N-(HO) EXCHANGE
N-(HO) EXCHANGE
H-0 EXCHANGE
H-0 EXCHANGE
N-(HO) EXCHANGE
H-0 EXCHANGE
H TRANSFER
H-0 EXCHANGE
-------
A-4
A
A .
A
A .
A .
A 58.
A .
A .
A .
A
A
A 59.
A991.
A .
A .
A .
A .
A 60.
A .
A .
A .
A .
A .
A .
A .
A .
A .
A .
A .
A .
A .
A 61.
A •
A
A 62.
A .
A 63.
A .
A 64.
A 65.
A .
A 66.
A .
A .
A .
A .
A992.
A .
A
A .
A
A .
A .
CH2
CH2
CH2
CH2
CH2
CH2
CH2
CH2
CH20
CH20
CH20
CH20
CH20
CH20
CH20
CH20
CH20
CH20
CH20
CH20
CH20
CH20
CH20
CH20
CH20
CH20
CH20
CH20
CH20
CH20
CH3
CH3
CH3
CH3
CH3
CH3
CH3
CH3
CH3
CH3
CH3
CH3
CH3
CH3
CH3
CH3
CH3
CH30
CH30
CH30
CH30
CH30
CH30
+ NO
+ N02
+ N20
+ 0
+ 0
+ 02
+ 02
+ 02
+ CH20
+ CH4
+ H
+ H
+ HN
+ HN
+ HNO
+ HNO
+ HO
+ HO
+ H02
+ H2
+ H2
+ H2
+ H20
+ H20
+ H20
+ N
+ 0
+ 0
+ 02
+ C02
+ H
+ HN
+ HNO
+ HNO
+ HO
+ HO
+ H02
+ HO?
+ H2
+ H20
+ H20
+ NO
+ N02
+ N20
+ 0
+ 02
+ H
+ HN
+ HNO
+ HO
+ H2
+ H20
MASTER LIST OF REACTIONS FOR 25 ALLOWED SPECIES
N-1H2) EXCHANGE
0 TRANSFER
0 TRANSFER
0 ADDITION
0-(H2) EXCHANGE
-f M
+ M
+ M
+ M
+ M
=
=
=
=
=
=
-
=
=
=
=
=
:=
a
=
a
=
=
=
=
=
=
=
=
=
s;
=
a
=
=
=
=
3
=
=
3
=
S
£
=
=
a
s
=:
s
s
=
a
=
=
=
=
=
CN
CH20
CH20
CH20
CO
CH20
CO
C02
CO
CH4
CHS
CH3
CH30
CHS
CH30
CH3
CH30
CH3
CH30
CH30
CH3
CH30
CH4
CH3
CH30
CH4
CN
CO
C02
C02
CH30
CH4
CH4
CH30
CH4
CH30
CH4
CH30
CH4
CH4
CH30
CH4
CH30
CH30
CH30
CH30
CH30
CH4
CH4
CH4
CH4
CH4
CH4
+ H20
+ NO
+ N2
+ H2
+ 0
+ H20
+ H2
+ H2
+ C02
+ CH30
+ 0
+ NO
+ N
+ N02
+ NO
i- 02
+ 0
+ 02
+ HO
+ H
+ 0
-I- H02
+ HO
+ 02
+ H20
+ H20
+ H2
+ H20
+ CO
+ N
+ HN
+ NO
* H
+ 0
+ HO
+ 02
+ H
-I- H2
+ HO
+ N
+ NO
+ N2
+ 0
+ 0
+ NO
+ N02
+ 02
+ HO
+ H02
M
+ M
+ M
M
0-(H2! EXCHANGE
C TRANSFER
(H2) ELIMINATION
-------
A-5
MASTER LIST OF REACTIONS FOR 25 ALLOWED SPECIES
A •
A t
A .
A 67.
A *
A .
A993.
A 68.
A .
A 69.
A 70.
A 71.
A 72.
A 73.
A 74.
A 75.
A 77.
A 78.
A 79.
A 80.
A 81.
A 82.
A
A 83.
A 84.
A 85.
A 86*
A 87.
A 88.
A 89.
A 90.
A 92.
A 91.
A .
A 93.
A 94.
A .
A 95.
A 96.
A 97.
A 98.
A 99.
A100.
A101.
A102.
A .
A .
A103.
A104.
A .
A .
A .
A
CN
CN
CN
CN
CN
CN
CN
CN
CN
CO
CO
CO
CO
CO
CO
CO
CO
CO
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
HN
HN
HN
HN
HN
HN
HN
HN
HN
+ HO
+ H02
+ HO?
+ NO
+ N02
+ NO?
4- 0
4- 02
4- 02
+ HNO
+ HO
+ HO?
+ H20
4- NO
4- N02
+ N20
4- 0
-t- 02
4- H
4- HN
+ HNO
+ HNO
4- HNO
+ HO
+ HO
+ H02
+ H02
+ H02
4- H20
4- N
+ NO
4- NO
+ NO
4- N02
+ N02
4- NO?
* N02
+ N2
4- N20
4- N20
-f- N20
4- 0
+ 02
-t- 02
4- HN
4- HNO
-t- HNO
4- HO
4- HO
4- H02
4- H02
4- H02
4- H20
+ M
M
+ M
+ M
+ M
a
a
s
a
=
a
=
s
=
s
=
s
=
=
=
s
=
a
X
=
s
3
=
=
=
S
a
s
a
s
s
=
=
s
=
=
^
=
Si
=
y
=
s
=
s
=
=
=
c
s:
=
s
=
CO
CO
C02
CO
CO
C02
CO
CO
C02
C02
C02
C02
C02
C02
C02
C02
C02
C02
H2
H2
HN
H2
H20
H2
H20
HO
H2
H20
HO
HN
HN
HNO
HO
HN
HNO
HO
H02
HN
HN
HNO
HO
HO
HO
H02
H2
H2
H20
H2
H20
HNO
H2
H20
HNO
-I- HN
+ HNO
+ HN
+ N2
+ N20
* N2
.+ N
+ NO
+ N
+ HN
+ H
+ HO
+ H2
4- N
4- NO
+ N2
4- 0
+ N
+ HO
4- NO
4- N
4- 0
4- HO
4- 02
4- 0
4- H2
4- 0
4- N
4- 02
4- 0
4- NO
4- N
4- N
4- NO
4- N
4- N2
4- 0
4- N2
4- N20
4- N2
4- NO
4- N
4- HO
4- N02
4- NO
4- H2
4- M
4- M
4- M
4- M
4- M
4- M
4- M
N-0 EXCHANGE
N-0 EXCHANGE
C-H EXCHANGE
N-0 EXCHANGE
C-N EXCHANGE
N-0 EXCHANGE
C TRANSFER
H-N EXCHANGE
N TRANSFER
H-N EXCHANGE
H-N EXCHANGE
H-N EXCHANGE
0 TRANSFER
H-N EXCHANGE
H-0 EXCHANGE
0 TRANSFER
X213
X214
X215
X216
X217
X218
X219
X220
X221
X222
X223
X224
X225
X226
X227
X228
X229
X230
X231
X232
X233
X234
X235
X236
X237
X238
X239
X240
X241
X242
X243
X244
X245
X246
X247
X248
X249
X250
X251
X252
X253
X254
X255
X256
X257
X258
X259
X260
X261
X262
X263
X264
X265
-------
A-6
A105.
A
A106.
A
A
A107.
A109.
A108.
A110.
A .
Alll.
A112.
A .
A
A113.
A .
A t
All*.
A .
A .
A115.
A .
A .
A
A116.
A117.
A118.
A .
A119.
A120.
A .
A121.
A122.
A .
A123.
A .
A *
A .
A124.
A125.
A126.
A127.
A129.
A130.
A131.
A132.
A133.
A .
A134.
A135.
A136.
A137.
A138.
HN
HN
HN
HN
HN
HN
HN
HN
HN
HN
HN
HNO
HNO
HNO
HNO
HNO
HNO
HNO
HNO
HNO
HNO
HNO
HNO
HNO
HO
HO
HO
HO
HO
HO
HO
HO
HO
H2
H2
H2
H2
H2
N
N
N
N
N
N
N
N
N
N
NO
NO
NO
NO
NO
+ NO
+ NO
+ NO?
+ N02
+ N02
+ N20
+ 0
+ 0
+ 02
+ 02
+ 02
+ HNO
4- HO
+ HO
+ H02
+ N
+ NO
4- NO
+ N02
4- 0
+ 0
+ 02
+ 02
+ HO
4- HO
+ H02
+ H20
+ NO
+ N02
+ N20
+ 0
+ 02
4- NO
-i- N02
+ N20
+ 0
+ 02
+ N
+ NO
+ NO
+ N02
+ N02
+ N02
+ N20
+ 0
4- 02
+ 02
+ NO
4- NO
4- N02
+ N20
+ 0
4- M
4- M
4- M
4- M
4- M
4- M
4- M
4- M
4- M
MASTER LIST OF REACTIONS FOR 25 ALLOWED SPECIES
H-N EXCHANGE
N-0 EXCHANGE
H-N EXCHANGE
HNO
HO
HNO
HO
H02
HNO
HNO
HO
HNO
HO
H02
HO
H20
H2
H20
H20
HO
HO
H02
H02
HO
H02
HO
H02
H2
H20
H20
H02
H02
H02
H02
H02
H02
H20
H20
H20
H20
H20
N2
N2
N20
NO
N2
N20
NO
NO
NO
N02
N2
N20
N20
N02
N02
-i- N
+ N2
+ NO
+ N20
+ N2
-t- N2
4- N
-t- 0
+ NO
+ N
•+• N
+ N20
-t- N02
4- NO
* N02
+ N2
+ N20
+ N2
+ N20
+ NO
+ N
4- N02
+ NO
+ 02
4- 0
+ 02
+ H2
4- N
+ NO
+ N2
+ 0
4- N
4- NO
+ N2
t- 0
4- 0
-»• NO
+ 02
+ 0
+ N2
+ 0
4- 02
4- 0
-i- 02
-»• N2
+ M
4- M
4- M
M
4- M
M
-»• M
H-0 EXCHANGE
H-N EXCHANGE
H-0 EXCHANGE
H-0 EXCHANGE
N TRANSFER
N-0 EXCHANGE
H-N EXCHANGE
N-0 EXCHANGE
H-0 EXCHANGE
H TRANSFER
H-0 EXCHANGE
0 TRANSFER
0 TRANSFER
0 TRANSFER
(H2> ADDITION
0 TRANSFER
N ADDITION
X266
X267
X268
X269
X270
X271
X272
X273
X274
X275
X276
X277
X278
X279
X280
X281
X282
X283
X284
X285
X286
X287
X288
X289
X290
X291
X292
X293
X294
X295
X296
X297
X298
X299
X300
X301
X302
X303
X304
X305
X306
X307
X308
X309
X310
X311
X312
X313
X314
X315
X316
X317
X318
-------
A-7
A139t NO + 02
A140. N2 -i-O + M
A141. N2 + 02
A142. 0 +0 + M
MASTER LIST OF REACTIONS FOR 25 ALLOWED SPECIES
0
= NO?
= N20 + M
= N20 + 0
= 02 + M
X319
X320
X321
X322
-------
B-l
APPENPIX B
CROSS-INDEX OF REACTIONS FOR 25 SPECIES
As an aid to seeking competitive reactions between the same
species or reactions between a given species and competitive partners,
a complete sorting of the reactions for each species is provided in
this section. For example, if one were seeking reactions to break the
NsN bond in molecular nitrogen, all the reactions of N2 are listed to-
gether. If one were seeking reactions to produce N atoms, all the
reactions involving N atoms are listed together. These lists are also
useful in determining the probable relative importance of competing
reactions as well as determining whether the relative rates used for
competing reactions are reasonable.
The species covered in this Appendix are:
CH HN
CHN HNO
CHO HO
CH2 HO 2
CH2° H2
CH3 H20
CH 0 N
CH4 NO
CN NO
CO N
H 0
0,
-------
B-2
REACTI
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
1.
2.
3.
4.
5.
6.
7.
8.
9.
10.
11.
12.
13.
14.
15.
16.
17.
18.
19.
20.
21.
22.
23.
24.
25.
ONS OF CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
CH
4-
4-
4-
4-
4-
+
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
CHN
CHO
CH20
CH20
CH3
CH30
CH30
CH30
CH4
C02
H 4- M
HN
HN
HN
HNO
HNO
HNO
HNO
HNO
HO
HO
HO 4- M
HO
H02
H02
= CH2
= CH2
= CHO
= CH3
= CH2
= CHO
= CH2
= CH4
= CH2
= CHO
» CH2
= CHN
= CH2
= CN
= CHN
« CHO
= CH2
= CH20
= CN
= CHO
= CH2
= CH20
= CO
= CHO
= CH2
+ CN
+ CO
+ CH2
4- CO
+ CH2
+ CH3
* CH20
+ CO
* CH3
+ CO
+ H
* N
* H2
4- HO
4- HN
+ NO
+ N
+ H20
4- H
4- 0
* H2
+ HO
* 02
M
4- M
-------
B-3
REACTIONS OF CH
A 26. CH + H02 = CH20 «• 0
A 27. CH + H02 = CO + H20
A 28. CH + H02 » C02 + H2
A 29. CH •»• H2 = CH2 + H
A 30. CH + H2 + M * CH3 * M
A 31. CH + H20 « CHO + H2
A 32. CH + H20 « CH2 * HO
A 33. CH + H20 = CH20 * H
A 34. CH * H20 = CH3 + 0
A 35. CH + H20 * M = CH30 «• M
A 36. CH + N + M = CHN + M
A 37. CH + N = CM + H
A 38. CH + NO » CHN •*• 0
A 39. CH + NO = CHO + N
A 40. CH + NO = CN + HO
A 41. CH + NO « CO + HN
A 42. CH + N02 « CHN * 02
A 43. CH + N02 « CHO + NO
A 44. CH + ,N02 = CN + H02
A 45. CH + N02 = CO + HNO
A 46. CH •»• N02 » C02 + HN
A 47. CH + N2 « CHN * N
A 48. CH * N2 = CN + HN
A 49. CH + N20 = CHN + NO
A 50. CH + N20 = CHO + N2
-------
B-4
REACTIONS OF CH
A 51. CH + N20 » CM + HNO
A 52. CH + 0 + M = CHO «• M
A 53. CH + 0 » CO * H
A 54. CH + 02 = CHO * 0
A 55. CH + 02 'CO * HO
A 56. CH + 02 = C02 + H
-------
B-5
REACTIONS OF CHM
C 36. CHN + M
A 57. CHN + M
B 1. CHN 4- CH
A 58. CHN * CHO
A 59. CHN * CH2
A 60. CHN + CH20
A 61. CHN 4- CH3
A 62. CHN + CO
C 12. CHN 4- H
A 63. CHN 4- H
A 64. CHN + H
A 65. CHN 4- HN
A 66. CHN * HNO
A 67. CHN + HNO
C 15. CHN 4- HO
A 68. CHN 4- HO
A 69. CHN * HO
A 70. CHN 4 HO
A 71. CHN 4- HO
A 72. CHN * H02
A 73. CHN 4- H02
A 74. CHN 4- H02
A 75. CHN 4- H2
A 76. CHN 4- H2
A 77. CHN 4 H20
CH + N
CN + H
CH2 * CN
CH20 4- CN
CH3 + CN
CH30 + CN
CH4 + CN
CHO 4- CN
CH -f HN
CH2 * N
CN 4- H2
CH2 4- N2
CH2 4- N20
CH20 4- N2
CH 4- HNO
CHO 4- HN
CH2 4- NO
CH20 4- N
CN 4 H20
CHO 4- HNO
CH2 4- N02
CH20 + NO
CH2 4 HN
CH3 * N
CH2 4- HNO
4- M
4- M
-------
B-6
REACTIONS OF CHN
A 78. CHN + H20 = CH20 * HN
A 79. CHN + H20 = CH3 + NO
A 80. CHN + H20 = CH30 + N
C 47. CHN + N = CH + N2
A 81. CHN + N = CN + HN
C 49. CHN + NO = CH * N20
A 82. CHN + NO = CHO + N2
A 83. CHN + NO = CM + HNO
A 84. CHN + N02 = CHO + N20
C 38. CHN +0 = CH + NO
A 85. CHN +0 = CHO + N
A 86. CHN -i-O = CN + HO
A 87. CHN +0 = CO + HN
C 42. CHN +02 = CH + N02
A 88. CHN + 02 = CHO + NO
A 89. CHN +02 = CN + H02
A 90. CHN +02 = CO + HNO
A 91. CHN +02 = C02 + HN
-------
B-7
REACTI
C 52.
A 92.
B 2.
B 58.
A 93.
A 94.
C 3.
A 95.
A 96.
A 97.
C 6.
A 98.
A 99.
A100.
A101.
A102.
A103.
C 62.
C 10.
C 20.
A104.
A105.
A106.
C 16.
C 68.
ONS OF C
CHO
CHO
CHO +
CHO +
CHO +
CHO +
CHO +
CHO +
CHO +
CHO +
CHO +
CHO +
CHO +
CHO +
CHO +
CHD «•
CHO +
CHO +
CHO +
CHO +
CHO +
CHO +
CHO +
CHO +
CHO +
HO
+ M
+ M
CH
CHN
CHO
CHO
CH2
CH2
CH20
CH20
CH3
CH3
CH3
CH30
CH30
CH*
CH4
CN
CO
H
H
H + M
H
HN
HN
= CH
= CO
= CH2
= CH20
= CH2
= CH20
* CH
= CH3
= CH3
= CH30
= CH
= CH2
- CH4
» CH20
= CH4
= CH2
= CH20
= CHN
* CH
- CH
« CH2
= CH20
= CO
* CH
= CHN
* 0
+ H
+ CO
* CM
* C02
+ CO
+ CH20
+ CO
* C02
+ CO
* CH30
+ CH20
+ CO
+ CH20
+ C02
•»• CH30
+ CH3
* CO
* C02
+ HO
* 0
+ H2
+ HNO
+ HO
M
M
M
-------
REACTIONS OF CHO
B-8
A107.
A108.
A109.
C 72.
A110.
Alii.
C 24.
A112.
A113.
All*.
A115.
A116.
A117.
C 31.
A118.
A119.
A120.
A121.
A122.
A123.
A124.
A125.
C 39.
C 85.
A126.
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHD
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
CHO
-t- HN
+ HN
* HN
+ HNO
+ HNO
+ HNO
+ HO
+ HO
+ HO
+ HO
+ HO
+ H02
+ H02
+ H2
+ H2
+ H2
+ H2
-»• H2 + M
+ H20
+ H20
+ H20
+ H20
•»• N
* N
+ N
= CH2
= CH20
= CN
= CHN
= CH2
= CH20
= CH
= CH2
= CH20
= CO
= C02
= CH20
= C02
= CH
= CH2
= CH20
= CH3
= CH30
= CH2
= CH20
» CH3
= CH30
= CH
= CHN
= CN
+ NO
+ N
+ H20
+ H02
+ N02
•»• NO
+ H02
+ 02
+ 0
+ H20
•f H2
+ 02
-»• H20
+ H20
••- HO
* H
+ 0
+ H02
+ HO
•»• 02
+ 0
+ NO
•»• 0
+ HO
M
-------
B-9
REACTIONS OF CHO
A127. CHO + N = CO •»> HN
C 43. CHO + NO = CH + N02
C 88. CHO + NO = CHN S- 02
A128. CHO * NO = CN + H02
A129. CHO + NO » CO + HNO
A130. CHO + NO = C02 •*• HN
A131. CHO + N02 « C02 * HNO
C 50. CHO * N2 = CH + N20
C 82. CHD + N2 « CHN + NO
A132. CHO * N2 = CN + HNO
C 84. CHO * ,M20 « CHN + N02
C 54. CHO +0 = CH + 02
A133. CHO * 0 « CO + HO
A134. CHO * 0 = C02 + H
A135. CHO -1-02 = CO * H02
A136. CHO +02 = C02 + HO
-------
B-10
REACTIONS OF CH2
C 11. CH2
B 59. CH2
D 3. CH2
B 95. CH2
C 5. CH2
C 7. CH2
C 98. CH2
A137. CH2
C 9. CH2
C102. CH2
A138. CH2
A139. CH2
C 1. CH2
C 2. CH2
C
A
C 29. CH2
A1<»1. CH2
C 75. CH2
A142. CH2
C 77. CH2
A143. CH2
A144. CH2
A145. CH2
C 32. CH2 +• HO
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
+
4-
4-
4-
4-
4-
4-
4-
4-
4- M
CHN
CHO
CHO
CH2
CH20
CH20
CH20
CH3
CH30
CH30
CH4
CN
CO
C02
C02
H
H * M
HN
HN
HNO
HNO
HNO
HNO
HO
= CH
= CH3
- CH
« CH3
= CH
= CH
= CHO
= CH4
= CH
= CHO
= CH20
= CH3
= CH
= CH
= CHO
= CH20
= CH
= CH3
= CHN
= CH3
= CHN
= CH20
= CH3
= CH30
= CH
4-
4-
4-
4-
4-
+
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
H
CN
CH20
CO
CH3
CH30
CH3
CO
CH4
CH4
CH3
CH3
CHN
CHO
CHO
CO
H2
H2
N
H20
HN
NO
N
H20
M
M
-------
B-ll
REACTIONS OF CH2
C118. CH2 4- HO
A146. CH2 4- HO
A147. CH2 + HO
A148. CH2 4- HO
C122. CH2 4- H02
A149. CH2 4- H02
A150. CH2 + H02
A151. CH2 4- H02
A152. CH2 4- H2
A153. CH2 4- H2
A154. CH2 4- H20
A155. CH2 4- H20
A156. CH2 + H20
A157. CH2 * H20
C 13. CH2 + N
C 63. CH2 4- N
A158. CH2 4- N
C 17. CH2 4- NO
C 69. CH2 4- NO
C107. CH2 + NO
A159. CH2 4- NO
A160. CH2 4- NO
C 73. CH2 4- N02
CHO. CH2 4- N02
A161. CH2 4- N02
= CHO 4- H2
= CH20 4- H
= CH3 + 0
4- M = CH3D 4- M
= CHO 4- H20
= CH20 4- HO
= CH3 4- 02
= CH30 4- 0
= CH3 4- H
4- M = CH4 + M
= CH20 4- H2
= CH3 4- HO
= CH30 4- H
= CH4 4- 0
= CH 4- HN
= CHN 4- H
= CN * H2
= CH 4- HNO
= CHN 4- HO
= CHO 4 HN
= CH20 4 N
= CN * H20
= CHN * H02
= CHO 4- HNO
= CH20 4 NO
-------
B-12
REACTIONS OF CH2
C 65. CH2 •*• N2
C 66. CH2 + N20
A162. CH2 + NI20
C 21. CH2 + 0
C104. CH2 «• 0
A163. CH2 +0
A164. CH2 + 0
C 25. CH2 + 02
C112. CH2 + 02
A165. CH2 + 02
A166. CH2 + 02
A167. CH2 + 02
M
CHN + HM
CHN + HNO
CH20 + N2
CH •«• HO
CHO + H
CH20
CD * H2
CH •»• H02
CHO •»• HO
CH20 -»• 0
CO -»- H20
C02 + H2
M
-------
B-13
REACTIONS OF CH20
C 22. CH20
C105. CH20
C163. CH20
A168. CH20
B 3. CH20
B 4. CH20
B 60. CH20
B 96. CH20
B 97. CH20
0 7. CH20
0 98. CH20
B137. CH20
C100. CH20
A169. CH20
C103. CH20
C138. CH20
A170. CH20
C 58. CH20
C 94. CH20
C140. CH20
C 33. CH20
C119. CH20 + H
C146. CH20
A171. CH20
A172. CH20
+• M
+ M
4- M
+ M
+ CH
+ CH
* CHN
+ CHO
* CHO
+ CH2
+ CH2
+ CH2
+ CH20
4- CH20
* CH3
+ CH3
* CH4
+ CN
4- CO
+ CO
* H
4- H
4- H
4- H
4- H + M
= CH
= CHO
= CH2
= CO
= CHO
= CH3
= CH30
= CH3
= CH30
= CH
» CHO
- CH4
= CHO
= CH4
= CHO
= CH2
= CH3
= CHN
= CHO
= CH2
= CH
= CHO
= CH2
» CH3
= CH30
*
4-
4-
4-
*
*
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
*
4-
HO
H
0
H2
CH2
CO
CN
C02
CO
CH30
CH3
CO
CH30
C02
CH4
CH30
CH30
CHO
CHO
C02
H20
H2
HO
0
4- M
+ M
4- M
* M
4- M
-------
B-14
REACTIONS OF CH20
C 78. CH20 + HN
C143. CH20 + HN
A173. CH20 + HN
A174. CH20 * HN
A175. CH20 + HNO
A176. CH20 + HNO
C123. CH20 + HO
C149. CH20 + HO
A177. CH20 + HO
A178. CH20 + HO
A179. CH20 + H02
C154. CH20 + H2
A180. CH20 + H2
A181. CH20 + H2
A182. CH20 «• H2
A183. CH20 * H20
A184. CH20 * H20
A185. CH20 * H20
C 18. CH20 + N
C 70. CH20 + N
C108. CH20 * N
C159. CH20 + N
A186. CH20 + N
C 74. CH20 •»• NO
Clll. CH20 + NO
= CHN + H20
= CH2 * HNO
= CH3 + NO
= CH30 * N
= CH3 + N02
= CH30 + NO
» CHO + H20
= CH2 + H02
= CH3 + 02
= CH30 * 0
= CH30 * 02
= CH2 + H20
= CH3 * HO
« CH30 * H
= CH4 •«• 0
= CH3 * H02
= CH30 + HO
= CH4 * 02
= CH + HNO
= CHN + HO
= CHO + HN
= CH2 + NO
= CN * H20
= CHN + H02
= CHO •»• HMO
-------
B-15
REACTIONS OF CH20
C161. CH20 + NO = CH2 * N02
C 67. CH20 + N2 = CHN * HNO
C162. CH20 * N2 = CH2 * N20
C 26. CH20 +0 = CH + H02
C113. CH20 +0 = CHO «• HO
C165. CH20 +0 = CH2 + 02
A187. CH20 +0 = CO * H20
A188. CH20 +0 = C02 + H2
C116. CH20 +02 = CHO + H02
A189. CH20 +02 = C02 + H20
-------
B-16
REACTIONS OF CH3
C 30. CHS
C141. CH3
B 5. CH3
B 61. CH3
D 6. CH3
B 98. CH3
B 99. CH3
D 9. CH3
0103. CH3
D138. CH3
C139. CH3
C170. CH3
C 59. CH3
C 4. CH3
C 95. CH3
C 96. CH3
A190. CH3
C152. CH3 +• H
A191. CH3
A192. CH3 * HN
A193. CH3
A194. CH3
C155. CH3 -»• HO
C180. CH3
A195. CH3
4-
4-
4-
-f
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4- M
4- M
CH
CHN
CHO
CHO
CHO
CH2
CH20
CH20
CH3
CH30
CN
CO
CO
C02
C02
H
H + M
HN
HNO
HNO
HO
HO
HO
= CH
= CH2
= CH2
» CH4
= CH
= CH2
= CH4
= CH
= CHO
= CH2
= CH2
= CH20
» CHN
= CH
» CHO
= CHO
= CH30
= CH2
= CH4
« CH4
* CH30
= CH4
= CH2
» CH20
= CH30
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
H2 + M
H + M
CH2
CN
CH30
CH20
CO
CH4
CH4
CH30
CH4
CH4
CH2
CH20
CH2
CH20
CO
H2
4- M
N
HN
NO
H20
H2
H
-------
B-17
REACTIONS OF CH3
A196. CH3 4- HO
C183. CH3 4- H02
A197. CH3 + H02
A198. CH3 4- H02
A199. CH3 4- H2
A200. CH3 + H20
A201. CH3 + H20
C 76. CH3 4- N
C142. CH3 4- N
C 79. CH3 * NO
C144. CH3 4- NO
C173. CH3 4- NO
A202. CH3 4- NO
C175. CH3 4- N02
A203. CH3 4- N02
A204. CH3 4- N20
C 34. CH3 * 0
C120. CH3 4- 0
C147. CH3 4- 0
C171. CH3 * 0
A205. CH3 4- 0
C124. CH3 + 02
C150. CH3 * 02
C177. CH3 4- 02
A206. CH3 + 02
CH4 + 0
CH20 + H20
CH30 + HO
CH4 + 02
CH4 + H
CH30 + H2
CH4 •«• HO
CHN 4- H2
CH2 4- H.M
CHN 4- H20
CH2 4- HNO
CH20 4- HN
CH30 4- N
CH20 4- HNO
CH30 + NO
CH30 4- N2
CH + H20
CHO 4- H2
CH2 4- HO
CH20 * H
CH30
CHO 4- H20
CH2 4- H02
CH20 4- HO
CH30 4- 0
-------
B-18
REACTIONS OF CH30
C 35. CH30
C121. CH30
C148. CH30
C172. CH30
C205. CH30
B 6. CH30 * CH
B 7. CH30
B 8. CH30 4- CH
B100. CH30
B101. CH30
D102. CH30
B138. CH30
D170. CH30
C 60. CH30
C 97. CH30
C190. CH30
C156. CH30
C181. CH30 4- H
C195. CH30
A207. CH30
C193. CH30
A208. CH30
A209. CH30
C184. CH30
C197. CH30
+ M
4- M
+ M
4- M
4- M
4- CH
+ CH
+ CH
4- CHO
+ CHO
4- CH2
+ CH2
4- CH3
4- CN
4- CO
4- CO
4- H
4- H
4- H
4- H
4- HN
4- HN
4- HNO
4- HO
4- HO
= CH
» CHO
= CH2
= CH20
= CH3
= CHO
= CH2
= CH4
= CH20
= CH4
= CHO
» CH20
= CH20
= CHN
= CHO
= CH3
= CH2
» CH20
= CH3
= CH4
= CH3
= CH4
= CH4
= CH20
= CH3
4- H20 +
4- H2 4-
4- HO +
4- H +
4-0 4-
4- CH3
4- CH20
4- CO
4- CH20
+ C02
4- CH4
4- CH3
+ CH4
4- CH20
4- CH20
4- C02
4- H20
4- H2
4- HO
4- 0
4- HNO
4- NO
4- N02
4- H20
4- H02
M
M
M
M
M
-------
B-19
REACTIONS OF CH30
A210. CH30
C200. CH30
A211. CH30
A212. CH30
C 80. CH30 4- N
C145. CH30
C174. CH30
C202. CH30
C176. CH30
C203. CH30
C20*. CH30
C125. CH30 + 0
C151. CH30 * 0
C178. CH30
C206. CH30
C179. CH30
+ HO
+ H2
+ H2
+ H20
+ N
* N
+ N
+ N
* NO
+ NO
+ N2
+ 0
* 0
* 0
+ 0
+ 02
= CH4 •»•
= CH3 +
= CH4 4-
= CH4 4-
= CHN +
= CH2 +
= CH20 +
= CH3 +
= CH20 *
» CH3 *
= CH3 *
= CHO «•
= CH2 +
» CH20 *
= CH3 +
= CH20 +
02
H20
HO
H02
H20
HMO
HN
NO
HNO
N02
N20
H20
H02
HO
02
H02
-------
B-20
REACTIONS OF
C153. CH4
C191. CH4
B 9. CH4
B102. CH4
8103. CH4
B139. CH4
B170. CH4
C 61. CH4
C 8. CH4
C 99. CH4
C137. CH4
C101. CH4
C169. CH4
C199. CH4
C201. CH4
C211. CH4
C212. CH4
C192. CH4
C194. CH4
C208. CH4
C209. CH4
C157. CH4
C182. CH4
C196. CH4
C207. CH4
4- M
4- M
+ CH
+ CHO
* CHO
+ CH2
+ CH20
+ CN
••• CO
+ CO
+ CO
•«• C02
+ C02
4- H
-»• HO
+ HO
+ H02
+ N
+ NO
+ NO
* N02
+ 0
+ 0
+ 0
+ 0
» CH2 +
= CH3 +
= CH2 +
» CH2 +
= CH20 *
= CH3 4-
= CH3 +
= CHN +
= CH +
= CHO +
* CH2 +
« CHO +•
= CH20 *
= CH3 +
» CH3 +
« CH30 +
= CH30 +
- CH3 +
= CH3 +
= CH30 +
= CH30 +
= CH2 4-
= CH20 •»•
= CH3 +
= CH30 4-
H2 + M
H 4- M
CH3
CH30
CH3
CHS
CH30
CH3
CH30
CH3
CH20
CH30
CH20
H2
H20
H2
H20
HN
HNO
HN
HNO
H20
H2
HO
H
-------
REACTIONS OF CH4
C185. CH4 * 02 = CH20 + H20
C198. CH4 +02 = CH3 + H02
C210. CH4 +02 = CH30 + HO
-------
B-22
REACTIONS OF CN
D 62. CN * CHO = CHN «• CO
D 1. CN + CH2 « CH * CHN
D 58. CN «• CH20 = CHN + CHO
D 59. CN * CH3 = CHN * CH2
D 60. CN + CH30 » CHN + CH20
0 61. CN + CH4 = CHN «• CH3
C 37. CN + H « CH * N
C 57. CN + H + M = CHN + M
C 48. CN * HN = CH * N2
C 81. CN * HN - CHN + N
C 51. CN «• HNO = CH * N20
C 83. CN * HNO = CHN + NO
C132. CN * HNO » CHO + N2
C 40. CN + HO = CH * NO
C 86. CN + HO = CHN + 0
C126. CN + HO = CHO + N
A213. CN + HO = CO + HN
C 44. CN + H02 = CH * N02
C 89. CN * H02 = CHN + 02
C128. CN + H02 = CHO + NO
A214. CN + H02 = CO + HNO
A215. CN + H02 = C02 + HN
C 14. CN + H2 = CH * HN
Z 64. CN + H2 = CHN + H
C158. CN -»• H2 » CH2 + N
-------
B-23
REACTIONS OF CN
C 19. CN + H20 = CH + HMO
C 71. CN + H20 = CHN •»• HO
C109. CN * H20 « CHO * HM
C160. CN + H20 = CH2 + NO
C186. CN + H20 = CH20 + N
A216. CN + NO = CO + N2
A217. CN + N02 = CO + N20
A218. CN •»- M02 = C02 + N2
A219. CN + 0 * CO + N
A220. CN + 02 » CO + NO
A221. CN + 02 = C02 * N
-------
B-24
REACTI
B
D
D
D
62.
10.
2.
94.
D140.
0
D
0
4.
95.
97.
D190.
D
D
8.
99.
0137.
C
c
C
c
c
53.
92.
41.
87.
127.
C213.
C
c
c
c
45.
90.
129.
214.
A222.
C
C
55.
133.
ONS OF CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
CHN
CHO
CH2
CH20
CH20
CH3
CH3
CH30
CH30
CH4
CH4
CH4
H
H + M
HN
HN
HN
HN
HNO
HNO
HNO
HNO
HNO
HO
HO
= CHO
= CH
= CH
= CHO
= CH2
= CH
= CHO
= CHO
= CH3
= CH
= CHO
= CH2
= CH
= CHO
= CH
= CHN
= CHO
= CN
= CH
= CHN
= CHO
= CN
= C02
= CH
= CHO
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
CN
C02
CHO
CHO
C02
CH20
CH2
CH20
C02
CH30
CH3
CH20
0
NO
0
N
HO
N02
02
NO
H02
HN
02
0
4- M
-------
B-25
REACT!
