JPS5827987B2 - Funmukahouhou Oyobi Sonosouchi - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION The invention also relates to the atomization of a combustible material and its combustion after said atomization.

Combustible materials contemplated by the present invention are gases, liquids, particulate solids, or liquids containing particulate solids that can be discharged or flowed at room temperature or temperatures up to 300°C.

For example, materials such as gaseous or liquid fuels will only burn completely when mixed with an oxygen-containing gas.

Burners for liquid fuel essentially include an atomization device.

This atomization device is generally fitted within a burner head which is located at the end of the burner body or tube.

The burner is a monolithic part of a more or less complex device containing suitable devices for mixing the atomized fuel and oxygen-containing gas and producing the desired flame.

Three types of atomization methods are utilized in known burners: atomization by auxiliary fluid, mechanical atomization by pressure of the fuel, and atomization by rotation of the cup.

Atomization with an auxiliary gas utilizes the energy liberated by expanding compressed air or steam under pressure for the diffusion of the fuel.

This diffusion is obtained by merging a jet of liquid fuel and a jet of auxiliary gas.

The atomization obtained in this way is very coarse, especially in the case of highly viscous fuels.

Moreover, the consumption of auxiliary fluids is extremely high, typically exceeding 10 kg of steam for 9 out of 100 industrial fuel oils.

Steam consumption of 15 to 20 kg per 100 kg of industrial fuel oil is common.

In burners with mechanical atomization by pressure, the fuel is injected tangentially into a cavity, where it undergoes a rapid rotational movement while moving toward the burner orifice.

The orifice is centrally located in a cap that covers the cavity and generates the burner jet.

At the exit or nozzle of the jet, the jet of liquid takes the form of a conical plate.

This type of atomization device can reduce the delivery amount by 120% to +20%.
It only makes possible fluctuations in .

Various improvements, particularly heavy oil return burners and dual-feed burners, can significantly increase operating flexibility.

Despite the complexity of these burners and their supply circuits, the maximum delivery rate is at most a 10:10 ratio.

All mechanical atomizing burners generate hot bodies that increase as the viscosity of the fuel increases.

The dimensions of the hot body also increase with the delivery volume.

Nozzles exposed to flame and furnace radiation are often blocked by coke formation.

Rotating cup burners are much less utilized than the previously mentioned burners.

A cup driven by compressed air or an electric motor 7 atomizes the fuel by centrifugal action.

From a technical point of view a satisfactory solution is provided to the problems inherent in the use of liquid fuels such as industrial fuel oil, while
While these solutions are imperfect from an economic point of view, they cannot similarly address the problems arising from the combustion of by-products that contain suspended solids and are much more viscous than normal fuel oils. do not have.

For example, known burners are not capable of atomizing some tars and burning them properly.

Either the burner will be blocked too early or the atomization of the fuel will be too coarse.

The object of the invention is to overcome this problem and thus make possible the combustion of very different types of fuel, requiring only a moderate consumption of auxiliary fluids and operating with respect to both the amount of fuel delivered and its material state. The aim is to increase the flexibility of

In the prior art for atomization with an auxiliary gas, the energy released by the expansion of the auxiliary gas is first of all used to create a gas jet, where this energy is converted into kinetic energy.

Then, in the impact generated between the gas jet and the liquid fuel jet, a portion of the kinetic energy of the two jets is used to overcome the adhesive forces of the liquid.

The efficiency of this method is low, since the mere impact of both jets uses only a small portion of the kinetic energy of both fluids to enable diffusion of the liquids.

Other prior art techniques involve generating an initial jet of the liquid by only partial expansion of an auxiliary gas, and forcing the mixture formed by the merging of the two jets to flow through a narrow passage or a series of narrow passages. This causes a further partial expansion and causes the liquid warm body to be subdivided anew within the passage by shear stress.

However, since most of the energy liberated under these conditions by expansion of the gas is dissipated in the form of heat, the consumption of auxiliary gas remains very significant in burners improved in this way.

Additionally, highly viscous fuel quickly clogs this type of tanker.

According to the present invention, the method for atomizing the combustible material comprises (a
) causing at least one stream of combustible material and at least one stream of auxiliary gas to flow through the extended region under pressure, and dividing and recombining the two streams over substantially the entire region; and (1)) causing the atomization of the combustible material in the region to be delayed by expansion of an auxiliary gas during frequent changes in rotational motion; adjusting the supply of the auxiliary gas and the combustible material into the atomization region to result in an atomized product whose volume is significantly larger than the volume occupied by the combustible material.

