U.S. patent number 3,848,548 [Application Number 05/419,299] was granted by the patent office on 1974-11-19 for incineration process for disposal of waste propellant and explosives.
This patent grant is currently assigned to Hercules Incorporated. Invention is credited to James William Bolejack, Jr., Truman Knox Daniel, Jr., Darrell Edward Rolison.
United States Patent |
3,848,548 |
Bolejack, Jr. , et
al. |
November 19, 1974 |
INCINERATION PROCESS FOR DISPOSAL OF WASTE PROPELLANT AND
EXPLOSIVES
Abstract
A process is provided for incineration of waste propellants and
explosives. In this process the waste propellant or explosives in
particulate form is mixed with water forming an aqueous suspension.
The aqueous suspension is burned in a rotary incinerator under
conditions which permit sequential evaporation of water from the
suspension, drying of the particulate propellant or explosive, and
then ignition of the propellant or explosive. The combustion gases
are scrubbed with water prior to passing into the atmosphere. The
invention herein described was made in the course of or under a
contract or subcontract thereunder with Department of the Army.
Inventors: |
Bolejack, Jr.; James William
(Blacksburg, VA), Daniel, Jr.; Truman Knox (Christianburg,
VA), Rolison; Darrell Edward (Blacksburg, VA) |
Assignee: |
Hercules Incorporated
(Wilmington, DE)
|
Family
ID: |
23661658 |
Appl.
No.: |
05/419,299 |
Filed: |
November 27, 1973 |
Current U.S.
Class: |
588/320; 110/212;
110/220; 110/246; 110/215; 110/222; 110/237; 588/312; 588/408;
588/403 |
Current CPC
Class: |
F23G
7/001 (20130101); F23G 5/02 (20130101) |
Current International
Class: |
A62D
3/00 (20060101); F23G 5/02 (20060101); F23G
7/00 (20060101); F23g 007/00 () |
Field of
Search: |
;44/1D
;110/7R,7S,8R,8P,14,119 |
References Cited
[Referenced By]
U.S. Patent Documents
Primary Examiner: Sprague; Kenneth W.
Attorney, Agent or Firm: Keehan; Michael B.
Claims
What we claim and desire to protect by Letters Patent is:
1. A process for incineration of waste liquid and solid propellants
and explosives comprising:
a. forming an aqueous suspension of propellant or explosive waste
in water having a dispersed phase comprising solid propellant or
explosive waste in particulate form, in which the solid particles
have an average maximum length of less than 0.25 inch, and a
continuous phase comprising water;
b. introducing air, and the suspension of step (a) into one end of
a rotary incinerator operating at a temperature of from about
1200.degree.F. to about 2200.degree.F., said suspension being fed
at a rate sufficient to initially form a thin aqueous layer of said
suspension on the walls of said incinerator and continuously
contacting said layer of suspension with dry surface of said
incinerator wall whereby the aqueous content of the continuous
phase of the suspension is evaporated and the propellant particles
are sequentially dried and ignited within;
c. drawing exhaust gases from the rotary kiln and contacting said
exhaust gases with water to remove particulate matter and noxious
gases from said gas, and
d. exhausting the resulting gases from step (c) to the
atmosphere.
2. The process of claim 1 in which the solid propellant or
explosive particles have an average maximum length of about 0.10
inch.
3. The process of claim 1 in which the particulate solid propellant
is ground single base propellant.
4. The process of claim 1 in which the particulate solid propellant
is a mixture of ground single base and double base propellant.
5. The process of claim 1 in which the dispersed phases comprises a
particulate carbonaceous combustible material which contains
absorbed liquid propellant or explosive.
6. The process of claim 5 in which the dispersed phase comprises
sawdust impregnated with nitroglycerin.