A223.
C135.
A224.
C 23.
C106.
C164.
0166.
C 27.
C114.
C166.
C187.
A225.
C219.
C220.
A226.
A227.
C216.
C217.
A228.
A229.
A230.
ONS
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
CO
OF CO
4- HO
+ H02
* H02
+• H2
+ H2
+ H2
* H2 4- M
+ H20
* H20
* H20
«• H20
* H20
4- N
+ NO
+ NO
+ N02
+• N2
+• N20
+• N20
4-0 + M
+ 02
= C02
= CHO
= C02
= CH
= CHO
» CH2
« CH20
« CH
= CHO
= CH2
= CH20
= C02
= CN
= CN
= C02
« C02
= CN
= CN
» C02
= C02
= C02
+ H
4- 02
+ HO
* HO
* H
+ 0
+ H02
4- HO
+ 02
+ 0
+ H2
+ 0
+ 02
+ N
+ NO
+ NO
* N02
+ N2
* 0
M
M
-------
B-26
REACTIONS OF C02
C229. C02
B 10. C02 4 CH
0 93. C02 4- C
B140. C02 4- C
D 96. C02 4 C
8190. C02 4 C
D101. C02 4- C
D169. C02 4 C
C 56. C02 4- H
C134. C02 4 H
C223. C02 4 H
C 46. C02
C 91. C02 4 HN
C130. C02
C215. C02 4 HN
C222. C02
C131. C02
C136. C02
C224. C02 4 HO
C 28. C02
C115. C02 4 H2
C167. C02
C188. C02
C225. C02
C117. C02
4
4
4-
4
4
4
+
4
4
4
*
4
*
4
+
4
+
4
+
4
+
+
+
+
4 M
CH
CH2
CH2
CH3
CH3
CH4
CH4
H
H
H
HN
HN
HN
HN
HN
HNO
HO
HO
H2
H2
H2
H2
H2
H20
= CO
« CHO
= CHO
= CH20
= CHO
= CH30
= CHO
= CH20
» CH
= CHO
» CO
= CH
= CHN
« CHO
= CM
= CO
= CHO
* CHO
= CO
« CH
= CHO
= CH2
= CH20
= CO
= CHO
4 0
4 CO
4- CHO
4 CO
4- CH20
4 CO
4 CH30
4 CH20
4- 02
* 0
4 HO
4 N02
4 02
4 NO
4 H02
4 HNO
4 N02
4 02
4 H02
4 H02
4- HO
4 02
4 0
4 H20
4 H02
4 M
-------
B-27
REACTIONS OF C02
C189. C02 + H20 = CH20 + 02
C221. C02 * N = CM + 02
C226. C02 + N = CO * NO
C227. C02 +1*40 = CO * N02
C218. C02 + N2 = CM * N02
C228. C02 + N2 » CO * N20
C230. C02 +0 = CO * 02
-------
B-28
REACTI
B 11.
D 12.
B 63.
B 64.
D 20.
B104.
BIOS.
B106.
D 29.
B141.
D 33.
D119.
0146.
B171.
B172.
0152.
B191.
0156.
0161.
0195.
B207.
0199.
D 37.
D 57.
D 53.
DNS
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
H
OF H
+ CH + M
+ CHN
+ CHN
* CHN
+ CHO
+ CHO
+ CHO + M
+ CHO
+ CH2
+ CH2 + M
+ CH20
+ CH20
+ CH20
+ CH20
+ CH20 + M
+ CH3
+ CH3 + M
+ CH30
+ CH30
+ CH30
+ CH30
* CH4
* CN
«• CN * M
+ CO
= CH2
= CH •»•
= CH2 «•
= CN •»•
= CH *
= CH2 +
» CH20
= CO +
= CH +
= CH3
= CH +
= CHO +
= CH2 +
= CHS *
= CH30
= CH2 +
= CH4
« CH2 *
= CH20 +
» CH3 +
= CH4 *
= CH3 +
= CH +
= CHN
= CH *
» PI
HN
N
H2
HO
0
+ M
H2
H2
+ M
H20
H2
HO
0
+ M
H2
+ M
H20
H2
HO
0
H2
N
+ M
0
-------
B-29
REACTI
D 92.
D 56.
0134.
D223.
A231.
A232.
A233.
A234.
A235.
A236.
A237.
A238.
A239.
A240.
A241.
A242.
A243.
A244.
A245.
A246.
A2
-------
B-30
REACTIONS OF H
A252. H + M20 « H,MO + N
A253. H + N20 = HO + N2
A254. H +0 + M =HO + M
A255. H +02 = HO + 0
A256. H + 02 * M * H02 + M
-------
B-31
REACTI
C242.
B 12.
B 13.
B 14.
B 65.
0 16.
0 68.
B107.
B108.
B109.
0 75.
B142.
D 78.
D143.
B173.
B174.
B192.
D193.
B208.
D 46.
D 81.
D 41.
D 87.
D127.
0213.
ONS OF HN
HN
HN
HN
HN
HN
HN
HN
HN
HN
HN
HN
HN
HN
HN
HN
HN
HN
HN
HN
HN
HN
HN
HN
HN
HN
4 M
* CH
+ CH
+• CH
4 CHN
4 CHO
* CHO
+ CHO
+ CHO
* CHO
+ CH2
* CH2
* CH20
4 CH20
* CH20
4 CH20
* CH3
4 CH30
4 CH30
4 CN
4 CN
+ CO
+ CO
+ CO
* CO
= H
= CHN
= CH2
* CN
= CH2
= CH
= CHN
* CH2
= CH20
= CN
» CHN
= CH3
= CHN
= CH2
= CH3
= CH30
« CH4
= CH3
= CH4
= CH
* CHN
« CH
= CHN
= CHO
= CN
4- N + M
4 H
+ N
* H2
* N2
+ HNO
+ HO
* NO
* N
+ H20
4- H2
+ N
«• H20
* HNO
4- NO
4 N
4 N
4 HNO
4 NO
4 N2
4 N
4 NO
4 0
4 N
4 HO
-------
B-32
REACTIONS OF HN
D 46. HN + C02 = CH + N02
D 91. HN + C02 = CHN + 02
0130. HN + C02 = CHO + NO
D215. HN + C02 = CM + H02
D222. HN -i- C02 = CO + HNO
B232. HN + H = H2 + N
A257. HN •»• HN = H2 •»• N2
A258. HN + HNO = H2 + N20
A259. HN + HNO = H20 + N2
C233. HN + HO = H + HNO
A260. HN + HO = H2 + NO
A261. HN + HO = H20 + N
A262. HN + H02 » HNO + HO
A263. HN + H02 = H2 + N02
A264. HN + H02 = H20 * NO
A265. HN + H20 = HNO + H2
C250. HN + N = H + N2
C251. HN + NO = H + N20
A266. HN + NO = HNO + N
A267. HN + NO = HO + N2
A268. HN -f N02 = HNO + NO
A269. HN + N02 = HO + N20
A270. HN + N02 = H02 + N2
A271. HN + N20 = HNO + N2
C243. HN •»• 0 = H + NO
-------
B-33
REACTIONS OF HN
A272. HN + 0 + M = HNO * M
A273. HN + 0 = HO + N
C246. HN + 02 « H * N02
A274. HN + 02 = HMO * 0
A275. HN + 02 = HO + NO
A276. HN + 02 = H02 * N
-------
B-34
REACTIONS OF HNO
C2^4. HNO
C272. HNO
A277. HNO
B 15. HNO * CH
B 16. HND
B 17. HNO * CH
B 18. HNO + CH
B 19. HNO
B 66. HNO
B 67. HNO
D 72. HNO
B110. HNO
Bill. HNO
D 77. HNO
B143. HNO
B144. HNO
4-
4-
4-
4-
*
4-
4-
4-
4-
4-
4-
4-
+
4-
4-
4-
4-
4-
4-
4-
4-
4-
4- M
4- M
4- M
CH
CH
CH
CH
CH
CHN
CHN
CHO
CHO
CHO
CH2
CH2
CH2
CH2
CH20
CH20
CH3
CH3
CH30
CN
CN
CN
= H
= HN
= HO
= CHN
= CHO
= CH2
= CH20
= CN
* CH2
= CH20
= CHN
= CH2
= CH20
= CHN
» CH20
« CH3
= CH30
= CH3
= CH30
» CH30
= CH4
= CH4
= CH
= CHN
= CHO
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
+
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
NO + M
0 4- M
N * M
HO
HN
NO
N
H20
N20
N2
H02
N02
NO
H20
HN
NO
N
N02
NO
HN
NO
N02
N20
NO
N2
-------
B-35
REACTIONS OF HNO
D 45. HNO 4- CO » CH + N02
D 90. HNO 4- CO = CHN + 02
D129. HNO + CO = CHO + NO
0214. HNO 4- CO = CM 4- H02
8222. HNO * CO = C02 + HN
0131. HNO + C02 = CHO 4 N02
B233. HNO * H * HN 4- HO
B234. HND 4- H = H2 + NO
B235. HNO + H = H20 + N
B258. HNO * HN = H2 4 N20
B259. HNO * HN = H20 + N2
A278. HNO * HNO = H20 + N20
C262. HNO 4- HO = HN 4- H02
A279. HNO + HO = H2 4- N02
A280. HNO 4- HO * H20 4- NO
A281. HNO 4- H02 = H20 4- N02
C265. HNO 4- H2 = HN 4- H20
C252. HNO 4- N » H + N20
C266. HNO 4- N = HN 4 NO
A282. HNO 4 M = HO 4 N2
C268. HNO 4- NO = HN 4- N02
A283. HNO 4- MO = HO + N20
A284. HNO 4- NO = H02 4 N2
A285. HNO 4- N02 = H02 4- N20
C271. HNO 4- N2 = HN 4- N20
-------
B-36
REACTIONS OF HNO
C247. HNO +0 = H -»- N02
C274. HNO +0 « HN + 02
A286. HNO * 0 = HO + NO
A287. HNO +0 = H02 + N
A288. HNO +02 = HO + N02
A289. HNO +02 = H02 + NO
-------
B-37
REACTI
C254.
B 20.
B 21.
B 22.
B 23.
D 15.
B 68.
B 69.
B 70.
B 71.
0 24.
B112.
B113.
B114.
8115.
D 32.
0118.
B146.
B147.
B148.
0123.
0149.
B177.
B178.
0155.
ONS
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
OF HO
4- M
+ CH
+• CH
4- CH 4- M
4- CH
* CHN
* CHN
+ CHN
+ CHN
+ CHN
4- CHO
* CHO
4- CHO
4- CHO
4- CHO
+ CH2
+ CH2
4- CH2
4- CH2
4- CH2 4- M
4- CH20
4- CH20
4- CH20
4- CH20
4- CH3
= H 4-
= CHO* 4-
= CH2 *
» CH20
= CO 4-
= CH 4-
= CHO 4-
= CH2 4-
= CH20 4-
= CN 4-
= CH +
= CH2 *
= CH20 4-
« CO +
= C02 4-
= CH 4-
= CHO 4-
= CH20 4-
= CH3 4-
= CH30
= CHO 4-
= CH2 4-
= CH3 4-
= CH30 4-
» CH2 4-
0
H
0
H2
HNO
HN
NO
N
H20
H02
02
0
H20
H2
H20
H2
H
0
H20
H02
02
0
H20
+ M
-------
B-38
REACTIONS OF HO
0180.
B195.
B196.
0184.
0197.
B210.
0201.
0211.
D 40.
0 86.
0126.
B213.
0 55.
0133.
B223.
0136.
0224.
B236.
B237.
0233.
B260.
B261.
0262.
B279.
B280.
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
+
+
4-
4-
4-
4-
4-
4-
4-
+
•f
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
CH3
CH3
CH3
CH30
CH30
CH30
CH4
CH4
CN
CM
CN
CN
CO
CO
CO
C02
C02
H
H 4- M
HN
HN
HN
HNO
HNO
HNO
= CH20
= CH30
= CH4
= CH20
= CH3
= CH4
= CH3
= CH30
= CH
= CHN
* CHO
= CO
= CH
= CHO
= C02
= CHO
= CO
= H2
- H20
*•* W
= H2
= H20
= HN
= H2
» H20
4-
4-
4-
4-
4-
4-
4-
4-
4-
4"
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
H2
H
0
H20
H02
02
H20
H2
NO
0
N
HN
02
0
H
02
H02
0
HNO
NO
N
H02
N02
NO
4- M
-------
B-39
REACTIONS OF HO
C238.
A290.
A291.
A292.
C241.
A293.
C245.
C273.
C277.
C248.
C275.
C286.
A294.
0288.
A295.
C253.
C267.
C282.
C269.
C283.
A296.
C255.
A297.
A298.
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
HO
4- HO
* HO
+ HO
+ H02
4- H2
* H20
4- N
+ N
4- N •*• M
4- NO
* NO
4- NO
* NO
4- N02
4- N02
4- N2
4- N2
+ N2
4- N20
4- N20
4- N20
4- 0
4-0 * M
4- 02
« H
= H2
= H20
= H20
= H
= H02
« H
= HN
= HNO
= H
= HN
= HNO
= H02
= HNO
= H02
= H
» HN
« HNO
= HN
= HNO
= H02
= H
= H02
= H02
4- H02
4- 02
4- 0
4- 02
4- H20
4- H2
4- NO
4- 0
4- N02
4- 02
4- 0
4- N
+ 02
4- NO
4- N20
4- NO
+ N
4- N02
4- NO
4- N2
4- 02
4- 0
M
M
-------
B-40
REACTI
C256.
C297.
B 24.
B 25.
B 26.
B 27.
B 28.
B 72.
B 73.
B 74.
B116.
B117.
D122.
B149.
B150.
B151.
B179.
D183.
B197.
B198.
D212.
D 44.
D 89.
0128.
8214.
ONS OF
H02
H02
H02
H02
H02
H02
H02
H02
H02
H02
H02
H02
H02
H02
H02
H02
H02
H02
H02
H02
H02
H02
H02
H02
H02
H02
4- M
*• M
+ CH
+ CH
+ CH
+ CH
«• CH
+ CHN
* CHN
* CHN
+ CHO
+ CHO
+ CH2
* CH2
+ CH2
* CH2
* CH20
+ CH3
+ CH3
* CH3
«• CH4
+ CN
+ CN
«• CN
* CN
= H *
= HO «•
= CHO +
= CH2 +
= CH20 +
= CO +
= C02 +
= CHO *
= CH2 +
« CH20 «•
= CH20 +
= C02 +
* CHO +
= CH20 +
= CH3 +
= CH30 +
» CH30 +
= CH20 +
» CH30 +
= CH4 +
» CH30 *
« CH +
= CHN +
= CHO +
» CO «•
02 + M
0 * M
HO
02
0
H20
H2
HNO
N02
NO
02
H20
H20
HO
02
0
02
H20
HO
02
H20
N02
02
NO
HNO
-------
B-41
REACTIONS OF H02
B215. H02 + CN
D135. H02 * CO
B224. H02 + CO
8238. H02 + H
8239. H02 + H
B240. H02 + H
8262. H02 + HN
8263. H02 + HN
B264. H02 + HN
8281. H02 + HN
B292. H02 + HO
C293. H02 * H2
C276. H02 + N
C287. H02 + N
C294. H02 + N
C298. H02 +0
+
+
+
+
+
+
+
*
+
*
+
*
•»•
*
+
+
*
+
*
+
+
+
+
CN
CO
CO
H
H
H
HN
HN
HN
HNO
HO
H2
N
N
N
N
NO
NO
N2
N2
N2
N20
0
= C02
* CHO
= C02
= HO
= H2
« H20
= HNO
= H2
= H20
= H20
= H20
= HO
« H
= HN
= HNO
» HO
« HNO
= HO
= HN
= HNO
= HO
* HNO
= HO
+ HN
* 02
+ HO
4 HO
+ 02
* 0
+ HO
+ N02
+ NO
* N02
+ 02
-»• H20
+ N02
* 02
* 0
* NO
+ 02
* N02
+ N02
* NO
* N20
+ N02
+ 02
-------
B-42
REACTI
C231.
B 29.
B 30.
B 75.
B 76.
0 31.
B118.
B119.
B120.
B121.
B152.
B153.
0154.
B180.
B181.
B182.
B199.
0200.
B211.
0 14.
0 64.
0158.
D 23.
0106.
0164.
ONS OF H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
+ M
4- CH
+ CH 4- M
4- CHN
4- CHN
+ CHO
4- CHO
+ CHO
* CHO
4- CHO 4- M
4- CH2
4- CH2 4- M
+ CH20
4- CH20
4- CH20
4- CH20
4- CH3
4- CH30
4- CH30
4- CN
4- CN
4- CN
4- CO
4- CO
4- CO
= H
= CH2
= CH3
= CH2
= CH3
= CH
= CH2
= CH20
= CH3
= CH30
= CH3
= CH4
= CH2
= CH3
= CH30
= CH4
» CH4
= CH3
= CH4
= CH
= CHN
= CH2
» CH
= CHO
= CH2
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
4-
+
4-
4-
4-
4-
H
H
HN
N
H20
HO
H
0
H
H20
HO
H
0
H
H20
HO
HN
H
N
HO
H
0
4- M
4- M
M
4- M
-------
B-43
REACTI
D168.
D 28.
D115.
D167.
D188.
D225.
D265.
D241.
D293.
C232.
C234.
C260.
A299.
C263.
C279.
A300.
C257.
C258.
A301.
C236.
A302.
C239.
C290.
A303.
3NS OF H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
H2
4-
4-
4-
4-
4-
4-
4-
4-
*
4-
4-
4-
4-
4-
4-
4-
*
4-
4-
4-
4-
+
*
+.
CO + M
C02
C02
C02
C02
C02
HNO
HO
H02
N
NO
NO
NO
N02
N02
N02
N2
N20
N20
0
0 * M
02
02
02
* CH20
= CH 4-
= CHO *
= CH2 +
= CH20 +
= CO +
= HN *
= H +
= HO +
= H +
= H +
= HN *
= H20 +
= HN +
= HNO *
= H20 +
= HN •«•
= HN +
= H20 +
= H •«•
= H20
» H *
= HO *
= H20 +
H02
HO
02
0
H20
H20
H20
H20
HN
HNO
HO
N
H02
HO
NO
HN
HNO
N2
HO
H02
HO
0
M
-------
B-44
REACTIONS OF H20
C237. H20 + M
C302. H20 * M
B 31. H20 + CH
B 32. H20 «• CH
B 33. H20 + CH
B 34. H20 * CH
B 35. H20 + CH + M
B 77. H20 + CHN
B 78. H20 + CHN
B 79. H20 + CHN
B 80. H20 * CHN
B122. H20 * CHO
B123. H20 + CHO
B124. H20 + CHO
B125. H20 * CHO
B154. H20 + CH2
B155. H20 + CH2
B156. H2D + CH2
B157. H20 + CH2
B183. H20 + CH20
B184. H20 + CH20
B185. H20 + CH20
B200. H20 * CH3
B201. H20 -i- CH3
B212. H20 + CH30
= H * HO + M
= H2 +0 •«• M
= CHO + H2
= CH2 * HO
= CH20 * H
« CH3 «• 0
= CH30 + M
= CH2 + HNO
= CH20 * HN
= CH3 + NO
= CH30 •«• N
= CH2 «• H02
= CH20 + HO
= CH3 + 02
= CH30 + 0
= CH20 + H2
= CH3 + HO
= CH30 + H
= CH4 «• 0
= CH3 + H02
» CH30 * HO
= CH4 + 02
= CH30 * H2
= CH4 + HO
= CH4 + H02
-------
B-45
REACTIONS OF H20
D 19. H20 * CN
D 71. H20 + CN
D109. H20 + CN
0160. H20 + CN
D186. H20 + CN
0 27. H20 * CO
Oil*. H20 + CO
D166. H20 + CO
0187. H20 + CO
B225. H20 + CO
0117. H20 + C0
0189. H20 + C0
82*1. H20 + H
B265. H20 4- HN
B293. H20 + HO
C235. H20 * N
C261. H20 * N
C299. H20 +• N
C264. H20 + NO
C280. H20 4- NO
C300. H20 * NO
C281. H20 + N0
C259. H20 4- N2
C301. H20 4- N2
*
*
+
+
+
4-
+
+
+
4-
+
*
*
+•
+
4-
•*•
4-
4-
4-
4-
4-
4-
4-
4-
CN
CN
CN
CN
CN
CO
CO
CO
CO
CO
C02
C02
H
HN
HO
N
N
N
MO
NO
NO
N02
N2
N2
N20
= CH
= CHN
= CHO
= CH2
* CH20
= CH
= CHO
= CH2
= CH20
» C02
= CHO
= CH20
« HO
= HNO
= H02
* H
= HN
= H2
* HN
= HNO
= H2
= HNO
= HN
= H2
» HNO
4- HNO
4- HO
4- HN
4- NO
4- N
4- H02
+ HO
4- 02
4- 0
4- H2
4- H02
4- 02
4- H2
4- H2
4- H2
4- HNO
4- HO
4- NO
4- H02
4- HO
4- N02
4- H02
4- HNO
4- N20
4- HNO
-------
B-46
REACTIONS OF H2Q
C240. H20 +0 » H + H02
C291. H20 +0 = HO + HO
C303. H20 +0 « H2 + 02
C292. H20 +02 * HO •*• H02
-------
B-47
REACTI
B 36.
B 37.
D 47.
B 81.
D 39.
D 85.
B126.
B127.
D 13.
D 63.
B158.
D 18.
D 70.
D108.
D159.
B186.
D 76.
0142.
D 80.
D145.
D174.
D202.
D192.
D219.
D221.
ONS
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
OF N
4- CH 4- M
* CH
-i- CHN
4- CHN
* CHO
+ CHO
4- CHO
4- CHO
* CH2
4- CH2
4- CH2
4- CH20
4- CH20
4- CH20
4- CH20
4- CH20
4- CHS
4- CH3
* CH30
4- CH30
4- CH30
4- CH30
4- CH4
+ CO
4- C02
= CHN
= CN
« CH
= CN
= CH
= CHN
« CN
= CO
= CH
= CHN
= CN
= CH
= CHN
= CHO
= CH2
= CN
= CHN
= CH2
= CHN
= CH2
= CH20
= CH3
= CH3
= CN
= CN
4- H
4- N2
4- HN
4- NO
4- 0
4- HO
4- HN
4 HN
4- H
4- H2
4- HNO
4- HO
4- HN
4- NO
4- H20
4- H2
4-. HN
4- H20
4- HNO
4- HN
4- NO
4- HN
4- 0
4- 02
M
-------
B-48
REACT
0226.
B242.
0250.
0252.
0266.
B282.
0245.
0273.
0277.
0249.
0276.
0287.
0294.
0232.
0235.
0261.
0299.
A304.
A305.
A306.
A307.
A308.
A309.
A310.
A311.
IONS
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
OF SI
+ C02
* H + M
+ HN
+ HNO
+ HNO
+ HNO
+ HO
+ HO
+ HO + M
+ H02
+ H02
+ H02
+ H02
+ H2
+ H20
+ H20
+ H20
+ N + M
+ NO
+ NO * M
+ N02
+ N02
+ N02
* N20
+ 0 + M
= CO
= HN
= H
= H
= H.M
= HO
= H
= HN
= HNO
= H
= HN
= HNO
= HO
= H
= H
= HN
= H2
= N2
= N2
= N20
= NO
= N2
= N20
« NO
= NO
* NO
-I- M
+ N2
+ N20
* NO
+ N2
+ NO
* 0
+ M
+ N02
+, 02
+ 0
+ NO
+ HN
+ H>40
+ HO
+ NO
+ M
* 0
+ M
+ NO
* 02
+ 0
+ N2
•»• M
-------
B-49
REACTIONS OF M
A312. N +02 = NO + 0
A313. N + 02 * M = N02 + M
-------
B-50
REACT!
C311.
B 38.
B 39.
B 40.
B 41.
D 49.
B 82.
B 83.
D 43.
D 88.
B128.
B129.
B130.
D 17.
D 69.
D107.
B159.
B160.
0 74.
Dill.
D161.
D 79.
D144.
D173.
B202.
ONS
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
NO
OF NO
+ M
+ CH
+ CH
+ CH
+ CH
+ CHN
+ CHN
+ CHN
+ CHO
* CHO
+ CHO
+ CHO
+ CHO
+ CH2
+ CH2
+ CH2
-i- CH2
+ CH2
+ CH20
+ CH20
+ CH20
+ CH3
+ CH3
+ CH3
+ CH3
= N
= CHN
= CHO
= CN
« CO
= CH
= CHO
» CN
= CH
= CHN
= CN
= CO
= C02
» CH
= CHN
= CHO
= CH20
= CN
= CHN
= CHO
= CH2
= CHN
= CH2
« CH20
= CH30
+ 0
* 0
* N
+ HO
+ HN
+ N20
+ N2
+ HNO
+ N02
+ 02
+ H02
+ HNO
+ HN
+ HNO
+ HO
+ HN
•»• N
+ H20
+ H02
+ HNO
+ N02
+ H20
* HNO
•»• HN
* N
M
-------
B-51
REACTIONS OF NO
0176. NO
D203. NO
0194. NO
0208. NO
B216. NO
0220. NO
B226. NO
0227. NO
B243. NO
B244. NO
B245. NO
0251. NO
B266. NO
B267. NO
0268. NO
B283. NO
B284. NO
0248. NO
0275. NO
0286. NO
B294. NO
0289. NO
0295. NO
0234. NO
0260. NO
* CH30
* CH30
+ CH4
«• CH4
+ CN
* CO
+ CO
+ C02
4- H
4- H + M
+ H
+ HN
4- HN
+ HN
+ HNO
+ HNO
* HNO
+ HO
+ HO
* HO
4- HO
* H02
4- H02
* H2
4- H2
= CH20 +
= CH3 4-
= CH3 +
= CH30 +
= CO +•
= CN 4-
= C02 4-
= CO *
= HN 4-
= HNO
» HO +
= H 4-
= HNO 4-
= HO 4-
= HN +
= HO •«•
= H02 +
= H 4-
= HN *
= HNO +
= H02 +
= HNO *
= HO +
= H +
= HN *
HNO
N02
HNO
HM
N2
02
N
N02
0
N
N20
N
N2
N02
N20
N2
N02
02
0
N
02
N02
HNO
HO
M
-------
B-52
REACTIONS OF NO
B299. NO
D264. NO
D280. NO
D300. NO
B305. NO
B306. NO
C307. NO
A314. NO
A315. NO
A316. NO
C310. NO
A317. NO
C312. NO
A318. NO
A319. NO
+ H2
+ H20
* H20
* H20
+ N
+ N + M
+ NO
+ NO
+ NO
+ N02
* N2
* N20
+ 0
+ 0 * M
+ 02
= H20
* HN
= HNO
= H2
= N2
= N20
= N
= N2
= N20
* N20
= N
= N02
= N
» NQ2
= N02
+ N
+ H02
+ HO
* N02
+ 0
+ M
+ N02
+ 02
+ 0
+ 02
+ N20
+ N2
+ 02
+ M
+ 0
-------
B-53
REACTIONS OF ,M02
C313. N02
C318. N02
B 42. N02
B 43. N02
B 44. N02
B 45. N02
B 46. N02
B 84. N02
B131. N02
D 73. N02
DUO. N02
B161. N02
\
0175. N02
B203. N02
0209. N02
B217. N02
B218. N02
B227. N02
8246. N02 + H
B247. N02
B248. N02
B249. N02
B268. N02 * HN
B269. N02
8270. N02
+ M
+ M
+ CH
* CH
+ CH
+ CH
+ CH
* CHN
+ CHO
+ CH2
+ CH2
+ CH2
+ CH3
* CH3
* CH4
* CN
+ CN
+ CO
+ H
* H
* H
+ H
+ HN
+ HN
«• HN
= N
= NO
= CHN
= CHO
= CN
= CO
= C02
= CHO
= C02
= CHN
= CHO
= CH20
= CH20
= CH30
» CH30
= CO
» C02
» C02
= HN
= HNO
= HO
= HD2
= HNO
= HO
= H02
+ 02 «• M
+ 0 •»- M
+ 02
+ NO
+ H02
+ HNO
+ HN
* N20
+ HNO
+ H02
•«- HNO
* NO
+ HNO
* NO
* HNO
+ N20
•»• N2
+ NO
+ 02
* 0
+ NO
* N
+ NO
* N20
* N2
-------
B-54
REACTIONS OF N02
8285. N02 + HNO = H02 + N20
0288. N02 + HO = HNO * 02
B295. N02 + HO = H02 + NO
D263. N02 + H2 = HN + H02
D279. N02 + H2 = HNO + HO
B300. N02 + H2 = H20 * NO
D281. N02 + H20 = HNO * H02
B307. N02 * N = NO + NO
B308. N02 «• N = N2 * 02
8309. N02 + N * N20 + 0
B316. N02 + NO = N20 + 02
C317. N02 + N2 = NO + N20
C319. N02 +0 = NO * 02
-------
B-55
REACTI
C304.
B 47.
B 48.
0 50.
0 82.
B132.
D 65.
D 67.
0162.
0204.
0216.
0218.
0228.
B250.
0271.
0253.
0267.
0282.
0270.
0284.
0296.
0257.
0259.
0301.
0310.
ONS
N2
N2
N2
N2
N2
N2
N2
N2
N2
N2
N2
N2
N2
N2
N2
N2
N2
N2
N2
N2
N2
N2
N2
N2
N2
OF ,M2
4- M
4 CH
* CH
+ CHO
4 CHO
4 CHO
4 CH2
4 CH20
* CH20
4 CH30
4- CO
* C02
+ C02
4- H
4- HNO
4 HO
4 HO
+ HO
4 H02
4- H02
4- H02
4- H2
4- H20
+ H20
+ NO
= N
= CHN
« CN
* CH
- CHN
* CN
« CHN
» CHN
» CH2
= CH3
* CN
= CN
= CO
= HN
« HN
= H
= HN
* HNO
» HN
= HNO
= HO
= HNI
= HN
= H2
= N
4- N
4 N
4 HN
4 N20
4- NO
4- HNO
4 HN
4 HNO
4 N20
* N20
4 NO
4- N02
4- N20
4 N
4 N20
4 N20
4 NO
4 N
4 N02
4 NO
4 N20
4 HM
4 HNO
4 N20
4- N20
M
-------
B-56
REACTIONS OF N2
D317. N2 «• N02 = NO * N20
C305. N2 + 0 = N * NO
A320. N2 * 0 + M = N20 * H
C308. N2 * 02 = N + N02
C314. N2 4- 02 = NO + NO
A321. N2 + 02 = N20 + 0
-------
B-57
REACTIONS OF
C306. N20
C320. N20
B 49. N20
B 50. N20
B 51. N20
D 84. N20
D 66. N20
B162. N20
B204. N20
D217. N20
B228. N20
B251. N20
B252. N20
B253. N20
B271. N20
0269. N20
D283. N20
B296. N20
0285. N20
D258. N20
B301. N20
D278. N20
B310. N20
8317. N20
C309. N20
N20
4- M
4- M
4 CH
4 CH
4 CH
* CHO
+ CH2
4 CH2
4 CH3
4- CO
4 CO
4- H
4- H
4- H
4- HN
4- HO
4- HO
4 HO
4 H02
4- H2
4- H2
4- H20
4- N
4 NO
4 0
= N
= N2
= CHN
= CHO
» CN
- CHN
= CHN
= CH20
= CH30
= CN
= C02
= HN
» HMO
« HO
= HNO
» HN
= HNO
= H02
= HNO
» HN
* H20
= HNO
* NO
= N02
= N
4- NO * M
+ 0 + M
4- NO
+ N2
4- HNO
4- N02
4- HNO
4- N2
4- N2
* N02
4- N2
4- NO
4- N
4- N2
4 N2
4- N02
4 NO
4 N2
4 N02
4 HNO
4 N2
4 HNO
4 N2
4 N2
4 N02
-------
B-58
REACTIONS OF ^20
C315. N2Q + 0 = NO + NO
C321. N20 +0 * N2 + 02
C316. N20 +02 = NO + N02
-------
B-59
REACT!
B 52.
B 53.
D 38.
B 85.
B 86.
B 87.
D 54.
B133.
B134.
D 21.
D104.
B163.
B164.
D 26.
D113.
D165.
B187.
B188.
D 34.
0120.
D147.
D171.
B205.
D125.
0151.
ONS
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
OF 0
+ CH + M
+ CH
* CHN
+ CHN
-i- CHN
+ CHN
+ CHO
+ CHO
* CHO
* CH2
+ CH2
+ CH2 + M
* CH2
+ CH20
+ CH20
+ CH20
+ CH20
+ CH20
+ CH3
+ CH3
+ CH3
+ CH3
+ CH3 + M
+ CH30
•»• CH30
= CHO
= CO *
= CH +
» CHO +
= CN +
= CO +
= CH +
= CO +
= C02 *
= CH +
= CHO +
= CH20
= CO +
= CH +
= CHO *
= CH2 *
= CO +
= C02 *
- CH +
= CHO +
= CH2 +
= CH20 +
= CH30
= CHO *
= CH2 +
•»• M
H
NO
N
HO
HN
02
HO
H
HO
H
* M
H2
H02
HO
02
H20
H2
H20
H2
HO
H
* M
H20
H02
-------
B-60
REACTI
0178.
0206.
0157.
0182.
0196.
0207.
B219.
B229.
0230.
B254.
D243.
B272.
B273.
0247.
0274.
B286.
B287.
0255.
B297.
0298.
0236.
B302.
0240.
0291.
0303.
ONS
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
OF 0
+ CH30
4- CH30
4- CH4
4- CH4
4- CH4
+ CH4
+ CN
4- CO * M
+ C02
4- H * M
4- HN
4- HN + M
4- HN
4- HNO
+ HNO
4- HNO
4- HNO
4- HO
4- HO + M
4- H02
4- H2
4- H2 + M
4- H20
4- H20
4- H20
- CH20
= CH3
= CH2
= CH20
= CH3
= CH30
= CO
= C02
= CO
= HO
= H
= HNO
= HO
= H
= HN
= HO
= H02
= H
= H02
= HO
= H
= H20
= H
= HO
= H2
4- HO
4- 02
4- H20
4- H2
4- HO
4- H
4- N
4- 02
4- NO
4- N
4- N02
+ 02
4- NO
4- N
4- 02
+ 02
4- HO
4- H02
+ HO
+ 02
M
M
«• M
M
M
-------
B-61
REACTIONS OF 0
+M
M
B311.
0312.
B318.
D319.
0305.
B320.
0309.
0315.
0321.
A322.
0
0
0
0
0
0
0
0
0
0
+ M + M
+ NO
+ NO + M
+ N02
+ N2
+ M2 + M
+ N20
«• N20
+ N20
+ 0 * M
= NO
= N
= N02
* NO
= N
= N20
= N
= NO
* N2
= 02
+ 02
* 02
+ NO
+ NO
+ NO
+ 02
+ M
+M
-------
B-62
REACT
C322.
B 54.
B 55.
B 56.
D 42.
B 88,
B 89.
B 90.
B 91.
B135.
B136.
0 25.
0112.
B165.
B166.
B167.
0116.
B189.
0124.
0150.
0177.
B206.
0179.
0185.
0198.