This method makes it possible, for example, to obtain a very fine diffusion of liquid fuel.

In this manner, the fuel stream can be mixed very intimately with the oxygen or oxygen-containing gas stream.

As a result, the production of unburnt material can be significantly reduced or avoided.

There is no critical limit determining the minimum value of this ratio.

The energy required to spread and propel a given delivery of liquid fuel is provided by the expansion of an auxiliary gas within the atomizer.

The use of a relatively small supply of auxiliary gas by injecting the auxiliary gas into the atomization device at high pressure, which on the other hand provides a high resistance to the flow of the fluid; It is likewise possible to use large delivery volumes of auxiliary gas which can be injected at low pressure into the interior.

However, for a given delivery amount of fuel, the amount of auxiliary gas supplied is too small even at a relatively increasing initial pressure, resulting in the formation of an emulsion in which the gas becomes the diffused phase or the formation of a mixed emulsion. brought about.

In either case this can result in the formation of an emulsion that does not mix well with the oxygen-containing gas.

In general, assuming that the pressure of the gas at the inlet of the atomizer is sufficient, the proportion of the gas at the outlet of the mixer is at least 20 to 30 times that of the liquid. The desired results of the present invention can be obtained by adjusting the amounts of gas and fuel delivered.

The amount of liquid fuel to be delivered can be arbitrarily small in relation to the amount of auxiliary gas to be delivered.

Indeed, one of the advantages of this method is that it is possible to reduce the fuel delivery rate to near zero, while maintaining a constant pressure of the gas at the inlet of the atomizer, and thus its delivery rate. It is in.

The atomization of very small delivery quantities of fuel is excellent, and when the auxiliary gas is compressed air, the subsequent combustion of atomized combustion is very satisfactory.

In principle, there is no maximum or minimum limit as to the pressure that can be used at the inlet of the atomization device.

In fact, as mentioned above, the required pressure is related to the gas delivery rate and the characteristics of the mixer.

In order to atomize a given delivery of fuel, pressures of about 2 bar or less may be used, provided that a moderately large amount of auxiliary gas is supplied and that the atomization device provides adequate resistance to fluid flow. I can do it.

In fact, at pressures higher than 3 bar and preferably higher than 5 bar, the fuel can be atomized by using a reasonable delivery of auxiliary air.

Although there is no upper limit on the usable pressure, there are no locations where extremely high pressures are used since the gas delivery rate must remain sufficiently high relative to the fuel delivery rate.

It is therefore reasonably possible to use pressures of 3 to 20 bar.

Preferably, the auxiliary gas is introduced into the inlet of the atomizer at a pressure of 5 to 10 bar.

For example, in order to burn viscous fuel or even more viscous industrial fuel oil, use an amount of auxiliary gas delivered such that the volume occupied by the gas at the outlet of the mixer is approximately 60 times or more the volume of the liquid. However, the fuel can be atomized by injecting the fuel and auxiliary gas at a pressure of about 6 bar into the inlet of a suitable atomization device, as described hereinafter, which is delivered to the furnace at atmospheric pressure.

The auxiliary fluid is a substance that is gaseous at the pressure and temperature at which it is used.

The auxiliary gas is preferably compressed air or steam under pressure, but many other gases can be used.

In particular, fuel gases such as methane can be employed.

Can be used in extremely small quantities. For example, to atomize 100 kg of industrial fuel oil, only 2 to 3 kg of steam is required.

Preferably, the pressure of the auxiliary gas at the inlet of the atomization device and thus its delivery rate is approximately constant.

Therefore, the amount of fuel delivered can be varied simply by acting on the fuel pressure at the inlet.

This method allows the delivery of atomized gas to be varied within unequal proportions.

The present invention allows multiple combustible materials to be used simultaneously or otherwise in the same device.

It will be appreciated that the combustible material can be heterogeneous and contain suspended, insoluble solid particles.

An example of a granular solid is pulverized coal.

Slurry of pulverized coal can also be used.

A particularly useful aspect of the invention exploits the possibility of using average- or extremely sticky materials, such as sticky petroleum byproduct tars, such as tars generated in petroleum refining steam cracking processes. At the point.