7. A process for incineration of waste solid propellant or
explosive comprising the steps of:
a. removing extraneous metal from said solid propellant or
explosive feed material,
b. grinding the substantially extraneous metal-free solid
propellant or explosive in the presence of water, to form solid
particles, substantially all of said particles having a (maximum)
average dimension of less than 0.25 inch,
c. mixing said water wet solid particles and additional water
necessary to form an aqueous suspension of said solid particles in
water, the weight ratio of water to said solid particles being from
about 19:1 to about 1:1,
d. introducing air, and the suspension of step (c) into one end of
a rotary incinerator operating at a temperature of from about
1,200.degree.F. to about 2,200.degree.F., said suspension being fed
at a rate sufficient to initially form a thin aqueous layer of said
suspension on the walls of said incinerator, and continuously
contacting said layer of suspension with dry wall surface of the
incinerator whereby the continuous phase of the suspension is
evaporated and the solid particles are sequentially dried and
ignited within said incinerator,
e. drawing exhaust gases from the rotary incinerator, and wet
scrubbing said exhaust gases with water to remove particulate
matter and to dissolve noxious gases present in said exhaust gases,
and
f. exhausting the resulting gases from step (e) to the
atmosphere.
8. The process of claim 7 in which the exhaust gases from the
rotary incinerator are drawn through a second incinerator prior to
wet scrubbing, said second incinerator operating at a temperature
of from about 1,200.degree.F. to about 2,200.degree.F., the
residence time of said gases in said second incinerator being from
about 0.3 seconds to about 0.5 seconds.
9. The process of claim 8 in which the weight ratio of water to
said particulate propellant or explosive is about 3:1 and the solid
particles have an average maximum dimension of about 0.10 inch.
Description
This invention relates to a process for incineration of waste
propellants, and explosives.
The commonly employed method for disposing of propellant and
explosive waste generally consists of manually spreading the waste
on pads or on the ground and burning the waste in open air. There
are several undesirable features associated with this commonly
employed method. Open air burning is limited by weather conditions
and produces combustion products which are a source of air
pollution. Further, personnel are exposed to a potential fire
hazard when the propellant or explosive waste is spread on the pads
or the ground prior to burning. Space and quantity distance
requirements for burning of waste propellants and explosives
introduce additional limitations on open-air burning.
The open burning method for solid waste propellants and explosives
is a source of pollution. A new method of disposal of waste
propellants and explosives must be devised in order to meet present
and future air pollution standards. To meet this need, a process
has been developed for incineration of waste propellants and
explosives, which eliminates many of the hazards inherent in the
open burning of waste propellants and explosives and which process
is capable of reducing pollution to within limits currently under
consideration for pollution standards.
Broadly, in accordance with this invention, a process is provided
for incineration of waste propellant and explosives comprising the
steps of:
A. forming an aqueous suspension of propellant or explosive waste
in water having a dispersed phase comprising solid propellant or
explosive waste in particulate form, in which the solid particles
have a maximum average length of less than 0.25 inch, and a
continuous phase comprising water;
B. introducing air and the suspension of step (a) into one end of a
rotary kiln operating at a temperature of from about
1,200.degree.F. to about 2,200.degree.F., said suspension being fed
at a rate sufficient to initially form a thin aqueous layer of said
suspension on the wall of said incinerator and continuously
contacting said layer of suspension with dry surface of said
incinerator wall whereby the continuous water phase of the
suspension is evaporated and the propellant or explosive particles
are sequentially dried and ignited within the rotary kiln;
C. drawing exhaust gases from the rotary kiln and contacting said
exhaust gases with water to remove particulate matter and noxious
gases from the exhaust gas, and
D. exhausting the resulting gases from step (c) to the
atmosphere.
The process of this invention is more fully described with
reference to the drawings. In the drawings like numbers refer to
like parts where applicable.
FIG. 1 is an overall flow diagram of the process of this invention
utilizing both solid and liquid propellant or explosive wastes as
feed materials.
FIG. 2 is a schematic diagram illustrating a preferred embodiment
of a system utilized in the process of this invention in which a
normally solid, waste propellant or explosive is incinerated.
FIG. 3 is a schematic diagram illustrating the interior of a rotary
kiln during the controlled burning process of this invention.
FIG. 4 is a schematic drawing illustrating the feed nozzle for
introducing the aqueous suspension of waste feed into the rotary
kiln.