IONS
02
02
02
02
02
02
02
02
02
02
02
02
02
02
02
02
02
02
02
02
02
02
02
02
02
OF 02
+ M
-i- CH
+ CH
+ CH
+ CHN
+ CHN
+ CHN
* CHN
* CHN
* CHO
+ CHO
+ CH2
+ CH2
* CH2
+ CH2
+ CH2
+ CH20
+ CH20
+ CH3
+ CH3
+ CH3
+ CH3
* CH30
* CH4
+ CH4
= 0
= CHO
= CO
= C02
= CH
« CHO
= CN
= CO
« C02
= CO
= C02
= CH
= CHO
= CH20
= CO
• C02
= CHO
= C02
= CHO
= CH2
* CH20
= CH30
= CH20
= CH20
= CH3
* 0
+ 0
* HO
•»• H
* N02
+ NO
+ H02
+ HNO
* HN
+ H02
+ HO
* H02
+ HO
* 0
+ H20
+ H2
+ H02
+ H20
+ H20
4- H02
* HO
* 0
+ H02
* H20
+ H02
M
-------
B-63
REACTIONS OF 02
0210. 02 * CH4 = CH30 * HO
B220. 02 * CN = CO + NO
B221. 02 + CN = C02 + N
B230. 02 + CO = C02 + 0
B255. 02 + H = HO + 0
B256. 02 * H + M = H02 + M
0246. 02 + HN » H «• N02
B274. 02 + HN = HMO + 0
8275. 02 * HN = HO + NO
B276. 02 * HN = H02 + N
B288. 02 * HNO = HO * N02
B289. 02 + HNO = H02 * NO
B298. 02 + HO » H02 + 0
0239. 02 + H2 » H + H02
D290. 02 + H2 » HO * HO
B303. 02 * H2 = H20 + 0
D292. 02 + H20 = HO + H02
B312. 02 + N * NO + 0
B313. 02 + N * M * N02 * M
B319. 02 + NO = N02 * 0
D308. 02 + N2 = N + N02
D314. 02 * N2 = NO + NO
B321. 02 + N2 - N20 + 0
D316. 02 * N20 « NO + N02
-------
C-l
APPENDIX C
KINETIC DATA ANALYSIS FOR JET-STIRRED COMBUSTOR
As an approach to testing kinetic models which couple nitric oxide
formation to combustion reactions, the jet-stirred combustor was used to
study NOX formation under kinetically controlled combustion conditions.
The experimental data were compared with kinetic calculations performed by
General Applied Science Laboratories for a well-stirred reactor. The agree-
ment between theory and experiment was quite good for the combustion of
hydrogen/air and carbon monoxide/air for which detailed mechanisms were
used. A quasi-global mechanism for the combustion of propane/air resulted
in substantial underprediction of NOX formation. The results described here
were presented at the Fourteenth Combustion Symposium (C-l).
The kinetic mechanism used in this study is based on a building-
block approach. The mechanism for hydrogen combustion is the basic ele-
ment. Additional reactions are included for carbon monoxide combustion
and a rate-limited global step for hydrocarbon reaction to carbon monoxide
and hydrogen is included to handle hydrocarbon combustion. The overall
mechanism for hydrocarbon combustion is based upon a "quasi-global" con-
cept originally developed to represent the combustion characteristics of a
variety of hydrocarbon fuels (C-2). The reactions for the oxidation of nitro-
gen are included in the model and are coupled to the combustion reactions
through common intermediates.
The mechanism for hydrogen combustion, given in Table C-1A, con-
sists of four exchange reactions and four dissociation/recombination
reactions. The values of the rates for these reactions were taken, when
available, from Reference (C-3).
Three reactions were added for carbon monoxide combustion
(Table C-1B); the carbon monoxide exchange reactions with hydroxyl radical
and molecular oxygen, and the dissociation/recombination reaction leading
to carbon dioxide.
The global step for hydrocarbon consumption
C H + £ 09 —» 7 H + nCO
n m 22 z /
is assigned a rate of
Q 1/2 _o
5.52 x 108 T exp(-12400/T)(CnHm) (0,,) (p) U'
in accordance with Reference (C-2), as noted above.
The principal reactions for the formation of nitric oxide in this
study were the Zeldovich exchange reactions
0 + N2 = N -1- NO
kf = 1.36 x 1014 exp(-3770Q/T)
-------
TABLE C-l
RATE PARAMETERS FOR KINETIC MODEL
kf = ATb exp(-E/RT)
REACTION A
b E/R Ref
A. Hydrogen Combustion
1 1
OH + H. = H00 + H 2.19 x 10
2 2
12
OH = OH = 0 + H20 5.75 x 10
13
0 + H2 = H + OH 1.74 x 10
14
H + 02 = 0 + OH 2.24 x 10
16
0 + H + M=0+M Ix 10
14
0+0+M=02+M 9.38 x 10
15
H + H + M = H+M 5x10
17
H + OH + M = H20 + M 1 x 10
0 2590 C-3
0 393 C-3
0 4750 C-3
n
0 8450 C-3 ^
0 0 C-4
0 0 C-5
0 0 C-4
0 0 C-3
B. Carbon Monoxide Combustion (additional reactions)
11
CO + OH = H + C0? 5.6 x 10
12
0 543 C-3
CO + 0, = CO + 0
£• £*
CO + 0 + M = C02 + M
3 x 10
1.8 x 10
0
-1
25000
2000
C-6
C-7
Reverse reaction rate, k , is obtained from kf and the equilibrium constant, K .
-------
C-3
and
NO + 0 = 02 + N
kf = 1.55 x 109 T exp(-19450/T)
The values for the rate constants were taken from Reference (C-3) . Other re
actions involving nitric oxide such as
and
NO + 02 = N02 + 0
as well as NO oxidation reactions of interest in atmospheric studies are
available in the model (C-2) for completeness but are not important under the
conditions of this study. The reaction (C-8)
N + OH = NO + H
1 "}
k = 4 x 10
was not included in the basic calculations; however, under fuel rich condi-
tions where H and OH concentrations became substantial, additional calcula-
tions including this reaction were made to test its importance.
The most crucial experimental measurements for this study were
the mixture ratios, the reaction temperatures and the concentrations of NOX.
The mixture ratios could be determined to + 2% with calibrated rotameters.
The reaction temperatures could be determined to + 10°K with consideration
given to radiant heat losses and reproducibility. The nitrogen oxide mea-
surements could be made to + 2 ppm with either the Enviometrics or Du Pont
analyzers (a Thermo Electron chemiluminescent analyzer now in use in our
laboratory can give results better than + 1 ppm) . Cross-checks have been
run with these instruments in selected experiments.
The temperatures for the calculations were determined in the
following manner. The measured temperatures were compared to the calculated
heat losses in a well-stirred reactor at the measured temperature. The
heat loss was converted to an overall heat transfer coefficient
H = mC(To -Tn)/(Tm-Ta)
where C is dQ/dT, To is the temperature of a well-stirred reactor operating
without heat losses, Tm is the measured temperature, and Ta is the ambient
temperature. The heat transfer coefficients so determined were averaged
and the average value was used to calculate a smoothed temperature curve
through the data. These temperatures were given by
T = (HT + mCT )/(H + mC)
a o
-------
C-4
The calculated temperature was found to be relatively insensitive to the
actual value of the heat transfer coefficient with a 10% difference in H
corresponding to about a 10°K difference in temperature. Because of this
insensitivity to H, it was decided to assume a constant H for all cases.
This method of temperature determination allows the calculations to be
performed at pre-selected mixture ratios while utilizing all the temperature
measurements for a given combustion system. Furthermore, in cases where
the combustion temperature exceeded the limits of measurement for a Pt/Pt
10% Rh thermocouple (2040°K), the heat transfer coefficient was used to
determine the experimental temperature. The measured (open symbols) and
calculated (solid symbols) values of the combustion temperatures for hydrogen
carbon monoxide and propane, respectively, with air are shown in Figure C-l.
The measurements of NOX for the three fuel/air combinations were
taken at mixture ratios ranging between about 50% and 160% stoichiometric
air. Temperatures were measured, where possible, simultaneously with
species measurements. The NOX measurements are believed to be within the
2 ppm error limits previously stated, with the exception of the hydrogen
data between 75% and 105% stoichiometric air, where the temperatures were
above those allowable for continuous operation of the combustor. The
uncertainty within this range of mixture ratios for hydrogen/air is assigned
at + 20% because of the shortened duration of testing at a given setting.
The results for the three fuel/air combinations are presented in Table C-2.
The NOX results for hydrogen/air are shown in Figure C-2. The
experimental results are reported on an "as measured" basis with water
removed to a 1% concentration. The calculated results plotted in the same
Figure were also corrected for water removal. The agreement between the
measured values and calculated values is good, with the calculated values
slightly higher than the experimental on the fuel-lean side and slightly
below the experimental on the fuel-rich side.
The results for carbon monoxide/air are shown in Figure C-3. To
aid combustion, hydrogen was added to the combustion zone at a constant
rate amounting to about 1% (volume) of the carbon monoxide rate at 150%
stoichiometric air and about 0.5% at 85% stoichiometric air. Although the
carbon monoxide was "moist", the correction for water is negligible. The
agreement between the experimental and calculated values of NOX is quite
remarkable considering the state of knowledge of the combustion reactions
and the temperature sensitivity of the NOX formation rates.
The agreement between the experimental values and the calcula-
tions is less satisfactory for propane/air (Figure C-4). The calculations
under-predict the measurements by about a factor of four on the lean side
and about an order of magnitude on the rich side. As will be discussed
later, since the mechanism used for propane combustion depends on the
mechanisms of hydrogen and carbon monoxide combustion, it is significant
that these values are low.
-------
C-5
FIGURE C-l
2000
5
>
H
TEMPERATURE (K
1500
REACTOR TEMPERATURES
I 1 1 i ill ! | I
/'^
- / - \
/ A
-/" -~A\°Q •
- / ^\j
/ \ V
A7 \ \^
- /& N \ (^
& \ \°
N V -
Q - HYDROGEN \ LJ
-Q - CARBON MONOXIDE &
/\- PROPANE
i i i i ii — i J — 1 1
50 100 150
PERCENT STOICHIOMETRIC AIR
FIGURE C-l - REACTOR TEMPERATURES FOR HYDROGEN/AIR, CARBON
MONOXIDE/AIR AND PROPANE/AIR IN THE JET-STIRRED
COMBUSTOR. OPEN SYMBOLS INDICATE EXPERIMENTAL
TEMPERATURES. SOLID SYMBOLS INDICATE TEMPERATURES
AT WHICH CALCULATIONS WERE MADE.
-------
C-6
TABLE C-2
COMPARISON OF EXPERIMENTAL AND THEORETICAL RESULTS
FOR THE JET-STIRRED COMBUSTOR
Per Cent
Stoichiometric
Air
Temperature
(calc from H)
(k)
NOX
measured
(ppm)
Reaction Volume = 14.5 cm
NOX
calculated
(ppm)
Fuel: Hydrogen Air rate: 0.70 I/sec T =
300°K
60
65
65
70
70
75
77
85
90
99
105
111
120
135
140
150
162
190
2030
2080
2080
2120
2120
2165
2180
2210
2210
2175
2140
2090
2000
1880
1830
1730
1640
1.5
13
15
20
20
25
35
34
60
45
70
40
40
16
7
3
0
0
Fuel: Carbon Monoxide
Air Rate 0.61 I/sec T = 450°K
76
76
85
87
87
98
105
118
120
135
146
150
2100
2100
2100
2080
2030
1965
1960
1870
1820
1805
80
110
—
118
120
97
—
80
—
—
20
—
140
105
70
30
16
-------
C-7
TABLE C-2 (Cont'd)
Per Cent
Stoichiometric
Air
Fuel: Propane
52
60
60
60
71
71
78
78
85
87
87
87
99
99
105
111
111
111
120
131
131
135
150
155
155
Temperature
(calc from H)
(k)
Reaction Volume =
Air Rate =0.61 I/sec T =
1800
1800
1800
1900
1900
1965
1965
2010
2015
2015
2015
2005
2005
1970
1925
1925
1925
1840
1750
1750
1715
1600
1570
1570
NOX
measured
(ppm)
14.5 cm
300°K
7
49
50
55
100
102
118
119
—
120
120
110
105
90
—
70
60
50
—
40
29
—
—
8
6
NOX
calculated
(ppm)
1
13
30
11
3
1
-------
C-8
150
I 100
CO
PH
a.
O* 50
55
0
FIGURE C-2
HYDROGEN - AIR
D - EXPERIMENTAL
• - CALCULATED
D
n
D
D
D
50
100 150
PER CENT STOICHIOMETRIC AIR
-B-
FIGURE C-2 - COMPARISON OF EXPERIMENTAL AND THEORETICAL CONCEN-
TRATIONS OF NO IN THE JET-STIRRED COMBUSTOR FOR
HYDROGEN/AIR. A
-------
C-9
150
FIGURE C-3
CARBON MONOXIDE - AIR
Q
g 100
W
1
s
0* 50
0
i • i i | i i i 1 1 1
• O - EXPERIMENTAL
• - CALCULATED
V*Ti
\~~J
o
o
o o
•
_ —
•
o. -
1 1 II 1 1 11 1 J 1
50
100 150
PER CENT STOICHIOMETRIC AIR
FIGURE C-3 -COMPARISON OF EXPERIMENTAL AND THEORETICAL CONCEN-
TRATIONS OF NOjj IN THE JET-STIRRED COMBUSTOR FOR
CARBON MONOXIDE/AIR.
-------
C-10
FIGURE C-4
PROPANE - Am
L— i
o
0
1
§
"x 50
55
^
0
/\- EXPERIMENT AI
A - CALCULATED
A A
A
A
A
//N \ /\
A
A
* A , i ,
50 100 150
PER CENT STOICHIOMETRIC AIR
FIGURE C-4 -COMPARISON OF EXPERIMENTAL AND THEORETICAL
CONCENTRATIONS OF NOx IN THE JET-STIRRED COMBUSTOR
FOR PROPANE/AIR.
-------
C-ll
The results of the calculations for hydrogen and carbon monoxide
combustion with air indicate that nitric oxide formation can be predicted
with good accuracy, even in a flame zone, provided the concentrations of
combustion intermediates can be calculated. The NOX values are under-pre-
dicted using a quasi-global treatment for propane. It should be stressed
that the values for the rate constants used in this study were pre-selected
and were not adjusted to give best fit to the data. The purpose of this
study was not to determine rate constants but to test the capabilities of
kinetic modeling and validate the use of the jet-stirred combustor for
testing kinetic models.
In the mechanisms used for this study, the reactions of primary
importance for nitric oxide formation are the exchange reactions of the
Zeldovich mechanism. However, the concentration of the oxygen atoms is not
assumed to be in equilibrium with molecular oxygen; it is determined by the
detailed kinetic mechanism. In fact, in the intensely backmixed system
with chain branching reactions occurring throughout the combustion zone,
the oxygen atom concentration can be substantially above that in equilibrium
with the molecular oxygen concentration.
"Superequilibrium" oxygen atom concentrations have been a matter
of discussion in the recent literature. In the case of this study, that
term is not unambiguous. There are two "types" of equilibrium concentra-
tions for oxygen atoms that can be considered. One is a "total" equilibrium
concentration calculated by minimization of free energy of the total system;
the other is a "partial" equilibrium concentration determined by combining
the measured or calculated molecular oxygen concentration with the equili-
brium constant for oxygen dissociation. In a well-stirred reactor, fresh
reactants are continuously mixed with products in the combustion zone.
Thus the concentration of molecular oxygen is above the value for total
equilibrium, especially under fuel-rich conditions where the concentration
of molecular oxygen can exceed the total equilibrium concentration by
orders of magnitude. For the purpose of this discussion the partial
equilibrium oxygen atom concentration will be used as the reference point.
Thus, under fuel-lean conditions, the well-stirred reactor
calculations indicate that oxygen atom concentrations exceed the partial
equilibrium value by up to a factor of 12 for hydrogen and up to a factor
of 100 for propane. Under fuel-rich conditions (60% stoichiometric air)
the oxygen atom concentrations exceed those calculated from K(02) •*•'^ by
a factor of 1.2 for hydrogen and about a factor of 50 for propane. The
calculated concentrations of molecular and atomic oxygen are shown in
Figure C-5.
The discussion of "superequilibrium" oxygen concentrations has an
interesting extension under fuel-rich conditions for propane-air combustion
in the jet-stirred combustor. The concentrations of nitric oxide observed
experimentally at 60% stoichiometric air are more than an order of magnitude
above those that would be calculated if the system were in "total"
-------
C-12
§
»—i
E-i
U
fc
W
O
10
-1
10
-2
10
-3
10
-4
FIGURE C-5
CALCULATED OXYGEN CONCENTRATIONS
50
MOLECULAR
OXYGEN
—r
ATOMIC
OXYGEN
HYDROGEN
— CARBON MONOXIDE;
__ PROPANE
,i.l.
100 150
PER CENT STOICHIOMETRIC AIR
FIGURE C-5 - CALCULATED CONCENTRATIONS OF MOLECULAR AND ATOMIC
OXYGEN IN THE JET-STIRRED COMBUSTOR FOR HYDROGEN,
CARBON MONOXIDE AND PROPANE COMBUSTION.
-------
C-13
equilibrium at the specified temperature. However, since both molecular
and atomic oxygen are also above their "total" equilibrium concentrations
by five and four orders of magnitude respectively under fuel rich conditions,
there is still a driving force to produce more nitric oxide. The model does
predict an NO level above that for "total" equilibrium at 60% stoichiometric
air for propane but still under-predicts the observed level by about an order
of magnitude. Thus, if a plug flow reactor were placed in series with the
jet-stirred combustor and sufficient residence time at combustion tempera-
ture were allowed for the combustion gases to approach equilibrium, the
concentration of nitric oxide would decrease to approach equilibrium.
In the case of hydrogen and carbon monoxide combustion, the ex-
change reactions of the Zeldovich mechanism (coupled to the combustion
reactions which determine the oxygen atom concentrations) appear to be
adequate for the prediction of nitric oxide formation. Under fuel rich
conditions for hydrogen, the measured values are somewhat higher than the
predictions suggesting that additional reactions may be required in the
model. In fact, when the reaction
N + OH = NO + H
was included for hydrogen combustion under rich conditions, the formation
of NO increased by up to 20%. The inclusion of this reaction in the propane
mechanism had about the same percentage effect under fuel-rich conditions.
As discussed earlier, a quasi-global mechanism was used for pro-
pane combustion. In this quasi-global mechanism, the hydrocarbon is oxidized
in a rate-limited single step to carbon monoxide and hydrogen, and the com-
bustion of these intermediates is then described by the same mechanism as
was used for carbon monoxide and hydrogen combustion. While substantial
oxygen atom concentrations are predicted by the model, the predictions for
nitric oxide formation fall below the measured values by about a factor of
four under lean conditions and about a factor of ten under rich conditions.
Alternatives to the quasi-global approach to propane combustion
coupled to the Zeldovich exchange reactions are possible. A more complete
mechanism for propane combustion might lead to better agreement between
calculations and experiments. Intermediates in the combustion mechanism
might alter the balance of atomic oxygen and atomic nitrogen and such inter-
mediates certainly exist throughout the reaction zone of the jet-stirred
combustor. However, under fuel-rich conditions for propane, it does not
appear likely that changes in oxygen atom concentration would be sufficient
to account for an order of magnitude in NOX production. Thus, the influence
of additional reactions directly involved in the formation of NO or perhaps
in the formation of readily oxidizable nitrogenous intermediates cannot be
dismissed at this time. One must, however, exercise great caution to avoid
adjusting parameters to fit existing data. Reactions which have little
-------
C-14
significance in the overall combustion scheme may be of importance in NO
formation under specific conditions. The valuation of the reactions signi-
ficant for the characterization of gross combustion phenomena is a formidable
task by itself. The numerous additional reactions which may be significant
under specific conditions for the formation of parts per million of nitric
oxide presents even more difficult problems. The jet-stirred reactor data
will provide a comparison point for parametric studies of the reaction
rates included in the kinetics evaluation described elsewhere in this report.
The comparison of NOX concentrations between experiment and cal-
culation for the case of hydrogen/air combustion in the jet-stirred combustor
indicates that the mechanism of coupled combustion and NOX formation is
fairly well determined. Under fuel-rich conditions the inclusion of the
reaction
N 4- OH = NO + H
in addition to the Zeldovich exchange reactions improves the agreement
between theory and experiment.
Good agreement is also found in the case of carbon monoxide/air
combustion. In both the hydrogen and carbon monoxide cases, substantial
oxygen atom concentrations are calculated and accounting for their presence
is apparently sufficient to allow prediction of nitric oxide formation.
For propane/air combustion, although substantial oxygen atom con-
centrations are also predicted, the use of a quasi-global mechanism for
hydrocarbon combustion results in underprediction of nitric oxide by about
a factor of four under fuel-lean conditions and about an order of magnitude
under fuel-rich conditions. It is not clear at present whether a more de-
tailed combustion mechanism would resolve the differences or whether
additional reactions for the formation of nitric oxide are required. How-
ever, it does not seem likely that an order of magnitude difference under
fuel rich conditions could be resolved by changes in oxygen atom concentra-
tion alone. It is clear that a quasi-global approach, which has been found
to be useful for the representation of combustion characteristics of a
variety of hydrocarbon fuels, is not adequate for the prediction of nitric
oxide formation.
In the jet-stirred combustor under fuel-rich conditions with
propane, the nitric oxide concentrations can be above those calculated
for total equilibrium at the specified mixture ratio. This NO "overshoot"
can be understood in terms of the model, in part by the "superequilibrium"
concentrations of molecular and atomic oxygen in a well-stirred reactor
under fuel-rich conditions. These "superequilibrium" molecular oxygen
concentrations are caused by the continuous mixing of fresh reactants with
products in the reaction zone.
-------
C-15
The jet-stirred combustor, operated in a manner that approaches
a well-stirred reactor, provides highly non-equilibrium behavior in a well-
defined system and, therefore, provides a severe test for any kinetic model.
As kinetic mechanisms become more complex, critical evaluation of the
component reactions becomes increasingly important. The coupling of kinetic
modeling with sophisticated fluid mechanic and heat transfer modeling is
ultimately required for application to pollutant formation in practical
combustion systems.
-------
C-16
REFERENCES
C-l Engleman, V. S., Bartok, W., Longwell, J. P., and Edelman, R. B.,
Fourteenth Symposium (International) on Combustion, p. 755, The
Combustion Institute (1973).
C-2 Edelman, R. and Fortune, 0., "A Quasi-Global Chemical Kinetic Model
for the Finite Rate Combustion of Hydrocarbon Fuels," AIAA Paper 69-86,
Seventh Aerospace Sciences Meeting, 1969.
C-3 Baulch, D. L., et al., "Critical Evaluation of Rate Data for
Homogeneous, Gas-Phase Reactions of Interest in High-Temperature
Systems," Nos. 1-5, Department of Physical Chemistry, The University,
Leeds, England.
C-4 Moretti, G. , AIM J. _3, 223 (1965).
C-5 Amman, P. R. and Timmins, R. S., AIChE J. 12, 956 (1966).
C-6 Brokaw, R. S., Eleventh Symposium (International) on Combustion,
p. 1063, The Combustion Institute, 1967.
C-7 Carnicom, M. L., "Reaction Rates for High Temperature Air with Carbon
and Sodium Impurities," Sandia Laboratories, SC-R-68-1797, May 1968.
C-8 Campbell, I. M. and Thrush, B. A., Trans. Faraday Soc. 64, 1265 (1968).
-------
'- NO
D-l
APPENDIX D
NO/NO PLOTS
X
- NO
x
Run Number 101, Premixed Flat Flame Burner (Laminar), Propane Fuel,
Stolchiometric Air, Cold Wall
250
Q 200
0)
CO
cd
CO
cd
O
25
150
100
50
60
80
100
120
140
160
Percent Stoichiometric Air
Run Number 102, Premixed Flat Flame Burner (Laminar), Propane Fuel,
106% Stoichiometric Air, Cold Wall
CO
cd
CO
cd
I
ex,
125
100 —
75 —
50 —
25
4 6
Axial Distance (Inches)
-------
D-2
0)
M
3
CO
«
I
W
cd
o
23
Run Number 103, Premixed Flat Flame Burner (Laminar), Propane Fuel,
103% Stoichiometric Air, Cold Wall
125
100 -
75 -
50 -
25
246
Axial Distance (Inches)
10
Run Number 103, Premixed Flat Flame Burner (Laminar), Propane Fuel,
122% Stoichiometric Air, Cold Wall
0)
t-l
CO
tfl
I
CO
cfl
e
ft
D,
O
25
125
100
75
50
25
J_
I
4 6
Axial Distance (Inches)
10
-------
D-3
Run Number 104, Premixed Flat Flame Burner (Laminar), Propane Fuel,
Stoichiometric Air, Cold Wall
-o
-------
D-4
I
03
CO
t
o
g;
Run Number 105, Stabilized Diffusion Flame Burner (Turbulent),
Methane Fuel, 101% Stoichiometric Air, Cold Wall
125
100
75
50
25
D
• •
D
>M
I
4 6
Axial Distance (Inches)
10
Run Number 106, Stabilized Diffusion Flame Burner (Turbulent),
Methane Fuel, 101% Stoichiometric Air, Cold Wall
CO
cfl
I
CO
tfl
p.
o
25
125
100
75
50
25
246
Axial Distance (Inches)
10
-------
V)
(0
I
CO
18
e
a
PL.
i
125
100
75
50
25
D-5
Run Number 108, Stabilized Diffusion Flame Burner (Turbulent),
Methane Fuel, 120% Stoichiometric Air, Cold Wall
_L
s
246
Axial Distance (Inches)
10
Run Number 109, Stabilized Diffusion Flame Burner (Laminar), Methane
Fuel, 107% Stoichiometric Air, Cold Wall
CD
CO
I
CO
CO
e
PL.
ft
i
125
100
75
50
25 -
4 6
Axial Distance (Inches)
-------
to
n)
-------
D-7
Run Number HO, Stabilized Diffusion Flame Burner (Laminar), Methane
Fuel, 86% Stoichiometric Air, Cold Wall
T)
0)
CO
cfl
125
100
75
I 50
p.
O
a
25
I
I
4 6
Axial Distance (Inches)
10
Run Number 111, Premixed Flat Flame Burner (Laminar), Methane Fuel,
104% Stoichiometric Air, Cold Wall
125
100
S 75
cn
t
ex
i
50
25
10
Axial Distance (Inches)
-------
D-8
3
to
cd
I
o.
o
2!
3
01
cd
CO
ct!
a
a.
Run Number 112, Premixed Furnace Burner (Turbulent), Methane Fuel,
96% Stoichiometric Air, Cold Wall
125
100
75
50
25
.D.
I
4 6
Axial Distance (Inches)
10
Run Number 113, Premixed Furnace Burner (Turbulent), Methane Fuel,
115% Stoichiometric Air, Cold Wall
125
100
75
50
25 -
10
Axial Distance (Inches)
-------
D-9
Run Number 114, Premixed Furnace Burner (Turbulent), Methane Fuel,
76% Stoichiometric Air, Cold Wall
•a
0)
CO
(fl
I
S
a
a,
i
125
100
75
50
25
4 6
Axial Distance (Inches)
10
s
3
CO
cfl
I
o
25
Run Number 116, Premixed Flat Flame Burner (Laminar), Methane Fuel,
119% Stoichiometric Air, Cold Wall
125
100
75
50
25
•g:
10
Axial Distance (Inches)
-------
D-10
Run Number 116, Premixed Flat Flame Burner (Laminar), Methane Fuel,
80% Stoichiometric Air, Cold Wall
T)
0)
l-i
3
CO
ed
cu
6
to
efl
t
&,
i
125
100
75
50
25
_L
_L
4 6
Axial Distance (Inches)
10
Run Number 117, Premixed Flat Flame Burner (Laminar), Methane Fuel,
161% Stoichiometric Air, Hot Wall 1430C
M
n)
E
0.
ex
125
100
75
50
25
4 6
Axial Distance (Inches)
10
-------
D-ll
Run Number 117, Premixed Flat Flame Burner (Laminar), Methane Fuel,
119% Stoichiometric Air, Hot Wall 1430C
-a
0)
M
CO
n)
I
e
CX.
P-
125
100
75
50
25
fp°-
pV
>D<
'D
••
I
I
4 6
Axial Distance (Inches)
10
Run Number 117, Premixed Flat Flame Burner (Laminar), Methane Fuel,
80% Stoichiometric Air, Hot Wall 1825C
13
0)
^
01
cfl
CO
-------
D-12
•a
(U
)j
ca
n)
ai
e
03
Cfl
I
P.
i
Run Number 118, Premixed Flat Flame Burner (Laminar), Propane Fuel,
61% Stoichiometric Air, Hot Wall 1565C
125
100
75
50
25
•
I
I
4 6
Axial Distance (Inches)
10
Run Number 119, Premixed Flat Flame Burner (Turbulent), Propane
Fuel, 110% Stoichiometric Air, Cold Wall
13
0)
05
td
i
125
100
75
50
25
a—a
_L
4 6
Axial Distance (Inches)
10
-------
D-13
Run Number 119, Premixed Flat Flame Burner (Turbulent), Propane
Fuel, 132% Stoichiometric Air, Cold Wall
125
100
75
50
25
_L
4 6
Axial Distance (Inches)
10
Run Number 119, Premixed Flat Flame Burner (Turbulent), Propane
Fuel, 88% Stoichiometric Air, Cold Wall
"d
-------
D-14
Run Number 120, Premixed Furnace Burner (Laminar), Propane Fuel,
156% Stoichiometric Air, Hot Wall 1495C
W
(8
s
Ifl
cfl
I
ft
Axial Distance (Inches)
Run Number 121, Premixed Furnace Burner (Laminar), Propane Fuel,
Stoichiometric Air, Hot Wall
•n
0)
M
w
ca
I
to
(X)
S
ft
ft
250
200 -
150 -
100
50 -
60
80 100 120
Percent Stoichiometric Air
140
160
-------
D-15
Run Number 122, Stabilized Diffusion Flame Burner (Turbulent),
Methane Fuel, 160% Stoichiometric Air, Hot Wall 1450C
CO
CO
C8
a,
a
o
53
125
100 -
75 -
50 -
25 -
10
Axial Distance (Inches)
Run Number 123, Stabilized Diffusion Flame Burner (Turbulent),
Methane Fuel, 140% Stoichiometric Air, Hot Wall 1590C
125
-d
3
CO
(fi
0)
e
I
100 -
75 -
50 -
25 -
4 6
Axial Distance (Inches)
10
-------
D-16
0)
M
03
cd
I
03
tfl
o
a
Run Number 123, Stabilized Diffusion Flame Burner (Turbulent),
Methane Fuel, 120% Stoichiometric Air, Hot Wall 1775C
250
200 -
150 -
100 -
246
Axial Distance (Inches)
10
Run Number 123, Stabilized Diffusion Flame Burner (Turbulent),
Methane Fuel, 80% Stoichiometric Air, Hot Wall 1825C
T3
-------
D-17
Run Number 124, Stabilized Diffusion Flame Burner (Turbulent),
Methane Fuel, Stoichiometric Air, Hot Wall
1250
60
80 100 120
Percent Stoichiometric Air
140
160
Run Number 125, Stabilized Diffusion Flame Burner (Turbulent),
Propane Fuel, 160% Stoichiometric Air, Hot Wall 1425C
250
200 -
-a
0)
M
3 150
CO
ca
B* 100
a
P.
i
50 -
4 6
Axial Distance (Inches)
-------
D-18
Run Number 126, Stabilized Diffusion Flame Burner (Turbulent),
Propane Fuel, 141% Stoichiometric Air, Hot Wall 1610C
T3
01
M
3
U]
CS
0)
CO
n)
e
P<
o.
o
2
500
400
300
200
100
4 6
Axial Distance (Inches)
10
Run Number 127, Stabilized Diffusion Flame Burner (Turbulent),
Propane Fuel, 114% Stoichiometric Air, Hot Wall 1870%
Cl)
N
3
w
cd
1
CD
CO
ex
o.
1000
800
600
400
200
Axial Distance (Inches)
-------
01
S-l
CO
nj
I
a
&
ft
D-19
Run Number 127, Stabilized Diffusion Flame Burner (Turbulent),
Propane Fuel, 80% Stoichiometric Air, Hot Wall 1870C
500
400
300
200
100
0 24 6 8 10
Axial Distance (Inches)
Run Number 127, Stabilized Diffusion Flame Burner (Turbulent),
Propane Fuel, Stoichiometric Air, Hot Wall
1250
1000 -
-o
cu
5 750
n»
I
CO
cfl
500 —
250 —
60
80 100 120
Percent Stoichiometric Air
140
160
-------
3
CD
CO
QJ
W
cd
B
ft
ft
O
a
D-20
Run Number 128, Stabilized Diffusion Flame Burner (Turbulent),
Methane Fuel, 140% Stoichiometric Air, Hot Wall 1590C
125
100
75
50
25
/ y
4 6
Axial Distance (Inches)
10
Run Number 128, Stabilized Diffusion Flame Burner (Turbulent)
Methane Fuel, 160% Stoichiometric Air, Hot Wall 1440C
125
0)
\-t
D
CO
tfl
I
CO
tfl
6
ft
ft
O
3
100 —
75
50 -
4 6
Axial Distance (Inches)
-------
T3
0)
(-1
CO
ta
01
CO
cd
i
D-21
Run Number 130, Premixed Flat Flame Burner (Laminar), Methane
Fuel, 140% Stoichiometric Air, Hot Wall 1585C
125
100
75
50
25
10
Axial Distance (Inches)
Run Number 131, Premixed Flat Flame Burner (Laminar), Methane
Fuel, 120% Stoichiometric Air, Hot Wall 1770C
3
CO
c«
I
CO
cd
t
OH
O
13
125
100
75
50
25
4 6
Axial Distance (Inches)
10
-------
3
en
cs
I
ex
o.
D-22
Run Number 131, Premixed Flat Flame Burner (Laminar), Methane
Fuel, 78% Stoichiometric Air, Hot Wall 1770C
125
100
75
50
25
_L
u 0 2 4 6 8
Axial Distance (Inches)
Run Number 131, Premixed Flat Flame Burner (Laminar), Methane
Fuel, 111% Stoichiometric Air, Hot Wall 1865C
10
p.
o
250
200 -
TJ
0)
a 150
I
100 -
50 -
4 6
Axial Distance (Inches)
10
-------
D-23
Run Number 131, Prefixed Flat Flame Burner (Laminar), Methane
Fuel, Stoichiometric Air, Hot Wall
M
01
cd
(0
CO
o
a
2000
1600 -
1200 -
800 -
400 -
60
80 100 120
Percent Stoichiometric Air
140
160
Run Number 132, Premixed Furnace Burner (Laminar), Methane Fuel,
160% Stoichiometric Air, Hot Wall 1440C
co
CO
CO
cfl
a,
a.
