CN86108138A - Slagging conbustion system - Google Patents
Slagging conbustion system Download PDFInfo
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- CN86108138A CN86108138A CN 86108138 CN86108138A CN86108138A CN 86108138 A CN86108138 A CN 86108138A CN 86108138 CN86108138 CN 86108138 CN 86108138 A CN86108138 A CN 86108138A CN 86108138 A CN86108138 A CN 86108138A
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A kind of slagging conbustion system that is applicable to boiler and industrial furnace, it has a main combustion chamber, and fuel is lower than the burning of stoicheiometry ground and gets rid of most ashes therein.Combustion product flows to a dual firing chamber, and gets rid of more ashes.Flow to the corresponding hot equipment of using then, as boiler.Adding additional oxidant at this place's combustion product finally burns.The speed of fuel and oxidant and mass flowrate can independently be controlled, make nitrogen oxide minimum simultaneously thereby burning condition can be adjusted to, isolated non-combustion material such as slag are maximum, avoid being with oil smoke, guarantee flameholding, produce that to contain the abundant gas products of carbon monoxide and hydrogen maximum.
Description
Traditional burning boiler factory and industrial furnace be reaction zone internal combustion coal in stove, is high enough to keep slag in its melt temperature in this reaction zone internal combustion temperature.They burn under greater than 1 situation at total stoicheiometry usually, and this just causes a large amount of nitrogen oxide and oxysulfide to generate, and cause quite high particulate discharging to enter in the atmosphere.The energy release ratio of these stove unit volumes is lower, and relies on the use refractory material to prevent the slag ablation.They are usually with the operation of very low power density, for the composition of carbon in the fuel that burnouts, collect remaining slag, and extract energy from flame, need a large amount of " fire-box ".
Recent years, oil price has improved about 9 times, and many boilers power plant and industrial furnace are subjected to the strike of price pressure.For example the sodium carbonate stone kiln requires a large amount of heat energy, and the operator of these industrial technologies is used for equipment with great amount of investment, considers the price of present oil and natural gas, is infeasible economically.These boilers and industry pot are changed into burning coal rather than scoria oil or natural gas, a large amount of energy savings costs of meeting, this often can be avoided factory to close, avoided abandoning investment, of kilowatt of of designing of and avoids the unemployment in the society.But be to use oil or natural gas and change fire coal in the boiler of thousands and building and exist some to think unsurmountable difficulty all the time originally:flying dust that produces from usual coal combustion and cinder can cover on the water pipe, and boiler efficiency is descended; Oxysulfide (Sox) and (or) discharging of nitrogen-containing oxide (Nox) be not only by society unacceptable, and, under existing clean air regulation, usually be forbidden in urban district and area, half urban district, the boiler power plant is usually located at these areas.Usually, the free space that coaling facilities and combustion apparatus be installed is subjected to strictness and places restrictions on.And be that the boiler that uses oil or natural gas design is not used in the device of collecting and handling slag usually originally.
Therefore, our society is for and industrial furnace conversion (remodeling) becomes to be suitable for coal-fired technology and device has caused social and economic obvious demand existing boiler.Any this kind device of being accepted from economy, technology and environmental protection viewpoint should satisfy following requirement:
The power density height-unit cube Foot volume approximately per hour is 1.0 mmbtus/hour (Btu/hour) in main combustion chamber.
Nox is low-be dispersed in the atmosphere gas all the time as-ground is less than 45,000 volume ratios (ppmV) very much, and preferably less than 25,000 volume ratios very much.
Sox is low-be lower than the standard that is reached so far with traditional combustion chamber substantially, and preferably make in the flue gas sulfide content be reduced to percent 50 to about 90.
Can remove non-combustion material-before the gas product is transported to terminal applies stove or boiler, from the burning gases product, collect and remove the non-combustion content of organics of fuel of 70%-90% according to special instructions for use;
The transfer of carbon-before the gas product enters boiler or other heat utilization equipment, basically whole carbon are transformed into oxycarbide,
Durability-protection chamber wall, make wall harmful corrosion and (or) ablating remains on commercial going up in the acceptable time limit;
The gaseous product flow of the thermal efficiency-be transported to end use application equipment has the chemical potential about carbon-containing fuel 85-90%.But these energy the pick ofs as perceive heat and part to be included in the gaseous product and the carbon monoxide of very fast burning and hydrocarbon form all are transported in the terminal applies equipment.
The invention provides the device that satisfies above-mentioned requirements.
For reference, here the United States Patent (USP) of quoting 4,217,132 that belongs to people such as Burge has been narrated the device that comprises the carbon-containing fuel of non-combustion inorganic matter component in order to burning, separate these components as liquid slag, and carry hot combustion product flow to a certain heat energy utilization equipment, such as in the boiler.In people's such as Burge device, solid carbon fuel (for example coal dust) is injected in a certain combustion chamber, and meanwhile oxidizer flow (for example preheated air) tangentially is input in the combustion chamber to produce the high-speed eddy condition: this condition is suitable for by action of centrifugal force most of liquid slags being driven to the combustion chamber inwall.4,217, the device of narrating in 132 patents is a first generation high power density slag tap combustion device.The present invention relates to the improvement of slag tap combustion device, this improvement results from extensive studies and development, comprising be identified as revise original design and the Industrial Boiler of building and electric power industry boiler can use oil and (or) the peculiar requirement of natural gas.Here our device of being narrated is the disclosed the sort of usual classes that belong to together of people such as a kind of slag tap combustion device and Burge.Our device comprises some improvement, and as far as our knowledge goes, it is a kind of unique outstanding technology, simultaneously, get rid of whole slags basically, controlled Nox and Sox emission, and unburned carbon and other particulate have been avoided carrying secretly, and, have commercial acceptable durability, and retrofited to such an extent that be small enough to enter the common available confined space in the industry of commercial scale and the government utility power plant with high-efficiency operation.
According to the present invention, a kind of apparatus and method of compactness are provided, in order to burning carbonaceous effectively particulate matter under the situation of per unit volume high energy output, and get rid of non-comburant to possible top, simultaneously, it is minimum that nitrogen oxide is generated, and got rid of the most sulfur content of fuel.
Our device integrates, and comprises the precombustion chamber with first axle; Main combustion chamber with second vertical with first axle substantially axis; The deflector that has aperture as the keyhole at described combustor exit end; In order to from combustion product, to reclaim the forced air-ventilating system of slag; Remove the device of molten slag, gaseous products is transported to the device of terminal applies; When gaseous products substantially during the incoming terminal device in order to add the device of supplemental oxidant in the gaseous products.
In a preferred embodiment, precombustion chamber comprises the first Cylinder oxidant addition room, and it is determined by this precombustion chamber end wall with a certain distance from the first air damper plate with holes of this end wall.It comprises equally in order to oxidant tangentially is input to the device of the first oxidant addition room.First combustion zone extends to the second oxidant input area along axis from described deflector, it comprises a forced air-ventilating system that is communicated with pipeline, pipeline receives the effluent of first combustion zone in the end, described pipeline comprises in order to import second oxidizer flow so that the device that mixes mutually with the effluent of first combustion zone.Roughly extend to the position, aperture of first deflector with holes from the end wall of precombustion chamber in order to the nozzle unit of carrying granular fuel.This nozzle unit be suitable for particle carbon containing thing at least with first axle first combustion zone that is ejected at 45 approximately.The described second oxidant input area terminates in the pipeline that extends to main combustion chamber, and it is connected in the rectangular aperture in abutting connection with main burning chamber wall, and it is in order tangentially to import oxidant and combustion product from precombustion chamber that rectangular aperture is set.The axis of precombustion chamber and horizontal line configuration are enough to make all precombustion chamber products inflow main chambers basically at an angle.