Additionally, it would be possible to dispose of sludge containing organic materials at Kijima.

Cleanup of municipal runoff and some industrial wastes involves separation of sludge containing organic materials.

This sludge is removed by sprinkling or ashing.

Ashing takes place in special furnaces.

Rotary furnaces are regularly used with staged combustion, and drying of the sludge takes place in the upper stage of the rotary furnace.

Thermal decomposition of organic materials cannot be avoided, and combustion occurs extremely slowly.

These furnaces produce nauseating smoke and require after-combustion to clean it.

The use of so-called fluidized hearth furnaces tends to become more common, especially for the treatment of wastewater produced in petroleum refining.

These furnaces have a number of advantages. These furnaces are not provided with any internal partitions or machinery.

These furnaces do not emit gaseous organic components and combustion within the furnace is complete.

Nevertheless, the operation of this type of incinerator is delicate, the operating costs are very high and the heat capacity is low.

The present invention allows incineration of sludge and substantially complete combustion of organic matter contained in the sludge.

The present invention makes it possible to incinerate ventable sludge obtained from industrial effluents, such as wastewater from paper mills, sugar mills, oil refineries, etc.

Therefore, the sludge from the sewage station can be burned.

The moisture content of the sludge is extremely high.

Even contaminated water can be directly incinerated using this method.

It is sufficient to use make-up fuel in connection with the delivery and composition of the sludge.

Gas or any liquid that can be discharged can be used as the supplementary fuel.

Natural gas, petroleum gas, LP gas, industrial fuel oil, etc. can be used.

In another aspect, the present invention provides a device for use in the atomization method and combustion method described above, which device comprises: (1) an atomization region; (11) a front chamber communicating with the atomization region; m) at least two supply inlets to the antechamber, at least one for said combustible material and at least the other for said auxiliary gas; (IV) for modifying the lateral profile of the atomized material exiting the area in use; In this case, the cross-section of the atomization region is generally cylindrical, and the inside of the atomization region has a generally cylindrical cross-section. A device is provided that is adapted to provide a complex shear effect and change in direction of rotation to the fluid flow.

A preferred form of the atomization region or atomization chamber is a known static mixer, i.e. of the type consisting of a cylindrical tube into which a suitable fixing device can be inserted with the effect of producing a combined shear and redirection of the fluid flowing through the tube. belongs to.

The mixer can in particular consist of a tube into which a gasket can be inserted.

This packing may be constructed from a laminate of elements having an appropriate shape.

Alternatively, the mixer may consist of a cylindrical tube into which a series of helical or static screw elements can be inserted.

A preferred form of atomization region is thus obtained which comprises a series of curved elements or vanes whose shape and arrangement are defined as follows.

(a) the width of each vane is very equal to the inner diameter of the region concerned, and the length of each vane is at least 1.2 of the inner diameter of the region;
It was made equal to 5 times.

(b) each vane is bent so as to impart, in use, to the fluid flowing through the region a rotational motion relative to the axis of the region;

(C) The shape of the vane is obtained from a rectangular plate having a width equal to the inside diameter of the tube by twisting the plate so that the short sides are rotated through an angle forming the long intermediate plane relative to each other. Shaped into shape.

(d) The long side of each vane rests on the inner surface of the region and each vane divides the lateral portion of the region into two.

(e) The vanes are positioned in such a way that the leading edge of each vane forms an angle with the trailing edge of the previous vane, except for the edge relative to the first vane above the mixer.

(f) the blades are secured within the area by any suitable device;

Furthermore, (a) the length of each blade is set to 1.3 to 3 times the inner diameter of the region; (1)) the angle formed between the blades by the leading edge and the rear edge of each blade is set to 1200 to 2400; , (e
) some blades bent in one direction, alternating with blades of approximately the same number and a total of 5 to 30 blades bent in the opposite direction; (d) except for the first blade on the upstream side; Preferably, the leading edge of each blade contacts and forms a 900 angle with the trailing edge of the previous blade.

There can be from 5 to 30 blades in the atomization area.

10 to 20 blades are preferred. The vanes can be fixed at a certain distance relative to each other.

Preferably, the leading edge of each vane, except for the first vane at the top of the mixer, contacts and forms a non-zero angle with the trailing edge of the previous vane.