125
100
75
50
25
4 6
Axial Distance (Inches)
10
-------
D-24
Run Number 133, Premixed Furnace Burner (Turbulent), Methane
Fuel, 140% Stoichiometric Air, Hot Wall 1590C
•o
-------
D-25
Run Number 135, Premixed Furnace Burner (Laminar), Propane Fuel,
139% Stoichiometric Air, Hot Wall 1625C
0)
M
3
CO
ta
01
a
CO
C8
125
100
75
50
25
4 6
Axial Distance (Inches)
10
Run Number 136, Premixed Furnace Burner (Turbulent), Propane
Fuel, 141% Stoichiometric Air, Hot Wall 1610C
3
(fl
cd
a
a.
a
i
125
100
75
50
25
4 6
Axial Distance (Inches)
10
-------
D-26
Run Number 137, Premtxed Furnace Burner (Turbulent), Propane
Fuel, 121% Stoichiometric Air, Hot Wall 1795C
T3
a)
S-l
3
01
cfl
I
CO
to
P.
a,
125
100 -
75 -
50 -
25 -
4 6
Axial Distance (Inches)
10
Run Number 138, Premised Furnace Burner (Laminar), Propane Fuel
121% Stoichiometric Air, Hot Wall 1795C
-a
-------
D-27
Run Number 139, Premixed Furnace Burner (Laminar), Methane Fuel,
120% Stolchiometric Air, Hot Wall 1770C
'O
-------
D-28
Run Number 141, Premlxed Flat Flame Burner (Laminar), Methane
Fuel, 101% Stoichiometric Air, Cold Wall
125
100
CD
3
CD
CO
g 75
CO
50
25
VF
r
,D.
i
i
4 6
Axial Distance (Inches)
10
-------
E-l
APPENDIX E
CQ/C02/HC/02 DATA PLOTS
Run Number 102, Premixed flat Flame Burner (Laminar), Propane Fuel,
106% Stoichiometric Air, Cold Wall
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
IDE -1
0)
o
9E -1
8E -1
7E -1
*
D
*
*
* t
. D
• *
• •
» »
t •
N
•H
i-H
td
o
•H
4->
cd
(U
6E -1
4E -1
2E -1
i
0
,0,
•
M
OE -1
Axial Distance (Inches)
.M
in F o
-------
E-2
Run Number 103, Premixed Flat Flame Burner (Laminar), Propane Fuel
103% Stolchiometric Air, Cold Wall
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide = D, Carbon Monoxide = M, Oxygen = 0, Hydrocarbon = H
iOE -1
• •
> •
9F -1
• tftftftftftftftftD
ftOftftftftftftft**
8E -1
*•• *••»••*•
• «•*••»••••
*•••••••>.•
g •<•«•••••«
a)
o
» 7E -1
a) • •
*
T3
a) • •
N .
•H • •
3 6E -1
§ • '
* *
§
Tj 5E -1
c *
o •
o •
0 4E -1 .
• •••***••••
*••••••••*•
• •••••••*••
• ftftftftftt.tftft
3E -1 «....
• *•••••••••
• ••••••••••
• ••••*•••••
• *•••«••*•*
2E -1
• •*••••••*•
• ••••••••••
• *••••**•••
• ••••*****•
IE -1 M
• 0**ft*ft«(««
• •»••••>*••
• ••••••ftftftO
• ••••(ft...*
OE -1 H .........M
0 1 2 3 i> 5 6 7 8 910EO
Axial Distance (Inches)
-------
E-3
Run Number 103, Premixed Flat Flame Burner (Laminar), Propane Fuel, 122%
Stoichiometric Air, Cold Wall
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
IDE -1
9E -1
8E -1
§ 7E -1
CJ
-------
E-4
Run Number 104, Premixed Flat Flame Burner (Laminar), Propane Fuel,
94% Stoichiometric Air, Cold Wall
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
10E -1
«.(•*.«•••*
.**•••*••*«
9E -1
8E -1
• ««•*****«
.ODD * . . « . * • .
D . . .......
..........
7E -1
•««••><«•»
.... .......
..*..*«....
3E -1
.
2E -1 .
IE -1 0,
0
HO 0 . . . . . . . . . .
OE -1 HH.C.O ,.0
0 1 2 3 4 5 6 7 8 910EO
Axial Distance (Inches)
-------
E-5
Run Number 104, Premixed Flat Flame Burner (Laminar), Propane Fuel,
83% Stoichiometric Air, Cold Wall
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
iUC. — J.
9E -1
8E -1
"v
§ 7E -1
o •*•
0)
•0
0)
N
TH^I
H 6E -1
0
^
c
3 5E -1
*n -/i— •«••*
*•••••••
• ••••••*
• ••••••*
• •••*••*
• ••••**•
• •*•«*••
• ••••••*
• *••••**
• ft..****
• **•••*•
• •••••••
• ••••ft. •
• . . . * . • D
*•••••*•
• •••••••
........
• *••••••
*•••••*•
........
• •••••••
• •••••*•
• ••••••*
««»>••*•
• •••••••
• ••*•***
*••**•**
«••*••••
«•••••••
• .»»>••«
• •••••••
• *••••**
***•••••
• •**••••
». *•••*•
........
«••••••*
• ••••*••
3 4 5 6 7 8 910EO
Axial Distance (Inches)
-------
E-6
Run Number 105, Stabilized Diffusion Flame Burner (Turbulent), Methane
Fuel, 101% Stoichiometric Air, Cold Wall
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, OxygenO, Hydrocarbon=H
10F -1
• ••**••*•**
<••••*•••«•
• ••***••••*
• *•••••*•**
9E -1
**••**••••«
• •*•••*••••
*•*•••*.*•*
8E -1 •
• »*•••*
. * • • • • •
• * • ....
w •••••••••
g 7E -1
£ .««. ••••••
,55 . . . . . D . . . .
T3 •»•••«****
N ,..•••«•••
3 6E -1
«
• •••••..**•
§ .......»»••
3 «•«••••••••
c •••••»...••
° 5E -1
1-1
« ••••«**
£l •«*•**.
§ •»••••*
c ••*••**
3 4E -1
3E -1
• •«««•*•••»
• •.•••**.**
2E -1
IE -1 M
..*•*......
• •••*••••• M
• ••••••••*•
• ••••Hftftftft*
OE -1 0 ...0
0 1 2 3 4 5 6 7 8 910EO
Axial Distance (Inches)
-------
E-7
Run Number 106, Stabilized Diffusion Flame Burner (Turbulent), Methane
Fuel, 101% Stoichiometric Air, Cold Wall
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
10E -1
9E -1
BE -1
§ 7E -1
V-i
cu
•o
0)
N
6E -1
ts
o
5E -1
c
0)
3E -1
2E -1
IE -1
**•»••»
• ••••••
• •••••*
**»••**
• •**••»
• *»«•*•
• *•*•*.
**•••••
• «•••••
• «•*•*•
• *•(•**
• ••••••
* * * • * • D «
• * . . . 0 .
*******
*•****•
**•••*•
• •*•*••
• ••••••
• •••••*
• •••*•*
• • • t * • *
• *•••*•
*•*•>*•
* • • * t * *
*•**••*
. « . , M * *
• ••••••
. • * . D . t •
M •
• •••»••
• ••••••
. • * . M . * *
• *•****
*••••••
. . D . . • •
..... H .
• ••••••
«•••••«••• M4«..««»Q«0««»«0«0»««»«
• * • t
• • * *
• • • •
• * • •
• • • *
• • * •
• * • *
• • • *
• • • •
• • • *
• • • •
. . . D
• * • *
• . • •
• * t •
* • * •
• • • •
» t * •
* • • *
• • * *
* * * *
* • • •
* * • •
• * * •
t • * •
• • • •
* • * *
• • • *
* * • •
* * *
. . • .
t • • *
• t * *
• • • •
* * * t
• * * *
• i • *
. . . M
••••••••••••••«»»0
0 1 2 3 4 5 6 7 8 910EO
Axial Distance (Inches)
-------
E-8
Run Number 108, Stabilized Diffusion Flame Burner (Turbulent), Methane
Fuel, 120% Stoichiometric Air, Cold Wall
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
10E -1
9E -1
8E -1
*i 7E -1
V4
*
• < * *
7 8 9 10 E 0
Axial Distance (Inches)
-------
E-9
Run Number 109, Stabilized Diffusion Flame Burner (Laminar), Methane
Fuel, 107% Stoichiometric Air, Cold Wall
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
g
o
fc
-------
E-10
Run Number 109, Stabilized Diffusion Flame Burner (Laminar), Methane
Fuel, 128% Stoichiometric Air, Cold Wall
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, OxygenO, Hydrocarbon=H
ft ft ft ft * *
• *••••
. 0 . . . *
» H • • • *
• » M . * *
• *•••»
M
• • H . • i
* H* . . . .
4j ft ft ft ft ft ft
U ft ft ft ft ft ft
£
_. • * * * • *
Q> • • • • • *
i ::::?:
o ••••••
B •
•f-|
« . . . H . .
M . . . . . .
g . * D . . .
u • « • • • •
C • • ft • • •
. M . . . .
. * . . M .
. . . . . 0
• «•••»
• * » • • *
* • * • • *
• • • » • •
• D . . . •
• » * . 0 .
• * 0 . . .
» * . 0 . .
* D. . . . .
. « . * « M
• * • • H *
. M
012345
. . . • •
• • • • •
* • • • *
• • • • *
. * • • •
• • * * *
• • • • •
* • • • •
* • * * •
• » * • «
• • • • •
* • * • *
• * • • •
• • • * •
• • • • *
• * • • •
. . . . 0
* * • * D
* • * * *
• • • • •
• * • • »
• • • • •
• * * • •
• • • • *
• • • • •
* • • • *
. . . . »
* • • • •
* • * * •
* • • * •
* * * • *
* • • * •
• • • • •
• * • * «
* * • • •
* * * * •
• • • • •
6 7 8 9 10
10 E 0
Axial Distance (Inches)
-------
E-ll
Run Number 110, Stabilized Diffusion Flame Burner (Laminar), Methane
Fuel, 145% Stoichiometric Air, Cold Wall
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
4J
S
O
M
01
13
* *
* < * * *
* * * * *
* * • * >
. . . . 0
ft ft ft 1 ft
ft ft ft ft ft
ft ft ft ft ft
ft ft ft ft ft
ft ft ft ft ft
ft ft ft ft ft
ft ft ft ft ft
ft ft ft ft ft
ft ft ft ft ft
* . . * D
• « • • •
• • • • •
• • * * *
• • • * •
• • * • •
• • • • •
• • * * •
. . . • .
• • • * •
• • • • •
• • » • •
* • * • •
* • * • •
• • • * •
* • • * •
• • • • •
.M,
5
• M
10 E 0
Axial Distance (Inches)
-------
E-12
Run Number 110, Stabilized Diffusion Flame Burner (Laminar), Methane
Fuel, 86% Stoichiometric Air, Cold Wall
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
• ••*••»
ft ft ft ft ft • •
ft ft ft ft ft * ft
ft ft ft ft ft ft *
• •*••••
ft ft ft ft ft * *
. . . . H * •
* » • • • * *
• * • • • * •
• * • • • • •
• * * » » * *
S
a
Q> »•••«••
_, *******
g
1
§ H .
g, ftftftftftO*
_, •(•••**
3
H •••••••
g
o •••••••
* * * * D * »
• • . . 0 » «
* • • * • • *
* . * D . . .
• • • • • • *
»*•••••
• • • * * • •
0 .
* • • • • * •
• • * * * • *
*••**••
* * • * • * •
• • • • • • *
• « « « « « *
» • • • • » •
. . *
* * *
• • •
» • *
.
• • *
. • •
• • *
• • •
< • •
* * •
• • •
• * *
• * •
• • •
• • •
* • *
• * «
• • •
• • •
.
« • •
« • •
. .
* * *
* • •
• • *
• « *
• * •
• * *
* * *
• * *
• • •
• * •
• • •
• • *
• • *
• • •
, « (
.
•
•
*
.
*
•
*
.
•
•
*
•
•
•
•
D
*
«
.
*
•
H
•
*
,
.
.
.
*
,
0
•
*
*
*
,
0 1 2 3 4 5 6 7 8 910EO
Axial Distance (Inches)
-------
E-13
Run Number 111, Premixed Flat Flame Burner (Laminar), Methane Fuel,
104% Stoichiometric Air, Cold Wall
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
10E -1 ,
**•*«»•••••
*••*•••••••
9E -1
***••***•**
*»»••*«**••
BE -i !.........!....!...*!..**!....!
...........
...........
• ••ftODftftftftD
Q .. D D .......
g IE -1 ,
g OD. . .......
£ . D
TJ ...........
0)
N *•*•*...•••
3 6E -1
g ........
a ...» « • » •
2 5E -I
3) •*••***««••
tJ *•••*••••••
§ «•••»»«•«»•
g D
3 4E -1 •....
H « . . . . . . . . .
M ..........
• ••««•»•»••
3E -1
...........
• ••*»»•••••
2E -1
* . « • • . • . • • .
,0. . . « • • • • • •
. 0 •
. M . 0 • • • • • •
IE -1 0....0
0
M 0
. . M ........
...MM......
OE -1 «•ftH.Hft»•»H....H....H...«M.*••««................. »M
0 l 2 3 4 5 6 7 8 910EO
Axial Distance (Inches)
-------
Run Number 112, Premlxed Furnace Burner (Turbulent), Methane Fuel,
96% Stoichiometric Air, Cold Wall
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide*=M, Oxygen=0, Hydrocarbon=H
1
-
c
o
•H
4J
tO
S-i
4J
a
0)
8
o
o
IDE -1
9E -1
8E -1
7E -1
6E -1
5E -1
4E -1
3E -1
2E -1
IE -1
OE -1
.
ft
ft
•
ft
ft
ft
•
•
ft
f
,
ft
ft
ft
ft
ft
ft
.M
.D
•
.0
•
*
•
*
*
*
•
•
»
,
•
•
•
.H
•
•
•
0
• • • • * •
• • • • • •
• * • • • •
• « • • • •
• • • • • *
* * • • * •
• * • * * •
*>•••*
• • • • • *
* • * • • •
• ..DO.
. . D . . .
. D . . . .
* • • • • •
* • • * * •
* • • • • *
D « < . . .
D * • • • • •
* * • • * *
• • • * • •
M . . . . . .
M • . . . *
* * • • • •
0 . . . . .
• « • • • *
0 » * * . i «
ft ft ft ft ft ft
ft ft ft ft ft ft
ft ft ft ft ft ft
ft ft ft ft ft ft
• M . . . .
* 0 • • • •
* * M . . .
. . . 0 . ,
* • • • * •
H * . . . . .
H . . M M .
* * * • * *
123456
. . • •
. • « •
• • • •
* • * •
. * . .
• • • •
. • • •
. . ft
. !
. . . D
• • * *
• • • •
» • * *
* * » •
• • * *
* • • *
• • * •
» * * *
.
» • • *
• • • •
• • • •
• • * *
• • • *
• * • *
• * * *
.
* • * •
» • • •
• » * *
* • * •
* * • *
• • * •
* * • *
• * • •
* • • •
* • * *
* • • •
* * * *
7 8 91-0
Axial Distance (Inches)
-------
E-15
Run Number 113, Premixed Furnace Burner (Turbulent), Methane Fuel
115% Stoichlometric Air, Cold Wall
Normalized Species Concentrations CC-2/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
*•**•••
*•*•*••
• • ft ft ft ft ft
• * t ft ft ft ft
• • ft ft ft * ft
• • ft ft ft ft ft
• * ft ft ft ft ft
• «•*•»•
ft ft ft ft ft ft ft
• ft ft ft ft * ft
**•••••
ft ft ft ft ft ft ft
| . 0
fl)
° *!(«•«*
8 » 0 . . . . . .
.0 0 . . , . .
•H ftftDftftft*
cd •••••••
H D ••••(•
o
55 o * . . . . »
o .DDOOOOft
•H
*J • ••••••
cd
M ftDftftftftftft
§ •*****•
o »»**••*
CJ
**•*•«*
• ••«•**
«»«••••
. M . • • • • *
•M « « • • • •
• » * * * * *
«•*••*•
«•••••*
* * • • • • *
• ••••••
• ••*•*•
... • • • «
.H H M • • • •
*•••**•
H . . M • • •
• •
• •
• •
* *
• *
• «
» •
• *
• *
• •
* •
• •
• •
• *
• *
» *
• •
• *
* *
* •
• •
* •
• •
• »
• *
• •
* •
• *
• *
» •
• *
• •
• •
• *
* *
• •
• •
• •
• *
• •
•
•
•
•
•
•
*
*
•
•
*
*
*
*
*
*
*
•
•
•
•
*
*
•
*
•
•
•
*
*
•
•
•
•
»
•
*
»
*
*
*
•
*
•
*
•
•
•
*
•
*
*
•
*
•
•
•
•
•
•
0
»
•
•
*
•
*
•
•
•
*
•
*
*
*
»
•
*
*
*
10 E 0
Axial Distance (Inches)
-------
S
o
M
0>
PM
H
N
g
O
z
O
1-1
J-)
CO
M
4-1
C
E-16
Run Number 114, Premlxed Furnace Burner (Turbulent), Methane Fuel,
76% Stoichiometric Air, Cold Wall
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
• M « . . . M •
<*.«••*
• •••••*
.......
*••••••
.......
• •••**«
.<•••«•
• •»••»•
00000*0
0000000
000*000
• ••••••
• • • 0 * 0 0
• *•***•
0 • 0 0 • 0 0
. . . . . D .
* . D . « • • *
• *•«***
*»...«.
« 0 , . • . . •
.......
ODD .
.......
...*...
• «•«•>•
*»*•...
*...*••
.......
*«««««>
C ......
H
.......
• • 0 « . . . .
i . H « • * * •
• »•«...
• ••«*•*
0123456
0
0
*
0
0
0
•
0
0
0
0
0
*
0
0
0
0
0
0
0
0
.
0
0
0
0
•
0
0
0
0
0
•
0
.
.
.
7
. * *
. . .
. • •
* • •
» • •
* • •
• * •
• • •
• • *
* • •
• • »
* * *
* * *
* • •
. » •
. . D
• * •
* * »
• * •
...
. • •
• • •
» • •
• * *
* . *
. . .
* * *
* . *
. * •
* * •
• • •
• . *
» * *
. • •
. * *
• * *
• • H
8 9 10 E 0
Axial Distance (Inches)
-------
E-17
Run Number 116, Premixed Flat Flame Burner (Laminar), Methane Fuel,
119% Stoichiometric Air, Cold Wall
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
* • • ft
* * ft ft
• ft ft ft
• ft ft ft
• • » ft
• • ft ft
• • ft ft
• • ft ft
* * ft ft
• ft ft ft
* * ft ft
£ ....
« ....
0 ....
PU «...
rrt ft ft ft ft
g . . D .
S ....
5 • • • *
c . . . .
£ .0 0 0 0 .
h * * • .
§ ....
• • • •
* * • •
M . * .
* • » >
• • • *
* ...
....
• • • .
* ...
... *
.M . . .
HM M . . .
0123
• • • • • •
• •»•••
• * * » • •
.... • *
• * ... •
..*••*
**••••
......
......
......
.»*••*
» • • * * •
* *
* • * • • •
. D ... .
..*•••
• * . * * .
*•*••>
• • • * . .
. 0 . .. .
• • « * • *
. * . . * *
* . • ...
......
.*••*•
• * • ...
• ... » .
......
• *».*.
• .....
. . . . . .
* • ....
• *••<•
• * • ...
*• ....
. • • • • .
• • • • » »
456789
.
.
.
.
.
*
*
«
.
•
*
•
•
»
D
.
•
.
•
0
•
.
•
•
•
»
•
.
.
•
•
.
*
'
•
*
.
10
10 E 0
Axial Distance (Inches)
-------
E-18
8'
u
•o
cm«=H
10E -1
9E -:
8E -1
7E -]
6E -1
5E -1
-1
3E -1
2E -1
IE -!
OE -]
» * »
a a a
a a a
a a a
a M M
a M a a
aM a
a a a
a a a
a a a
D a a
a a a
M a
a a a
a a a
.D a a
aD D D a
. . D
a a a
a • a
a a a
• a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
0 a a
0 1 2
a a a
a a a
a a *
a a a
a a •
• t a
a a a
a a a
a a M
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a D
a a a
a a a
a a •
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
a a a
345
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
6
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
7
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
8
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
*
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
9
a
a
a
a
a
a
a
a
a
a
a
M
a
.
a
D
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
a
10 E
Axial Distance (Inches)
-------
E-19
Run Number 117, Premixed Flat Flame Burner (Laminar), Methane Fuel,
161% Stoichiometric Air, Hot Wall 1430C
Normalised Species Concentrations C02/15, CO/5, 02/10, HC/5
Lagancl - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon**
10E -1
9E -1
BE -1
0)
o
o
S5
s-/
C
3
•u
n)
g
o
6E -1
5E-'
4E -1
3E -1
2E -1
IE -1
OE -1
7E -1 H
*
*
*
*
*
«
*
*
*
•
•
•
.H
•
•
.
t
*
.H
*
*
,
•
*
•
*
•
.
t
•
.D
,
*
.M
• D
.M
• rl
M
*
*
•
• •••••••
*•**••*•
»•••••••
• *••*«••
*•••*•••
*••••«••
*•**••»•
• *««««.«
*•••••••
*•••**••
• •«*««««
»•••••••
• .......
........
*»•••**•
. .......
*•••*»••
»»......
• «•••••>
• **••«•*
*••*»••*
........
ODD
. . t . D . .
........
........
........
........
........
...*•*.*
........
....***.
........
........
........
..««*•«>
*.*...*.
....*»*.
..*•«««•
M ........
.
.
.
.
.
.
.
•
.
*
*
*
.
.
*
.
.
»
.
•
,
.
.
.
.
*
•
.
.
.
.
.
.
•
.
*
.
•
•
*
•
.
.
.
,
.
.
•
.
.
.
«
,
«
*
.
.
•
.
.
.
.
.
•
.
.
*
•
.
*
.
*
.
.
.
.
.
*
•
.
10 E 0
Axial Distance (Inches)
-------
E-20
Run Number 117, Premlxed Flat Flame Burner (Laminar), Methane Fuel,
119% Stoichiometric Air, Hot Wall 1430C
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Lagend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=O, Hydrocarbon*
10E -1
ft ft
ft ft
9E -1
-------
E-21
Run Number 117, Premixed Flat Flame Burner (Laminar), Methane Fuel,
80% Stoichiometric Air, Hot Wall 1825C
Normalized Species Concentrations O>2/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide-D, Carbon Monoxide-M, Oxygen-0, Hydrocarbon**
10E -1
1
0
ft
n
I
C
5
I
4-1
a
M
i
o
o;
o
ft ft
ft ft
ft ft
. M M
* *
• •
* *
* »
• *
* *
• t
• •
• •
.DO
• t
• *
• *
• •
• •
• •
* t
• •
• •
• •
• •
* •
• *
• •
• *
• •
* *
0 1
*•**••*••
• ****••*•
*•»*••••*
»••*»•*•*
*••*••*•*
. . . M . . . . .
*•*••••*•
*••*•**•*
*•*»•*•*•
• ••*»••*•
• *••»*•**
• **•*»•*•
**•*«»*••
• •*•*•*•*
• *•**•*•*
. • . D * * . * •
• •••***••
*•*»••*••
• *•**•**•
• *•***•**
*********
• ••*•••*»
• ••*•***»
*•***•••*
• ••*•*•*•
• •«••**••
*«•*••**•
,)••**•*•
• •*•*•*»*
• ••••••••
.••••*•*•
.••«••*•*
• •••****•
. . . ***** *
23456789 10
10 E 0
Axial Distance (Inches)
-------
E-22
Run Number 118, Premixed Flat Flame Burner (Laminar), Propane Fuel,
161% Stoichiometrlc Air, Hot Wall 1450C
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Lagend - Carbon Dioxide™D, Carbon Monoxide*^, Oxygen=0, Hydrocarbon=H
o
id
o
&
a
o
§
o
CJ
10E -1
9E -1
8E -1
7E -1
6E -1
5E -1
-1
3E -1
2E -1
IE -1
OE —1
.0.
•
•
•
t
.
*
•
t
,
H
•
• H
*
•
•
*
*
*
»
*
.
•
•
•
.
t
*
*
.
*
•
*
.
t
•
*
.D
• M
M
D
0
• *•*•**•
* ... 0 ...
.. ..••••
• •••••••
• «••»•••
***•*»**
• *••••••
*••••••»
*»**•**•
• •••«•••
..»«•«••
»*<•••«*
• ••>••••
• •••••••
• •>«»*•>
*•>««•«*
........
........
.*.»**..
. D
«»«.D...
i.....*.
*•••**•*
H* t • t * t • •
• •••*»••
• <*«•««•
• ....«..
D* • • . • • . .
• »««•«••
• ••«*•»*
(•*.«>..
• *•«•*••
*•••***•
• •«.....
• <««•«<«
• •.«•...
*•••****
*••***••
• ••***••
12345678
• *
• *
* *
• •
• *
• *
• *
* •
* *
* •
• •
• *
* *
* >
• .
• *
. .
• i
• »
* i
* t
i *
• *
* •
• *
• *
* •
• *
. .
• *
* *
• *
f .
. .
* t
• *
» *
, ,
t •
t •
9 10
10EO
Axial Distance (Inches)
-------
E-23
"d
-------
E-24
Run Number 119, Premixed Flat Flame Burner (Turbulent), Propane Fuel,
110% Stoichiometric Air, Cold Wall
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Lagend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen-0, Hydrocarbon=H
10E -1
• *••*•***»•
• ••*•••*•••
»«*««««*•••
«*•«««*«*••
9E -1
»»*••*•••••
««.«••«««»«
«*•«.*«««•*
• «•«.. •««**
8E -1 D.......... D
...D.......
• •Dt. ......
. D D . • . • • . * • •
DD * * *
IT 7E -1
-------
E-25
Run Number 119, Premlxed Flat Flame Burner (Turbulent), Propane Fuel,
132% Stoichiometric Air, Cold Wall
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxlde=M, Oxygen«0, Hydrocarbon-H
§
u
111
N
H
fl)
U
4J
§
O
I
10E -1
9E -1
8E -1
7E -1
6E -1
5E -1
4E -1
3E -1
2E -1
IE -1
OE -1
•
•
*
•
•
•
•
•
•
•
*
*
•
00
•
*
DD
•
•
•
•
•
•
t
•
*
t
•
•
•
•
•
*
MM
•
•
*
•
t
t
••••««
**••*»
*•**••
• ****•
• **•**
*••••*
*•***•
*•*•*•
• *••••
*•••••
«••««•
* • » • • •
0 • » t • * *
• D D • D •
• ••*••
0 * • * t •
• 00.**
D * * * * 0 »
*•••*•
******
• *••*•
*••*••
*«•**•
• ••••*
******
• ••«*•
*•••*•
• ••**•
****••
**•••*
• **•*•
******
******
*•••*•
M « • • • •
******
******
• •***•
t M * * * *
H H * * * * •
• * * *
• * * *
• * * *
* * * *
* * * *
* * * *
* * * *
• * * *
• * * *
• * * *
• * * *
• * * *
* * * *
* * * D
• * * *
• • • •
• * * *
. . • 0
• • • »
* * * *
* * • •
* * * *
• • • •
• * * *
• * * *
* * * *
• • • •
• * * *
* * * *
* * * *
* * * *
* * * *
* * * *
• * * *
• * * *
* * * *
* * * *
* * * *
* * * *
* * * *
,M.
3
,M<
5
234567
Axial Distance (Inches)
.M
10 E
-------
E-26
Run Number 119, Premixed Flat Flame Burner (Turbulent), Propane Fuel,
88% Stoichiometric Air, Cold Wall
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Moapxide=M, Oxygen=0, Hydrocarbon=H
10E -1 *.*•» «i •«
§
y
o
S3
O
o
*••*»••
**•**••
*.««.**
• ••••**
• »•»*«•
• »••***
• *•••*•
• ••»•••
*««««*•
. t • M « . .
« t . • . M .
• • M • « * •
. M .....
.*..***
*•««*«*
. M . . . . . *
•M » . . . . .
.*....*
M * .....
.......
. i . . . t *
......*
«•<««•»
«*«««»•
.......
.......
....**.
.......
.......
. t . . * * *
.....*•
.*.....
.*...**
.*...*.
.......
• •««••«
• «««•*•
*......
DD D D D D . D .
* 0 0 0 ...
0123456
. * * *
. . * •
. . • •
« . • .
* . * .
. * • .
«...
....
....
. . • .
. • . .
....
. . . M
. . * .
. * * *
....
....
....
. • . .
....
. • . .
....
....
....
....
....
....
....
. . . .
....
....
. • * .
• * * .
• . . .
....
. t * .
* * * .
* * • .
. • . D
• • « .
7 8 9 10
Axial Distance (Inches)
-------
§
•H
4J
ed
M
u
§
G
O
u
E-27
Run Number 120, Premixed Furnace Burner (Laminar), Propane Fuel,
156% Stoichiometric Air, Hot Wall 1495C
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=O, Hydrocarbon-*!
10E -1 ...0.0 0 ,
9E -1
8E -1
£ 7E -1
S
o
2 6E -1
5E -1
3E -1
2E -1
IE -1
OE -1
•
*
•
•
.
•
•
.
.
H
*
•
•
•
.
*
*
.
.
,
*
*
.
.
i
.H
.D
*
.
.
*
.D
.M
•
•
D
MM
•
.
0
* ...
• • * .
* ...
* ...
* ...
* * * *
• ...
* ...
....
• ...
• ...
• • * .
....
....
• ...
• ...
....
• ...
t * . .
....
D D . . .
• D * •
• ...
....
....
«...
* ...
* ...
«...
«...
* ...
. • • •
«...
• ...
....
•
• * * *
* ...
• « • •
...»
1234
..... 0
......
*.*.*.
• •••••
......
......
......
«••*•«
......
......
* . . i . .
*...*•
......
......
......
......
......
......
......
......
......
D * . . . D
......
......
......
......
......
......
......
......
......
......
......
......
......
......
......
• *....
......
......
5 6 7 8 9 10 E
Axial Distance (Inches)
-------
E-28
Run Number 122, Stabilized Diffusion Flame Burner (Turbulent), Methane
Fuel, 160% Stoichiometric Air, Hot Wall 1450C
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide-D, Carbon Monoxide=*M, Oxygen=0, Hydrocarbon=H
I
Hi
•o
0>
10E -1
9E -I
BE -1
7E -1
6E -1
o 5E -1
•H
-------
E-29
Run Number 123, Stabilized Diffusion Flame Burner (Turbulent), Methane
Fuel, 140% Stoichiometric Air, Hot Wall 1590C
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide-D, Carbon Monoxide=M, Oxygen=0 , Hydrocarbon=H
• •
• •
• *
• •
* •
• *
• t
• •
* t
t »
• *
/•N • •
fl)
0 • •
ti
1) • *
* t .
•o
$ * t
N AE-1
« • •
C * •
o
53 • *
O
• t
u . «
(I)
M * *
4J
c • •
•**
• *D*****0
• i*««**0*
• ••**»••*
»««Mt»»«»
**••****•
• ••**•••*
«M«»«Ot««
• t*******
»••••••••
t********
«iO<*»*<*
• ••••*»*•
»•*••*•»•
(*••«*••»
«•••*•**•
«•»••*••*
,,.»tM»««
• •••*•**•
«••*•***•
,.ti«t»M«
(••f****M
2 3456789 10
Axial Distance (Inches)
-------
E-30
Run Number 123, Stabilized Diffusion Flame Burner (Turbulent), Methane
Fuel, 120% Stoichiometric Air, Eot Wall 1775C
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Lagend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen-0, Hydrocarbon=I&
««««
• (*•••*••
«>••<•«•»
.H .......
. . * M . . . . .
.........
...*...**
.........
.........
.........
. M .......
.........
.........
* * * D . * . . *
.........
. . D . . . . * *
*•<«•••*.
.........
.....M...
.........
. .
........ 0
....... 0 *
.........
.D .......
.........
. . 0 . . 0 . . .
*.....*..
.......M.
. . . 0 . . . . M
• ......•*
* • . H . . . . .
• •*».....
i H i
7
• HI
9
i.H .
10 E 0
Axial Distance (Inches)
-------
E-31
Run Number 123, Stabilized Diffusion Flame Burner (Turbulent), Methane
Fuel, 80% Stoichiometric Air, Hot Wall 1825C
NennalSzed Species Concentrations COa/15, CO/5, 02/10, HC/5
Legand - Carbon Dioxide-D, Carbon Monoxide-M, Oxygen=0, Hydrocarbon-H
§
o
"3
N
e
o
•H
•U
a
w
o
o
10E -1
9E -1
8E -1
7E -1
6E -1
5E -1
4E "
3E -1
2E -1
IE -1
OE -1
*••••••••
• • • . M . . . .
••••**••*
•••••••••
•*••**•••
•*•*•••••
• • . H . . . . .
**•••*•••
• •*••••••
• • • . H . . . .
• •••t****
• *««•«««•
• •••*•**•
• »•••••••
» * • • 0 • • . *
• •««•••*«
• •***••••
**••»••»•
• ***•••**
• *******•
• •*«..*««
• *««..«••
• »*******
• ***•••••
• •*•*•*••
...... D . .
• •««•««.«
0 ...
0 ...
• «<*«<«*.
. * . . D • • • •
...... H * .
«••«•*•*•
.«•<««•*•
. . * 0
• ••••••••
...... 0 « •
....... H .
.....*•••
....... 0 .
. .
. .
. .
. .
. ,
. .
. (
. .
. .
. .
* .
. .
, .
. *
. .
. .
. .
• .
. •
. .
. .
. .
. .
. 4
* .
• .
. .
*
.
. (
• .
*
. .
. •
. .
. .
. .
* .
. .
• 0
10EO
Axial Distance (Inches)
-------
E-32
Run Number 125, Stabilized Diffusion Flame Burner (Turbulent), Propane
Fuel, 1602 Stoichiometric Air, Hot Wall 1425C
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen«0,
10E -1
9E -1
BE -1
a
•*
• ••••••»•
. 0
• •••••»**
«**.«••»*
....... M .
• * • 0 ... . .
• • 0 • . . . . M
.........
• ••••••*•
» ........
M
7
iH.ftft.H
9 10 E 0
Axial Distance (Inches)
-------
fi-33
Run Number 126, Stabilized Diffusion Flame Burner (Turbulent), Propane
Fuel, 141% Stoichiometric Air, Hot Wall 1610C
normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
L«g«nd - Carbon Dioxide«=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
10E -1
9E -1
8E -1
7E -1
a
ai
u
h
0)
CM
O
O
% 6E -1
4-1
2
4J
§
-1
4E -1
-1
IE -1
•
•
•
•
.
•
•
•
.
*
*
•
.
•
•
•
*
•
•
•
.
•
•
,
.
,
.
•
*
t
•
•
,
t
,
•
*
•
•
*
• »••••••
**••••**
***•***•
**H**«tt
• «•<•••>
• *•*•*•»
t • • H t * . •
• *•••*•»
• «««•«••
*•*•*•**
*««••••«
**••»»*•
• »*<••••
*«•«•««<
« • * » H . • •
*•••••••
• «*..•••
• *•••* D •
• *•••••!
* • • • * » • »
. . • • • D * .
• •*•*•••
...*••••
««•«••••
• ••§••••
*.«*•»••
• •••••••
. • • D » • • •
• »•••••»
. . D . . H . .
• *••••»•
(*•*»•••
...... 0 .
• »•*••**
• •***•**
. . . . • 0 . .
, . . . 0 . H .
• •••••••
• •«•••••
• •••••••
• .
• •
* .
* *
* *
• •
* *
* *
. .
« •
« •
* .