FIG. 1 illustrates the overall process of this invention in block
diagram form. It is seen from FIG. 1 that either solid or liquid
waste propellants or explosives can be incinerated in accordance
with the process of this invention by forming a suspension of solid
or liquid propellant or explosive, in solid particulate form in
water, and incinerating the suspension.
As illustrated in FIG. 2, waste solid propellant or solid
explosive, is fed into feed hopper 10. The feed hopper 10 is
equipped with vibratory means (not shown) for uniformly feeding the
waste solids through a bottom opening 12 in said feed hopper 10
onto a fiber glass conveyor 16. Conveyor 16 is used to convey the
waste solids through a metal detection and removal device 18
wherein any extraneous metal, i.e., metal which is not associated
with or part of either the solid propellant or solid explosive
waste feed is detected and after detection said metals are removed
from the feed to wet grinder. Extraneous metal-free waste solid
propellant or solid explosive is then conveyed into a wet grinder
20 at a controlled rate. In the wet grinder 20, the solid waste is
ground in the presence of water. The resulting solid particles have
a length or maximum dimension averaging 0.25 inch or less.
The ground water-wet solid waste particles are washed into mixer
22. In mixer 22, the particles are admixed with additional water,
as necessary, to form a suspension of solid waste particles in
water. This suspension is pumped by pump 24 through feed line 26
into the inlet-end 30 of kiln 32. Flow through the feed line 26
must be maintained in the turbulent range, i.e., at a Reynolds
Number of at least about 6,400 to maintain the solid particles in
suspension.
Kiln 32 is lined with refractory brick. Kiln 32 rotates about its
longitudinal axis through use of drive means (not shown). The
aqueous suspension of waste solids is deposited on the wall of the
kiln 32 and immediately flows to a thin layer of suspension.
Movement of the wall 34 of kiln 32 constantly provides continual
contact of a hot-dry surface to the layer of suspension. Air is
continuously introduced into the kiln 32 at the inlet-end 30
through air line 36. Air passes through the inner chamber 38 of
kiln 32 and through exhaust outlet 40 at the burner-end 42 of kiln
32. A burner 44 is used constantly during incineration to maintain
the temperature in the inner chamber 38 of the kiln 32. Exhaust
gases from combustion of the waste solid propellant or explosive
within inner chamber 38 of kiln 32 pass through exhaust line 40
into a second incinerator 46 consisting of a refractory lined wall
48 and burner 50. The second incinerator 46 functions as an
afterburner for further combustion of combustible products
contained in the exhaust gas from kiln 32. The resulting exhaust
gas passes out of the exit-end 52 of second incinerator 46 through
a precooler 54 and through feed line 56 into a wet scrubber 58. In
wet scrubber 58 particulate matter and noxious gases are removed
from the exhaust gas. An exhaust fan 60 draws the exhaust gas
through the wet scrubber 58 and exhausts the resulting product gas
to the atmosphere.
In FIG. 3 the sequential nature of the incineration of solid
particles as it occurs in the kiln 32 is illustrated. The
suspension of solid waste particles in water initially forms a thin
layer of suspension along the refractory lined wall 48 of the
incinerator. As the layer of suspension is continually contacted
with the hot surface of the rotating kiln wall, the water content
of the suspension is evaporated. The solids 64 are then heated
rapidly to dryness and then are ignited. The various factors which
must be controlled to insure that the sequential burning process
takes place in the rotary kiln are more fully described
hereinafter.
In FIG. 4 the stationary, inlet-end 30 of rotary kiln 32 is shown.
The feed inlet 31 to said kiln is close to the lower wall of the
kiln. The feed spout 33 is jacketed with water. The cooling
provided by the jacketed spout prevents vaporization of the water
phase of the aqueous suspension in the feed lines. Any such
vaporization is detrimental to sequential burning of the waste
particles in suspension.
The following examples further illustrate the process of this
invention. In the examples, parts and percentages are by weight
unless otherwise specified.