In order to carry the particle carbonaceous material, fuel injector extend into main combustion chamber from its end wall.
Main combustion chamber is provided with internal face, and the slag layer that is produced by the burning particles carbonaceous material keeps thereon, and the set oxidant inlet that stretches into main combustion chamber is divided into two plumes with the effluent of precombustion chamber: one is towards the top, and another strand is towards outlet side.This precombustion chamber is preferably in the rectangular aperture place and comprises an air damper, flows into the flow velocity of main combustion chamber with control, and has nothing to do with rate of discharge, thereby tangential inflow velocity is remained in a certain predetermined scope.
Combustion product leaves main combustion chamber, passes through the aperture as the keyhole on the deflector with holes in the mode of high-speed eddy.Simultaneously, the liquid slag slotted portion of downward extension of hole of button of flowing through.So these combustion products flow into expanding chamber from main combustion chamber, gaseous products expands therein, thereby eddy velocity is reduced.Therefore, separate bulk slag and the combustion product of little slag in expanding chamber, rely on gravity to flow in the slag treatment servicing unit.Combustion product to the upper reaches, is transported to terminal applies equipment with lower speed then, such as boiler or industrial furnace.When these gases arrive our device and during the interface between the terminal applies equipment, combustion product is added supplemental oxidant, its quantity is enough to make still unburned so far component in the air-flow, and (as carbon monoxide, oil smoke and (or) hydrogen) are finished oxidation.
In operation, oxidant is transported to first mixing chamber of premix burner, and forms the aperture of leaving first deflector with holes with eddy current.This oxidant mixes mutually with about 10-25% of the whole particle carbonaceous materials that join this device.The oxidant content that is transported to this mixing chamber generally is to be enough to make whole fuel of supplying with premix burner to reach the stoicheiometry burning.This combustion product is diluted by second oxidant stream, flow out thing to form dense oxidant, for example be equivalent to premix burner and approximately be 2 times to 5 times stoicheiometry, be suitable for being injected to main combustion chamber, and therein as oxidizer source, in order to the carbon-containing fuel of the initial input of burning.The balance of particle carbonaceous material is approximately with 45 ° to 90 ° angle (with respect to the axis of main combustion chamber) fuel to be supplied with main combustion chamber by fuel injection device to reach, with flow out thing from the dense oxidant of precombustion chamber and mix mutually, this effluent is transferred with about 1200 to 2000 temperature.Burning in the main combustion chamber is that whole oxidants of utilize supplying with main combustion chamber carry out to be lower than the stoicheiometry mode, approximately is in the combustion fuel in 0.7 to 0.9 scope of the required stoicheiometry amount of whole combustibles.In main combustion chamber, burning occurs in all non-combustion things basically and changes into substantially on the stage of molten slag, because the rotation effect of velocity field in the main combustion chamber, slag is thrown on the wall of main combustion chamber by centrifugal force, and gathers on it as top layer slag fused lamination.In quiet rum, slag flows to the deflector with holes of main combustion chamber, through slotted opening, flows to slag collection device.The hot oxidant inflow that comes precombustion chamber is for stoping near the slag that gathers condensation the oxidant stream hand-hole to be good.Perhaps the more important thing is that by the heat radiation of combustion product, it has kept hot environment, thereby guarantee to promote and stablize the fuel combustion of adjacent fuel injector assembly, and guarantee that the carbon of fuel particle 85%-90% before arriving main burning chamber wall transforms.Combustion product is gone into expanding chamber through the deflector orifice flow, and wherein large scale residue slag separated with combustion product before being transported to the terminal applies device.The oxidant that replenishes is being transported in the combustion product with terminal applies equipment intersection, therefore, when gaseous products enters terminal applies equipment, has just finished Co and H in the main combustion chamber of low stoicheiometry
2Final burning.
Especially in a preferred embodiment of the invention, this precombustion chamber has 3/1 length/diameter ratio; And main combustion chamber has the length/diameter ratio of 1.5-2/1; Expanding chamber has 1/1 length/diameter ratio; Main combustion chamber deflector area is than in the scope that is in 2/1-4/1.As mentioned above, supply with whole oxygen of main combustion chamber preferably for contained whole carbon in the fuel are become about the 0.7-0.8 of carbon dioxide and water aequum with hydrocarbon completing combustion.Therefore, the combustion product that leaves main combustion chamber is comprising a large amount of carbon monoxide and hydrogen, thereby is suitable in terminal applies equipment, for example in boiler or industrial furnace, and further completing combustion.Preferred carbon containing feed is a coal.Can be transported to main combustion chamber at the steering handle sulfur absorbing agent of back reaction owner body stream, form so that can adsorb the sulfur-bearing of carbon-containing fuel.
Fig. 1 is the perspective layout that absorbs furnace apparatus about effluent.
Fig. 2 illustrates premix burner.
Fig. 3 illustrates main burner, slag separation and collection, combustion product pipeline and second burner.
The reactant in Fig. 4 detailed icon master's burner and the expanding chamber and the interaction of product.
Fig. 5 diagram is in order to provide the structure arrangement of heat protection to device wall.
Fig. 6 represents to be used for the thin portion of the pipe-diaphragm structure of apparatus container wall.
Fig. 7 and Fig. 7 A represent the thermal sleeve injector assembly.
Fig. 8 and Fig. 8 A represent to be suitable for using the fuel injector assembly of suspension.
Fig. 9 is illustrated in the cutaway view of the assembled assembly of premix burner and main burner junction.
According to system applies provided by the present invention special apparatus and method burning particles carbonaceous materials fully, and on possible extent, remove the non-combustion thing of solid, make the generation nitrogen oxide minimum simultaneously, a kind of high efficiency device of removing sulfide is provided, and before gaseous products is transported to relevant heat energy utilization equipment, collects and remove 70% to 90% molten slag.
These are improved successfully by adopting following method and apparatus to finish: their allotment particle carbonaceous materials and be used to the oxidant of these materials that burns, so that in fluid dynamic flow velocity field, light rapidly and react.Used device comprises four mechanical components that link together: premix burner, main burner, slag collection device and the pipeline that has whole second burner, whole device is compact, and the energy release rate of the per unit volume of device is more much bigger than what can reach in traditional coal-fired stove.
Terminology used here " particle carbon-containing fuel ", we refer to the carbonaceous material that comprises non-combustion mineral, it can be used as the fuel that is in the state of dusting, perhaps be suspended in the delivery fluid, promptly supply wherein typical carbonaceous material and comprise that coal, charcoal, solid waste reclaim organic residue of operation extraction, can be dispersed in tar in the liquid or the like as suspension as free particle.Whole needed be that carbonaceous material is that part is oxidable at least in main combustion chamber, and as being suitable for being dispersed in the combustion chamber at the dispersed particle of delivery in the liquid.This fuel is coal dust generally speaking.
Term " oxidant " is meant air or oxygen-enriched air
" delivery fluid " is meant gas or liquid, they can be inertia or oxidant.Oxidant is best carrier gas, and water is best delivery liquid.
The preliminary treatment of oxidant is to finish in the Cylinder premix burner of short compactness, and whole first oxidants are sent to the there.First oxidant be used for burning about 10%-25% of whole carbon containing feed is to form first product.The second portion of oxidant enters premix burner and first product is mixed to form the dense oxidizer flow of heat, and their in check modes are imported into main burner.Dense oxidizer flow also carries all remaining premix burner fuel and non-combustion thing, comprises the carbonaceous particles of still burning that is diffused in its whole volume.As a result, the premix burner outlet temperature can be in about 1200-2000 scopes.