* *
. D
* •
* *
• *
• •
* *
* •
. .
• •
* .
• «
• t
• 0
* »
• *
• •
• •
* *
.
• •
* •
* *
• *
• •
• *
* *
OE -1 H
0 1 2 T> 4 5 6 7 8 910EO
Axial Distance (Inches)
-------
E-34
Run Number 127, Stabilized Diffusion Flame Burner (Turbulent), Propane
Fuel, 114% Stoichiometric Air, Hot Wall 1870C
Normalized Species Concentrations C02/15, CO/5, 02/10, EC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, OxygenO, Hydrocarbon*H
a)
u
PM
£
a
o
iH
4J
rt
l-l
4J
1
C
O
U
10E -1
9E -1
8E -1
7E -1
6E -1
5E -1
4E -1
3E -1
2E -1
IE -1
OE -1
• «
* t
» »
* •
* •
* •
* •
• •
• *
* t
• *
* «
. .
* *
• *
* (
. .
t •
* t
* •
• *
• •
• *
* f
• *
* *
• *
•
. .
1 t
t •
, ,
• •
* *
• •
. .
• •
* (
* •
0 1
**••(•*••
««•«««««*
«•«•••••*
*•••*•••*
• ••*••***
• ••*••*•*
• H.**»...
• •••••»*•
.........
...*..*..
**...***.
*....*.*.
• ««*..«*D
..**..**.
.........
*..*...«.
..... D ...
.........
.0
.........
• ••D.*...
.........
.....*...
.........
.........
.........
.........
.«....***
*D.......
.........
........0
«««H<«»««
*....**..
.........
*
-------
E-35
Run Number 127, Stabilized Diffusion Flame Burner (Turbulent), Propane
Fuel, 80% Stoichiometric Air, Hot Wall 1870C
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide8"]*, Oxygen^O, Hydrocarbon=H
10E -1
9E -1
8E -1
*? 7E -1
8-
o
K
-------
E-36
Run Number 128, Stabilized Diffusion Flame Burner (Turbulent), Methane
Fuel, 160% Stoichiometric Air, Hot Wall 1440C
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Leg«ad - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
10E -1
9E -1
8E -1
4-1
f 7E -1
•8
N
I
6E -1
5E -1
a
d
a
a
3E -:
2E -]
IE -1
OE -1
ft ft
ft ft
ft ft
• •
ft ft
ft ft
ft ft
ft ft
ft ft
ft ft
ft t
ft ft
ft ft
ft ft
ft ft
ft ft
, ,
ft ft
ft ft
ft ft
ft ft
ft ft
ft ft
• *
ft .
ft ft
ft ft
ft 1
ft ft
• •
ft ft
ft ft
ft ft
ft ft
ft ft
• •
ft ft
ft ft
t ft
• •
0 1
• ••••••ft*
• ••*•••*•
• •••••••ft
ft********
****•»•••
• *••***•*
****•*»••
• *••*•*••
• ..**•*».
**•••••••
• •*****•»
ft********
»*•••*•»•
*••****»•
• ••*•*•*•
0
• MftftftftfttO
0 * . .
• •ftftftftftO*
• •***•»••
. * M . • * . D •
* . . D . * * . .
. . D
•
*•••**••*
. . . M * . « • .
. D . . . . . . .
***•*•••*
• ••••••••
• ••••••••
• • . * * M * * *
**•*•*•*»
• •H*ft*ftt«
• ••*•*•••
• ••••** M .
• •*•*••* M
• •**•*•••
• • . H . * . , .
• **••***•
2 3 4 5 6 7 8 910EO
Axial Distance (Inches)
-------
E-37
•u
3
•o
-------
E-38
0)
N
Run Number 130, Premlxed Flat Flame Burner (Laminar), Methane Fuel,
140% Stoichlometric Air, Hot Wall 1585C
Normalized Species Concentrations C0£/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=*M, Oxygen»0, Hydrocarbon=H
10E -1
9E -1
8E -1
g 7E -1
o
N-
****ftft*********»«**>M
OE -1
3 4 5 6 7 8 910EO
Axial Distance (Inches)
-------
E-39
™*. Premlxed Flat Flaffie Burner (Laminar), Methane Fuel,
120% Stolchiometrlc Mr, Hot Wall 1770C
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide-D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon-H
10E -1
8
o
M
0)
PU
•o
M*********M»***********************M
3 4 5 6 7 8 910EO
Axial Distance (Inches)
-------
E-40
Run Number 131, Premlxed Flat Flame Burner (Laminar), Methane Fuel,
78% Stolchlometric Air, Hot Wall 1770C
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon«H
10E -1
9E -1
8E -1
7E -1
o
FM
•a
i«*»t>«*H**>************»»****it«H
0 1 2 3 4 5 6 7 8 910EO
Axial Distance (Inches)
-------
E-41
Run Number 131, Premised Flat Flame Burner (Laminar), Methane Fuel,
111% Stoichlometrlc Air, Hot Wall 1865C
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon^H
IDE -1
g
o
o
a
o
2
.u
-------
E-42
Run Number 131, Premixed Flat Flame Burner (Laminar), Methane Fuel,
101% Stoichiometric Air, Hot Wall 1945C
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
a
-------
E-43
Run Number 132, Premised Furnace Burner (Laminar), Methane Fuel,
160% Stoichiometric Air, Hot Wall 1440C
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
a)
o
01
H
o
a)
M
4-1
ti
-------
E-44
Run Number 133, Premixed Furnace Burner (Turbulent), Methane Fuel,
160% Stoichiometric Air, Hot Wall 1440C
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
y
M
10E -1
9E -1
8E -1
7E -1
•O
0>
.2 6E -1
§ 5E -1
•H
a
0)
g 4E -1
*
t
•
*
,
*
•
•
.
•
•
•
*
t
»
t
.
«
•
•
,
*
*
*
*
*
.
*
*
•
•
«
.
*
*
*
t
*
•
•
*
•
t
t
*
.
*
*
*
*
t
*
t
•
*
t
•
*
*
*
•
•
,
1
•
*
*
.
*
•
I
*
*
t
*
.
*
D
*
*
•
*
•
t
.
•
*
.
t
*
*
,
H
*
•
*
*
•
*
.
•
*
*
.
a
«
*
.
*
*
*
.
*
*
,
•
.
M
*
* • • »
* • § *
• » « •
• * * *
. 0 .
• « • •
• * • •
* • * *
* * i *
• • * «
• * * *
* * * •
* • * •
* • * •
* • • i
* * • *
tt*«
* • * *
* * * *
* * * *
• • • •
* * * *
• * * *
* . D * *
* • * *
* H D . .
* * * *
* D * * *
* * * *
• D » » «
• * * *
• * * *
* * * *
* * * *
. H . .
M MMM. * .
* M . *
. . M . .
* * * *
* * * *
* * * *
* * * *
* * * *
* * * *
. * * 0
• * * *
* * * *
* * * *
* * * *
• * • *
* * * *
. . . .
• * * *
• * * •
• * * •
* * • *
• • * •
* • • •
* * * *
• * * *
• • * *
* * * *
* * • *
* • • •
• * * •
* • * *
* • * *
• * * •
* * * *
* • * *
• * * •
* * * *
* • • *
* * * •
• * * *
* • • *
• • • *
* • • *
• * * *
3E -1
2E -1
IE -1
OE -1 M .....M....... ........M
0 1 2 3 4 5 6 7 8 910EO
Axial Distance (Inches)
-------
E-45
Run Number 133, Premixed Furnace Burner (Turbulent), Methane Fuel,
140% Stoichiometrlc Air, Hot Wall 1590C
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
0)
o
§
-------
E-46
Run Number 134, Prefixed Furnace Burner (Laminar), Methane Fuel,
140% Stoichiometric Air, Hot Wall 1585C
Normalized Species Concentrations C02/15, GO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
IDE -1
a
01
u
M
- A
AC ^1
*r u 4t
?E -1
£. L. ifc
IE -1
OE -1
*
*
•
*
.
•
*
«
*
•
*
,
•
•
«
•
•
•
•
,
D
•
•
.
•
•
*
•
*
•
•
.
«
*
•
•
•
•
M
H.
0
* * •
i « *
* » •
• * *
* * *
* • •
* • *
• * »
• • •
. 0 0
ft ft ft
0 • .
ft ft ft
ft ft ft
ft ft ft
ft ft ft
ft ft ft
ft ft ft
ft ft ft
ft ft ft
t ft ft
ODD
* . .
* • •
• * •
• * •
* • •
* • »
. * .
* * *
* * •
* * *
* * •
* • •
• • •
* • •
• « •
• * •
* • •
* * •
• •ftMftftftftMftftftftMft*
1 2 3
* * * • • *
« * • • • *
. * • • • *
* * • • • *
. . • * • *
* « • • • *
* • * * * •
**•»••
• • * * * •
0 0 . . . .
• > • • • •
• • * * • •
• • • * * *
• • * • * •
• • • • * •
• * * * * *
. . . . . *
• * * • * *
• * • * • •
* < • • • «
» « * • • •
0 • * • * *
* D * • • *
* * * • • •
• * * * • •
• * * • • *
• * * * * *
• • * • • •
* • • • • *
• * • * « •
• » • * * •
• * * • • •
• * • • • *
* • • » • *
. • * * • •
• * * * * *
• * • * • *
* * » * • *
• • * * • •
• * * « * *
••Mftft**M*ft*ftft***ft**ftftftftft*ftftft*
456789
*
*
•
•
.
*
*
*
,
*
0
*
*
•
*
•
.
•
*
•
*
,
D
•
*
*
•
•
.
•
*
*
.
•
•
•
*
•
.
t
...M
10
Axial Distance (Inches)
-------
E-47
Run Number 134, Premixed Furnace Burner (Laminar), Methane Fuel,
65% Stoichiometric Air, Hot Wall 1600C
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
a
01
o
M
0)
PH
"S
N
•H
I
a
o
•rl
4-1
td
M
4J
§
o
o
10E -1
9E -1
8E -1
7E -1
6E -1
5E ..
4E -1
3E -1
2E -1
IE -1
OE -1
ft ft
ft t
« ft
ft ft
ft
* ft
ft ft
• •
ft ft
ft ft
ft ft
• •
ft .
ft ft
ft t
ft ft
ft .
ft 1
ft ft
ft ft
ft ft
ft ft
* ft
ft *
ft ft
ft ft
ft ft
ft ft
t t
ft t
ft •
•
ft ft
ft ft
ft ft
ft ft
ft ft
ft ft
t t
t
• •«**•*•
• *•***•*
• <•*•***
• •••(••ft
*»•••**(
• •••**•*
. H
*«*•••**
• ••*•••*
. * H * * . . •
• •**••••
• *••••*•
• •••«••*
• •*••••*
* * «H» • • • •
• •••••••
• **•*•••
• •***•»•
. M
.
**••***•
• »••••••
**•*••*•
• *•»•*••
• *•*•**•
• *••••••
. . . 0 . . . . •
*••*••••
• ••••*••
. . . D D . D . .
. * . H • • • •
. D . . . • *
........
. . 0
• •»•*•••
..*•••••
...OH...
..*.*•••
H .
. . . 0 . 0 . *
•
*
«
*
*
t
*
•
*
*
•
•
.
•
•
*
*
*
•
•
*
*
*
•
•
»
*
*
*
D
*
•
«
•
•
•
•
»
•
0
'•H
10 E 0
Axial Distance (Inches)
-------
0)
o
E-48
Run Number 135, Premixed Furnace aurner (Laminar), Propane Fuel,
139% Stoichlometric Air, Hot Wall 1625C
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide«D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
o
o
10E -1
9E -1
8E -1
7E -1
6E -1
5 5E -1
(0
M
g 4E -1
3E -1
2E -1
IE -1
ft ft ft ft ft ft ft
• **•*••
ft ft ft ft ft ft ft
ft t ft ft ft ft *
***•••*
ft ft ft ft ft ft ft
. . . 0. . . .
ft ft ft ft ft ft ft
ft ft ft ft ft ft ft
. » . 0 0 0 «
• ••••»•
ft ft ft ft ft • •
* . H . . * •
• * « • • * *
» • « • • • •
• • • • • • »
• • • • • * *
• * • • • * *
• • * * * t •
> » • • • » •
• » * • • * *
• ft.*D* • * •
* « * • • * •
• • • • • • *
• * • • • • •
. . . D . . . .
• . . H . . • •
• • • • • * •
• • • • • * *
• ft • • • » *
.0 . . * .
• • • > * • •
• . . . . . •
• • D • • * *
• • * • • « *
. . *M MH. . . .
M . .
. . M. . . .
• • • • • * *
• * • *
• • • •
• * * *
. * • •
.
• » » •
« • • •
. . » .
. . • 0
• • • •
• • • .
.
• • * *
• • • •
• • * •
• • * *
. . . .
* • * •
• * * *
* • • •
* . D
• • * *
* * * •
. .
• • • •
• • * •
. • • •
• * * •
• * * *
• * • *
* * • •
* • • *
* • * *
• » • •
• • * •
• * • •
• * * *
• • • •
• • * *
• * • *
OE -1 M....M....M..* M
0 1 2 3 4 5 6 7 8 910EO
Axial Distance (Inches)
-------
E-49
Run Number 136, Premlxed Furnace Burner (Turbulent), Propane Fuel,
141% Stoichiometric Air, Hot Wall 16 IOC
Normalized Species Concentrations C02, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
10E -1
9E -1
8E -1
S 7E -1
0)
y
•o
0)
N , r ,
•H 6E -1
§ 5E -1
2
4J
g
o
§ 4E -1
u
3E -1
2E -1
««*«••«.
**«•«««*
•4.0.....
••••••••
• »••*»•*
• »•••«••
• «»*••*•
*»«o.,,«
* . . . 0 . .
««««««»•
• « • • 0. * • •
* * H » * * • •
. . . * 0 0 . .
*•«.•>«*
«.««•<.<
»•»••»«•
* * * • D D . .
• «»«•»••
. ... D. ...
«**D«**«
*»...*.*
***«••*•
. . . D. . . . .
. . . D
. . . H. • * * *
««*.*•**
• •••••*•
• «••••••
. . .MM. . . • •
. . M. . .
..MM....
**•««••»
. . . .M . * * *
. . . . M . • • •
. . . . HM. . • •
... HM ...
* • «
...
...
.
...
...
...
...
...
...
...
...
...
. • 0
...
. . .
...
...
. * D
. . .
• . .
...
...
...
. . .
...
• . *
. . .
...
. . .
...
...
. . *
. . .
. . .
. . .
. * *
• . •
. . .
. . .
IE -1
OE -1 H....M M
0 1 2 3 4 5 6 7 8 910EO
Axial Distance (Inches)
-------
E-50
Run Number 137, Premixed Furnace Burner (Turbulent), Propane Fuel,
121% Stolchlometric Air, Hot Wall 1795C
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dloxlde=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
• •«••*•
• »••***
**•••••
• <*•*<*
ft ft ft ft ft ft ft
• t ft ft ft ft *
ft ft ft ft ft ft ft
ft ft ft ft ft * ft
ft ft ft ft ft ft ft
. « . . . D .
"£• . • . D D . .
g D
0)
PH • * . . . • •
13 ••*••••
H>**ftHftftft«Hftft*ftHft>ftft*ftftft*ftftftft*ft**ftftftftft»ftM
0 1 2 3 4 5 6 7 8 910EO
Axial Distance (Inches)
-------
E-51
Run Number 138, Premixed Furnace Burner (Laminar), Propane Fuel,
121% Stoichiometric Air, Hot Wall 1795C
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, OxygenO, Hydrocarbon=H
0)
o
•a
g
•rt
4-1
a
0)
a
o
IDE -1
9E -1
8E -1
7E -1
6E -1
5E -1
4E -1
3E -1
2E -1
IE -1
* * 4 4
* * 4 4
* 4 4 ft
4 * ft ft
• * 4 4
* * 4 4
* * 4 4
* 4 4 4
* * * 4
* * ft 4
0 . . .
44*4
* * 4 4
* 4 DD D D
* D D 4 4
* 4 0 4
* 4 404
4*40
4*44
4*44
4 ft ft ft
ft 4 4 4
4444
4444
4444
4444
4444
4444
• 4 4 4
4444
4 * * 4
4 * ft •
4*44
4444
ft * • 4
4444
4444
4*44
M * . .
• * «
ft 4 4
444
444
4 4 4
444
444
444
444
444
444
444
444
4*4
4 D 4
4 4 ft
ft ft 4
4 0 4
444
444
444
444
444
ft ft 4
4 4 ft
ft ft ft
ft ft ft
ft ft ft
ft ft ft
ft ft ft
ft ft •
ft ft •
ft ft ft
ft ft 4
444
ft ft •
ft 4 4
444
44*
4
ft
ft
ft
ft
ft
ft
ft
4
4
4
4
4
4
4
4
4
4
4
4
4
4
4
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
4
4
4
4
4
4
4
4
4
4
4
4
4
4
4
4
4
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
4
4
4
4
4
4
4
4
4
4
4
4
*
4
4
4
4
4
4
4
4
4
4
4
4
4
4
4
4
4
4
4
4
4
4
4
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
4
4
D
4
4
0
4
4
4
4
4
4
4
4
4
4
4
4
ft
ft
ft
ft
4
ft
ft
ft
ft M M 4 ft
OE -1 H.44.H44H.KM.M.M
0123
ft ft ft ft ft ft
i :"••«••«••••••««•••••••••• M
5 6 7 8 910EO
Axial Distance (Inches)
-------
E-52
Run Number 139, Premlxed Furnace Burner (Laminar), Methane Fuel,
120% Stoichiometric Air, Hot Wall 1770C
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
x-x
JJ
c
0)
o
0)
FM
(U
N
•H
fH
I
O
\^X
P
O
•H
^ i
to
^
•U
(3
(U
o
a
o
*->
IUC
9E
7 Imp.
8E
7E
6E
5E
-X i—
4E
3E
2E
IE
OE
-i
-1
-1
-1
-1
-i
J.
-1
-1
-1
-1
-1
•
•
*
•
•
*
t
•
•
•
*
•
•
*
•
D
•
•
*
•
*
•
•
0
•
•
*
*
•
•
•
ft
*
•
•
•
•
•
(/
•
H. ..
0
*
•
•
*
t
»
•
t
*
i
*
•
»
*
,
D
•
•
*
*
t
*
0
*
•
*
*
•
.
*
•
*
*
•
•
•
*
*
«
M
• H*
1
»
*
•
•
•
•
•
•
•
•
»
•
•
•
,
D .
n
•
•
•
*
§
0 0
•
•
•
*
t
*
.
•
»
•
t
•
*
•
•
•
•
M .
.H.M.
2
•
•
•
•
•
•
•
*
•
•
•
•
t
•
,
.
.
,
•
•
0
•
•
•
•
•
•
•
•
•
*
•
*
*
*
•
>
•
•
• • • M • <
3
ft
*
•
•
•
•
*
•
t
*
*
•
*
•
*
*
•
*
*
•
*
*
•
ft
»
•
ft
ft
ft
ft
ft
ft
•
ft
ft
ft
ft
ft
ft
ft
t • * • •
4
•
•
•
•
*
*
*
*
*
t
•
•
f
•
*
D
•
•
•
•
•
0
•
•
•
•
•
•
•
•
•
*
t
*
•
•
•
•
•
•
• • »M • • i
5
ft
•
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
ft
•
ft
ft
ft
ft
ft
ft
ft
•
ft
ft
ft
ft
ft
,
,
9 • ft ft
6
»
•
•
•
•
*
•
•
•
•
*
•
•
•
•
•
•
•
•
•
•
•
•
•
•
•
•
*
•
•
•
•
•
•
•
•
•
•
.
.
• • * t • •
7
•
•
•
•
•
*
•
*
•
•
•
•
•
•
•
•
*
t
•
•
•
•
*
*
•
•
*
»
•
*
•
*
*
•
*
*
*
•
.
,
••••••
8
*
»
•
•
•
*
•
•
•
»
*
•
t
•
•
*
*
•
*
•
•
*
•
•
•
•
•
•
•
•
§
•
•
•
•
•
*
•
*
•
« • » •
9
*
•
*
•
*
•
»
•
•
•
•
»
t
•
•
•
•
D
•
«
t
•
0
»
•
•
•
•
•
•
t
•
•
•
•
•
•
•
•
•
• «M
10
10 E 0
Axial Distance (Inches)
-------
E-53
Run Number 140, Premixed Furnace Burner (Turbulent), Methane Fuel,
120% Stoichiometric Air, Hot Wall 1775C
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, Carbon Monoxlde^-M, Qxygen=0, Hydrocarbon=H
* * * ft ft ft ft
•••**••
• * * ft ft ft ft
• • ft ft ft ft ft
• • ft ft ft ft ft
*•**•»•
• ft ft ft ft ft ft
»*•*•*•
^ *•••*..
4J
(3 •••••••
j[j •*•»**•
GU
m •*••••(
"3 •••••••
£ . . D D . D .
jjj D D . . . * .
,g •••*•••
^ » . . . . . *
o »*•••••
o •••••••
* •••••••
s • '
v •••«•••
0 ••«••••
§ 00
• * • •
• * * •
* • • *
• • * *
• « « •
• • * *
• • * •
• • • •
• * * •
• • • •
• • • •
• • • •
* • * •
* * » •
• • • *
. . . D
• • * *
• • • •
• * * •
• • • •
* • • »
. . * .
* • • ft
. . • •
0 . 0 . . . . 0
ft ft •
• •••**
3E -1
2E -1
• •ft******
«•••*••*•
• ft*******
M * * *
(*•••**••
• ••*••**•
• ••*••••»
• •*****•*
. . M
. . . M . * * * *
..... M . . .
, .
• •
• •
• •
» *
• *
• •
• •
.
• •
* •
IE -1 H
OE -1
0 1 2 3 4 5 6 7 8 910EO
Axial Distance (Inches)
-------
E-54
Run Number 141, Premixed Flat Flame Burner (Laminar), Methane Fuel,
101% Stoichiometric Air, Cold Wall
Normalized Species Concentrations C02/15, CO/5, 02/10, HC/5
Legend - Carbon Dioxide=D, 'Carbon Monoxide=M, Oxygen=0, Hydrocarbon=H
f ft ft ft ft ft •
• *••••*
• ft ft ft ft ft ft
• »*••*«
ft ft ft ft ft ft ft
ft ft ft ft ft ft ft
ft ft ft ft ft ft ft
ft • ft ft ft ft ft
• * . D . >Dft *
•£ » • D • • • • •
• • *
• • • *
» * * «
* * • •
• • * •
. . * .
• . • •
• • • »
* • • •
* • • t
• * » «
• • » •
.
* * * •
* » • »
* * t •
. . . M .
7 8 9 10
Axial Distance (Inches)
-------
APPENDIX F
DATA LISTINGS
RUN NUMBER 101
PREMIXtD FLAT FLAME BURNER
PROPANE
WALL-COLD AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.036
0.030
0.043
0.036
O.C36
AIR
FLOW
(CFM)
0.854
0.854
0.854
C.S54
0.854
PCT
STOIC
AIR
9S.3
119*4
83.0
9 3 . 3
98.3
AXIAL
DIST
(IN)
10.00
10.00
10.00
10.00
10.00
RADIAL WALL
DIST TEMP
( IN) (C)
0.00
0.00
0.00
0.00
0.00
NO
(PPM)
145
50
72
145
NOX
(PPM)
57
02
(PCT)
0.06
3.40
0.04
O.C5
0.05
CO
(PCT)
0.707
0.003
4.510
0.599
CC2 HC
(PCT) (PPM)
13.79
11.73
10.73
13.79
-------
RUN NUMBER 102
PREFIXED FLAT FLAME BURNER
PROPANE
WALL-COLD AIR PREHEAT-NONE
FUEL
FLOW
(CF'-n
0.071
0.021
0.021
0.022
0.022
0.022
0.0?1
0.071
0.071
0.021
0 . C ? 1
C.C71
0.021
0.021
0.021
0.071
0.021
0.071
0.021
0.071
0.071
0.021
0.021
AIR
FLOW
(CFM>
0.546
0.5^6
0.546
0.546
0.546
0.546
0.546
0.546
0.546
C.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
PCT
STOIC
AIR
106.1
106.1
106.1
100.7
100.7
100.7
106.1
106.1
106.1
106.1
106.1
106.1
106.1
105.1
106.1
106.1
106.1
106.1
106.1
106.1
106.1
106.1
106.1
AXIAL
DIST
(IN)
10.05
5.05
1.05
1.05
0.40
0.30
1.00
1.00
1.00
1.00
1.00
1.00
1.00
1.00
1.00
1.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
RADIAL
DIST
(IN)
0.00
0.00
0.00
0.00
0.00
0.00
0.00
0.20
0.40
0.60
0.80
-0.80
-0.60
-0.40
-0.20
0.00
0.00
0.20
0.40
0.60
0.80
1.00
-0.80
WALL
TEMP
(C)
NO
(PPM)
98
88
75
88
50
40
63
74
65
en
88
92
87
70
62
66
103
105
106
106
100
103
103
NOX
(PPM)
101
98
98
108
65
58
87
80
75
85
95
97
92
80
70
83
110
107
108
107
103
107
105
02
(PCT)
1.15
1.10
1.20
0.43
0.53
0.54
1..40
1.35
1.25
1.20
1.50
1.80
1.40
1.25
1.30
1.45
1.30
1.40
1.35
1.55
2.25
1.75
2.10
CO
(PCT)
0.003
0.024
0.389
1 .068
1.269
1.328
0.466
0.258
0.079
C.01S
0.008
0.005
0.010
0.036
0.159
0.209
0.003
0.003
0.003
0.003
0.003
0.003
0.003
CC2
(PCT)
13.01
13.01
12.50
12.50
12.50
12.24
12.50
12.50
13.01
13.27
13.27
13.01
13.27
13.27
12.75
12.75
13.01
12.75
12.75
12.50
12.50
12.24
12.24
HC
< PPM
2.
3.
2.
2.
2.
2.
25.
10.
6.
5.
4.
4.
4.
3.
3.
3.
2.
2.
2.
2.
2.
2.
2.
to
-------
RUN NUMBER 102 CONT
PREMIXED FLAT FLAME BURNER
PROPANE
WALL-COLD AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.071
0.021
0.021
0.021
AIR
FLOW
(CFM)
0.546
0.546
0.546
0.546
PCT
STOIC
AIR
106.1
106.1
106.1
106.1
AXIAL
DIST
(IN)
10.00
10.00
10.00
10.00
RADIAL WALL
DIST TEMP
(IN) (C)
-0.60
-0.40
-0.20
0.00
NO
(PPM)
106
99
101
101
NOX
(PPM)
108
102
103
103
02
(PCT)
1.50
1.40
1.60
1.70
CO
(PCT)
0.003
0.003
0.003
0.003
C02
(PCT)
12.75
12.75
12.75
12.75
HC
(PPM)
2.
2.
2.
2.
u>
-------
RUN NUMBER 103
PREMIXED FLAT FLAME BURNER
PROPANE
WALL-COLD AIR PREHEAT-NONE
FUEL AIR PCT AXIAL RADIAL WALL NO NOX 02 CO C02 HC
FLOW FLOW STOIC DIST DIST TEMP
(CFM) (CFM) AIR (IN) (IN) (C) (PPM) (PPM) (PCT) (PCT) (PCT) (PPM)
0.021 0.546 106.1 10.00 0.00 103 108 1.10 0.003 12.75 2.
0.022 0.546 103.4 10.00 0.00 108 116 0.38 0.007 13.01 3.
0.022 0.546 103.4 10.00 1.00 111 118 0.83 0.005 13.01 1.
C.022 0.546 103.4 10.00 0.80 106 113 1.30 0.004 12.50 1.
0.022 0.546 103.4 10.00 0.60 113 118 0.75 0.004 12.75 1.
0.022 0.546 103.4 10.00 0.40 113 120 0.55 0.005 13.01 1.
O.C?2 0.546 103.4 10.00 0.20 115 119 0,50 0.006 13.27 1.
0.322 0.546 1C3.4 10.00 -0.80 113 120 1.30 0.004 12.75 1.
0.022 0.546 103.4 10.00 -0.60 115 120 0.60 0.004 13.01 1.
0.022 0.546 103.4 10.00 -0.40 113 120 0.50 0.005 13.01 1.
O.C72 0.546 103.4 10.00 -0.20 111 118 0.60 0.005 13.01 1.
0.022 0.546 103.4 10.00 0.00 111 118 0.50 0.006 13.27 1.
0.022 0.546 103.4 1.00 0.00 60 90 1.10 0.352 12.24 1,
0.022 0.546 103.4 1.00 1.00 88 95 1.25 0.016 13.01 1.
0.022 0.546 103.4 1.00 0.80 «5 100 0.80 0.026 13.27 1.
0.022 0.546 103.6 1.00 0.60 65 77 0.70 0.113 13.27 1.
C.OP2 0.546 103.4 1.00 0.40 62 85 0.75 0.337 12.75 1.
0.022 0.546 103.4 1.00 0.20 76 108 0.85 0.028 12.50 1.
0.022 0.546 103.4 l.OC -0.80 97 100 1.20 0.009 13.01 2.
0.022 0.54-6 1C3.4 1.00 -0.60 93 98 0.35 0.036 13.27 3.
C.022 0.546 103.4 l.CO -0.40 67 80 0.45 0.199 13.27 1.
0.022 0.546 103.4 1.00 -0.20 75 95 0.75 0.455 12.50 1.
0.022 0.546 103.4 1.00 0.00 75 95 0.73 0.464 12.50 1.
-------
RUN NUMBER 103 CONT
PREMIXED FLAT FLAME BURNER
PROPANE
WALL-COLD AIR PREHEAT-NONE
FUEL AIR PCT AXIAL RADIAL WALL NO NOX 02 CO C02 HC
FLOW FLOW STOIC DIST DIST TEMP
(CFM) (CFM) AIR (IN) (IN) (C) (PPM) (PPM) (PCT) (PCT) (PCT) (PPM)
C.018 0.546 122.0 1.00 0.00 45 60 4.00 0.075 10.98 1.
0.013 0.546 122.0 1.00 0.20 40 54 3.90 0.072 11.23 2»
0.01S 0.546 122.0 1.00 0.40 47 55 3.90 0.059 10.98 1.
0.018 0.546 122.0 1.00 0.60 38 43 3.90 0.025 11.23 1.
0.018 0.546 122.0 1.00 0.80 42 43 4.00 0.004 11.48 1.
0.013 0.546 122.0 1.00 1.00 41 45 4.20 0.003 11.48 1.
0.018 0.546 122.0 1.00 -0.80 43 46 4.00 0.005 11.48 1.
0.018 0.546 122.0 1.00 -0.60 37 42 3.90 0.006 11.48 1.
0.018 0.546 122.0 LOO -0.40 31 39 3.95 0.020 11.23 1.
0.013 0.546 122.0 1.00 -0.20 37 42 3.95 0.072 10.98 1.
0.0-18 0.546 122.0 10.00 0.00 50 50 3.90 C.OC3 10.98 1. f
0.018 0.546 122.0 10.00 0.20 50 51 4.00 0.003 11.23 1. w
0.019 0.546 122.0 10.00 0.40 49 50 4.00 0.003 10.93 1.
O.C1S 0.546 12?.0 10.00 0.60 50 51 4.20 0.002 11.23 1.
0.018 0.546 1?2«0 10.00 0.80 47 48 4.60 0.002 10.73 1.
0.018 0.546 122.0 10.00 1.00 46 47 4.70 0.002 10.98 3.
0.018 0.546 122.0 10.00 -0.60 45 46 5.00 0.002 10.73 3.
C.018 0.546 122.0 10.00 -0.60 49 50 4.30 0.003 11.23 2.
0.013 0.546 122.0 10.00 -0.40 49 50 4.20 0.003 11.23 3.
0.018 0.546 122.0 10.00 -0.20 50 51 4.10 0.003 11.23 8.
0.013 0.546 122.0 5.00 0.00 39 48 4.00 0.005 11.23 9.
0.01S 0.546 122.0 2.00 0.00 36 45 4.10 0.031 10.98 3.
0.018 0.546 122.0 1.00 0.00 31 37 4.20 0.066 10.73 5.
-------
RUN
PREMIXED
WALL-COLO
NUMBER 103 CONT
FLAT FLAME BURNER
PROPANE
AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.018
0 . 0 1 S
0.0 IS
0.013
0.01S
0.018
0.013
0.018
0.018
0.018
AIR
FLOW
(CFM)
0.546
0.552
0.552
0.55?
0.552
0.552
0.546
0.546
0.546
0.546
PCT
STOIC
AIR
122.0
123.3
123.3
123.3
123.3
123.3
122.0
122.0
122.0
122.0
AXIAL
DIST
(IN)
1.00
1.00
1.00
1.00
1.00
l.OC
1.00
1.00
1.00
1.00
RADIAL WALL
DIST TEMP
(IN) 1C)
0.20
0.80
0.60
1.00
0.40
-0.20
-0.20
-0.40
-0.20
-0.30
NO
(PPM)
32
31
NOX
(PPM)
36
35
02
(PCT)
4.20
4.40
4.30
4.60
4.30
4.30
3.90
3.90
3.90
3.90
CO
(PCT)
0.073
0.005
0.014
0.004
0.046
0.044
0.066
0.023
0.060
0.042
C02
(PCT)
10.98
10.98
10.98
10.98
10.98
10.98
10.98
10.98
10.98
10.98
HC
(PPM)
7.
7.
7.
7.
8.
7.
7.
7.
7.
i
cy.
-------
RUN NUMBER
PREMIXED FLAT FLAME BURNER
PROPANE
WALL-COLD AIR PREHEAT-NONE
FUEL
FLOW
(CFv>
0 . 0 1 B
C . 0 1 8
C.018
0.018
C.0-18
C.018
0.013
O.C18
c.ois
o.oi a
0.0-13
0.024
C.024
0.024
0.074
0.024
0.0?4
C.024
0.024
0.024
0.024
0.024
0.024
AIR
FLOW
(CFM)
0.546
0.546
0.546
0.546
0.546
C.546
0.546
0.546
0.546
0.546
C.546
0.546
0.546
0.546
C.546
C.546
0.546
C.546
0.546
0.546
0.546
0.546
0.546
PCT
STOIC
AIR
122.0
122.0
1 2 ? . 0
122.0
122.0
122.0
122.0
122.0
122.0
122.0
122.0
93.5
93.5
93.5
93.5
Q3.5
93.5
93.5
93.5
93.5
93.5
93.5
93.5
AXIAL
DIST
(IN)
1.00
l.CO
1.00
1.00
1.00
1.00
l.CO
1.00
1.00
1.00
1.00
1.00
1.00
1.00
1.00
1.00
1.00
l.CO
1.00
1.00
1.00
1.00
0.70
RADIAL
DIST
(IN)
0.00
-0.80
-0.60
-0.40
-0.20
0.00
0.20
0.40
0.60
O.PO
l.OC
1.00
0.80
0.60
0.40
0.2.0
0.00
-0.20
-0.40
-0.60
-0.80
0.00
0.00
WALL
TEMP
(O
NO
I PPM)
32
63
65
60
72
93
78
70
60
67
69
77
73
NOX
(PPM)
41
02
(PCT)
3.90
4.50
4.10
3.95
3.97
3.90
4.00
4.05
4.00
4.20
4.60
C.15
0.05
0.03
0.04
0.03
0.07
0.05
0.03
0.04
0.23
0.08
0.09
CO
(PCT)
0.076
0.004
0.006
0.018
O.C55
0.079
0.073
0.046
0.016
0.006
C.CC4
1.927
2.012
2.012
2.273
2.724
2.632
2.362
2.099
1.927
1.421
2.451
2.451
C02
(PCT)
10.73
10.98
10.98
10.98
10.73
10.73
10.49
10.73
10.98
10.98
10.73
12.75
12.24
12.24
11.99
11.23
11.48
11.48
11.99
12.50
12.75
11.48
11.48
HC
(PPM)
1.