EXAMPLE 1
A waste single base propellant (IMR) charge is passed through a
metal detection and removal device wherein extraneous metals are
removed from the propellant charge. The propellant is then passed
at a controlled rate into a flying blade grinder where it is mixed
with water and ground into small particles. The particle size of
the ground propellant is determined by Tylers Screen Analysis. The
propellant particles have an average length or maximum dimension of
about 0.04 inches. The water-wet particles are transferred to a
mixing vessel wherein additional water is added. The weight ratio
of water to particles in the mixing vessel is 2.8:1. The particles
are slurried in the mixing vessel to form a suspension of the
propellant particles in water. The propellant suspension is
introduced into an incinerator operating at a temperature of
1,600.degree.F. and in which the air flow rate through said
incinerator is 1,248 cubic feet per minute. The incinerator
consists of a high-alumina refractory brick lined rotating chamber,
6 feet long and having an inside diameter of 5 feet. The chamber
rotates at a speed of 1.1 revolutions per minute. The feed line in
the rotary incinerator is cooled to maintain the liquid phase of
the suspension in the liquid state. The suspension of waste
propellant in water is fed at one end of the rotary kiln near the
rotating walls. The suspension immediately starts to flow and very
rapidly forms a thin layer of suspension on the moving walls of the
incinerator. The water phase of the suspension is rapidly
evaporated and the propellant particles are sequentially dried and
ignited. The product gases from the combustion are exhausted
through a second incinerator operating at a temperature of about
1,600.degree.F. The residence time of the exhaust gases in said
second incinerator is about 0.3 seconds. The second incinerator
which is sometimes referred to as an afterburner is high-alumina
refractory lined chamber, seven feet in length and having an inside
diameter of 23/4 feet. The hot exhaust gases are drawn through a
pre-cooler where the temperature of the gases is reduced to about
250.degree.F. and the gases are then drawn through a wet scrubber
in which the gases are in intimate contact with water. In the wet
scrubber, water soluble gas contained in the exhaust gases and some
particulate matter are removed from the exhaust gas stream. The
resulting gases are subsequently exhausted to the atmosphere. The
gases being exhausted are analyzed for NO, NO.sub.2, SO.sub.2 ,
Hcl, CO.sub.2 and hydrocarbons. The analysis of the gases exhausted
to the atmosphere is set forth in Table I.
EXAMPLES 2-6
Example 1 is repeated utilizing a mixture of single base and double
base propellant as the waste feed charge. This waste feed is ground
under water. The resulting particles have an average length or
maximum dimension of about 0.08 inches as measured by Tyler Screen
Analysis. The particles are admixed with water to form a
suspension. The suspension is introduced into the rotary kiln.
Processing conditions differing from Example 1 are set forth in
Table II. The exhaust gas analysis from incineration of the mixture
of single and double base waste propellant is set forth in Table
I.
TABLE I
__________________________________________________________________________
STACK GAS ANALYSIS EXAMPLE (PPM) CO.sub.2 * No. HYDROCARBON
HYDROGEN SULFIDE NO NO.sub.2 HYDROGEN CHLORIDE SULFUR DIOXIDE %
__________________________________________________________________________
1 0 100 80 0 -- 0 2% 2 90 58 170 6 -- 10 2.0% 3 90 0 160 0 -- 83
1.6% 4 50 35 235 0 -- -- 1.0% 5 28 0 200 0 -- -- 3.4% 6 23 80 200 0
0 30 2.1%
__________________________________________________________________________
* % Increase of CO.sub.2 in stack gas when burning propellant and
fuel as compared to CO.sub.2 in exhaust burning fuel only.
TABLE II
__________________________________________________________________________
TEMPERATURE .degree.F. EXAMPLE TYPE FEED RATE PARTICLE SIZE WEIGHT
RATIO ROTARY SECOND AIR FLOW NO. MATERIAL LBS./MIN. (average)
WATER/SOLIDS KILN INCINERATOR CU.FT./MIN.