Particle carbonaceous material in the premix burner is transported in the gas flow rate field of the strong rotation that is in the premix burner top as solid in the ordinary course of things.Conveying is to be undertaken by the injector that install at a center, and injector produces a kind of taper particle carbonaceous material stream, is mixed in the rotation velocity field of oxidant.The rotation velocity field of oxidant and the product of generation have produced a strong hot gas recirculating zone, in case obtain to light just burning particles.When air was transferred under about 300 °-500 or higher temperature as oxidant and this air, the geometry of premix burner provided self-sustaining burning.Premix burner preferably be configured to horizontal angle be 22.5 degree, make whole air-flows flow to rectangle outlet downwards, to guarantee not have solid or liquid slag left in premix burner from the top along this angle.The total stoicheiometry of premix burner approximately is for making 2-5 that the fuel carbon content that is transported to premix burner obtains complete oxidation requisite oxygen tolerance doubly.This stoicheiometry is to control by the flow of regulating particle carbonaceous material inleting oxidant stream, to keep above-mentioned outlet temperature.
The oxidant that results from reactant in the preheater and heating flows in the main burner of Cylinder geometry by the rectangle outlet.This premix burner effluent air-flow is oriented in a tangential direction with the main combustion chamber inwall substantially and is transferred.The rectangle outlet size of premix burner is decision like this, makes the size that is parallel to main burner axis greater than the size perpendicular to main burner axis.Length/height ratio is best with 2.5/1.The center line of rectangle outlet preferably and the longitudinal axis of premix burner be arranged in a straight line, and be configured in the upper reaches of main combustion chamber longitudinal axis mid point, promptly about from the top to the 1/3-1/2 place of the deflector distance with holes of main combustion chamber.
Because the rectangle outlet of premix burner is set in a manner described, and the premix burner effluent has just caused eddy motion, passes to the air-flow in the main burner.We have found that, are positioned at the gas flow adjusting flange of premix burner rectangle outlet area by means of use, are controlled at the magnitudes of 330 Foot/seconds by the muzzle velocity with premix burner, just can reach satisfied burning in the main burner fuel delivery rate scope of broadness.Above-mentioned facility also makes described effluent be divided into two almost equal air-flows: to the top vortex, and another air-flow is made total spiral along its main burner wall to its outlet and is moved along its wall for air-flow.The axial component that flows to the eddy current on top has lower speed, is in 50 Foot/second-time.This air-flow inwardly changes at main burner top end wall place, yet towards the axially anti-stream of main burner outlet, flows with vortex or helical trajectory all the time.In main right device exit one deflector is set, it is configured to the axis perpendicular to main burner, and it has a hole that roughly is in the center.
The solid carbon main bulk of fuel is imported into main burner by a fuel injector assembly, roughly is in the center on top.This assembly makes particle carbon containing thing as the solid in gas or the liquid-carrier, is imported in the vortex gas velocity field with the pattern of taper flow.This injector assembly puts in main combustion chamber and goes up flow point a little up to premix burner outlet rectangular aperture from the top.
As mentioned above, the oxidant that enters main combustion chamber flows into thing and is divided into two strands of air-flows, makes about 50% premix burner effluent flow to the top, and there, initial lighting appears in the dense fuel reaction district, and the total stoicheiometry of top zone is approximately 0.4-0.5.The oxidant stream of input is to the main burner port of export.Taper fuel stream fully and rapidly mixes fuel, oxidant and fuel Products with the interaction in high speed vortex flow flow field.Subsequently, can become more obvious by detailed narration, this just for accurately with control stoicheiometry in the several sections of combustion zone highly beneficially, composition and acceleration have been created condition, and these characteristics are important for reaching the purpose and the requirement that propose above.The main part of fuel combustible was burnouted in the stage of the oxidant flow velocity field of passing heating, emitted energy with the form of reaction heat, and further heated total combustion product.Particle in the free flight flows to the port of export of main combustion chamber usually by helical trajectory.
In service usually, a spot of, preferably be not more than the form of about 12% phosphorus content of fuel with unburned carbon, promptly general flammable charcoal reaches the wall of main burner, and it continues to be burnouted again.The liquid slag layer flows to port of export deflector along main burning chamber wall with spiral form with the tractive force and the gravity of aerodynamic force layer.Usually, the burning of fuel is by the heating of passing through that rapid heating fuel particle just takes place the organic matter of volatilization to be gasified, and it may be in the magnitude of total combustible weight 50-80%.Its remainder mainly is awing basically as carbon granule and burned.
The dense fuel that forms in main burner top when keeping eddy motion, generally speaking flows to port of export deflector.Initial and top flow point from premix burner effluent that part of that flows to port of export deflector outer zone with eddying motion be forced to during by deflector inside, thereby with fuel and mixing of dense fuel gas and reaction, so that total stoicheiometry of main burner is approximately brought up to the scope of 0.7-0.9, preferably be approximately 0.7-0.8, and produce one as the output product of main burner and contain dense Co and H
2Hot combustion product stream, from this combustion product, most of non-combustion thing is excluded as liquid slag.
In main burner, by the strong secondary back along main burner center line, inner mixing and reaction are further strengthened, and this refluxes along center line, total top of shifting to main burner.This backflow is vortex equally, therefore, be screw type basically, but its axial component is the top of shifting to main burner.It has produced a dense fuel core in main combustion chamber.The average diameter of this backflow core and mass rate of flow are to select institute to determine and control by the pod apertures diameter of premix burner exit velocity and main combustion chamber.Preferably the premix burner muzzle velocity was about for 330 Foot/seconds, and best deflector orifice diameter and main combustion chamber diameter ratio are approximately 0.5 or big again, in the case, produce desirable secondary back, thereby increase is to the control with whole burning of lighting in the main combustion chamber.
Approximately inside from the radius of pod apertures, tangential velocity is reduced to zero basically in the centerline of main burner.This vortex velocity field radially quickens the fuel particle in their early stage consumption processes, makes the particle that burnouts simultaneously, drops to about 10 microns, is collected in the main burner as slag.
The fuel injector assembly of main combustion chamber is designed to be convenient to slag flows to particle carbon containing thing along its outer surface from the top spray site.This very hot (slag) outer surface on injector assembly has played the flame retainer, lights rapidly when guaranteeing that the fuel particle leaves injector, thereby has promoted and reach active combustion to greatest extent.Be in operation, the slag that flows along injector is producing disengaging nearby from the solid particle fuel spray site, and is that strong point center radiation and the dense fuel gas of lighting top formation have been created condition.
When adopting gaseous state delivery fluid, granular fuel is imported main burner with intensive phase mode of movement, and wherein solid and delivery fluid weight are in about 3: 1 to 10: 1 scope than in the rated power scope.When fuel was supplied with as liquid suspension, the weight ratio of fuel and delivery fluid can adopt about 2: 1 or higher.The combustion product heat of main combustion chamber is to being enough to keep the molten slag layer temperature to be higher than the slag fusion temperature.Therefore, slag flows freely along main burning chamber wall.The cooling agent stream of metallic walls is controlled.The granular fuel mass rate of flow is controlled, is controlled from the mass rate of flow and the speed of the oxidant of premix burner.Collaborative these independently variablees of regulating remain in a certain scope primary zone temperature, thereby have avoided the slag vaporization, keep a protectiveness slag layer on the metal wall, and liquid slag continue to flow through that slag layer, flows to slag cleaning sub-unit.Be convenient to Nox is controlled in the dense fuel combustion of top zone and core and be lower than environmentally acceptable level.