1.
2.
2.
2.
2.
2.
2.
2.
2.
2.
3.
3.
4.
4.
4.
4.
4.
4.
4.
4.
4.
4*
-------
RUN NUMBER 104 CONT
PREMIXED FLAT FLAME BURNCR
PROPANE
WALL-COLD AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.024
C * 0 2 4
0.024
0.024
0.024
0.024
0.024
0.024
0.024
0.024
0.324
0.024
0.024
0.024
0.024
0.024
0.027
O.C27
0.027
0.027
0.027
0.027
0.027
AIR
FLOW
(CFM)
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
C.546
0.546
0.546
0.546
0.546
0.546
PCT
STOIC
AIR
93.5
93.5
93.5
93.5
93.5
93.5
93*5
93.5
93.5
93.5
93.5
93.5
93.5
93.5
93.5
93.5
83.2
83.2
83.2
83.2
R3.2
P.3.2
83.2
AXIAL
DIST
( IN)
0.50
0.30
0.20
0.10
0.05
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
RADIAL WALL
DIST TEMP
(IN) ( C >
0.00
0.00
0.00
0.00
0.00
0.00
0.20
0.40
0.60
0.80
1.00
-0.80
-0,60
-0.40
-0.20
0.00
C.OO
0.20
0.40
0.60
0.80
1.00
-0.80
NO
(PPM)
65
55
48
38
20
84
83
81
80
70
66
63
80
63
86
86
61
62
64
64
55
56
49
NOX
(PPM)
02
(PCT5
0.16
0.24
0.27
0.46
1.00
0.03
0.03
0.08
0.10
0.50
0.50
0.80
0.20
0.07
0.04
0.03
0.03
0.03
0.04
0.09
0.40
0.38
0.70
CO
(PCT)
2.451
2.451
2.541
2.632
3.007
1.757
] .841
1.757
1.672
1.337
1.421
1*421
1 .588
1.757
1.757
1.757
4.274
4.274
4.153
4.274
3.824
4.045
3.824
C02
(PCT)
11.48
11.48
11.48
11.23
10.49
12.75
12.24
12.24
12.24
12.24
12.24
12.24
12.24
12.24
11.99
11.99
9.99
10.24
10.24
10.24
10.24
10.24
9.99
HC
(PPM)
4.
4.
4.
80.
1200.
2.
2.
2.
2.
2.
2.
2.
2.
2.
2.
2.
2.
2.
2«
2.
2.
2.
2.
-------
RUN NUMBER 104 CONT
PREMIXED FLAT FLAME BURNER
PROPANE
WALL-COLD AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.027
0.027
0.027
0.027
0.027
0.027
0.027
0.027
0.027
0.027
0.027
0.027
0.027
0.0?7
0.027
0.027
C.027
0.027
0.027
0.027
0.027
0.027
0.027
AIR
FLOW
(CFM)
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
PCT
STOIC
AIR
83.2
83.2
83.2
83.2
P3.2
83.2
R3«2
83.2
83.2
83.2
83.2
83.2
83.2
83.2
83.2
83.2
83.2
83.2
83.2
83.2
83.2
83.2
83.2
AXIAL
DIST
(IN)
10.00
10.00
10.00
10.00
10.00
1.00
1.00
1.00
1.00
1.00
1.00
1.00
1.00
1.00
1.00
0.70
0.50
0.30
0.20
0.10
0.00
0.05
0.10
RADIAL
DIST
( IN)
-0.60
-0.40
-0.20
0.00
0.00
0.20
0.40
0.60
0.80
1.00
-0.80
-0.60
-0.40
-0.20
0.00
0.00
0.00
c.oo
0.00
o.oo
-0.20
-0.20
-0.20
WALL
TEMP
(C)
NO
(PPM)
65
66
65
65
63
68
67
56
54
51
54
63
50
65
66
62
59
55
52
46
14
25
51
NOX
(PPM)
02
(PCT)
0.18
0.05
0.03
0.02
0.01
0.01
0.01
0.01
0.05
0.17
C.20
0.04
0.02
0.02
0.03
0.03
0.03
0.04
0.05
0.18
3.60
1.75
0.08
CO
(PCT)
4.045
4.158
4.158
4.274
4.882
4.882
5.011
4.391
4.158
3.824
3.933
4.158
4.391
4.756
5.011
4.756
4.756
4.756
4.632
4.632
4.274
4.632
4.510
C02
(PCT)
10.24
10.24
10.24
10.24
9.51
9.51
9.51
10.24
10.73
11.23
10.98
10.49
10.24
9.51
9.51
9.75
9.51
9.51
9.75
9.51
7.60
8.54
9.75
HC
(PPM)
2.
2.
2.
1.
1.
1.
2.
10.
15.
15.
4.
5.
4.
1.
1*
1.
1.
1.
1.
600.
20000.
8500.
550.
*i
-------
RUN NUMBER 105
STABILIZED DIFFUSION BURNER
METHANE
WALL-COLD AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.2?5
0.225
0.225
C.225
0.225
0.225
0.225
0.225
0.225
C.225
0.?25
0 . 2 ? 5
0.225
0.225
0.225
0.725
0.225
AIR
FLOW
(CFM)
2.172
2.172
2.172
2.172
2.172
2.172
2.172
2.172
2.172
2.172
2.172
2.172
2.172
2.172
2.172
2.372
2.172
PCT
STOIC
AIR
101.2
10] .2
101.2
101.2
101.2
101,2
101.2
101 .2
101 .2
101.2
30] .?
101.2
101.2
101,2
101.2
101.2
101.2
AXIAL
DIST
( IN)
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
1U.OO
5.00
5.00
5.00
5.00
5.00
5.00
RADIAL WALL
DIST TEMP
(IN) < C )
-0.03
0.80
0.60
0.40
0.20
0.00
-0.20
-0.40
-0.60
-0.80
-0.86
0.00
0.20
0.00
0.20
0.40
0.60
NO
(PPM)
40
28
31
33
35
34
33
33
30
26
27
25
22
37
35
28
23
NOX
(PPM)
44
33
35
38
41
41
47
41
38
34
34
33
30
46
42
35
27
02
(PCT)
0.05
0.08
0.07
0.05
0.05
0.04
0.04
0.04
0.05
0.06
0.07
0.05
0.06
1.25
3.50
2.60
4.00
CO
(PCT)
0.304
0.017
0.045
0.147
0.204
0.304
0.285
0,304
0.190
0.073
0.050
0.501
0.501
1.689
1.039
0.493
0.109
C02
(PCT)
11.23
10.73
10.73
10.98
10.98
10.98
10.98
10.98
10.73
10. 9B
10.98
9.99
10.24
9.99
10.24
10.24
9.75
HC
(PPM)
1.
1.
1.
1.
1.
1.
1.
1.
1.
1.
1.
900.
300.
400.
110.
20.
20.
-------
RUN NUMBER 106
STABILIZED DIFFUSION BURNER
METHANE
WALL-COLD AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.225
0.725
0.225
0.225
0.225
0.225
0.225
0.225
0.225
0.225
0.225
0.225
0.225
AIR
FLOW
(CFM)
2.172
2.172
2.172
2.172
2.172
2.172
2.172
2.172
2.172
2.172
2.172
2.172
2.172
PCT
STOIC
AIR
101.2
101.2
101.2
101.2
101.2
101.2
101.2
101.2
101.2
101.2
101.2
101.2
101.2
AXIAL
DIST
( IN)
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
5.40
5.00
4.00
3.50
2.00
RADIAL WALL
DIST TEMP
(IN) (C)
0.00
0.20
0.40
0.60
-0.60
-0.40
-0.20
0.00
0.00
0.00
0.00
0.00
0.00
NO
(PPM)
39
36
34
26
34
36
49
40
33
33
2
1
0
NOX
(PPM)
48
43
38
35
41
46
45
44
39
49
19
9
1
02 CO
(PCT) (PCT)
0.151
0.089
0.046
0.020
0.102
0.124
0.143
0.131
1.068
1.537
1.387
0.707
0.031
C02
(PCT)
10.73
10.49
10.49
10.24
10.49
10.49
10.73
10.73
10.24
9.99
5.97
3.54
0.84
HC
( PPM )
1.
1.
1.
1.
1.
1.
1.
1 .
200.
2000.
25000.
25000.
25000.
-------
RUN NUMBER 107
STABILIZED DIFFUSION BURNER
METHANE
WALL-COLD AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.
0.
0.
0.
0.
C.
0.
189
189
189
189
189
189
189
AIR
FLOW
(CFM)
2.
2.
2.
2.
2.
2.
2 »
172
172
172
172
172
172
172
PCT
STO
A
i
1
1
1
I
I
I
IK
20
20
20
20
?G
20
20
I
C
AX
DI
IAL
ST
( IN)
•
»
«
•
•
*
*
4
4
4
4
4
4
4
10
10
10
10
10
10
10
.00
.00
.00
.00
.00
.00
.00
RADIAL WALu
DIST TEMP
( I
0
0
0
0
-0
-0
-0
N ) 1C)
.00
.20
.40
.60
.60
.40
• 20
NO
(PPM)
21
19
17
17
18
20
20
NOX
(PPM)
27
23
21
21
24
27
23
02
(PCT)
6.10
6.45
6.55
7.00
6.50
6.10
5.80
CO
(PCT)
0.006
0.005
0.003
0.004
0.009
0.009
0.009
C02
(PCT)
8.30
8.54
8.30
3.07
8.30
8.54
8.54
HC
(PPM)
0.
0.
0.
13.
0.
0.
0.
-------
RUN NUMBER 108
STABILIZED DIFFUSION BURNER
METHANE
WALL-COLD AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.189
0.189
0.189
0.129
0.1 fi9
0 . 1 R 9
0.189
0.1 89
0.189
0.1-39
0.189
0.189
0.189
0.189
0,1 P.9
0.189
0.189
0.189
0.1S9
0.189
AIR
FLOW
(CFM)
2.172
2.172
2.172
2.172
2.172
2.172
2.172
2.172
2.172
2. 172
2.172
2.172
2.172
2.172
2.172
2.172
2.172
2.172
2.172
2.172
PCT
STOIC
AIR
120.4
120.4
120.4
120.4
120.4
1?0.4
120.4
120.4
120.4
120.4
120.4
1?0.4
120.4
120.4
120.4
120.4
120. 4
120.4
120.4
120.4
AXIAL
DIST
( IN)
10.00
5.00
5.50
5.50
5.50
5.50
5.50
5.50
5.50
5.50
5.00
4.50
4.00
3.50
3.00
2.00
1.00
1.00
1.00
1.00
RADIAL
DIST
(IN)
0.00
0.00
0.00
0.20
0.40
0.60
-0.60
-0.40
-0.20
0.00
0.00
.0.00
0.00
0.00
0.00
0.00
0.00
0.20
0.10
0.30
WALL
TEMP
(C)
NO
(PPM)
20
23
33
30
24
16
25
22
27
34
23
14
7
2
2
2
0
0
0
0
NOX
(PPM)
26
36
46
39
28
24
27
33
36
37
33
24
14
6
3
1
1
1
1
1
02
-------
RUN NUMBER 109
STABILIZED DIFFUSION BURNER
METHANE
WALL-COLD AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.026
0*026
0.026
0.026
0.026
0.026
0.026
0.026
0.026
O.G26
0.026
0.026
0.026
C.026
0.026
0.026
0.026
0.026
0.026
0.026
0.026
0.026
0.026
AIR
FLOW
(CFM)
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
PCT
STOIC
AIR
106.5
106.5
106.5
106.5
106.5
106.5
106.5
106.5
106.5
106.5
106.5
106.5
106.5
106.5
106.5
106.5
106.5
106.5
106.5
106.5
106.5
106.5
106.5
AXIAL
DIST
( IN)
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
5.00
5.00
5.00
5.00
5.00
5.00
5.00
5.00
4.00
3.00
2.00
1.00
0.80
0.60
0.40
RADIAL
DIST
(IN)
0.00
0.20
0.40
0.60
-0.60
-0.40
-0.20
0.00
0.00
0.20
0.40
0.60
-0.60
-0.40
-0.20
0.00
0.00
0.00
0.00
0.00
0.00
0.00
0.00
WALL
TEMP
NO
(PPM)
35
42
40
42
33
31
35
28
26
28
35
23
13
17
20
26
27
12
13
7
8
6
6
NOX
(PPM)
47
48
50
47
42
41
43
41
38
48
47
42
40
43
42
43
43
51
19
12
11
9
02
(PCT)
1.50
l.SO
2.20
2.50
2.20
1.80
1.80
1.50
1.40
0.90
2.30
3.70
3.40
3.00
2.50
1.90
2.40
2.75
5.90
17.25
17.25
17.00
16.00
CO
(PCT)
0.116
0.131
0.063
0.095
0.219
0.172
0.194
0.285
2.362
3.007
1.211
0.493
0.273
0.446
0.844
1.597
1.973
3.403
2.724
0.181
0.181
0.209
0.066
C02
(PCT)
4.56
10.49
9.99
10.24
9.99
10.24
10.49
10.49
9.02
8.78
9.26
9.02
9.26
9.26
9.51
9.26
8.78
4.64
5.15
0.73
0.72
0.61
1.33
HC
( PPM )
500.
250.
100.
100.
500.
250.
1000.
1000.
12500.
hrf
20000. i
5000. £
1500.
1000.
2250.
3500.
10000.
15000.
39000.
41500.
40000.
41500.
41500.
41500.
-------
RUN NUMBER 109
STABILIZED DIFFUSION
METHANE
WALL-COLD AIR PREHfj
FUEL
F LOW
(CFM)
0.0?6
0.021
0.021
0.021
O.C21
0.021
0.021
0.021
0.021
0.0-21
0.0? 1
0.021
0.021
0.021
0.021
O.C21
0.021
C.C21
0.021
0.021
0.021
0.0?1
0.021
AIR
FLOW
(CFM)
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.26^
0.264
0.2.64
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
PCT
STOIC
AIR
106.5
127.6
127.6
127.6
127.6
127.6
127.6
127.6
127.6
127.6
127.6
127.6
127.6
127.6
127.6
127.6
127.6
127.6
127.6
1?7.6
127.6
127.6
127.6
AXIAL
DIST
( IN)
0.20
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
5.00
5.00
5.00
5.00
5.00
5.00
5.00
5.00
4.00
3.00
2.00
1.00
o.so
0.60
RADIAL WALL
DIST TEMP
(IN) ( C )
0.00
0.00
0.20
0.40
0.60
-0.60
-0.40
-0.20
0.00
0.00
0.20
0.40
0.60
-0.60
-0.40
-0.20
0.00
0.00
0.00
0.00
0.00
0.00
0.00
NO
(PPM)
6
65
63
63
62
' 63
64
63
64
64
61
54
52
51
52
64
59
54
34
10
7
3
3
CONT
BURNER
J-NONE
NOX
(PPM)
8
66
65
65
64
65
65
65
67
70
65
61
58
57
62
67
68
68
02
(PCT)
16.50
5.80
5.70
5.50
6.15
6.05
5.65
5.85
5.50
3.50
'+.65
5.70
6.40
5.70
5.20
3.95
3.50
1.70
1.15
1.35
9.50
17.00
10.50
CO
(PCT)
0.116
0.003
0.003
0.003
0.003
0.003
0.003
0.003
0.003
0.291
0.245
C.095
0.016
0.022
0.095
0.245
C.352
1.783
4.158
4.391
1.909
0.120
1.387
C02
(PCT)
1.21
8.54
7.83
8.04
7.73
7.52
7.83
8.04
7.93
8.87
8.35
8.14
7.62
7.83
8.14
8.56
8.98
8.66
7.42
6.59
3.15
1.09
2.48
HC
(PPM)
43500.
0.
0.
0.
0.
0.
0.
0.
0.
50.
75.
15.
0.
0.
25.
100.
50.
2500.
24400.
41500.
46500.
38500.
49000.
in
-------
RUN NUMBER 109 CONT
STABILIZED DIFFUSION BURNER
METHANE
WALL-COLD AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.021
0.021
AIR
FLOW
(CFM)
0.264
0.264
PCT
STOIC
AIR
127.6
127.6
AXIAL
DIST
( IN)
0.40
0.20
RADIAL
DIST
( IN)
2.70
2.70
WALL
TEMP
(C)
NO
(PPM)
3
3
NOX
(PPM)
7
7
02
(PCT)
16.50
16.00
CO
(PCT)
0.078
0.172
C02
(PCT)
1.37
1.21
HC
(PPM)
38000
44000
-------
RUN NUMBER 110
STABILIZED DIFFUSION BURNER
METHANE
WALL-COLD AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.019
0.019
0.019"
0.019
0.019
0.019
0 . 0 1 9
0.019
0.019
0.019
0.019
0.019
0.019
0.019
0.019
0.019
0.019
0.019
0.019
0.019
0.019
0.019
0.019
AIR
FLOW
(CFM)
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
C.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
PCT
STOIC
AIR
144.5
1*4.5
144.5
144.5
144.5
144.5
144 .5
144.5
144.5
144.5
144.5
1 44 . 5
1*4.5
1*4.5
1*4.5
144.5
144.5
14*. 5
144.5
144.5
1*4.5
144.5
144.5
AXIAL
DIST
(IN)
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
5.00
5.00
5.00
5.00
5.00
5.00
5.00
3.00
4.00
3.00
2.00
•1.00
0.30
C.60
0.40
RADIAL WALL
DIST TEMP
(IN) (C)
0.00
0.20
0.40
0.60
-0.60
-0.40
-0.20
0.00
0.00
0.20
0.40
0.60
-0.60
-0.40
-0.20
0.00
0.00
0.00
0.00
0.00
0.00
0.00
0.00
NO
(PPM)
61
63
63
61
60
63
62
61
30
33
45
44
56
54
56
55
62
46
27
14
8
4
4
NOX
(PPM)
64
64
64
63
62
64
64
65
35
44
52
51
60
61
64
67
73
57
47
42
11
10
02
(PCT)
7.65
8.00
8.30
8.20
8.40
7.70
7.65
7.40
6.40
6.70
7.50
8.30
7.60
7.20
6.60
5.90
4.20
2.15
3.80
8.70
16.75
16.50
16.25
CO
(PCT)
0.003
0.003
0.003
0.003
0.003
0.003
0.003
0.003
0.030
0.026
0.013
0.004
0.004
0.005
0.009
0.016
0.331
2.912
3.302
2.451
0.250
0.131
0.172
C02
(PCT)
7.21
7.10
6.79
6.79
6.59
6.79
7.10
6.90
7.42
7.42
7.00
6.79
6.90
7.10
6.38
7.83
8.77
8.35
6.48
4.34
1.46
1.17
1.59
HC
(PPM)
0.
0.
0.
0.
0.
0.
0.
0.
5.
0.
0.
0.
0.
0.
0.
0.
0.
2500.
30000.
43000.
36000.
39000.
37500.
-------
RUN NUMBER 110 CONT
STABILIZED DIFFUSION BURNER
METHANE
WALL-COLD AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.019
0.032
0.032
0.032
C.032
0.032
0.032
0.032
0.032
0.032
0,032
0.032
0.032
0.032
0.032
0.032
0.032
0.032
0.032
AIR
FLOW
(CFM)
0.264
C.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
0.264
PCT
STOIC
AIR
144.5
P6.0
36.0
86.0
86.0
86.0
86.0
86.0
86.0
86. 0
86.0
86.0
86.0
F,6.0
86.0
86.0
86.0
86*0
86.0
AXIAL
DIST
( IN)
0.20
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
5.00
5.00
5.00
5.00
5.00
5.00
5.00
5.00
4.00
3.00
RADIAL WALL
DIST TEMP
(IN) !O
0.00
0.00
0.20
0.40
0.60
-0.60
-0.40
-0.20
0.00
0.00
0.20
0.40
0.60
-0.60
-0.40
-0.20
0.00
0.00
c.oo
NO
(PPM)
3
19
21
20
14
12
13
14
18
8
13
33
22
13
15
20
16
12
10
NOX
(PPM)
9
40
43
43
43
38
41
44
37
36
43
44
44
41
43
48
49
36
31
02
(PCT)
16.00
1.65
1.^8
1.50
1.75
2.75
2.25
1.75
1.65
2.80
1.60
2.30
2.90
2.10
2.40
2.20
2.30
3.70
5.00
CO
(PCT)
0.079
2.724
2.070
7.070
1.973
1.814
1.909
2.005
1.973
3.104
2.541
1.537
1.476
1.446
1.417
1.567
2.037
3.506
3.007
C02
(PCT)
0.30
8.35
8.35
3.14
8.25
7.93
8. 14
8.25
8.25
6.18
7.93
8.35
8.14
S.46
8.14
8.46
8.04
5.77
4.85
HC
(PPM)
44000.
25000.
17500.
17500.
16500.
18500.
20000.
23000.
21000.
40000.
31000.
12000.
13000.
1^000.
15000.
15000.
28000.
42500.
45000.
I
1-1
00
-------
RUN NUMBER 111
PREMIXED FLAT FLAME BURNER
METHANE
WALL-COLD AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.054
0.054
G.054
O.C54
0.054
0.054
0.054
C.054
0.054
0.054
0.054
0.054
0.054
0.054
O.C54
0.054
C.C54
0.054
0.054
0.054
0.054
0.054
0.054
AIR
FLOW
(CFM)
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
C.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
0.546
C.546
0.546
0.546
0.546
PCT
STOIC
AIR
104.3
104.3
104.3
1C4.3
104.3
104.3
104.3
104.3
104.3
104.3
104.3
104.3
104.3
104.3
104.3
104*3
1 04 . 3
104.3
104.3
104.3
104.3
104.3
104.3
AXIAL
DIST
(IN)
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
5.00
5.00
5.00
5.00
5.00
5.00
5.00
5.00
4.00
3.00
2.00
1.00
0.50
0.00
0.10
RADIAL
DIST
( IN)
C.OO
0.20
0.40
0.60
-0.60
-0.40
-0.20
0.00
0.00
0.20
0.40
0.60
-0.60
-0.40
-0.20
o.oo
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
WALL
TEMP
1C)
NO
(PPM;
83
83
84
84
74
75
78
77
70
67
67
68
70
64
72
76
69
76
71
58
40
6
16
NOX
(PPM)
88
90
90
89
78
81
84
84
82
79
74
78
77
74
82
87
74
91
87
79
62
15
26
02
(PCT)
0.78
0.65
0.80
0.90
1.25
1.15
0.70
0.66
0.74
0.69
0.65
0.79
0.83
0.83
0.85
0.84
0.95
1.10
1.20
1.50
1.60
6.80
2.40
CO
(PCT)
0.004
0.003
0.003
0.003
0.003
0.003
0.004
0.004
0.037
0.026
0.018
0.008
0.008
0.015
0.026
0.025
0.054
0.099
0.163
0.311
0.626
1.720
1.597
C02
(PCT)
10.98
11.23
10.98
10.98
10.73
10.98
10.98
10.98
10.98
11.23
11.23
10.98
11.23
11.23
10.98
10.98
10.98
10.73
10.73
10.24
9.99
6.44
8.78
HC
(PPM)
5.
5.
5.
5.
5.
5.
5.
5.
5.
5.
5.
5.
5.
5.
5.
5'.
5.
5.
5.
5.
5.
19000.
70.
-------
RUN NUMBER 112
PREMIXED FURNACE BURNER
METHANE
WALL-COLD AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.225
0.225
0.-225
C.225
0.225
0.225
0.225
0.225
0.225
C . 2-2 5
0.225
0.225
0.225
0.225
0.225
0.225
0.225
0.225
0 . ?. 2 5
0.225
0.225
0.225
0.225
AIR
FLOW
(CFM)
2.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
PCT
STOIC
AIR
96.3
96.3
96.3
96.3
96.3
96.3
96.3
96.3
96.3
96.3
96.3
96.3
96.3
96.3
96.3
96.3
96.3
96.3
96.3
96.3
96.3
96.3
96.3
AXIAL
OIST
( IN)
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
5.00
5.00
5.00
5.00
5.00
5.00
5.00
5.00
4.00
3.00
3.00
2.00
1.00
0.50
0.25
RADIAL WALL
DIST TEMP
(IN) ( C !
0.00
0.20
0.40
0.60
-0.60
-0.40
-0.20
0.00
0.00
-0.20
-0.40
-0.60
0.60
0.40
0.20
0.00
0.00
0.00
-0.17
-0.17
-0.17
-0.17
-0.17
NO
(PPM)
33
32
32
33
32
32
32
32
27
26
26
26
31
23
27
25
21
18
17
11
6
6
7
NOX
(PPM)
37
38
37
38
37
37
37
37
37
38
37
37
37
37
37
37
35
35
36
33
27
27
32
02
(PCT)
1.05
1.00
1.00
0.95
0.95
1.00
1.00
1.00
1.10
1.10
1.10
1.10
1.00
0.9.5
1.00
1.05
1.15
1.20
1.35
1.60
3.55
3.20
4.35
CO
(PCT)
0.008
0.008
0.007
0.007
0.003
0.003
0.008
0.008
0.155
0.181
0.155
0.106
0.028
0.053
0.106
0.151
0.229
0.324
0.653
0.872
2.135
2.168
2.646
C02
(PCT)
10.98
10.98
10.98
10.98
10.98
10.98
10.98
10.98
10.73
10.73
10.73
10.73
10.98
10.98
10.73
10.73
10.73
10.49
10.24
9.99
8.07
7.83
7.13
HC
(PPM)
2.
2.
2.
2.
2.
2.
2.
2.
3.
3.
3.
3.
3.
3.
3.
3.
3.
3.
3.
13.
2500.
3500.
4250.
-------
RUN NUMBER 112 CONT
PREMIXED FURNACE BURNER
METHANE
WALL-COLD AIR PREHEAT-NONE
FUEL
FLOW
ICFM)
0.225
0.225
AIR
FLOW
(CFM)
2.C67
2.067
PCT
STOIC
AIR
96.3
96.3
AXIAL
DIST
(IN)
0.00
-0.20
RADIAL
DIST
( IN)
-0.17
-0.17
WALL
TEMP
(C)
NO
(PPM)
10
11
NOX
(PPM)
33
34
02
(PCT)
1.80
1.35
CO
(PCT)
1.567
1.182
C02
(PCT)
9.75
10.24
HC
(PPM)
200.
21.
to
-------
RUN NUMBER 113
PREMIXED FURNACE BURNER
METHANE
WALL-COLD AIR PREHEAT-NONE
FUEL
FLOW
(CFM>
0.189
0.169
C . 1 0 9
0.189
0.1R9
C.1R9
0.1R9
C . 1 B 9
0.189
C . 1 R 9
0.189
0.189
0.189
0 . 1 fl 9
0.139
C . 1 ?. 9
0 .189
0.19 9
0 . 1 3 9
C . 1 S 9
0.189
0.189
C.189
0.189
AIR
FLOW
(CFMJ
2.067
2.067
2. 067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
7.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
2.067
PCT
STOIC
AIR
114.6
114.6
114.6
11^.6
114.6
114.6
114.6
1 1 4 . 6
114.6
114.6
114.6
114.6
114.6
114.6
114.6
114.5
114.6
114.6
114.6
114.6
114.6
114.6
114.6
114.6
AXIAL
DIST
( IN)
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
5. no
5.00
5.00
5.00
5.00
5.00
5.00
5.00
4.00
3.00
2.00
1.00
0.75
0.50
0.25
0.00
RADIAL WALL
DIST TEMP
(IN) CO
0.00
0.20
0.40
0.60
-0.60
-0.40
-0.20
0.00
0.00
0.20
0.40
0.60
-0.60
-0.40
-0.20
0.00
o.oo
0.00
0.00
0.00
0.00
0.00
0.00
0.00
NO
(PPM)
12
11
12
11
11
11
11
11
9
9
9
9
9
9
9
9
8
6
^
2
2
2
3
3
NOX
(PPM)
13
13
13
12
12
13
12
12
12
12
11
11
11
11
12
12
12
12
12
10
10
11
12
12
02
(PCT!
4.95
4.85
4.95
4.90
4.80
4.90
4.80
4.85
4.85
4.80
4. SO
4.80
4.80
4.80
4.80
4.80
4.80
4.80
4.90
6.20
6.80
6.50
6.20
5.30
CO
(PCT)
0.004
0.004
0.003
0.002
0.002
0.003
0.003
0.002
0.012
0.010
0.008
0.005
0.006
0.009
0.012
0.013
0.033
0.085
0.262
1.476
1.506
1.387
1.269
0.983
C02
(PCT)
9.26
9.02
9.02
9.02
9.02
9.02
9.02
9.02
9.02
9.02
9.02
9.02
9.02
9.02
9.02
9.02
9.02
9.02
8.78
7.13
6.67
7.13
7.36
8.07
HC
(PPM)
2.
2.
2.
2.
2.
2.
2.
2.
2 • h3
2 . to
2.
2.
2.
2.
2.
2.
2.
2.
45.
3500.
5500.
5000.
3250.
1200.
-------
RUN NUMBER 114
PREMIXED FURNACE BURNER
METHANE
WALL-COLD AIR PREHEAT-NONE
FUEL
FLOW
-------
RUN NUMBER 115
PREMIXED FLAT FLAME BURNER
METHANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.031
0.031
0.031
C.031
0.035
C.035
0.035
0.035
0.035
0 . 0 H 4
G.OS4
0.084
0.084
0.034
AIR
FLOW
(CFM)
0.481
0.4S1
C.4R1
0.481
0.481
0.481
C.481
0.481
0.431
0.481
C.4S1
0.481
0.481
0.481
PCT
STOIC
AIR
161.0
161.0
161.0
161.0
140.7
140.7
140.7
140.7
140.7
60. C
60.0
60.0
60.0
60.0
AXIAL
DIST
( IN)
5.00
5.00
5.00
5.00
5.00
5.00
5.00
5.00
5.00
5.00
5.00
5.00
5.00
5.00
RADIAL
DIST
(IN)
0.00
-O.?0
-0.40
-0.60
-0.60
-0.40
-0.20
-0.20
0.00
0.00
-0.20
-0.40
-0.60
-0.20
WALL
TEMP
(C)
1430
1430
1430
1430
15BO
1580
1580
1580
1580
1510
1510
1510
1510
1510
NO
(PPM)
2
2
2
2
12
13
14
13
13
2
2
2
2
2
NOX
(PPM)
2
2
2
2
13
14
15
15
15
02
(PCT)
9.40
9.40
9.30
9.10
6.90
7.00
7.10
7.10
7.10
0.03
0.03
0.03
0.03
0.03
CO
(PCT)
0.002
0.002
0.002
0.003
0.003
0.004
0.004
0.005
0.004
8.380
8.380
8.186
7.996
8.380
C02
(PCT)
5.87
5.97
5.87
5.77
6.69
6.79
6.90
6.90
6.90
4.24
4.14
4.04
4.04
4.14
HC
(PPM)
8.
B.
7.
7.
6.
6.
6.
6.
6.
1000.
780.
1050.
1550.
900.
NJ
-------
RUN NUMBER 116
PREMIXED FLAT FLAME BURNER
METHANE
WALL-COLD AIR PREHEAT-NONE
FUEL AIR PCT AXIAL RADIAL WALL NO NOX 02 CO C02 HC
FLOW FLOW STOIC DIST DIST TEMP
tCFM) (CFM) AIR (IN) (IN) (C) (PPM) (PPM) (PCT) (PCT) (PCT) (PPM)
0.042 0.481 119.2 10.00 0.00 24 25 4.90 0.002 9.26 0.
0.042 0.481 119.2 10.00 -0.20 23 24 4.88 0.002 9.26 0.
0.042 0.481 119.2 10.00 -0.40 23 24 4.90 0.002 9.26 0.
0.042 0.481 119.2 10.00 -0.60 23 24 5.05 0.002 9.02 0.
0.042 0.481 119.? 5.00 -0.6C 21 22 4.90 0.002 9.26 0.
0.042 0.481 119.2 5.00 -0.40 21 23 4.88 0.002 9.26 0.
0.042 0.6.81 119.2 5.00 -0.20 21 23 4.90 0.003 9.26 0.
0.042 0.481 119.2 5.00 0.00 21 24 4.90 0.002 9.26 1.
0.042 0.431 119.2 2.00 0.00 21 25 4.88 0.019 9.26 1. *j
0.042 0.481 119.2 1.00 0.00 18 23 4.90 0.034 9.02 0. s>
0.042 0.481 119.2 0.70 0.00 16 21 4.90 0.048 9.02 0. w
O.C42 0.481 119,2 0.50 0.00 13 19 4.95 0.067 9.02 1.
0.042 0.481 119.2 0.30 0.00 9 15 4.90 0.131 9.02 0.
042 0.481 119.2 0.20 0.00 7 13 5.00 0.168 9.02 1.
0.04? 0.481 119.? 0.10 0.00 2 10 6.00 1.659 7.36 I25o!
0.063 C.481 80.2 0.10 0.00 40 0.27 3.302 10.73 200.
O.C63 0.4S1 80.2 0.20 0.00 48 0.07 4.045 8 78 5
0.063 0.481 80.2 0.30 O.OC 51 0.06 4.158 8.54 I'
0.063 0.481 80.2 0.50 0.00 55 0.05 4.274 8.54 *
0.063 C.431 80.2 0.70 0.00 55 0.06 4.274 8.54 \*
0.063 0.481 80.2 1.00 O.OC 57 0.05 4.391 8.30 4
0.063 0.481 80.2 2.00 0.00 59 0.05 4.391 8.07 4!
0.063 0.481 80.2 5.00 0.00 56 0.05 3.933 8 78 3
-------
RUN NUMBER 116 CON
PREFIXED FLAT FLAME BURNER
METHANE
WALL-COLD AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.063
0.063
0.063
0.063
0.063
0.063
0.063
AIR
FLOW
(CFM)
0.4R1
0.481
0.4R1
0.481
0.481
0.481
0.481
PCT
STOIC
AIR
80.2
80.2
80. 2
00.2
80.?
80.2
80.2
AXIAL
DIST
(IN)
5.00
5.00
5.00
10.00
10.00
10.00
10.00
RADIAL WALL
DIST TEMP
(IN) ( C )
-0.20
-0.40
-0.60
-0.60
-0.40
-0.20
o.oc
NO
(PPM)
54
53
51
49
52
54
54
NOX
(PPM)
02
(PCT)
0.04
0.05
0.05
0.14
0.07
0.06
0.05
CO
(PCT)
3.824
3.610
3.506
3.403
3.506
3.506
3.610
C02
(PCT)
9.02
9.26
9.51
9.26
9.26
9.26
9.26
HC
(PPM)
1.
1.
1.
1.
1.
1.