This angle can be, for example, between 30° and 150°.

Preferably, this angle is approximately 90°.

Preferably, a static mixer is used which has approximately the same number of blades curved in both directions.

Both types of vanes can be placed anywhere.

Preferably, the blades are arranged in the same cluster, with clusters of blades bent in one direction and clusters of blades bent in the other direction alternately arranged.

The following arrangement, i.e. the twist angle of each blade is approximately 180
Particularly preferred is an arrangement in which adjacent vanes are twisted in opposite directions, the vanes are in contact with each other, and the edges in contact form an angle of about 90°.

Preferably, the vanes are fixed to each other by their points of contact.

This fixing can be effected in particular by soldering, welding or brazing.

The vanes thus assembled can be held stationary within the tube by any suitable device.

The lateral edge of the first vane above the tube is preferably welded, soldered or brazed inside a ring with the same internal diameter as the tube and supported on the tip of the tube.

This type of device allows removal of the mixer and replacement of the vanes.

Any knowledgeable engineer will know the characteristics of the mixer, regardless of the type of mixer to be used, and in particular, as fully explained previously, that the mixer will impede the flow of auxiliary gas with a suitable resistance. In connection with the delivery volume and the initial pressure of the gas, it would be possible to calculate the internal diameter of the tube, the length of the tube occupied by the fixing device inserted into the tube, etc.

Some static mixers impart rotational motion to the fluid flow through the tube.

If there is a significant swirl component of the flow in the tube below the last element of the mixer, the velocity of the fluid at the exit from the tube may be such that the opening angle of the jet is poorly matched to the furnace geometry or aerodynamic characteristics. It has a horizontal component.

In such cases, it may be desirable to insert a suitable device into the tube directly below the last element of the mixer to reduce or eliminate the swirl component of the flow.

These devices specifically consist of curved elements or vanes having bends and lengths to impart the necessary momentum to the fluid to reduce or eliminate the swirling component of the flow.

For example, if a mixer contains a series of adjacent vanes, and two successive vanes are twisted in opposite directions, this mixing can be achieved by connecting the last vane about 1/4 of its length. It is possible to modify the device.

The swirl component of the flow below the last vane of the mixer modified in this way is virtually eliminated.

Preferably, the curved element or vane is forced into the tube and the last vane downstream of the tube rests on the nozzle of which it forms a part.

This method of assembly has many advantages.

The vane will not flow out of the tube unless the weld is damaged.

The vanes, especially the last vane on the downstream side, are completely stationary, thus avoiding the need to weld the last vane to the tube.

In case of damage, the blades can be easily replaced.

A nozzle is fixed at the outlet of the mixer to impart a desired profile to the jet of atomized fuel and thus to the flame during subsequent combustion of the atomized fuel.

The nozzle can be bored with one or more cylindrical or conical holes.

The diameter of the hole is large enough so that the fluid flow experiences only a small pressure loss as it passes through the hole.

If the nozzle is a single cylindrical perforated nozzle, suitably its diameter is 0.5 to 0.9 times, preferably 0.6 to 0.8 times, the inner diameter of the atomization area. .

If the nozzle has a plurality of holes, they are suitably arranged so that the side profile produces a conical jet.

The effect of the nozzle is to give the jet of atomized fuel and auxiliary gas the desired profile.

The nozzle also significantly improves the homogeneity of the fuel distribution within the auxiliary gas.

This result could not have been foreseen in any way.

Finally, the nozzle is conveniently used as a stop to hold the curved element in the atomization tube.

The fluid flow experiences a pressure loss as it flows through the atomization device and a further pressure loss as it flows through the nozzle.

According to a preferred feature of the invention, the atomization device and the nozzle t-3 cooperate in such a manner that the pressure losses caused by the nozzle t-3 are relatively small.

It is preferable to design the mixing amount and nozzle so that the pressure loss due to the nozzle is less than 80%, or even better, less than 50% of the total pressure loss.

The flow rate of the fluid within the atomization device has a decisive influence on the atomization of the fuel.

The atomization device is designed to provide considerable turbulence in the fluid flow with the desired delivery volume.