Best, main burning chamber wall is made of water-cooled, pipe-diaphragm structure.Pipe-diaphragm structure is also equipped slag and is kept pillar.Chamber wall is looked at first with the refractory material that consumes, and adopts the standard thickness of about 0.5 inch, and protects with pillar.Be in operation, the refractory material that is adopted makes slag adhere to this refractory material tightly, form a thin condensate layer, and remaining slag flows through this condensation slag layer.After long-time running, this refractory material is washed away, and promptly loses.But the very fast slag that is condensed of the very serious part that is flushed away replaces.Refractory material is with condensation and this combination slag fused layer, provides heat and chemoproection to the pipe-baffle wall structure of welding.Local slag stream provides from replenishing for the refractory material of any loss.The structure of cooling circuit provides about 325 °-600 temperature for metallic walls, and it has prevented condensing of acid compound, thereby makes corrosion minimum.With regard to some coal, as sequence number for-co-pending patent application (summary 31-0143) in be described in detail owing to provide assurance for collecting sulfide on the spot, the slag fusion temperature can further reduce.
The longitudinal axis of main combustion chamber preferably is configured to approximately become with horizontal line 15 ° angle, to guarantee to produce slag stream completely, avoids at bottom, combustion chamber accumulation residue.This slag normally is with to port of export deflector by spiral way along the wall of main burner.Along with slag stream forms along wall, because gravity has surpassed gas dynamical power, most of slag flows to the bottom of main burner.The slag that collect the bottom flows to deflector.Deflector has hole and that a center is provided with extends to main burner diapire from this hole rectangle, keyhole-shaped opening.The narrow groove of this rectangle can make slag stream pass the deflector of contiguous combustion chamber diapire.When using 200 order coals, about 80-95% of the non-combustion thing content of coal is removed from gaseous product flow, is collected as liquid slag, and is removed by being arranged on the dirty slag of deflector that the has hole of button sub-unit of slagging tap.
Nominally owing to adopted main burner length/diameter than being 2/1; Deflector diameter and main combustion chamber diameter ratio are 0.5 or greater than 0.5, and with regard to 200 order coals, are the free flight burning basically, as in this narration, in fact do not lose (carrying secretly) unburned carbon in the main combustion chamber outside.The slag that preferably flows into Cylinder from the combustion product and the liquid slag of main combustion chamber reclaims the chamber.The slag retracting device comprises a length/diameter than little chamber, and its diameter approximates the diameter of main combustion chamber greatly.In its bottom is a slag scum hole.At its top is shape hole, a garden, has certain excessive geometry, and it is perpendicular with the center line of slag recovery chamber basically.Reclaim the hole at top, chamber from slag, extend an air-flow discharge line, go so that dense fuel gas continued transported in the final application apparatus.This pipeline leaves the slag recovery area with subvertical angle, and before combustion product flowing water level land turns to its final application, and the length/diameter of approximately press 1-2 is than (preferably 1) extension.The slag retracting device is provided with the stroke of one section weak point extraly between the deflector of main combustion chamber and vertical row are portalled, make that most of residue slag drips on the wall that is collected in the slag recovery area in the gaseous product flow.The gravity that vertical outlet has strengthened the slag granules that is collected sinks.Settle the slag scum hole basically facing to vertical outlet, strengthened the internal heat radiation that slag is slagged tap, the slag that helps to keep good flows, so that enter the slag knockout drum through the slag scum hole.
The slag recovery area together with deflector, provides the hot reflux gas source equally, and reflux gas flow back into the core in main combustion chamber district spirally.The diameter of this backflow, promptly the core of gas is about the 70-75% in main combustion chamber deflector aperture usually.This tangential and axial velocity that has just caused discharging combustion product stream at water conservancy diversion plate hole place increases.Slag in this gas stream drips further and reclaims the locular wall acceleration to slag, so that be collected as slag.The more important thing is that this core provides a zone that turbulent flow is less, can import additive in it, to collect potential air pollutants, as sulfide.It has created condition for best configuration in order to the sorbent injector of control sulphur blowdown.Certain point near the main combustion chamber centerline of water conservancy diversion plate hole is injected to this adverse current stamen portion with adsorbent, for condition has been created in the fabulous preheating and the chemistry preparation of adsorbent.The adverse current velocity field carries the core that most adsorbent enters main combustion zone, and adsorbent and sulfide react in dense fuel environment there.Use adsorbent to make the rate of recovery of sulfur content in the fuel effectively up to 60-70%.
In experimental implementation of the present invention, with the total stoicheiometry operation of about 0.75 main combustion chamber.Make the discharging degree of nitrogen oxide be in 250 scopes to about 300 PPMs (ppm).This just can make our device meet clean air regulation, and not by means of the gas cleaning measure of costliness.
Fluid and combustion reaction principle have been used in our invention, can be sure about from a kind of power scale conversion to another kind of power yardstick.We use same conversion principle and have built the device that power capacity reaches 100,000,000 7 thousand ten thousand British thermal units/hour (170million BTU/hr.).As the example of these conversion principles, preheater, main burner and slag reclaim the transverse cross-sectional size of chamber, roughly directly are estimated as the square root of power demand capacity.With regard to the yardstick of commercial interest, roughly remain on 3/1 for its length/diameter of premix burner than often, be 1.5-2 for main combustion chamber: 1, then be 1/1 for the slag retracting device.Be bordering on its length/diameter ratio of vertical outlet conduit and be about 1/1, collect slag and carry thermal exhaust to create condition to other specific terminal applies device for final.The outlet of the rectangle of precombustion chamber is design like this, the diameter ratio of using open height and main burner approximately from 0.2 to 0.3, and the width of rectangle outlet can be aligned, so that produce 330 Foot/seconds of inlet velocity normally greatly under 1200 ° of-2000 temperature conditions.Air inlet with slip airflow regulator device helps to reach the downward modulation ratio of 3-1 equally, to be suitable for the different requirements of different places to use.Downward modulation is to regulate premix burner inner oxidizing agent stream and particle carbonaceous stream and finish by the particle carbonaceous stream that adjusting enters main burner by in direct ratio or intimate direct proportion.
For input air stream, this device makes full use of traditional blowing plant and supplies the input oxidant of input pressure near 25-45 inch water column.This device that makes us also is directly applied for ready-made terminal applies equipment except being suitable for stipulating the newly-designed boiler power plant with the atmospheric pressure burning, such as initial design be constructed to industrial furnace and the electric power industry boiler that uses oil or natural gas.Successfully used the coal/water slurry of about 70% solid and 30% liquid fraction.
Referring now to Fig. 1,2 and 3, slag tap combustion device 10 is made up of the slag recovery chamber 16 that premix burner part 12, main combustion chamber 14 and slag reclaim servicing unit 18 collaborative works.The delivery fluid can be a gas, steam or liquid, and be used for the particle carbon-containing fuel in the holder 20 is transported to the injector assembly 24 that is loaded on the end plate 26 through conduit 22.In general operation, approximately the fuel of 75%-90% is transported to main burner 14, and reaches by dense phase conveyer for the balance of premix burner 12, and is not shown.