1.
i
to
-------
RUN NUMBER 117
PREMIXED FLAT FLAME BURNER
METHANE
WALL-HOT AIR PRE.HEAT-NONE
FUEL
FLOW
(CFM)
0.031
C.C31
0.031
0.031
0.031
0.031
0.031
0.031
C.031
0.031
0.031
0.042
0.042
0.042
0.042
0.042
0.042
0.042
0.042
0.042
0.042
0.042
0.042
AIR
FLOW
(CFM)
0.431
0.481
0.481
0.481
0.431
0.481
0.481
0.481
0.481
0.481
0.481
0.481
0.481
0.481
0 . 4 fi 1
0.481
0.481
0.481
0.431
0.481
0.481
0.481
0.481
PCT
STOIC
AIR
161.0
161.0
161.0
161.0
161.0
161.0
161.0
161.0
161.0
161.0
161.0
119.2
1 1. 9 . 2
119.2
119.2
119.2
119.2
119.2
119.2
119.2
119. 2
119.2
119.2
AXIAL
DIST
( IN)
5.00
5.00'
5.00
5.00
2.00
1.00
0.70
0.50
0.30
0.20
0.10
0.10
0.20
0.30
0.50
0.70
1.00
2.00
5.00
5.00
5.00
5.00
5.00
RADIAL
DIST
( IN)
-0.20
0.00
-0.40
-0.60
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
0.00
-0.40
-0.60
C.CO
WALL
TEMP
(C)
1430
1430
1430
1430
1430
1430
1430
1430
1430
1430
1430
1430
1430
1430
1430
1430
1430
1430
1430
1430
1430
1430
1430
NO
(PPM)
3
3
3
3
3
3
3
2
1
0
0
4
9
13
21
26
29
33
32
32
29
26
32
NOX
(PPM)
4
5
4
4
5
5
4
4
2
1
1
12
20
26
33
37
40
43
42
41
38
33
41
02
(PCT)
9.00
9.00
9.00
9.00
9.00
9.00
9.00
9.00
14.00
13.50
17.00
5.75
4.75
4.75
4.70
4.65
4.60
4.60
4.50
4.50
4.55
4.60
4.65
CO
(PCT)
0.002
0.001
0.001
0.001
0.000
0.003
0.000
0.057
0.653
0.466
0.361
1 . 8 4 5
0.239
0.172
0.106
0.057
0.050
0.028
0.010
0.011
0.008
0.004
0.010
C02
(PCT)
6.38
6.38
6.28
6.28
6.48
6.48
6.48
6.48
3.31
1.92
1.25
6.79
3.35
8.46
8.46
8.46
8.46
8.46
8.46
8.35
8.35
8.35
8.35
HC
(PPM)
0*
0.
0.
0.
0.
0.
0.
o.
26000.
330CC.
35000.
800.
26.
14.
L> .
2.
3.
2.
2.
1.
1.
1.
1.
-------
RUN NUMBER 117 CONT
PREMIXED FLAT FLAME BURNER
METHANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.042
0.042
0.042
0.042
0.042
0.042
0.0^2
0.042
0.042
0.042
0.04?
0.042
0.042
0.063
0.063
0.063
0.063
AIR
FLOW
(CFM)
0.481
0.481
0.481
0.481
0.481
0.431
0.481
0.481
0.431
0.481
0.481
0.481
0.481
0.481
0.481
0.481
0.481
PCT
STOIC
AIR
119.?
119.2
119.2
119.?
119.?
319.2
J 19.2
119.2
119.2
119.2
119.2
119.?
119.?
fiO.2
80.?
80.?
80.2
AXIAL
DIST
(IN)
5.00
5.00
5.00
5.00
5.00
5.00
5.00
5.00
5.00
5.00
2.00
1.00
0.50
0.50
1.00
5.00
5.00
RADIAL
DIST
(IN)
0.00
0.00
0.00
0.00
o.oo
0.00
0.00
-0.20
-0.40
-0.60
-0.60
-0.60
-0.60
-0.20
-0.20
-0.20
0.00
WALL
TEMP
(C)
1480
1530
1580
1630
1680
1730
1780
1780
1780
1780
1780
1780
1780
1825
1825
1825
1825
NO
(PPM)
33
32
35
36
37
39
40
40
38
37
23
17
14
62
63
60
57
NOX
(PPM)
42
43
45
46
47
50
52
52
49
48
29
24
19
02
(PCT)
4.66
4.69
4.70
4.70
4.72
4,. 70
4.75
4.80
4.77
4.75
4.70
4.57
4.30
0.07
0.06
0.06
0.06
CO
(PCT)
0.011
0.012
0.013
0.015
0.016
0.017
0.019
0.019
0.018
0.016
0.009
0.007
0.004
4.158
4.158
3.933
3.933
C02
(PCT)
8.35
8.35
8.35
8.35
8.35
8.25
8.25
8.25
8.25
8,14
6.04
7.83
7.31
7.83
7.83
7.73
7.62
HC
(PPM)
1.
1.
1.
2.
3.
3.
3.
2.
2 . HrJ
2 . to
2.
2.
2.
3-
3.
2.
2.
-------
RUN NUMBER 118
PREFIXED FLAT FLAME BURNER
PROPANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.012
0.012
0.012
0.012
0.012
0.012
0.012
0.012
0.012
0.012
0.012
0.012
0.012
0.033
0.033
0.033
0.0?3
0.033
0.033
C.033
0.033
0*033
AIR
FLOW
(CFM)
0.4R1
0.481
0.481
0.481
0.481
0.481
0.481
0.481
0.481
0.481
0.431
0.481
0*481
0.481
0.4R1
0.481
0.481
0.4R1
0.481
0.481
0.481
0.481
PCT
STOIC
AIR
161.1
161.1
161.1
161.1
161.1
161.1
161.1
161.1
161.1
161.1
161.1
161 .1
161.1
60.8
60. S
60.8
60.fi
60.8
60.8
60.8
60.3
60.8
AXIAL
DIST
(IN)
5.00
5.00
5.00
5.00
2.00
1.00
0.50
0.25
0.10
O.JO
0.10
0.10
0.10
0.10
0.25
0.50
1.00
2.00
5.00
5.00
5.00
5.00
RADIAL
DIST
(IN)
0.00
-0.20
-0.40
-0.60
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.40
-0.60
0.00
WALL
TEMP
(C)
1450
1450
1450
1450
1450
1450
1450
1450
1450
1475
1500
1525
1565
1565
1565
1565
1565
1565
1565
1565
1565
1565
NO
(PPM)
4
3
3
3
3
2
1
0
0
0
0
0
0
1
33
39
43
46
45
40
33
48
NOX
(PPM)
5
5
4
4
4
4
3
1
1
0
0
0
0
02
(PCT)
9.55
9.60
9.50
9.30
10.25
10.00
13.75
17.50
19.50
19.00
19.00
18.75
18.70
10.25
0.08
0.08
0.08
0.07
0.07
0.07
0.07
0.07
CO
(PCT)
0.002
0.002
0.002
0.002
0.003
0.004
0.473
0.250
0.155
0.168
0.17?
0.190
0.199
4,756
10.539
10.539
10.539
10.304
10.074
9.848
9.408
10.074
C02
(PCT)
7.13
6.90
6.90
6.67
7.13
7.36
4.14
1.17
0.43
0.61
0.63
0.67
0.70
2.38
5.05
4.95
4.95
4.95
4.85
4.75
4.75
4.85
HC
(PPM)
0.
0.
0.
0.
2.
1.
19500.
36500.
38000. *f
37500. N>
37500. *
37500.
37500.
42500.
4500.
650.
185.
90.
34.
75.
100.
13.
-------
RUN
PREMIXED
WALL-COLD
NUMBER 119
FLAT FLAME BURNER
PROPANE
AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.079
0.079
0..079
C.079
C.079
0.079
0.079
0.079
0.079
0.079
C.079
0.079
0.079
0.079
C.066
0.066
0.066
0.066
0.066
0.066
0.066
0.066
0.066
AIR
FLOW
(CFM)
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
PCT
STOIC
AIR
110.2
110.2
110.2
110.2
110.2
110.2
110.2
110.2
110.2
110.2
110.2
110.2
110.2
110.2
131.3
131. 8
131.8
131.8
131.8
131.8
131.8
131.8
131.8
AXIAL
DIST
(IN)
10.00
10.00
10.00
10.00
5.00
5.00
5.00
5.00
3.00
2.00
1.00
0.50
0.25
0.10
0.10
0.25
0.50
1.00
2.00
3.00
5.00
5.00
5.00
RADIAL WALL
DIST TEMP
(IN) ( C )
0.00
-0.20
-0.40
-0.60
-0.60
-0.40
-0.20
0.00
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
0.00
-0.40
NO
(PPM)
15
16
15
15
14
13
13
12
10
7
5
4
3
2
0
1
1
1
2
3
3
3
3
NOX
(PPM)
19
18
18
18
18
18
19
19
18
17
16
16
15
13
5
5
5
5
5
5
5
5
5
02
(PCT)
2.15
2.15
2.20
2.15
2.25
2.27
2.30
2.25
2.37
2.60
2.95
3.40
3.55
3.70
6.70
6.65
6.80
6.30
5.80
5.75
5.70
5.68
5.65
CO
(PCT)
0.005
0.005
0.005
0.005
0.026
0.044
0.076
0.124
0.234
0.344
0.599
0.734
0.734
0.680
0.762
0.844
1.011
0.653
0.151
0.046
0.015
0.013
0.008
C02
(PCT)
11.99
12.24
11.99
11.99
11.99
11.99
11.99
11.99
11.73
11.48
11.23
10.98
10.73
10.73
8.78
8.78
8.54
9.02
9.75
9.99
9.99
9.75
9.99
HC
(PPM)
0.
0.
0.
2.
0.
2.
1.
2.
2.
2.
15.
13.
2.
2.
50.
200.
1500.
1200.
100.
5.
3.
2.
2*
-------
RUN NUMBER 119 CONT
PREMIXEO FLAT FLAME BURNER
PROPANE
WALL-COLD AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.066
0.066
0..066
0.066
0.066
0.009
0.099
0.099
C.099
C.099
0.0^9
0.099
0.099
0.399
0.099
0.099
C.C99
0.099
0.099
AIR
FLOW
(CFM)
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
PCT
STOIC
AIR
131.8
131.8
131.8
131.8
131.8
S8.0
PH.O
88.0
88.0
88.0
Sfi.O
82.0
38.0
88.0
88.0
88.0
°8.0
88.0
88.0
AXIAL
DIST
(IN)
5.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
5.00
5.00
5.00
5.00
3.00
2.00
1.00
0.50
0.25
c.io
RADIAL WALL
DIST TEMP
(IN) (C)
-0.60
-0.60
-0.40
-0.20
0.00
0.00
-0.20
-0.40
-0.60
-0.60
-0.40
-0.20
0.00
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
NO
(PPM)
3
4
4
4
4
30
30
30
30
29
30
31
32
31
31
29
28
27
25
NOX
(PPM)
5
5
6
5
5
02 '
(PCT)
5.65
5.68
5.66
5.60
5.60
0..08
0.08
0.08
O.OS
0.08
o.oa
0.09
0.09
0.1.1
0.13
0.22
0.32
0.37
0.40
CO
(PCT)
0.004
0.003
0.003
0.002
0.003
3.403
3.403
3.403
3.506
3.610
3.610
3.716
3.824
3.824
3.610
3.403
3.104
2.912
2.724
C02
(PCT)
9.99
9.99
9.99
9.99
9.99
0.5S
0.58
0.58
0.57
0.57
0.56
0.56
0.56
0.56
0.56
0.57
0.58
0.60
0.60
HC
(PPM)
2.
2.
0.
0.
0.
2.
2.
1.
1.
2.
1.
1.
1.
10.
35.
80.
35.
3.
1.
**!
I
CO
I-1
-------
RUN NUMBER 120
PREMIXED FURNACE BURNER
PROPANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.012
0.012
0.012
0.012
0.012
0.012
0.012
0.012
C . 0 1 2
0 . 0 1 2
0.012
0.012
0.012
0.012
0.012
AIR
FLOW
(CFM)
0.481
0.481
0.4B1
0.481
0.481
0.481
0.481
0.481
0.481
0.481
0.481
0.431
0.481
0.481
0.481
PCT
STOIC
AIR
155.5
155.5
155.5
155.5
155.5
155.5
155.5
] 5b.5
155.5
155.5
155.5
155.5
155.5
155.5
155.5
AXIAL
DIST
( IN)
10.00
10.00
10.00
10.00
5.00
5.00
5.00
5.00
2 . 00
1.00
0.70
0.50
0.30
0.20
0.10
RADIAL
DIST
(IN)
0.00
-0.20
-0.40
-0.60
-0.60
-0.40
-0.20
0.00
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
WALL
TEMP
(C)
1495
1495
1495
1495
1495
1495
1495
1495
1495
1495
1495
1495
1495
1495
1495
NO
(PPM)
4
4
4
4
3
3
3
3
2
3
3
2
1
0
0
NOX
(PPM)
5
5
5
4
3
3
3
3
3
3
3
3
2
1
0
02
(PCT)
9.80
9.85
9.80
9.80
9.70
9.75
10.00
10.00
10.50
10.00
10.00
10.00
13.50
16.00
18.50
CO
(PCT)
0.003
0.003
0.003
0.004
0.003
0.003
0.003
0.003
0.003
0.005
0.008
0.019
0.844
0.256
0.285
C02
tPCT)
6.90
6.90
6.79
6.90
6.69
6.90
6.90
7.00
7.00
7.31
7.31
7.31
4.65
2.76
1.17
HC
(PPM)
3.
4.
3.
3.
3.
3.
3.
3.
3.
3.
3.
3.
17000.
35000.
38000.
to
-------
RUN NUMBER 121
PREMIXED FURNACE BURNER
PROPANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.016
0.016
0.016
0.016
0.016
0.016
0.016
0.020
0.020
0.024
C . 0 1 7
0.025
0.021
C.C17
0.021
0.025
0.020
AIR
FLOW
(CFM)
0.431
0 . 43 1
0.481
C.4R1
0.481
0.481
0.481
0.481
0.481
0.481
0.481
0.481
0.481
0.481
C.4S1
0.481
0.481
PCT
STOIC
AIR
124.9
124.9
124.9
124.9
124.9
174.9
124.9
100.6
100.6
a i.o
117.0
78.2
95.2
117.0
95.2
78.2
100.6
AXIAL
DIST
( IN)
10.00
10.00
10.00
10.00
5.00
5.00
5.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
10.00
RADIAL
DIST
( IN)
-0.20
0.00
-0.40
-0.60
-0.60
-0.40
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
WALL
TEMP
(C)
1795
1795
1795
1795
1795
1795
1795
1795
1865
1865
1795
1795
1795
1865
1865
1865
1865
NO
(PPM)
100
98
125
160
52
55
55
182
240
70
145
64
135
235
158
65
255
NOX
(PPM)
115
108
140
175
63
64
65
192
253
150
138
255
160
260
02
(PCT)
4.75
4.80
4.80
4.80
4.80
4.82
4.90
0.70
0.70
0.09
3.50
0.10
0.11
3.60
0.14
0.10
0.70
CO
(PCT)
0.037
0.036
0.039
0.037
0.020
0.023
0.021
0.190
0.256
5.693
0.052
6.444
1.476
0.071
1.357
6.444
0.262
C02
(PCT)
10.49
10.49
10.24
10.24
10.24
10.49
10.49
12.75
12.75
3.66
11.23
7.93
12.24
10.98
12.50
8.54
12.75
HC
(PPM)
5.
5.
5.
5.
4.
4.
5.
4.
4. tij
4. u>
2. w
3.
2.
3.
3.
3.
2.
-------
RUN NUMBER 122
STABILIZED DIFFUSION BURNER
METHANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.137
0.137
0.137
0.137
0.137
0.137
0.137
0.137
0.137
0.1-37
0.137
0.137
0.137
0.137
0.137
AIR
FLOW
(CFM)
2.094
2.094
2.094
2.094
2.094
2.C94
2.094
2.094
2.094
2.094
2.094
2.C94
2.094
2.094
2.094
PCT
STOIC
AIR
159.7
159.7
159.7
159.7
159.7
159,7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
AXIAL
DIST
( IN!
15.00
10.00
5.00
3.00
4.00
6.00
7.00
5.00
5.00
5.00
5.00
4.00
4.00
4.00
4.00
RADIAL
DIST
(IN)
0.00
0.00
0.00
0.00
0.00
0.00
0.00
0.00
-0.20
-0.40
-0.60
-0.60
-0.40
-0.20
0.00
WALL
TEMP
(O
1450
1450
1450
1450
1450
1450
1450
1450
1450
1450
1450
1450
1450
1450
1450
NO
( PPM )
64
75
63
3
40
72
72
70
55
43
30
12
24
30
40
NOX
(PPM)
82
96
83
25
59
89
95
90
80
67
43
31
48
55
60
02
(PCT)
7.80
6.90
2.80
9.80
3.60
4.50
5.40
3.20
3.70
5.60
8.30
8.85
5.70
4.30
3.60
CO
(PCT)
0.003
0.028
1.597
2.646
2.472
0.546
0.258
1.357
1.039
0.361
0.104
0.219
0.789
1.814
2.506
C02
(PCT)
6.07
7.52
8.56
4.14
7.21
8.46
8.14
8.56
8.46
7.93
6.69
6.38
7.42
7.93
7.42
HC
(PPM)
8.
6.
175.
42000.
7500.
25.
5.
200.
250.
300.
150.
3000.
4500.
7500.
7500.
I
10
-------
RUN NUMBER 123
STABILIZED DIFFUSION BURNER
METHANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
C.137
0.157
0.157
0.157
0.157
0.157
0.157
0.157
0.157
0.1-57
0.157
0.157
0.157
0.157
C.157
0.157
0.157
0.157
0.157
0.183
0.183
0.183
0.183
AIR
FLOW
(CFM)
2.094
2.094
2.094
2.094
2.094
2.094
2. 094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
PCT
STOIC
AIR
159.7
119.9
139.9
139.9
139.9
139.9
139.9
139.9
139.9
139.9
139.9
139.9
139.9
139.9
139.9
139.9
139.9
139.9
139.9
119. a
119.8
119.8
119.8
AXIAL
DIST
(IN)
15.00
15.00
10.00
5.00
4.00
3.00
4.00
4.00
4.00
4.00
5.00
5.00
5.00
5.00
7.00
9.00
9.00
9.00
9.00
15.00
10.00
7.00
5.00
RADIAL
DIST
(IN)
0.00
0.00
0.00
0.00
0.00
0.00
0.00
-0.20
-0.40
-0.60
-0.60
-0.40
-0.20
0.00
0.00
0.00
-0.20
-0.40
-0.60
0.00
0.00
0.00
0.00
WALL
TEMP
(C)
1440
1590
1590
1590
1590
1590
1590
1590
1590
1590
1590
1590
1590
1590
1590
1590
1590
1590
1590
1775
1775
1775
1775
NO
(PPM)
40
130
120
70
35
0
35
28
30
24
38
53
59
60
95
110
110
100
90
415
265
155
72
NOX
(PPM)
55
155
155
95
57
17
54
51
52
46
58
75
80
80
120
135
130
125
110
475
315
190
90
02
(PCT)
8.25
5.85
5.20
2.00
2.50
12.50
2.65
2.85
3.40
5.60
6.30
3.80
2.50
2.10
3.70
4.85
4.95
5.25
5.95
3.70
2.80
1.60
0.79
CO
(PCT)
0.009
0.037
0.106
2.186
2.912
1.841
2.817
2.632
1.757
0.455
0.190
0.955
1.357
1.845
0.573
0.151
0.143
0.120
0.079
0.143
0.359
1.783
3.716
C02
(PCT)
6.69
7.93
8.35
8.56
7.73
3.05
7.73
7.62
8.04
7.62
7.42
8.46
8.66
8.56
8.66
8.25
8.25
8.14
7.93
8.87
9.08
8.87
7.93
HC
(PPM)
5*
6.
6.
500.
5500.
35000.
6500.
7500.
3850.
1750.
35.
100.
250.
500.
5.
5.
5.
5.
5.
5.
5.
60.
1650.
Ul
-------
RUN NUMBER 123 CONT
STABILIZED DIFFUSION BURNER
METHANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.183
0.183
0.1B3
C.1B3
0 . 1 R 3
0.183
0 . 1 P 3
0.183
0.133
0.163
0.1S3
o.ias
0 . 1 S 3
0. 1«3
0.275
C.275
G.275
0.275
0.275
0 . ? 7 5
0.275
0.275
0.275
AIR
FLOW
(CFM)
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2*094
2.094
2.094
2.094
2.094
2.094
PCT
STOIC
AIR
119.8
119.8
119.8
119.8
119.8
119.8
119.8
119.8
119.8
119.8
119.8
119.8
119.8
1 1 9 . «
79.9
79.9
79.9
79.9
79.9
79.9
79.9
79.9
79.9
AXIAL
DIST
(IN)
4.00
3.00
4.00
4.00
4.00
4.00
5.00
5.00
5.00
5.00
9.00
9.00
9.00
9.00
15.00
10.00
7.00
5.00
4.00
3.00
5.00
5.00
5.00
RADIAL
DIST
(IN)
0.00
0.00
0.00
-0.20
-0.40
-0.60
-0.60
-0.40
-0.20
0.00
0.00
-0*20
-0.40
-0.60
0.00
0.00
0.00
0.00
0.00
0.00
0.00
-0.20
-0.40
WALL
TEMP
(C)
1775
1775
1775
1775
1775
1775
1775
1775
1775
1775
1775
1775
1775
1775
1825
1825
1825
1825
1825
1825
1825
1825
1825
NO
(PPM)
30
0
32
29
41
32
50
65
65
66
210
210
200
200
110
100
71
8
0
0
9
5
20
NOX
(PPM)
67
24
58
56
63
57
75
87
82
80
240
240
240
240
02
(PCT)
1.60
9.25
1.50
1.60
1.45
4,30
5.20
2.00
1.00
0.82
2.55
2.65
2.90
3.45.
0.11
0.11
0.20
2*90
6.50
11.75
2.70
3.30
1.85
CO
(PCT)
4.510
2.912
4.510
4.391
3.104
0.899
0.440
1.783
3.506
3.933
0.599
0.599
0.493
0.304
6.444
6.444
6.765
6.287
4.756
2.451
6.931
6.134
5.984
C02
(PCT)
6.90
3.25
6.90
7.10
8.14
8. 14
7.73
8.56
8.04
7.73
9.08
9.08
8.98
8.87
6.28
6.07
5.87
4.65
3.54
1.98
4.65
4.34
5.46
HC
(PPM)
10000.
37500.
10000.
9000.
3000.
250.
25.
300.
1500.
2250.
6.
5.
5.
5.
5.
50.
3500.
30000.
38500.
42500.
29000.
32000.
20000.
-------
RUN NUMBER 123 CONT
STABILIZED DIFFUSION BURNER
METHANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.275
C.275
0.775
0.275
0.275
0.275
C.275
C.275
0.275
0.2-75
AIR
FLOW
(CFM)
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
PCT
STOIC
AIR
79.9
79.9
79.9
79.9
79.9
79.9
79.9
79.9
79.9
79.9
AXIAL
DIST
(IN)
5.00
6.00
6.00
6.00
6.00
6.00
10.00
10.00
10.00
10.00
RADIAL
DIST
( IN)
-0.60
-0.60
-0.40
-0.60
-0.20
0.00
0.00
-0.20
-0.40
-0.60
WALL
TEMP
(C)
1825
1825
1825
1825
1825
1825
1825
1825
1825
1825
NO NOX
(PPM) (PPM)
65
93
56
87
32
38
91
92
93
94
02
(PCT)
0.77
0.28
0.7?
0.31
1.05
0.83
0.11
0.11
0.11
0.11
CO
CPCT)
4.158
4.882
6.287
5.276
6.931
6.931
6.444
6.444
6.287
6.287
C02
(PCT)
7.42
7.10
5.87
6.79
5.25
5.36
6.07
6.07
6.18
6.18
HC
(PPM)
4500.
2250.
10000.
3000.
14000.
11500.
50.
45.
50.
50.
-------
RUN NUMBER 124
STABILIZED DIFFUSION BURNER
METHANE
WALL-HOT AIR PREHEAT-NONE
FUEL AIR PCT AXIAL RADIAL WALL NO NOX 02 CO C02 HC
FLOW FLOW STOIC DIST DIST TEMP
(CFM) (CFM) AIR (IN) (IN) (C) (PPM) (PPM) (PCT) (PCT) (PCT) (PPM)
0.137
0.157
0.183
0.219
0.?75
0.219
0.219
2.094
2.094
2.094
2.094
2.094
2.094
2.094
159.7
139.9
119.8
100.0
79.9
100.0
100.0
15.00
15.00
15.00
15.00
15.00
15.00
10.00
0.00
0.00
0.00
0.00
0.00
0.00
0.00
1955
1955
1955
1955
1955
1955
1955
300
520
1200
990
140
920
410
350
630
1300
1000
920
420
7.50
6.00
3.30
0.43
0.17
0.39
0.47
0.049
0.092
0.256
1*845.
6.603
1.927
2.273
7.36
8.07
9.51
9.99
6.44
9.75
9.51
2.
4.
5.
5.
4.
4.
4.
I
w
00
-------
RUN NUMBER 125
STABILIZED DIFFUSION BURNER
PROPANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.055
0.055
0.055
0.055
0.055
0.055
0.055
0.055
0.055
0 . C 5 5
0.055
0.055
0.055
C.C55
C.C55
0.055
0.055
0.055
AIR
FLOW
(CFM)
2.094
2 .094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
PCT
STOIC
AIR
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
AXIAL
DIST
( IN)
15.00
10.00
7.00
5.00
4.00
3.00
4.00
4*00
4.00
4.00
5.00
5.00
5.00
5.00
9.00
9.00
9.00
9.00
RADIAL
DIST
( IN)
0.00
0.00
0.00
0.00
0.00
0.00
0.00
-0.20
-0.40
-0.60
-0.60
-0.40
•-0.20
O.CO
0.00
-0.20
-0.40
-0.60
WALL
TEMP
(C)
1425
1425
1425
1425
1425
1425
1425
1425
1425
1425
1425
1425
1425
1425
1425
1425
1425
1425
NO
(PPM)
200
200
160
100
55
15
52
62
63
39
49
R3
100
90
185
170
145
105
NOX
(PPM)
235
230
190
120
35
88
95
65
72
115
125
112
210
200
170
130
02
(PCT)
7.10
5.45
3.30
1.25
0.87
2.40
0.87
1.80
5.20
10.25
11.00
6.90
2.95
1.40
5.10
6.20
7.90
9.90
CO
(PCT)
0.043
0.381
2.168
5.412
7.627
7.627
7.448
5.142
2.099
0.331
0.181
1.211
3.104
5.412
0.734
0.352
0.172
0.049
C02
(PCT)
9.02
9.51
9.99
8.54
7.13
5.75
7.13
8.30
8.30
6.18
5.K7
7.83
8.66
8.14
9.19
8.66
7.73
6.59
HC
(PPM)
7.
8.
250.
5000.
17500.
37500.
17500.
7500.
1250. ^
350. ^
225. ^
225.
1500.
5000.
25.
13.
10.
8.
-------
RUN NUMBER 126
STABILIZED DIFFUSION BURNER
PROPANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.062
0 .062
O.C62
.0.062
0.062
0.062
0.062
0.062
0.062
0.062
0.062
0.062
0.062
0.062
0.062
0.062
0.062
0.062
AIR
FLOW
(CFM)
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
PCT
STOIC
AIR
140.7
140.7
140.7
140.7
140.7
140.7
] 4 0 . 7
140.7
140.7
140.7
140.7
140.7
140.7
140.7
140.7
140.7
140.7
140.7
AXIAL
DIST
(IN)
15.00
10.00
7.00
5.00
4.00
3.00
5.00
5.00
5.00
5.00
6.00
6.00
6.00
6.00
10.00
10.00
10.00
10.00
RADIAL
DIST
( IN)
0.00
0.00
0.00
o.oo
0.00
0.00
0.00
-0.20
-0.40
-0.60
-0.60
-0.40
-0.20
0.00
0.00
-0.20
-0.40
-0.60
WALL
TEMP
(C)
1610
1610
1610
1610
1610
1610
1610
1610
1610
1610
1610
1610
1610
1610
1610
1610
1610
1610
NO
(PPM)
440
325
165
59
16
6
54
76
81
49
71
120
130
105
355
355
320
280
NOX
(PPM)
495
350
195
110
67
90
150
160
380
380
350
305
02
(PCT)
4.95
3.45
1.75
0.90
1.95
5.00
0.90
2.35
7.40
13.00
12.25
8.00
3.30
1.25
3.55
4.55
6.45
8.80
CO
(PCT)
0.374
1.973
5.142
8.380
8.985
7.448
8.380
5.551
1.659
0.151
0.190
1.387
4.158
6.765
1.783
1.269
0.573
0.181
C02
(PCT)
9.99
9.75
8.30
5.97
4.85
3.84
6.07
7.31
7.00
4.55
4.35
6.90
7.83
7.31
9.99
9.51
8. 54
7.36
HC
(PPM)
2 .
£. •
75.
4500.
32500.
42500.
46000.
32500.
12500.
1250.
1 bO.
i «V W *
50.
450.
4250.
13000.
100.
•at; .
j -* .
?0 .
£. \J 9
9.
-------
RUN NUMBER 127
STABILIZED DIFFUSION BURNER
PROPANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.077
0.077
0.077
0.077
0.077
0.077
C.077
0.077
0.077
0.0-77
0.077
0.077
0.109
0.109
0.109
0.109
0.109
0. 109
AIR
FLOW
(CFM)
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
PCT
STOIC
AIR
114.0
114.0
114.0
114.0
114.0
114.0
114.0
114.0
114.0
114.0
114.0
114.0
00.4
80.4
80.4
80.4
80.4
80.4
AXIAL
DIST
( IN)
15.00
10.00
7.00
5.00
4.00
3.00
5.00
5.00
5.00
5.00
6.00
6.00
5.00
10.00
15.00
7.00
4.00
15.00
RADIAL
DIST
(IN)
0.00
0.00
0.00
0.00
0.00
o.co
0.00
-0.20
-0.40
-0.60
-0.60
-0.40
-0.00
0.00
0.00
0.00
0.00
0.00
WALL
TEMP
(C)
1870
1870
1870
1870
1870
1870
1870
1870
1870
1870
1870
1870
1870
1870
1870
1870
1870
1870
NO
(PPM)
975
535
255
98
47
12
95
140
195
150
275
280
22
370
800
175
30
900
NOX
(PPM)
1030
570
275
203
180
290
300
02
(PCT)
1.95
1.75
1.10
0.55
0.88
5.50
0.57
1.20
4.60
8.30
6.80
3.90
1.65
0.25
0.35
0.61
5.30
0.30
CO
(PCT)
1.476
2.472
5.142
7.810
8.779
6.931
7.810
5.412
5.412
0.172
0.181
1.506
9.848
8.578
6.765
7.272,.
7.627
6.931
C02
(PCT)
10.98
10.24
8.78
7.13
5.98
4.04
6.79
8.04
8.56
7.73
8.04
9.08
4.24
6.48
7.31
6.79
3.54
6.90
HC
(PPM)
7.
35.
1250.
8500.
25000.
42500.
8000.
2750.
100.
20.
15.
75.
41000.
1750.
25.
12500.
50000.
50.
.e-
-------
RUN NUMBER 128
DIFFUSION FLAME BURNER
METHANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.137
0.137
0.137
0.137
0.137
0.137
0.137
0.137
0.137
G.137
0.137
0.137
0.137
0.137
0.137
C.137
0.137
0.137
0.157
0.157
0.157
0.157
0.157
AIR
FLOW
(CFM)
2.094
2.094
2.C94
?.094
2.094
2*094
2.094
2.094
2. 094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
PCT
STOIC
AIR
159.7
159.7
159.7
159.7
159.7
159,7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
139.9
139.9
139.9
139.9
139.9
AXIAL
DIST
(IN)
15.00
10.00
7.00
5.00
4.00
3.00
4.00
4.00
4.00
4.00
5.00
5.00
5.00
5.00
9.00
9.00
9.00
9.00
15.00
10.00
7.00
5.00
4.00
RADIAL
DIST
( IN)
0.00
0.00
0.00
0.00
0.00
0.00
0.00
-0.20
-0.40
-0.60
-0.60
-0.40
--0.20
0.00
0.00
-0.20
-0.40
-0.60
0.00
0.00
0.00
0.00
0.00
WALL
TEMP
(C)
1440
1440
1440
1^40
1440
1440
1440
1440
1440
1440
1440
1440
1440
1440
1440
1440
1440
1440
1590
1590
1590
1590
1590
NO
(PPM)
75
66
49
30
18
6
17
9
5
3
4
3
17
28
62
45
26
14
165
95
58
34
19
NOX
(PPM)
93
86
76
61
53
36
52
37
23
16
17
27
43
61
87
63
43
27
195
130
92
71
57
02
(PCT)
5.80
5.80
5.60
5.10
4.75
6.30
4.95
8.80
12.50
14.50
14.00
11.75
9.00
5.35
5.50
8.25
11.00
13.00
3.80
4.45
5.10
3.95
4.30
CO
(PCT)
0.124
0.413
1.125
1.783
2.403
2.912
2.335
0.927
0.267
0.120
0.089
0.172
0.464
1.720
0.626
0.229
0.057
0.032
0.789
1.328
1.597
2.788
3.203
C02
(PCT)
8.07
7.60
7.36
6.90
6.67
5.05
6.38
5.56
4.14
2.95
3.05
4.24
5.66
6.79
7.21
6.07
5.05
3.84
7.83
7.10
6.79
6.48
6.07
HC
(PPM)
5.
35.
400.
2000.
8500.
35000.
8500.
3500.
2750.
2750.
1750.
1400.
1250.
2250.
75.
145.
225.
250.
6.
125.
800.
9000.
21000.
-------
RUN NUMBER 128 CONT
DIFFUSION FLAME BURNER
METHANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
C.157
0.157
0.157
C.157
0.157
0.157
0.157
0.157
0.157
0 . i 5 7
C.157
0. 157
0.157
0.157
AIR
FLOW
(CFM)
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2,094
2.094
2.094
2.094
2.094
2.094
PCT
STOIC
AIR
139.9
139.9
139.9
139.9
139.9
139.9
139.9
139.9
13V. 9
139.9
139.9
139.9
139.9
139.9
AXIAL
DIST
( IN)
3.00
5.00
5.00
5.00
5.00
6.00
6.00
6.00
6.00
10.00
1C. 00
10.00
10.00
10.00
RADIAL
DIST
( IN)
0.00
0.00
-0.20
-0.40
-0.60
-0.60
-0.40
-0.20
0.00
0.00
-0.60
-0.40
'0.20
0.00
WALL
TEMP
(C)
1590
1590
1590
1590
1590
1590
1590
1590
1590
1590
1590
1590
1590
1590
NO
(PPM)
6
33
20
11
6
9
19
33
43
80
16
23
38
0
NOX
(PPM)
37
70
54
33
22
24
41
60
83
110
28
38
57
02
(PCT)
6.55
4.50
8.50
12.50
15.00
14.25
11. DO
8.50
4.40
2.30
12.75
12.75
11.00
8.30
CO
(PCT)
3.104
2.541
1.068
0.239
0.071
0.059
0.172
1.153
2.302
2.017
C.C38
0.037
0.074
0.262
C02
(PCT)
4.24
6.48
5.36
4. 14
2.85
3.15
4.34
5.77
6.69
7.52
3.05
3.64
5.05
6.18
HC
( PPM )
42500.