According to a preferred embodiment of the invention, the characteristics of the atomization device, in particular the internal diameter of the tube and the length occupied by the parts inserted into the tube, are such that the auxiliary gas is at a pressure of 3 bar between the inlet and the outlet of the atomization device. with a pressure drop of more than or preferably at least 50 to 15 times the volume of fluid flowing into the
The value should be such that it occupies 0 times the volume.

Under the pressure and delivery volume conditions thus determined, the flow rate of the fluid in the atomization device is 10rrL.
It is also preferred that the characteristics of the atomization device be designed such that the speed is greater than or equal to 25 m/sec, or even better, greater than or equal to 25 m/sec.

In all cases, it is necessary to make the dead space downstream of the last element in the atomization region as narrow as possible to prevent coalescence of the atomized fluid.

Therefore, either the shortened last curved element is placed at the outlet of the chamber or the last complete element abuts the nozzle.

Some embodiments of the apparatus for use in the atomization and combustion method of the invention will now be described, by way of non-limiting example, with reference to the accompanying drawings.

Referring to FIG. 1, the device includes an inner supply tube 1 extending into the forechamber 3 through an injection orifice 9. Referring to FIG.

A concentric tube 2 with an inlet 20 also leads to the anterior chamber 3.

The anterior chamber 3 has 15 curved elements 4 and 1 curved elements inside.
leading to an atomization region containing a tube 6 in which several semi-drying elements 5 can be accommodated.

The inner diameter of the tube 6 is 14 mm.

The length of each curved element 4 is 20 mm and is twisted through an angle of 1800 alternately to the left and to the right.

The elements are fitted into the wall of the tube 6 and are brazed or otherwise fixed to each other at their contact points.
At the point of contact, the contact edges are approximately 900 degrees apart from each other.

The first of the curved elements 4 is a ring 8 that is fixed to the tube 6.
It is fixed to .

The length of the last bent half-element 5 is reduced, being approximately 3/4 of the length of the bent element 4, with a twist angle of approximately 135°.

The tip of the tube 6 is conical so that a conical spray can be obtained.

Referring to FIG. 2, the basic structure is very similar to that of FIG. 1, and like parts have the same reference numerals.

However, a modification has been made to the outlet portion of the atomization region.

The curved element 4 ends with a complete element and not with a shortened semi-circular element 5.

At the tip of the tube 6 there is a nozzle 10 which determines the shape of the spray exiting the atomization region and retains the curved element in the tube when it begins to be ejected for any reason. It is a work of art in the form of .

In FIG. 3, the nozzle /l/10 is a member fixed to the end of the tube 6. In FIG.

The inner girth of the nozzle is frustoconically shaped with an angle α between 600 and 120°.

In FIG. 4, the nozzle 10 is drilled with several cylindrical holes 21 distributed in a conical manner to produce a conical spray with an angle of inclination β.

To eliminate wasted space, the nozzle 10 is preferably provided with an inwardly projecting portion 22.

Referring to FIG. 5, the device can be equipped with a device for changing the injection orifice 9.

The changing device includes a needle valve stem 13, 14 which is movable toward and away from a corresponding valve seat in the injection orifice 9.

Finally, referring to FIG. 6, a modification is made to provide another supply population section such as 24 (-).

Furthermore, the bent elements 4 have been replaced by a first set 26a, the length of each element of which is equal to that of the immediately following element in the 7-piece 26b. It's about 10 times more than that.

The examples below illustrate the method according to the invention in a non-limiting sense.

Example 1 The apparatus described with reference to FIG. 1 was employed.

The combustible material used was a hydrocarbon tar with the following properties:

At 15'C 1.131 becomes insoluble 17.5%
Density of butane at 50℃ 975 cst Insoluble -\ 43.2
% density xane 100℃ 31 cst carbon 87.8%
Viscosity residual carbon 20.5% Hydrogen 7.1% (Conrad Non U Sulfur 5.1% Tar is 1
Preheated to 40 °C and heated at a pressure of 8 to 15 bar.
00 to 900 kg/hour.

The auxiliary gas was steam fed at a constant pressure of 6 bar and a feed rate of 30 ky/h.

After exiting the atomization zone, the atomized components were combusted in an industrial furnace.

A white flame occurred without unpleasant smoke.

This is the main advantage, since it was previously not possible to burn this type of hydrocarbon tar without producing black smoke.

FIG. 7 of the accompanying drawings is a graph showing the amount of tar added to the burner as a function of its pressure.