Fuel is transported to premix burner 12 through nozzle 28.Premix burner 12 is a kind of garden column structure basically, at one end seals with Seal end plate 30, and injection assembly 28 passes this plate and stretches.Oxidant stream preferably is preheating to about 300 °-500 or higher temperature, and the carrier pipe 32 through tangentially being connected on the premix burner 12 is transported to mixed zone 34.The tangential importing of oxidant has produced one and has rotatablely moved in 34 districts.Rotatablely moving of oxidant stream can strengthen by air damper plate 36, so that improve the oxidant speed that flows into the combustion zone 38 of premix burner 12 through the hole 40 of deflector 44.34 is normally identical with the diameter in 38 districts.Fuel injector injection assembly 28 stretches into premix burner 12 and reaches at least and preferably pass hole 40 to such position, makes in 34 districts not react.Suitable igniter 42 is passed that end plate inserts and is fixing, for oxidant and granular fuel provide initial lighting.Particle carbonaceous material and oxidant react in 38 districts, the carbon that makes initial total stoicheiometry be reached for all existence is converted into about 0.5-1.5 times of carbon dioxide requisite oxygen tolerance, therefore produced a certain stable reaction temperature, for oxidant and carbonaceous material mixture, it generally approaches adiabatic flame temperature.
The typical tangential velocity of the oxidant stream in 34 districts is in the magnitude of 150 Foot/seconds approximately.Be arranged at the means of the air damper plate 36 conduct desirable tangential velocity of maintenance in 34 districts when desired power parameter changes in the appendix 32.The diameter in the hole 40 in the deflector 44 preferably is about half of diameter of premix burner 12.Rotatablely moving continues to enter combustion zone 38, has played stable wherein burning.
Through appendix 48, additional oxidant is transported in the premix burner 12, appendix pass to around forced draught chamber 50, the latter surrounds distribution network 52.This additional oxidant is followed the thermal response product from 38 districts, and promptly hydrocarbon and remaining oxidant mix, and produce one reacting product stream, the appendix 56 of flowing through, and appendix 56 is changed into rectangular cross section to the Cylinder section.This airflow passes opening 58 tangentially enters main chamber 14.In order to control the air velocity of premix burner product, appendix 58 is equipped with two gas flow adjusting flanges 60 and 62, effective aperture of its control rectangular aperture 58.The product in supplemental oxidant and 38 districts is mixed, and has generated temperature and has been approximately 1200 °-2000 overall reaction product gas flow.This air-flow is an oxygen enrichment, and the required about 2-5 of manying of amount of oxygen is doubly during than the whole fuel complete oxidation of supplying with injector 28 for the amount of oxygen that comprises usually.
If any, also have only a spot of burning to occur in the slag recovery area 16.The air-flow of the combustion product of next autonomous burner 14 is further removed slag fused owing to upwards pass through along pipeline 77.Pipeline 77 is vertical basically, and the diameter with such size, makes the main body air-flow velocity be in the magnitude of 100-150 Foot/about second, is preferably about 125 Foot/seconds.The aerodynamics tractive force that these lower speed have guaranteed to act on the big slag granules is small enough to be overcome by gravity.Simultaneously, slag fused flows to 18 parts bottom downwards along wall 77 and 79, and this part comprises slag scum hole 73, and it is arranged in the short coupling pipeline 71, and and slag holder 76 connections.Gaseous reaction products has been cleared up molten slag, ashes and particle basically now, upwards flow through about one times of distance along pipeline 77 near vertical ground to two times of diameters, then along the approximate steering horizontals of pipeline 81, be transported to final application places in the stove 78 afterburning districts 72 through the combustion product of pipeline 81.According to specific terminal applies, additional oxidant (being air) is input to from forced draught chamber 80 in the air-flow of combustion chamber effluent through circulating line 83.Like this, burning finishes in 72 districts of terminal applies stove 78.Described terminal applies for example can be boiler power plant or Industrial Boiler or the heating furnace of supplying industrial heating installation.Stoicheiometry at the product stream of the stoicheiometry of pipeline 85 place entire reaction products stream and main burner 14 ports of export is the same.For in 72 districts, reaching the required whole oxidants of completing combustion from forced draught chamber 80.
Refer again to Fig. 2, the operation of premix burner 12 comprises that the oxidant that enters 34 districts tangentially flows, nominally its jet velocity is about 150 Foot/seconds.When oxidant during by the aperture in the deflector 44, eddy velocity increases, and reduction in 38 districts.Particle carbon-containing fuel and delivery fluid are imported into 38 districts with the angle about 45 °-90 ° with respect to the center line of premix burner 12.Injected fuel and oxidant flow velocity field have caused that a strong spiral refluxes.This just the hot combustion gas band to nozzle 28, the result forms a strong combustion zone on the top in 38 districts.Although it is very strong that fuel transforms, yet there is no need to make in premix burner 12 its completing combustion.But preferably control this device, the outlet temperature that makes premix burner at opening 58 everywhere in about 1200 °F-2000 °F.The oxidant that enters forced draught chamber 50 radially is drawn into the transition region that is formed by Oxidizer distribution grid 52, as with the vector representation of rill speed like that and the reaction logistics mixing that enters pipeline 56 from 38 districts.Like this, premix burner sub-unit 12 is supplied with main burner 14 with high temperature, high-speed oxidation agent stream, and it is suitable for producing an eddy current at the wall portion place of contiguous main burner 14, and promptly spiroid flows.The volume of premix burner, diameter and length be chosen such that so that, if any, also have only a spot of slag to accumulate on the pre-burning wall.In addition, premix burner 12 is tilting at an angle with horizontal line, is discharged in the main combustion chamber 14 to guarantee solid-state and liquid total overall reaction product.
In Fig. 4, very at length illustrate velocity field main burner 14 in and slag and reclaimed velocity field interaction in the chamber 16.This velocity field is compound, by the time function, and some disturbance, but Fig. 4 illustrates time average operating mode and characteristic thereof on a macro scale.Combustion chamber 12 enters the oxidant stream of main combustion chamber 14, enters main burner 14 through opening 58 in the mode of slipstream from the oxidant stream of premix burner 12, and has produced one total eddy current 2.Several strands of important secondary streams are superimposed on the vortex field 2.Gas stream from opening 58 is divided into the basic two halves that equates: the part of contiguous endoseptum has a spiral flow at least, flows to guide plate 64; Another part flows to top 26 substantially.Produce vortex at nearly wall place, and go back to, as using shown in the vector 5 at top end.Pulverized fuel and delivery fluid are therefrom felt at ease and are ejected in the fuel injector of putting 24, and the nominal angle that is tapered and main burner 14 longitudinal axis substantially is approximately 45 °-90 °.The weight ratio of granular fuel and carrier gas is in 3 to 10 the scope, when this device preferably approaches 10 during by specified generated energy operation.The speed of input fuel and carrier gas flow approximately is 50-200 Foot/second.Oxidant from premix burner 12 flows out provides initial incendiary source with its input temp for spraying into fuel.The Size Distribution scope that is sprayed into fuel is with regard to typical 200 order coals, and is general little to several microns, greatly to 150 microns.Preferably the mean mesh size is approximately 75 microns, and full-size is approximately the 125-150 micron.Fluid is very fast is taken away by strong rotating flow 2 for injected granular fuel and delivery, and quickens to the direction of main burner 14 walls.Meanwhile, the axial flow component acts on the particle carbon containing thing.In the free flight burning of particle carbon containing thing, the combustible volatile that accounts for common this order of magnitude of ature of coal amount 50%-80% is come out by fractionation.Undersized particle had been close to completing combustion before running into wall, remaining only is that slag fused is dripped.Only there is the fraction fuel carbon to arrive wall, and on slag fused, burns.Velocity vector 2,3,4 and 5 causes the solid particle diffusion with the interaction (concentrated area is represented with 6) that sprays between the granular fuel, as shown in the figure.The intensity of inner rotating flow 2 is by being determined by the ratio of the diameter of the speed of spray oxide and water conservancy diversion plate hole 68 with the internal diameter of main combustion chamber 14.With regard to diameter than be 0.5 and the length/diameter ratio of main combustion chamber be 2/1, the residue molten slag of being made up of 10 microns minimum fuel particles and bigger material combustion particle is intercepted at air deflector.The outer big solid particle of the possessive case strikes against points different on the main burner wall by other tracks and is blocked, as shown in the figure.Collected slag has its oneself flow behavior equally on main burner wall 14.In periphery or the bottom near deflector 64, slag flows to deflector 64 as the wash layer by general screw type.On the top or the top of main burner 14, the thin layer slag partly flows to end wall 26, inside subsequently Radial Flow, injection assembly 24 axial flow of settling then along the center, slag in this place's axial flow breaks away from subsequently, and is taken to radially outwardly on the main burning chamber wall, represents with slag track 8.The slag stream of helicoid slag stream and inside Radial Flow has produced the scissors stress on the aerodynamics on the top.When aerodynamic force no longer can drive whole slag fused stream by the helical flow mode, the part slag flowed to deflector 64 along the bottom of main burner 14.The keyhole-shaped slit allows slag fused to flow to slag recovery area 16 on deflector, flows to slag collection district 18 at last.Simultaneously, on deflector 64, the combustion product of radial inflow inwardly produces a gas dynamical shearing traction to the partial melting slag, makes some slag and gaseous product flow through aperture 68 together.Strong eddy current 2 is together with deflector aperture 68, makes that roughly 9 li have produced the reverse backflow core in the boundary layer, and this adverse current originates in the core of slag recovery area 16.In the volume 70 of main burner 14, counter-current gas is passed border 9 diffusions, shown in velocity vector 11.On average, this core attendant of a stage actor encloses its annular section and compares, and fuel is denseer.When dense fuel gas moved past border 9, they and oxidant mixed, thus further burning.From the reverse flow border 9 outside during by deflector aperture 68 when gaseous product flow 13, it has certain eddy velocity that has strengthened, and this eddy velocity mainly is by the speed decision of the stream of the raw oxidizer in 68 areas of aperture 2.Gaseous product 13 has certain axial velocity component equally, and it is that flow by the annulus area that must form by diameter and the reverse flow border 9 with deflector aperture 68 is determined.On average, the diameter on reverse flow border 9 and deflector aperture 68 diameter ratios are about 0.7, and along with the variation of service condition, this value approximately is in the 0.50-0.75 scope.