8000.
3500.
1500.
7500.
900.
750.
750.
900.
6.
350.
350.
150.
175.
•n
i
j>
UJ
-------
RUN NUMBER 129
STABILIZED DIFFUSION BURNER
METHANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.157
0.157
0..157
0.157
0.157
0.157
0.157
0. 137
0.157
AIR
FLOW
(CFM)
2.094
2.C94
2.094
2.094
2.094
2.094
2.094
2.094
2.094
PCT
STOIC
AIR
139.9
139.9
139.9
139.9
139.9
139.9
139,9
139.9
139.9
AXIAL
DIST
( IN)
15.00
10.00
15,00
15.00
15.00
15.00
15.00
15.00
15.00
RADIAL
DIST
(IN)
0.00
0.00
0.00
-0.20
-0.40
-0.60
0.20
0.40
0.60
WALL
TEMP
(O
1590
1590
1590
1590
1590
1590
1590
1590
1590
NO
(PPM)
145
145
130
140
135
130
145
130
140
NOX
(PPM)
173
180
160
150
160
155
160
150
155
02
(PCT)
7.20
6.60
7.30
7.55
7.70
7.50
6.90
7.20
6.95
CO
(PCT)
0.020
0.072
0.017
0.017
0.016
0.016
0.021
0.018
0.021
C02
(PCT)
7.00
7.21
6.90
6.79
6.69
6.79
7.00
6.90
7.00
HC
(PPM)
1.
1.
2.
1.
1.
0.
0.
0.
0.
-------
RUN
PREMIXED
WALL-HOT
NUMBER 130
FLAT FLAME BURNER
METHANE
AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
C.035
0.035
C.935
0.035
C.035
0.035
0.035
C.035
0.035
0.035
0.035
0.035
0.035
0.035
0.035
0.035
C.035
0.035
AIR
FLOW
(CFM)
0.481
0.481
0.481
0.4R1
0.481
0.481
0.481
0.481
0.4R1
C.481
0.431
0.481
0.4R1
C.4S1
0.481
0.481
C.4S1
0.481
PCT
STOIC
AIR
140.4
140.4
140.4
140. 4
140.4
140.4
140.4
140.4
140.4
140.4
140.4
140.4
140.4
140.4
140.4
140.4
140. 4
14C.4
AXIAL
DIST
(IN)
15.10
15.10
15.10
15.10
10.10
10.10
10.10
10.10
5.10
5.10
5-10
5.10
3. 10
2.10
1.10
0.10
C.60
0.35
RADIAL
DIST
! IN)
0.00
-0.20
-0.40
-0.60
-0.60
-0.40
-0.20
0.00
0.00
-0.20
-0.40
-0.60
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
WALL
TEMP
-------
RUN NUMBER 131
PREMIXED FLAT FLAME BURNER
METHANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.042
0.042
0.042
0.042
0.042
0.042
0.042
0 .042
0.042
0.042
0.042
0.0^2
0.042
0.042
0.042
0.0/i2
0.042
0.042
0.042
0.042
0.065
0.065
0.065
AIR
FLOW
(CFM!
0.481
0.431
0.431
0.481
0.401
0.481
0.481
0.481
0.431
0.431
0.431
0.431
0.4S1
0.481
0.431
0.481
0.481
0.481
0.481
0.481
0.481
0.481
PCT
STOIC
AIR
120.1
120.1
1?0.1
1?0.1
170.1
1?0.1
170.1
170.1
170.1
120.1
170.1
170.1
170.1
120.1
170.1
170.1
120, 1
120.1
120.1
77.5
77.5
77.5
AXIAL
DIST
( IN)
15.10
15.10
15.10
15.10
10.10
10.10
10.10
10.10
5.10
5.10
5.10
5.10
3. 10
2.10
1.10
0. 10
0.05
0.35
0.60
0.85
15.10
15.10
15.10
RADIAL
DIST
( IN)
0.00
-0.20
-0.40
-0.60
-0.60
-0.40
-0.20
0.00
0.00
-0.20
-0.40
-0.60
-0.20
-0.20
-0.20
-0.70
-0.20
-0.20
-0.20
-0.20
0.00
-0.20
-0.40
WALL
TEMP
(C)
1770
1770
1770
1770
1770
1770
1770
1770
1770
1770
1770
1770
1770
1770
1770
1770
1770
1770
1770
1770
1770
1770
1770
NO
(PPM)
150
150
160
165
110
100
85
80
58
60
55
53
57
52
40
4
2
17
25
32
57
57
55
NOX
(PPM)
170
170
180
190
120
115
100
100
72
74
69
65
70
68
54
19
14
31
38
45
02
(PCT)
4.00
4.00
3.95
3.95
4.00
4.00
4.05
4.00
4.15
4.10
4.10
4.10
4.20
4.25
4.30
4.60
5.00
4.40
4.35
4.35
0.17
0.17
0.17
CO
(PCT)
0.028
0.030
0.029
0.026
0.024
0.026
0.025
0.026
0.021
0.020
0.019
0.017
0.028
0.040
0.056
0.374
1.476
0.120
0.085
0.060
6.444
6.134
6.287
C02
(PCT)
8.14
8.25
8.14
8.14
8.14
8.04
8.14
8.14
8.35
8.25
8. 14
8.14
8.46
8.46
8.46
8.04
7.52
8.46
8.46
8.46
5.77
5.77
5.77
HC
(PPM)
10.
15.
20.
28.
17.
6.
2.
2.
"> ***
2 * i
2 » CT\
2.
2.
2.
1.
1.
1.
7500.
4.
3.
2.
16.
15.
38.
-------
RUN NUMBER 131 COMT
PREMIXEO FLAT FLAME BURNER
METHANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFX)
0.065
0.065
C.065
C.065
0.065
0.065
C.065
0.065
0.065
C.065
O.C65
C . 0 6 5
0.065
O.C65
C.O&5
C .CAS
0.045
0.045
0.045
0.045
0.045
0.0&5
0.045
AIR
FLOW
(CFM)
0.481
C.4R1
0.481
0.481
0.481
0.4fll
0.481
0.481
0.431
0.481
0.481
0*481
0.481
0.481
C.481
C . 4 8 1
C.431
0.481
0.481
0.431
0.431
0.431
0.481
PCT
STOIC
AIR
77.5
77.5
77.5
77.5
77.5
77.5
77.5
77.5
77.5
77.5
77.5
77.5
77.5
77.5
77.5
110. 7
110.7
110.7
110.7
110.7
110.7
110.7
110.7
AXIAL
DIST
(IN)
15.10
10.10
10.10
10.10
10.10
5.10
5. 10
5.10
5.10
3.10
2.10
1.10
0.10
0.35
C. 15
15.10
15.10
15.10
15.10
10.10
10.10
10.10
10.10
RADIAL
DIST
( IN!
-0.60
-0.60
-0.40
-0.20
0.00
0.00
-0.20
-0.40
-0.60
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
O.CO
-0.20
-0.40
-0.60
-0.60
-0.40
-0.20
0.00
WALL
TEMP
(O
1770
1770
1770
1770
1770
1770
1770
1770
1770
1770
1770
1770
1770
1770
1770
1865
1065
1865
1865
1865
1865
1865
1865
NO
(PPM)
55
59
61
62
62
67
69
68
66
70
71
71
23
62
55
390
400
430
450
23?
210
175
170
NOX
(PPM)
430
440
480
490
270
250
210
200
02
(PCT)
0.17
0.17
0.17
0.17
0.17
C.17
0.17
0.17
0.17
0.17
0.17
0.18
2.65
0.19
0.20
1.95
1.90
1.90
1.S5
1.90
1.90
2.00
2.00
CO
(PCT)
6.134
5.984
5.984
5.984
6.134
6.134
6.134
5.984
5.934
6.287
6.444
6.444
5.837
6.287
6.134
0.113
0.102
0.106
0.099
0.073
0.071
0.077
0.078
C02
(PCT)
5.66
5.56
5.66
5.66
5.66
5.77
5.77
5.66
5.56
5.87
5.97
5.97
4.95
6.18
6.18
8.77
8.66
8.56
8.56
8.35
8.35
8.46
8.66
HC
(PPM)
43.
20.
4.
3.
2.
2.
2.
2.
2 .
2 .
2.
2.
14000.
15.
40.
15.
25.
55.
65.
55.
33.
4.
3.
-------
RUN
PREFIXED
WALL-HOT
NUMBER 131 CONT
FLAT FLAME BURNER
METHANE
AIR PREHEAT-NONE
FUEL
FLOW
(CFV)
0.045
0.045
0.045
0.045
0.045
0.045
0.045
0.045
0.045
0.050
0.050
0 . 0 0 0
0.050
0.05 C
.050
.050
.050
.050
0.045
0.042
0.03S
0.035
0.033
AIR
FLOW
(CFM)
0.481
0.481
C.4S1
0.481
0.481
0.481
0.481
0.481
0.481
0.481
C.481
0.481
0.481
C.4S1
0.431
0.481
0.481
0.481
0.481
0.481
0.481
0.431
0.481
PCT
STOIC
AIR
110.7
110.7
110.7
110.7
110.7
110.7
110.7
110.7
110.7
100.3
100.8
100.3
100.3
100.8
ioc. a
100.8
100.8
100.8
110.7
1 ? 0 . 1
131.0
140.4
151.3
AXIAL
DIST
(IN)
5.10
5.10
5.10
5.10
3.10
2.10
1.10
0,10
0.25
15.10
15.10
10.10
10.10
5.10
15.10
15.10
15*10
15.10
15.10
15.10
15.10
15.10
15.10
RADIAL
DIST
(IN)
0.00
-0.20
-0.40
-0.60
-0.20
-0.20
-0.20
-0.20
-0.20
-0.20
-0.60
-0.60
-0.20
-0.20
0.00
-0.20
-0.40
-0.60
-0.20
-0.20
-0.20
-0.20
-0.20
WALL
TEMP
(C)
1865
1865
1865
1865
1865
1865
1865
1865
1865
1945
1945
1945
1945
1945
1945
1945
1945
1945
1945
1945
1945
1945
1945
NO
(PPM!
100
110
100
95
95
80
60
5
15
800
920
565
310
775
810
900
945
1425
1530
1725
1750
1800
NOX
(PPM)
135
130
130
120
120
110
90
25
35
840
950
62 C
390
830
865
960
980
1500
1750
1900
1975
2025
02
(PCT)
2.10
2.10
2.10
2.05
2.20
2.25
2.30
2.70
2.60
0.83
0.77
0.84
0.93
1.00
0.80
0.80
0.80
0.75
2.45
3.60
5.10
6.15
7.30
CO
(PCT)
0.059
0.060
0.055
Oi050
0.076
0.092
0.147
0.734
0.267
0.285
0.298
0.250
0.245
0.181
0.304
0.304
0.291
0.291
0.124
0.092
0.066
0.054
0.043
C02
(PCT)
8.87
8.77
8.66
8.46
9.08
9.19
9.75
9.26
9.51
9.26
9.26
9.26
9.51
9.75
9.75
9.02
8.78
9.02
8.07
7.63
6.79
6.38
5.77
HC
(PPM)
2.
2.
1.
1.
1.
2.
2.
2.
2.
27.
40.
26.
17.
4.
10.
13.
13.
12.
10.
10.
10.
10.
10.
00
-------
RUN NUMBER 131 CONT
PREMIXED FLAT FLAME BURNER
METHANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFMJ
0.055
C.063
AIR
FLOW
(CFM)
0.481
0.481
PCT
STOIC
AIR
90. 8
79.9
AXIAL
DIST
( IN)
15.10
15.10
RADIAL
OIST
UN)
-0.20
-0.20
WALL
TEMP
(C>
1945
1945
NO
(PPM)
210
90
NOX
(PPM)
230
90
02
(PCT)
0.25
0.25
CO
(PCT)
2.369
5.142
C02
(PCT)
7.52
5.66
HC
(PPM)
9.
15.
-------
RUN NUMBER 132
PREMIXED FURNACE BURNER
METHANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.031
0.031
0.031
0.031
0.031
0.031
0 . C 3 1
0.031
0.031
0.031
O.C31
0.031
C.031
AIR
FLOW
(CFM)
0.481
0.481
0.481
0.^81
0.481
0.481
C.4P1
0.4.°1
0.481
0.491
0.481
0.481
0.481
PCT
STOIC
AIR
159.5
159.5
159.5
159.5
159.5
159.5
15°. 5
159.5
159.5
159.5
159.5
159.5
159.5
AXIAL
DIST
( IN)
15.00
10.00
5.00
3.00
2.00
1.00
4.00
3.50
3.35
15.00
15.00
15.00
15.00
RADIAL
DIST
(IN)
0.00
0.00
0.00
0.00
0.00
0.00
0.00
0.00
0.00
0.00
-o.?o
-0.40
-0.60
WALL
TEMP
(0
1440
1440
1440
1440
1440
1440
1440
1440
1440
1440
1440
1440
1440
NO
(PPM)
2
1
1
0
0
0
1
0
0
1
1
1
1
NOX
(PPM)
2
2
2
1
1
0
2
2
1
2
2
2
2
02
(PCT)
8.80
a. so
8.80
12.00
17.00
18.00
9.05
9.70
10.25
8.95
8.95
8.90
8.90
CO
(PCT)
0*002
0.003
0*002
0.304
0.076
0*010
0.022
0.155
0.219
0.003
0.003
0.002
0*003
C02
(PCT)
5.66
5.77
5.77
3.84
1.46
0.81
5.66
5.15
4.85
5.66
5.66
5.66
5.66
HC
(PPM)
0.
13.
17.
15000.
33000.
345CO.
350.
4000.
7000.
25.
15.
10.
11.
m
i
Ul
o
-------
RUN NUMBER 133
PREMIXED FURNACE BURNER
METHANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.137
0.137
0.137
0.137
0.137
0.137
0.137
0.137
0.137
0.1-37
0 . 1 37
0.137
0.137
0.137
C.137
0. 157
0.157
0.157
0.157
0.157
0.157
0.157
C.157
AIR
FLOW
(CFM)
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.09^
2.094
2.094
2.094
2.094
2.094
2.094
2. 094
2.094
2.094
2.094
2.094
2.094
2.094
PCT
STOIC
AIR
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159.7
159. 7
159.7
159,7
159.7
139.9
139.9
139.9
139.9
139.9
139.9
139.9
139.9
AXIAL
DIST
( IN)
15.00
10.00
5.00
4.00
3.00
2.00
1.00
3.50
4.50
15.00
15.00
15.00
15.00
3.75
3.35
15.00
15.00
15.00
15.00
10.00
5.00
4.00
3.00
RADIAL
DIST
(IN)
0.00
c.oo
0.00
0.00
0.00
0.00
0.00
0.00
o.oo
c.oo
-0.20
-0.40
-O.60
0.00
0.00
-0.60
-o.^c
-0.20
0.00
0.00
0.00
0.00
0.00
WALL
TEMP
(C)
1440
1440
1440
1440
1440
1440
1440
1440
1440
1440
1440
1440
1440
1440
1440
1590
1590
1590
1590
1590
1590
1590
1590
NO
(PPM)
2
2
1
0
0
0
0
0
0
2
2
2
2
0
0
7
7
7
7
6
5
5
0
NOX
(PPM)
3
3
3
2
1
1
0
2
2
3
3
3
3
2
2
10
10
9
10
8
7
7
6
02
(PCT)
8.65
8.70
8.80
10.00
13.75
16.00
18.00
11.50
9.00
8.70
8.70
8.70
8.60
10.50
12.25
6.60
6.60
6.60
6.60
6.60
6.65
6.65
7.30
CO
(PCT)
0.003
0.003
0.042
0.285
0.413
0.185
0.031
0.413
0.151
0.003
0.003
0.003
0.003
0.359
0.429
o.ooe
0.007
o.ooa
0.008
0.008
0.010
0.021
0.285
C02
(PCT )
5.97
5.87
5.87
5.15
3.05
1.64
0.69
4.14
5.66
5.97
5.97
5.97
5.97
4.44
3.74
6.90
6.90
6.90
6.90
6.90
6.90
6.90
6.38
HC
(PPM)
0.
0.
400.
6000.
25000.
33500.
35000.
15500.
2100.
25.
22.
16.
11.
10000.
17500.
2.
2.
2.
2.
2.
1.
15.
2500.
-------
RUN NUMBER 133 CONT
PREFIXED FURNACE BURNER
METHANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
1CFM)
0.157
0.157
0.157
C.157
0.157
C.157
AIR
FLOW
(CFM)
2.094
2.094
2.094
2.094
2.094
2.094
PCT
STOIC
AIR
139.9
139.9
139.9
139.9
139.9
139.9
AXIAL
DIST
( IN)
2.00
1.00
3.50
2.50
2.75
2.25
RADIAL
DIST
( IN!
0.00
0.00
0.00
0.00
0.00
0.00
WALL
TEMP
(C)
1590
1590
1590
1590
1590
1590
NO
(PPM)
0
0
2
0
0
0
NOX
(PPM)
3
1
6
4
5
3
02
(PCT)
13.25
17.00
6.60
9*35
8.00
11.00
CO
(PCT)
0.816
0.163
0*073
0.789
0*546
Ci844
C02
(PCT!
3.05
1.01
6.90
5.05
5.87
3.94
HC
( PPM)
30000.
36000.
350.
12000.
6000.
22500.
I
Ui
ro
-------
RUN NUMBER 134
PREMIXED FURNACE BURNER
METHANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFV)
0.035
0.035
0.035
0.035
0.035
0 . C 3 5'
0.035
0.035
O.C35
0.0-35
0.035
0.035
0.077
C.C77
0.077
0.077
0.077
0 .077
0.077
C.077
C.077
0.077
0.077
AIR
FLOW
(CFM)
0.481
0.481
0.481
0.431
c.4£i
0.481
0 . 4 P 1
0.481
0.481
0.4R1
0.481
0.4? 1
0.481
C.4P1
0.481
0.4P1
0 . 4 ° 1
0.481
0.481
0.481
0.481
0.481
0.481
PCT
STOIC
AIR
140.4
140.4
140.4
140.4
140.4
14Q.4
140. 4
140.4
140.4
140.4
140.4
140.4
65.3
65.3
65.3
65.3
65.3
65.3
65.3
65.3
65.3
65.3
65.3
AXIAL
DIST
(IN)
15.00
15.00
15.00
15.00
10.00
5.00
4.00
3.00
2.00
1.00
0.00
-0.05
15.00
15.00
15.00
15.00
10.00
5.00
4.00
3.00
4.50
7.50
6.00
RADIAL
OIST
! IN)
0.00
-0.20
-0.40
-0.60
0.00
0.00
0.00
0.00
0.00
0.00
0.00
o.oo
0.00
-0.20
-0.40
-0.60
O.CO
0.00
0.00
0.00
0.00
o.oo
0.00
WALL
TEMP
(C)
1585
1585
1585
1585
1585
1585
1585
1585
1585
1585
15«5
1565
1600
1600
1600
1600
1600
1600
1600
1600
1600
1600
1600
NO
(PPM)
10
10
9
9
6
4
3
3
3
2
2
1
1
1
1
1
0
0
0
0
0
0
0
NOX
(PPM)
12
12
12
12
8
6
5
5
5
5
5
5
02
(PCT)
7.40
7.40
7.35
7.35
7.40
7,50
7.50
7.50
7.50
7.25
7.10
7.10
0.24
0.24
0.24
0.24
0.24
0.71
7.10
12.75
3.50
0.23
0.23
CO
(PCT)
0.003
0.003
0.004
0.004
0.003
0.003
0.005
0.007
0.019
0.029
0.063
0.068
9.194
9.194
9.194
9.194
8.985
8.186
5.276
2.724
6.765
8.779
8.578
C02
(PCT)
6.59
6.43
6.59
6.59
6.69
6.69
6.79
6.79
6.79
6.90
7.00
7.10
4. 14
3.64
3.84
3.84
3.94
3.94
2.46
1.41
3.25
3.94
4.04
HC
( PPM )
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
8.
5.
4.
3.
500.
12000.
37500.
42000.
32000.
2100.
4500.
Ui
-------
RUN NUMBER 135
PREMIXED FURNACE BURNER
PROPANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.014
0.014
0 . 01 4
0.014
0.014
0.014
0.014
0.014
0 . 0 1 4
0.014
0.014
0.014
AIR
FLOW
(CFM)
0.481
C .API
0.461
0.481
0 . A ? 1
0.481
0.481
0.481
0.4B1
0.4S1
0.431
0.481
PCT
STOIC
AIR
133.8
133.8
n« .=>
133. 8
133. S
133 .3
1 3 S . 3
13. ".8
1 3 S . 8
1 3 ?- « 8
138.8
138.8
AXIAL
DIST
(IN)
15.00
15.00
15.00
15.00
10.00
5.00
4.00
3*00
2.00
2.50
2.75
2.25
RADIAL
DIST
( IN)
0.00
-0.20
-0.40
-0.60
0.00
0.00
C.OO
0.00
0.00
0.00
0.00
0.00
WALL
TEMP
(C)
1625
1625
1625
1625
1625
1625
1625
1625
1625
1625
1625
1625
NO
(PPM)
13
14
16
17
6
3
3
2
0
0
0
0
NOX
(PPM)
18
19
21
22
8
5
5
5
1
3
4
1
02
(PCT)
7.70
7.70
7.70
7.70
7.75
7.70
7.70
7.70
16.00
11.00
8.50
13.50
CO
(PCT)
0.008
0.008
0.007
0.008
0.006
0.004
0.004
0.030
0.291
0.421
0.229
0.438
C02
(PCT)
7.42
7.42
7.31
7.31
7.31
7.42
7.42
7.42
2.37
5.36
6.79
3.64
HC
( PPM )
0.
0.
0.
0.
0.
0.
0.
200.
34000.
17000.
4000.
30000.
-------
RUN NUMBER 136
PREMIXED FURNACE BURNER
PROPANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CF.vj
0.062
0.062
0.062
0.062
0.062
0.062
0.062
0.062
0.062
0.062
0.062
0.062
0.062
0.062
0.062
AIR
FLOW
(CFM)
2.094
2.094
2.094
2.094
2.094
2.C94
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
PCT
STOIC
AIR
140.7
140.7
140.7
140.7
140.7
140.7
140.7
140.7
140.7
140.7
140.7
140.7
140.7
140.7
140.7
AXIAL
DIST
(IN)
15.00
15.00
15.00
15.00
10.00
5.00
4.00
3.00
2.00
2.50
3.25
3.50
3.75
2.75
2.90
RADIAL
DIST
( IN)
0.00
-0.20
-0.40
-0.60
0.00
0.00
0.00
0.00
0.00
0.00
0.00
0.00
0.00
0.00
0.00
WALL
TEMP
1610
1610
1610
1610
1610
1610
1610
1610
1610
1610
1610
1610
1610
1610
1610
NO
(PPM)
12
12
12
12
9
7
6
0
0
0
1
1
2
0
0
NOX
(PPM)
15
15
15
16
13
11
10
6
2
4
6
6
7
3
4
02
(PCT)
6.50
6.50
6.50
6.45
6.65
6.60
6.60
fi.25
14.75
11 .25
8.00
7.50
7.20
10.50
9.50
CO
(PCT)
0.012
0.013
0.012
0.014
0.011
0.019
0.055
0. 707
0.734
0.899
0.352
0.267
0.172
0.899
0.762
C02
(PCT)
8.25
8.25
8.25
8.25
8. 14
8.25
8.25
7.00
3.05
5.05
7.62
7.52
7.73
5.35
5.87
HC
(PPM)
9.
8.
5.
5.
3.
2.
75.
7000.
34000.
25000.
4000.
2500.
1000.
18000.
l^OOO.
I
Ul
-------
RUN NUMBER 137
PREMIXED FURNACE BURNER
PROPANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
C.072
0.072
C.07?
0.072
0.072
0.072
0.072
0.072
0.072
0.072
0.072
0.072
AIR
FLOW
(CFM)
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
PCT
STOIC
AIR
120.9
120.9
IPO. 9
170.9
120.9
170.9
170.9
120. 9
170.9
120.9
IPO. 9
120.9
AXIAL
DIST
(IN)
15.00
15.00
15.00
15.00
15.00
10.00
5.00
4.00
3.00
2.00
1.00
0.00
RADIAL
DIST
(IN)
0.00
-0.20
-0.40
-0.60
0.00
0.00
0.00
0.00
0.00
0.00
0.00
0.00
WALL
TEMP
(C)
1795
1795
1795
1795
1795
1795
1795
1795
1795
1795
1795
1795
NO
(PPM)
74
72
72
73
69
43
24
19
16
9
5
1
NOX
(PPM)
91
91
92
94
90
63
37
24
21
02 CO C02 HC
(PCT) (PCT) (PCT) (PPM)
3.80 0.063 10.98 3.
3.85 0.060 10.98 2.
3.85 0.064 10.73 2.
3.85 0.062 10.98 4.
3.85 0.062 10.98 3.
3.85 0.054 10.98 3.
3.95 0.091 10.98 1.
4.10 0.151 10.73 1.
4.30 0.245 10.73 1. f
4.50 0.374 10.49 2. £
4.80 0.626 10.24 15.
5.70 1.537 9.02 100.
-------
RUN NUMBER 138
PREMIXED FURNACE BURNER
PROPANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
C.016
0.016
O.C16
0.016
0.016
0.016
0.016
0.016
0.016
0.016
0.016
0.016
0.016
AIR
FLOW
(CFM)
0.481
0.4*1
0.4P1
o.48i
0.481
0.481
0 . 4 « 1
0.481
0.481
0.481
0.481
0.481
0.481
PCT
STOIC
ATR
'~ « * >
170.8
170.3
120.8
170.8
12C.B
120.8
120.S
170.3
170.3
120.8
170. e
120.8
120.8
AXIAL
DISf
t T M 1
V i >* I
15.00
15.00
15.00
15.00
10.00
5.00
3.00
1.00
0.00
2.00
2.50
2.75
1.50
RADIAL
OIST
/ T fc i t
(IN)
0.00
-0.70
-0.40
-0.60
o.cc
0.00
0.00
0.00
0.00
0.00
0.00
0.00
0.00
WALL
TEMP
(C)
1795
1795
1795
1795
1795
1795
1795
1795
1795
1795
1795
1795
1795
NO
(PPM)
200
170
160
160
70
10
8
4
2
7
7
7
6
NOX
(PPM)
240
210
200
200
95
20
16
11
6
13
13
14
12
02
(PCT)
5.20
5.20
5.20
5.20
5.40
5.55
5.70
6.40
7.40
5.95
5.85
5.95
6.20
CO
(PCT)
0.028
0.024
0.025
0.025
0.016
0.012
0.024
0.139
0.239
0.043
0.030
0.035
0.064
C02
(PCT)
9.26
9.26
9.26
9.26
9.26
9.51
9.75
9.51
9.02
9.75
9.75
9.75
9.51
HC
(PPM)
2.
2.
4.
5.
2.
2.
1.
1.
50.
1.
1.
1.
1.
N
i
Ul
•vj
-------
RUN NUMBER 139
PREMIXED FURNACE BURNER
METHANE
WALL-HOT AIR PREHEAT-NONE
FUEL
FLOW
(CFM)
0.042
0.042
0.042
.0.062
0.042
0.042
0.042
0.042
0.042
0.042
0.042
AIR
FLOW
(CFK)
0.481
0.481
0.431
0.481
C.481
C . 4 8 1
0.481
0.451
0.481
0.481
0.481
PCT
STOIC
AIR
1?0.1
120.1
1/0.1
120.1
120.1
1 ? 0 . 1
120.1
120.1
12C.1
120.1
120.1
AXIAL
DIST
(IN)
15.00
15.00
15.00
15.00
10.00
5.00
3.00
1.00
0.00
2.00
1.50
RADIAL
DIST
( IN)
0.00
-0.20
-0.40
-0.60
0.00
0.00
0.00
0.00
0.00
o.co
0.00
WALL
TEMP
(C)
1770
1770
1770
1770
1770
1770
1770
1770
1770
1770
1770
NO
(PPM)
95
95
100
105
31
12
11
10
7
11
10
NOX 02 CO C02 HC
(PPM) (PCT) (PCT) (PCT) (PPM)
120 4.25 0.019 8.54 5.
120 4.25 0.017 8.30 6.
130 4.20 0.021 8.30 8.
130 4.20 0.021 8.30 8.
43 4.35 0.010 8.54 2.
23 4.60 0.012 9.26 1.
21 4.60 0.022 9.02 1.
20 4.50 0.116 9.26 1.
18 4.30 0.172 9.26 1. ^
19 4.60 0.039 9.02 1. ^
19 4.60 0.060 9.26 1. °°
-------
RUN NUMBER 140
PREMIXED FURNACE BURNER
METHANE
WALL-HOT AIR PREHEAT-NONE
FUFL
FLOW
(CFM)
0.133
0.183
0.1-83
0.183
0.183
0.1 = 3
0.183
0.183
0.1S3
C.1S3
AIR
FLOW
(CFM)
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
2.094
PCT
STOIC
AIR
119.8
119.8
119.8
119.8
119.8
119.8
119.8
119.8
119.8
119. S
AXIAL
DIST
(IN)
15.00
15.00
15.00
15.00
10.00
5.00
3.00
2.00
1.00
0.00
RADIAL
DIST
(IN)
0.00
-0.20
-0.40
-0.60
0.00
0.00
0.00
0.00
0.00
0.00
WALL
TEMP
(C)
1775
1775
1775
1775
1775
1775
1775
1775
1775
1775
NO
(PPM)
45
47
49
49
31
19
15
10
4
2
NOX
(PPM)
66
67
69
70
47
31
29
26
22
18
02
(PCT)
3.75
3.75
3.70
3.70
3.75
3.80
3.90
4.00
4.30
4.25
CO
(PCT)
0.045
0.045
0.044
0.045
0.038
0.063
0.135
0.291
1.011
1.068
C02
(PCT)
9.26
9.26
9.26
9.26
9.26
9.26
9.26
9.26
8.78
8.78
HC
(PPM)
7.
7.
6.
6.
5.
3.
2.
3.
200.
5000.
-------
RUN NUMBER 141
PREMIXED FLAT FLAME BURNER
METHANE
WALL-COLD AIR PREHEAT-NONE
FUEL AIR PCT AXIAL RADIAL WALL NO NOX 02 CO C02 HC
FLOW FLOW STOIC DIST DIST TEMP
(CFM) (C.FM) AIR (IN) (IN) (O (PPM) (PPM) (PCT) (PCT) (PCT) (PPM)
0.050 0.481 100.8 12.60 0*00 47 43 0.53 0.219 10.98 5.
0.050 0.481 100.8 12.60 0.20 49 49 0.36 0.181 11.23 5.
O.D50 C.481 100.8 12.60 0.40 49 49 0.35 0.190 11.48 4.
O.C50 C.481 100.S 12.60 C.60 49 49 0.32 0.172 11.99 4.
O.C5C C.AS1 100.3 9.60 0.60 49 49 0.30 0.163 11.48 4.
0.050 0.431 100.3 9.60 0.^0 49 49 0.31 0.151 11.23 4.
0.050 0.481 100.8 9.60 0.20 49 49 0.26 0.139 11.£-8 3.
C.050 0.491 100.9 9.60 0.00 50 51 0.26 0.143 11.23 3.
0.050 0.481 100.3 4-.60 0.20 55 56 0.45 0*181 11.23 4. ?
C.050 0.481 100.8 2.60 0.20 57 60 0.66 0.324 10.98 4. o
0.050 0.4P1 100.8 1.60 0.20 49 60 0.79 0.599 10.73 4.
0.050 0.431 100.3 0.60 0.20 40 5C 1.00 0.789 10.49 4.
0.050 0.481 100.8 0.30 0.20 23 35 1.20 0.983 10.24 4.
0.050 0.481 100.8 0.20 0.20 16 29 1.25 1.125 9.99 25.
-------
G-l
TECHNICAL R'EPORT DATA
(Please read Jiiztructioiis on the reverse before completing)
1. REPORT NO.
EPA-600/7-76-009a
2.
3. RECIPIENT'S ACCESSION NO.
4. T,TLE AND SUBTITLE MECHANISM AND KINETICS OF THE
FORMATION OF NOx AND OTHER COMBUSTION
POLLUTANTS; Phase I. Unmodified Combustion
5. REPORT DATE
August 1976
6. PERFORMING ORGANIZATION CODE
7. AUTHOR(S)
8. PERFORMING ORGANIZATION REPORT NO
V.S. Engleman and W. Bartok
GRU. 2DJAM. 76
9. PERFORMING OR9ANIZATION NAME AND ADDRESS
Exxon Research and Engineering Co.
P. O. Box 8
Linden, New Jersey 07036
10. PROGRAM ELEMENT NO.
1AB014; ROAP 21BCC-013
11. CONTRACT/GRANT NO.
68-02-0224
12. SPONSORING AGENCY NAME AND ADDRESS
EPA, Office of Research and Development
Industrial Environmental Research Laboratory
Research Triangle Park, NC 27711
13. TYPE OF REPORT AND PERIOD COVERED
Phase I Final; 4/73-2/74
14. SPONSORING AGENCY CODE
EPA-ORD
15. SUPPLEMENTARY NOTES Project officer for
Ext 2432, Mail Drop 65.
repOrt is W.S. Lamer , 919/549-8411
16• ABSTRACT Tne repOrt gjves Phase I results of an investigation of the mechanisms and
kinetics of the formation of NOx and other combustion pollutants. It gives results of
experimental investigations of unmodified combustion and supporting theoretical cal-
culations. The combustion of hydrogen, carbon monoxide, methane, and propane
with air in a jet-stirred combustor (JSC) was studied to facilitate the assessment of
coupled combustion/pollutant formation. The JSC tests also extended the range and
accuracy of data taken in previous studies. Experiments also included a flow reactor
capable of accepting multiple burner types and operating with selected wall tempera-
ture. Premixed flat and focused flames, as well as laminar and turbulent diffusion
flames, were studied in the flow reactor using methane and propane fuels. The tests
included heat-loss and adiabatic conditions and a limited number of wall heat
addition cases. Stirred reactor calculations, supporting the experimental program,
indicated the need for more detailed kinetics in hydrocarbon/air combustion before
NOx formation can be predicted. Similarly, plug flow calculations indicated strong
coupling between combustion reactions , specie diffusion, and NOx formation in the
flame zone. Further kinetic data on reactions between hydrocarbon fragments and
nitrogenous species is required to properly assess the importance of those inter-
actions inNOx formation.
17.
KEY WORDS AND DOCUMENT ANALYSIS
DESCRIPTORS
b.IDENTIFIERS/OPEN ENDED TERMS
c. COSATI Field/Group
Air Pollution
Reaction Kinetics
Combustion
Nitrogen Oxides
Methane
Propane
Hydrogen
Carbon Monoxide
Mathematical Models
Diffusion Flames
Air Pollution Control
Stationary Sources
Well Stirred Reactor
Plug Flow Reactor
Unmodified Combustors
13B
07D
21B
07B
07C
12A
B. DISTRIBUTION STATEMENT
Unlimited
19. SECURITY CLASS (This Report)
Unclassified
21. NO. OF PAGES
310
20. SECURITY CLASS (This page)
Unclassified
22. PRICE
EPA Form 2220-1 (9-73)
------- |