__________________________________________________________________________
1 Sgl. Base 4.9 .040 inch 2.8:1 1600.degree.F. 1600.degree.F. 1248
Propel. 2 Sgl. Base 4.2 .080 2.8:1 Dbl. Base Propel. 3 4.2 2.9:1 4
4.2 3.0:1 5 4.2 3.0:1 6 4.1 3.3:1
__________________________________________________________________________
EXAMPLES 7-24
Example 1 is repeated utilizing various waste solid propellants and
explosives as feed materials. Operation of the process proceeds
satisfactorily in all cases. Water evaporation drying and ignition
of propellants and explosives proceeds smoothly in the kiln in all
cases. Visual observation of the stack gases shows no visible smoke
from the exhaust gas stack. A white exhaust plume of gas saturated
with water vapor can be observed. The exhaust gases for each
propellant and explosive charge are analyzed. Process conditions
and gas analysis for each example are set forth in Tables III and
IV, respectively.
TABLE III
__________________________________________________________________________
TEMPERATURE .degree.F. EXAMPLE TYPE FEED RATE PARTICLE SIZE WEIGHT
RATIO ROTARY SECOND AIR VELOCITY NO. MATERIAL LBS./MIN. (average)
WATER/SOLIDS KILN INCINERATOR CU.FT./MIN.
__________________________________________________________________________
7-15 Comp. A-5.sup.(1) 3.0 Granular 3:1 1600 1700 1000 4.2
Sugar-like 1600 1700 1350 3.3 (<0.10 inch) 1600 1700 1800 3.3
1500 1600 1000 3.2 1700 1800 1000 4.2 1800 1800 1000 3.6 1600 1700
1000 -- 1500 1600 1350 1.8 1500 1600 1350 16 Mixture 1.7 0.10 inch
5.5:1 1600 1700 1000 Comp. B.sup. (2) Dbl. Base.sup. (4) Sgl.
Base.sup. (3) 17 Sgl. Base.sup. (3) 1.7 0.10 inch -- 1600 1700 1000
18 Sgl. Base.sup. (3) 1.2 >.10 inch 3.7:1 1600 1700 1000 Dbl.
Base.sup. (4) 19 TNT.sup.(5) 1.1 Flake .020 inch 4.4:1 1600 1700
1000 thick .times. 1/8 inch length 20-22 3.9 3:1 1800 1800 1000 3.0
3:1 1700 1800 1350 3.0 3:1 1500 1600 1000 23 Aluminized 2.9 3:1
1700 1800 1000 Dbl. Base.sup. (4) 24 Dbl. Base.sup. (4) 3.7 3:1
1700 1800 1000
__________________________________________________________________________
.sup.(1) Composition A-5 is 98.5% cyclotrimethylenetrinitraamine
(RDX) an 1.5% stearic acid. .sup.(2) Composition B is 60% (RDX) and
40% trinitrotoluene. .sup.(3) Single Base propellant consists
primarily of nitrocellulose. .sup.(4) Double Base propellant
consists primarily of nitrocellulose and nitroglycerin. .sup.(5)
TNT is trinitrotoluene.
TABLE IV
__________________________________________________________________________
STACK GAS ANALYSIS EXAMPLE (PPM) CO.sub.2 NO. HYDROCARBONS HYDROGEN
SULFIDE NO NO.sub.2 HYDROGEN CHLORIDE SULFUR DIOXIDE %
__________________________________________________________________________
7 130 41 160 4 0 60 8.4 8 0 42 160 10 0 68 8.2 9 0 80 240 2 0 69
10.5 10 280 130 130 0 0 54 10.5 11 170 29 230 0 0 0 6.6 12 0 15 610
10 0 10 8.3 13 0 9 250 24 0 0 7.2 14 0 5 160 32 0 2 7.2 15 0 10 152
23 0 0 7.6 16 0 29 270 0 0 0 13.5 17 0 16 190 0 0 0 9.7 18 7 55 95
0 0 0 6.0 19 0 130 230 112 0 92 9.0 20 0 11 300 99 0 17 9.2 21 0 0
350 160 0 5 5.7 22 0 25 310 50 0 0 8.3 23 60 21 128 49 0 0 -- 24
170 50 80 0 0 0 --
__________________________________________________________________________
EXAMPLE 25
Example 1 is again repeated utilizing a nitroglycerin slum as
explosive liquid. The nitroglycerin slum contains triacetin,
acetone and some water. The nitroglycerin slum is poured onto
sawdust particles to wet the sawdust with the nitroglycerin slum.