The longitudinal axis of main combustion chamber is preferably with respect to horizontal line about 15 ° of angles that tilt.This inclination angle provides assurance to the liquid slag stream of the satisfaction in the keyhole-shaped aperture 68 of flowing through from main combustion chamber 14.According to being flow velocity, power density and the running temperature that specific terminal applies is selected, this inclination angle may diminish to about 5 °.When big gradient, may carry molten slag too much secretly through the slag flow of deflector aperture 68 cores, this peels off molten slag from deflector 64 edges and causes owing to gaseous product flow.
On the total inner surface of 16 bottoms, slag recovery area, and on the part at least at an upper portion thereof, covered by a molten slag thin layer that flows.Molten slag streams in the main burner 14 narrow groove of keyhole in the deflector 64 of flowing through continues to flow into slag recovery area 16, and enters slag collection device 18 therefrom.The combustion product of discharging from main combustion chamber 14 is 68 flow velocity maximums in the aperture, flow velocity decline when air-flow expands slag recovery area 16 in subsequently.
Reacting product stream 2 is divided into two basic parts 3 and 4 that equate, makes stoicheiometry in the top zone that comprises injector assembly 24 be approximately half of total stoicheiometry of main combustion chamber 14.When being reflected between heated oxidizer product stream and the granular fuel began to take place in the main burner 14, this low stoicheiometry had stoped the generation of nitrogen oxide.All gases is such as NH
3With the formation of HCN, reduced the generation of nitrogen oxide.Total stoicheiometry that main burner 14 is reducing has further stoped the formation of nitrogen oxide.In addition, when the average stoicheiometry of total space approximately remains in the 0.7-0.8 scope in the main combustion chamber 14, temperature in 70 districts is just up to being enough to keep the slag fusing, but is not so high as to this degree, promptly makes molten slag produce a large amount of steam before being discharged to slag collection district 18.Slag returns total stoicheiometries of obtaining in district 16 and the discharge pipe 81,85, and the stoicheiometry in dirty is identical with 70 districts, and this has just preserved the thing that the low-nitrogen oxide discharging system is pressed for.Generally speaking, this makes after the second-time burning that Nox is reduced to 250-450 hundred order of magnitude of volume ratio very much in the flue gas.
During injection assembly 28 is input to premix burner 12 with regime flow, comprise some still at particle and many particles that burnouts that is in solid flying dust and slag form of burning at fuel from the reacting product stream of opening 58.Flying dust and slag are uniformly distributed in the entire reaction product in fact, and may be more taller than the oxidant stream mean temperature that flows into.Its result, the oxygen-rich stream that flows into main burner 14 has played radiant body, therefore, the whole head portion in 70 districts is exposed among the intense radiation from this radiating system, thereby in top zone, in injector assembly 24 and on every side, light, burning and slag stream strengthened.Equally, in whole combustion zone 70, the gas that is loaded with particle has produced strong heat radiation, has promoted that just temperature is even in 70 districts, and has helped and stablize whole burning.
Because the pipeline 71,77 and 79 over against near vertical is provided with slag scum hole 73, the result strengthens the heat radiation of slag scum hole.The heat radiation of this enhancing helps to keep molten slag flowing into slag collection device 76 under the liquid flowing state completely.
Fig. 5 illustrates the preferred structure scheme that heat protection and corrosion protection are provided for described device wall.Be in the passages that surround of surface 88 and 90, cooling agent stream 86 provides cooling with suitable speed.Passage can be a pipe, double wall baffle plate configuration etc.When beginning to build, with a kind of fire clay 92 of suitable loss,, place the hot gas side on surface 90 such as the Missouri hard paste, its standard thickness is about 0.5 inch.In when operation, gravity and cause some physical phenomenon generation with the hot gas that vector 94 is represented; Fusion clay 98 is deposited on the inner surface of clay 92; By convection current and heat radiation the slagging scorification surface is produced heat transfer; The gas 94 that is flowing is surfacewise to traction and shearing on the operative liquid slag generation aerodynamics; Gravity tends to make liquid slag to flow to minimum point on the inner surface; Heat transfer to cooling agent also makes slag form the slag layer 96 of a condensation on clay 92; And local heat transfer makes liquid slag 98, condensation slag 96 and fire clay 92 combinations, adapts to local hot-fluid to regulate thickness.Along with the progress of time, original fire clay is partly or wholly replaced by solid and liquid slag layer.Like this, coolant channel wall 90 has been subjected to hot protection, because the coolant channel that is made of wall 88 and 90 also works, thereby has prevented the cohesion of acid compound under desirable temperature, and has made corrosion reduce to minimum.In addition, the molten slag 98 of Liu Donging provides a heat-barrier material source for the heat protection that solves and additional wall 90 loses.In cooling agent stream 86 temperature ranges that remain on about 325 °-600.Surpassing 325 work down, can make the sour corrosion on surface 90 reduce to minimum.It is remained on below 600 °F can prevent hydrogen sulfide corrosion.Preferably water is used as cooling agent.Have found that; the Missouri hard paste can provide existing surface 92 for general slag; it adheres to into tough and tensile state; like this; here the device of being narrated can be activated and close and need not worry that the heat protection damages, and other wants argillic horizon 92 to be bonded in fully at first and remains on the coolant channel surfaces 90.