The tar pressure, which can be measured in bars upstream of the inner feed pipe 1, is plotted on the abscissa.

The corresponding feed rate of tar in kg/h is plotted on the ordinate.

The vapor pressure measured upstream of the concentric tube 2 is constant and equal to 6 bar.

In this graph, curve A represents the tar delivery obtained with a device according to the invention with an injection orifice 9 of 2.5 diameter.

Curve B represents the delivery amount obtained when the diameter is set to 3.5 mm.

One test was conducted in which the same tar was burned under the same conditions using a conventional injection method and atomized with an auxiliary fluid.

This conventional injection system was the same as that shown in FIG. 1, except that no device was inserted into the tube 6 and the injection orifice 90 had a diameter of 2.5 mm.

Regardless of the pressure and delivery rate of tar and steam applied to the burner, atomization was incomplete and the resulting flame emitted black smoke.

Example 2 The apparatus shown in the attached FIG. 6 was used to burn sludge produced from petroleum refining waste liquid in a furnace.

The length of the tube 6 is 3.90 mm and the inner diameter is 14 mm.

Inside this tube, there are 18 drawn elements 26a with a length of 200 mm, and a series of bent elements 26b with a length of 20 mrlL.
15 were inserted.

The leading and trailing edges of each element formed a 180° angle.

Elements twisted in one direction of rotation and elements twisted in the opposite direction of rotation were provided alternately.

The sludge obtained from the residual liquid of petroleum refining was atomized by this apparatus and then combusted.

) This sludge contains 65% water and 28% organic material.
%, solid particles 7%.

This sludge was fed into the inner feed pipe 1.

A make-up fuel was used which was an industrial fuel oil with a viscosity of 200 cat at 50°C.

This fuel oil was preheated to 140° C. and supplied to the concentric tube 2.

To ensure atomization and propulsion of the sludge and fuel oil, an auxiliary gas in the form of steam is used at a pressure of 6 bar and the tube 24
supplied within.

The delivered amount was as follows.

The sludge contained 700 kg/hour of fuel oil, 200 kg/hour of steam, and 50 kg/hour of steam.The fuel oil and organic materials contained in the sludge were completely combusted.

Example 3 The same operation was carried out to burn a sludge containing 20% water, 70% liquid organic material and 10% solid particles.

As in Example 2, this sludge was obtained from petroleum refinery effluent.

The auxiliary gas was steam at a pressure of 6 bar.

The delivered amount was as follows.

Sludge is 700 kg/hour 50kg of steam at 1 hour No supplementary fuel was required.

The sludge was completely burned.

[Brief explanation of drawings]

FIG. 1 is a longitudinal cross-sectional view of the device. FIG. 2 is a longitudinal cross-sectional view of another device. 3 and 4 show a modification of the outlet section of the device shown in FIG. 2. FIG. FIG. 5 shows a modification of the device of FIG. 2 in which the injection orifice is changed. FIG. 6 shows another modification of the device of FIG. FIG. 7 is a graph of the relationship between the amount of tar supplied and its pressure. 1...Inner supply pipe, 2...Concentric pipe,
3...Anterior chamber, 4...Curved element, 5
...Bent half element, 6...Pipe, 7,
8...Ring, 9...Injection orifice, 10°゛°°°°nozzle, IL13, 14...
・Needle valve stem, 20... Population department, 21...
...Cylindrical hole, 22...Protruding portion, 23,2
4...Tube, 26a. 26b...Set.

Claims (1)

[Claims] 1. An apparatus for atomizing a flowable combustible material, comprising: (1) an elongated region 6; (11) a front chamber 3 communicating with the elongated region;
at least two concentric supply ports 1, 20 for supplying fluid to the region 6 through the antechamber 3 in a substantially non-impacted, non-atomized state, at least one said supply inlet being said combustible at least one other said supply inlet is for an auxiliary gas; (1v) an outlet device 5 arranged adjacent to the outlet of the region 6 for deforming the profile of the atomized material; , 10, and further comprising: the elongate region having a generally cylindrical cross-section and having therein devices 4゜26a > 26b which exert a substantial resistance to the flow, so as to provide a number of shearing effects on the flow. , change the direction of rotation, and exit device 5 along almost the entire length of region 6.
, 10 homogeneously disperses atomized combustible material.