The sawdust absorbs all of the slum. The nitroglycerin wet sawdust
is then screened to remove any foreign objects, particularly
metals, and is then added to a mixer containing water,
nitrocellulose, and single and double base propellant to form a
suspension of explosive solids (nitroglycerin impregnated sawdust,
nitrocellulose and propellant) in water. Some of the nitroglycerin
is extracted from the sawdust into the water, up to the limit of
the solubility of nitroglycerin in water at the mixing temperature
of about 70.degree.F. The suspension is mixed for a minimum of 15
minutes and then pumped to the incinerator under conditions of
turbulent flow following steps and conditions for operation of the
process as set forth for Example 1. After most of the suspension
has been incinerated, additional water-wet solid propellant
particles and water is added to the mixer and pumped to the
incinerator using the steps and conditions for operation of the
process as set forth in Example 1. The process operates smoothly in
the incineration of the waste containing nitroglycerin wet sawdust
and visual observation of the exhaust gas reveals no smoke.
In the examples heretofore described, a second incinerator is
employed in series with the rotary kiln for purposes of achieving
more complete combustion of the exhaust gas from the rotary kiln,
whereby hydrocarbonaceous particulate matter in the exhaust
undergoes further combustion. Also, the level of noxious gases is
further reduced in the secondary incinerator. In practice, the need
for a secondary incinerator will depend, in part, on the
permissible level of noxious gases and hydrocarbonaceous and other
particulates in the exhaust stream. In theory, the first
incinerator can be designed and operated to avoid the necessity of
utilization of a second incinerator. In practice, however, this may
not be practical, i.e., the size (length and diameter) of the kiln
may become excessive, and the operating temperatures, etc., may not
be readily controlled in such a unit. The need for a second or more
incinerators in series will be determined on an overall system
design basis. When a second incinerator is employed it is generally
operated at from about 1,200.degree.F. to about 2,200.degree.F.
Residence time of exhaust gas in the second incinerator may vary
depending on system design, however, a residence time of from about
0.3 seconds to about 0.5 seconds is generally acceptable.
In the process of this invention sequential evaporation of water
from the aqueous suspension of waste propellant or waste explosive
is essential. Thus, the operational variables such as feed rate,
feed condition (liquid suspension), air flow rate through the
incinerator, incinerator temperature, incinerator residence time
and the like must be controlled to produce sequential evaporation,
drying of the waste feed, and ignition and burning in order to
achieve safe and effective incineration of the waste feed while
achieving reduction in the level of pollutants in the exhaust gases
to acceptable levels.
The waste material which can be incinerated in the process of this
invention includes all types of solid and liquid propellants and
explosives. Illustrative solid propellants which can be incinerated
include single base propellant, double base propellant, triple base
propellant, high energy propellant, rocket casting powder, cast
propellant grains, rolled sheet propellants, nitrocellulose,
trinitrotoluene, inorganic oxidizers such as ammonium perchlorate,
ammonium nitrate; organic oxidizers such as HMX
(cyclotetramethylenetetranitraamine), RDX
(cyclotrimethylenetrinitraamine), and the like. Illustrative waste
liquid propellants and explosives which can be incinerated in the
process of this invention included nitrate esters such as
nitroglycerin, diethyleneglycol dinitrate, triethylene glycol
dinitrate, and the like.