Fig. 6 illustrate in order to keep reliably refractory material and (or) the now preferred wall structure and the arrangement of slag.Coolant channel surfaces 90 and 88 is inside and outside surfaces of the cooling agent stream 86 cylinder metal pipes that pass through.Pillar 100 is by being welded to connect on surface 90, and bolt is along size 1 in the name of on the coolant channel length
1The centre-to-centre spacing of/4 inch separately, 7/8 inch of being separated by approximately of the interval between the row.The clay 90 that is consumed is at the beginning in corbeling and around the corbeling moulding.
Fig. 6 also illustrates and is used for pipe-diaphragm structure that premix burner 12, main burner 14 and slag reclaim the chamber wall of chamber 16.Form the every pipe on surface 88 and 90, the place welds together by dividing plate 102 usefulness fine melt deep weldings and adjacent management in middle footpath.Even the local damage slag and (or) under the situation of refractory heat protection, pipe-diaphragm structure also can keep suitable wall temperature.
Owing to adopted outer hot fuel injection device, in 70 districts of main burner 14, to light with smooth combustion and strengthened, its example is depicted in Fig. 7,7A, 8,8A.The main ejector component placement in sleeve 104, can be obtained the appearance of heat.Shown in Fig. 7 and 7A, injector is a kind of coaxial device, is suitable for supplying the intensive phase coal dust with carrier gas.In Fig. 8 and 8A, injector assembly is a kind of carbonaceous particles that is suitable for being suspended in the liquid, for example coal-water slurry nozzle.
With reference to Fig. 7,7A, 8 and 8A sleeve 104 usefulness vertical sections represent that and injector is represented with part section.Sleeve 104 can have been cut rectangular channel 106 as shown in Figure 8, forms garden shape and help sheet on sleeve 104.On the other hand, in Fig. 7, represented to help sheet 108.Sleeve 104 is designed to have the gap of about 0.25 inch, so that allow axonometer 110 or nozzle 112 is put in the sleeve 104 gently.The end of sleeve 104 is positioned in the scope of aperture 116 about 0.25-1.0 inch of the spray orifice 114 of axonometer 110 or nozzle 112 subsequently, and granular fuel and delivery fluid flow are crossed spray orifice or aperture.Referring to Fig. 8, rectangular channel 106 preferably has nominal size 0.25 inch * 0.25 inch.On the surface of the sleeve 104 in groove 106, or as shown in Figure 7, in the periphery that helps sheet 108, slag forms a condensate layer.Axially led to the molten slag aerodynamic end to sleeve 104, and produce a thermal boundary layer in fuel injection point, in 70 districts that are ejected into main burner 14, it has strengthened burning.
Fig. 7 and 7A have represented the typical section of pintaux injector 110.Particle carbon containing thing and delivery fluid enter injector assembly through circulating line, and approximately to discharge 60 ° the spray tank 114 of jet angle on being distributed in surface 118.Whole injector assembly is installed on end wall 26 and 30.For flow particles carbon containing thing that prevents to cause and undesirable sintering and the coking effect that delivers fluid, be necessary to cool off internally the nozzle 110 and 112 that is in the thermal response environment because of the heat that is radiated 38 and 70 districts.With reference to Fig. 7, cooling fluid is by means of adopting carrier pipe 130 and return duct 132 to supply with by the passage 124 and the top manifold 128 of pipeline 116 peripheries.Provide sealing with between the external world by suitable seal filler (not shown) in 38 districts and 70 districts, the sealing filler is to control air tightness by suitable regulating measure.
Referring now to Fig. 8 and 8A, nozzle 112 can be used to carry the suspension fuel that is spray pattern.Its work and close spraying in 38 and 70 districts, the maintenance of the burning of suspension spray site, be based on and adopted spray gas, promptly such as a kind of oxidant of air, it intersects with direction and the suspension that is substantially perpendicular to suspension flow, mix with suspension and make its atomizing, so that-when making the particle of atomizing reach rapid expansion when injector spray immediately, this has just promoted the burning of pressing close to spray all around.
Nozzle 112 remains in the sleeve 104.Suspension is along being input to sprayer perpendicular to the nozzle injection direction through pipeline 137 substantially.The carrier gas of atomizing, oxidant normally, such as air by pipeline 134 inputs, substantially intersecting with suspension perpendicular to the direction of suspension from the trace of connected entrance 136 to 138, this just makes the suspension that enters 38 or 70 districts to approach relatively its axis and become 90 ° angle to produce to shear and to atomize at the intersection of connected entrance 136 to 138.
The suspension that is transfused to is transferred in many pipelines 135 by tapered bosses 140 supplies with eductor ports 136.Consider the shear flow input, eductor ports 138 best some flaring of streamwise, optimal angle of flare approximately is 5 °, and its diameter is greater than cooperating mouth 136.Cooling agent such as water is input to manifold 142 through pipeline 140, and returns through pipeline 144.This has just protected the head of nozzle 112.With reference to Fig. 7,7A and 8, sleeve 104 is to use fluid, cools off separately such as water, and it enters and discharge through pipeline 148 through pipeline 146, this just protected axonometer and (or) nozzle, and guaranteed slag condensate layer on sleeve 104 outer surfaces.General jet velocity through groove 114 and camber line duct 136 is in the order of magnitude of 50-200 Foot/second.The surface of adopting tungsten carbide, ramet or suitable high-abrasive material to make in the place that flow direction changes can obtain the satisfied life-span.
Be illustrated in Fig. 7,7A, 8 and 8A in outer hot fuel injector structure, work and advantage common unsettled sequence number for _, title done sufficient description in the patent application of " slagging chamber of hot fuel injector outside having ", this application (summary 31-0113) and the application apply for simultaneously, and transfer same assignee, quoting this hereby, to close pending application altogether be for for referencial use.Quote as a reference simultaneously also have sequence number for _, title for " sulphur removal slagging chamber " (summary 31-0143) and sequence number be _, title is some common pending applications of " sulphur suspending liquid combustion chamber " (summary 11-0304).How can be employed in order more properly to understand this subject content together with our application, can be with reference to these common pending application cases.
Some details of the pipe of Fig. 9 presentation graphs 5 and Fig. 6-dividing plate cooling system especially connect the structure scheme of premix burner 12 and main burner 14. Air damper plate 60 and 62, the speed and the mass rate of flow of the oxidant stream that enters main burner 14 have been controlled, be to drive by suitable operating parts 150 and motor 152, the air damper plate inwardly and is outwards rotated forms rectangular aperture 58, in order to oxidant stream is transported to main burner 14 from premix burner 12.
The design principle that embodies in the present invention provides a kind of easy conversion method to different power brackets.Because course of reaction is strong volume combustion process basically, wherein qigong mechanism control, sizing are finished by adopting the cross section flow area, but then oxidant inlet speed are done small levelling.Its basic conversion relation is as follows:
1. premix burner, main burner and slag recovery area area of section:
(power of device 1)/(power of device 2)=((1 diameter)/(diameters of 2))
2
In other words, when device 1 was converted to large scale, power capacity was roughly pressed square increase of Cylinder combustion chamber diameter.
2. the length/diameter ratio requires L/D:
Main combustion chamber (1.5-2)/1
3. the deflector face ultimate ratio of stepped driving cone: (2-4)/1
These relations only just can be regulated when equipment tool requires.
For the nominal power that adopts No. 6, Ohio, 200 order coals is the device of 5,000 ten thousand British thermal units/hour (50-million BTU/hour), and the typical scale result of this equipment is as follows:
Premix burner
Diameter 17 inch
Length 55 inch
Main burner
Diameter 34 inch
Inlet hole 25 inch * 10 inch
Water conservancy diversion plate hole 17.125 inch
High 8.417 inch of wide 3 inch of deflector keyhole
The slag recovery area
Diameter 34 inch
Outlet equivalent diameter 30 inch
For the burner with above-mentioned size, used coal best 80% is by 200 orders.For handle assembly is converted to high power capacity, can adopts a little slightly fuel of a bit, and still obtain more above-mentioned advantages of the present invention.