When incinerating liquid propellants or explosives in accordance
with this invention it is necessary that the liquid propellant or
explosive be abosrbed by a particulate absorbent carbonaceous
combustible material such as sawdust. The explosive-wet or
propellant-wet carbonaceous combustible materials are considered
solid propellants or solid explosives for purposes of this
specification and claims. These particulate propellants or
explosives are admixed with water to form aqueous suspensions and
processed in accordance with the incineration process heretofore
described. In the step of forming the aqueous suspensions, normally
solid propellants which absorb propellant or explosive liquids can
be added. Thus, for example, it is oftentimes desirable to admix
nitrocellulose or single or double base propellant, in particulate
form, to nitroglycerin wet carbonaceous material.
In order to successfully operate the process of this invention it
is necessary to have the waste propellant or explosive material
reduced to a substantially uniform particle size. Small particle
sizes are needed because propellants and explosives burn rapidly
and propagate flame easily. In this case of normally solid, waste
propellant or explosives, the waste is ground under water for
safety purposes and the particle size of the resulting ground
particles should average less than about 0.25 inches and preferably
the average particle length or maximum dimension shall be less than
about 0.10 inches. In the case of normally liquid, explosives or
propellants, the explosive is absorbed in particulate carbonaceous
combustible material within the size envelope heretofore described.
The resulting particulate waste propellant or explosive is then
formed into a suspension by mixing the water-wet explosive with
water, as necessary, to form a suspension having a weight ratio of
water to waste propellant or explosive of from about 19:1 to about
1:1. It is generally preferred to employ a
water/propellant-explosive ratio of about 3:1. The suspension of
the small particles in water is pumped into the rotary kiln under
conditions to maintain turbulent flow within the feed lines.
Turbulent flow conditions in the feed lines is necessary for safety
purposes. The feed is then discharged into the rotary kiln for
incineration. Feed rate must be controlled so that all the
explosive or propellant waste is consumed within the incinerator.
If feed rate is excessive, unburned propellant can be discharged
with ash.
The temerature within the rotary kiln is maintained at between
1,200.degree.F. and 2,200.degree.F. In order to achieve low
concentrations of NO.sub.x it is preferred to operate the rotary
kiln at a temperature at about 1,500.degree.F. to about
1,800.degree.F. At temperatures of below 1,500.degree.F. and above
1,800.degree.F. the NO.sub.x concentration in the exhaust gases
from the incinerator is substantially increased. At temperatures
above about 2,000.degree.F., evaporation of the water portion of
the suspension of propellant or explosives and ignition of the
waste is more difficult to control which can result in incomplete
combustion of the propellant or explosive waste. The higher
temperature, i.e., above 2,000.degree.F., sometimes prevents the
thin layer of aqueous suspension from forming on the chamber wall,
allowing unburned propellant and explosive waste to be discharged
with the ash. Unburned waste in the ash is a safety hazard, since
propellant and explosive waste could ignite and burn outside the
rotary kiln.
In the operation of the process of this invention, the rotary kiln
is heated by burning of a fuel such as fuel oil, propane, natural
gas, or a substitute therefor. The burner fuel does effect the
combustion occurring within the rotary kiln. Thus, propane is a
preferable fuel to fuel oil to use to fire the rotary kiln because
the propane combustion products function as a reducing agent
thereby lowering the NO.sub.x content in the exhaust gases. It is
understood that the composition of exhaust gases will vary
depending on the composition of the waste material being
incinerated.
In the process of this invention the air provided to the
incinerator should be thoroughly mixed with the exhaust gases prior
to exit from the rotary chamber. Therefore, it is preferable to
fire the burner in the rotary kiln, countercurrent to the air flow
through the kiln. The amount of air in which the waste explosives
and propellant is burned should be as near the stoichiometric
amount as possible. The stoichiometric amount of air required for
each propellant or explosive waste can be readily calculated based
on the feed material to be burned.
The wet scrubber employed in the process of this invention is used
to reduce particulate matter and water soluble gases in the exhaust
stream. Wet scrubbing of the exhaust gases can be achieved by
passing the exhaust gas through a scrubbing liquid, for example, a
water spray or water bath. The exhaust gas can then pass to an
entrainment section to remove the water from the gas, while
contaminated scrubbing liquid is drained to the scrubbing
section.
* * * * *