When we have illustrated and have narrated specific embodiments of the invention, be to be understood that, do not exceeding under the situation of the present invention and can be used for various modifications, therefore, our purpose is allly to drop on all modifications in practicalness of the present invention and the scope and improvement and be the present invention and cover.
After the preceding revisal of the capable revisal of file name page or leaf
26 15 increase by one section word:
In other words, when device 1
When being converted to large scale,
Power capacity is roughly by the garden post
Body combustion chamber diameter square
Increase.
Claims (21)
1, in order to carbon-containing fuel in the combustion zone and the device that the non-combustion thing in the fuel is separated from combustion gas product of burning, wherein the combustion zone is enclosed in the combustion chamber, this combustion chamber remains on such temperature with its wall temperature, slag layer is remained on the inner surface of described wall, wherein oxidant is imported into described combustion chamber in some way to set up and to keep the high-speed eddy of oxidant and combustion product mixture, it is in the combustion chamber annulus of contiguous described inner surface, wherein carbon-containing fuel is by a certain mode and direction, being that low speed is transfused to the combustion chamber than oxidant speed, so that keep the stoicheiometry of denseer fuel in the essential part in described combustion zone, wherein, fuel input rate is controllable with respect to the input rate of oxidant, flow velocity and ignition temperature are remained in such scope, the carbon that major part is contained in the fuel converts oxycarbide to, and the most of non-combustion thing in the fuel is dissolved, and deposit as liquid slag, thereby separate with gas combustion product, the feature of described device also comprises following improvement:
Be suitable for reclaiming the chamber with the slag that is lower than the stoicheiometry operation, be used to receive gas combustion product from described combustion chamber, from described molten slag product, reclaim remaining non-combustion thing, and respectively described molten slag is removed, thereby the dense fuel gas product that does not have slag comparatively speaking is provided, has gone so that be transported in the relevant heat use equipment;
2, by the described burner of claim 1, its characteristics also are to be used for preheating when importing the device of described combustion chamber oxidant and entering relevant heat utilization equipment when gas combustion product, are used for an additional oxidant is fully joined the device that described product goes.
3, by the described burner of claim 1, its feature is that also described device comprises a precombustion chamber, is used for oxygen-enriched air after the preheating and combustion product mixture are input to described combustion chamber.
4, by the described burner of claim 3, its feature is that also the stoicheiometry in the above-mentioned preheater is controlled, follows the speed and the mass rate of flow of the product of the preheater that flows to described combustion chamber to have nothing to do.Speed when importing described combustion chamber with carbon-containing fuel and mass rate of flow are irrelevant.
5, by the described burner of claim 3, its feature is that also the temperature of premix burner output stream is adjustable in 1200 to 2000 scope, so that reach best smooth combustion in the combustion zone.
6, by the described burner of claim 3, its feature also be described premix burner comprise one elongated, be cylindrical precombustion chamber basically, it has a top and a port of export, one fuel injector is arranged near the center, top, in order to carbonaceous particles fuel is imported described precombustion chamber, also comprise in order to oxidant is imported the device of described precombustion chamber.
7, by the described burner of claim 3, wherein said fuel comprises a kind of particle carbon-containing fuel that is suspended in the delivery fluid, its feature is that also described device comprises in order to the oxygen-rich mixture after the described preheating is in the device that 1200 to 2000 airflow patterns in the scope are imported described combustion chamber approximately with temperature, and in order to regulating the device of described fuel and described delivery fluid weight ratio,, the burning in the described combustion chamber is higher than the molten grey temperature of described non-combustion thing to keep wherein ignition temperature thereby being adjusted to certain state.
8, by the described burner of claim 1, its feature also is to be disposed at the deflector with holes between described combustion chamber and described slag recovery chamber, in order to combustion product and molten slag are imported described slag recovery chamber from described combustion chamber.
9, by the described burner of claim 8, its feature is that also described deflector with holes determined that a hole combustion gas product that becomes the lockhole shape substantially enters described slag through this hole with the form of high speed vortex flow from described combustion chamber and reclaims the chamber, and molten slag flows into described slag quite slowly and reclaims the chamber.
10, by the described burner of arbitrary claim in the claim 1 to 9, its feature is that also described fuel mainly is made up of less than 150 microns pulverized coal the average diameter of most of coal grains.
11, by the described burner of arbitrary claim in the claim 1 to 10, its feature is that also carbon-containing fuel is imported near in the combustion chamber at one end center, thereby has produced a kind of fuel of relative oxygen enrichment and the mixture of combustion product in the longitudinal extension centre of combustion zone.
12, in the combustion process of the carbon-containing fuel in the slag tap combustion district, and the non-combustion thing that is present in the fuel is followed in the separation process of gas combustion product wherein, described combustion zone is enclosed in a certain combustion chamber, its wall portion keeps such temperature, slag layer is remained on the inner surface of wall, and oxidant wherein is imported in the combustion zone in some way, so that the high speed vortex flow of the mixture that in the combustion chamber annular section of contiguous combustion chamber inner surface, forms and keep forming by combustion product and oxidant, and wherein carbon-containing fuel being low speed than oxidant, and be imported in the described combustion chamber by certain mode and direction, so that in the major part of described combustion zone, keep the condition of relative oxygen enrichment, and wherein said fuel input rate is adjustable with respect to oxidant input rate, so that flow velocity and ignition temperature remain in such scope, make the most of carbon that is included in the fuel be converted to oxycarbide, and the non-combustion thing that is present in the fuel is melted, and deposit as liquid slag, thereby separate with gas combustion product, described improvement comprises following method:
Remaining non-combustion thing is separated from described product, become the molten slag state, do not have the gaseous product of slag comparatively speaking, go so that be transported in the described heat utilization equipment thereby provide;
13, by the method for the burning carbonaceous fuel of claim 12, its feature also is to enter when going in the relevant heat utilization equipment when above-mentioned product, and the oxidant that adds is fully added to does not have other method of going in the oxysome of the slag product comparatively speaking.
14, by the described combustion method of claim 12, be included in described product enter go in the relevant heat utilization equipment after, the additive method that additional oxidant and gaseous product are mixed, supply described additional oxidant with a certain mass rate of flow, this additional oxidant is enough to finish all carbon monoxide basically and the hydrocarbon burning that is included in the gaseous product at least.
15, by the described combustion method of claim 12, its feature is that also preheating is imported into other method of the oxidant of described combustion zone.
16, by the described combustion method of claim 12, the oxidant that its feature also is to be imported into the combustion zone is a kind of mixture of being made up of air and combustion product of the oxygen enrichment through preheating.
17, by the described combustion method of claim 15, its feature is that also the pre-heating mean of described oxidant is to finish by fuel being sprayed near in the precombustion chamber at its center, top in elongated being substantially in the cylindrical precombustion chamber with a top and a port of export, oxidant is input in the described precombustion chamber with combustion fuel, and the temperature of precombustion chamber output stream is adjusted in approximately in 1200 to 2000 the scope, thereby in the combustion chamber, produce stable burning.
18, by the method for the described burning carbonaceous fuel of claim 12, the mean temperature that wherein is imported into the oxidant of described combustion zone is controlled, and is irrelevant with the mass rate of flow and the flow velocity of oxidant.
19, by the described method at combustion zone internal combustion carbon-containing fuel of claim 12, its feature also is:
20, by the described combustion method of claim 12, its feature is that also ignition temperature remains in a certain temperature range in the combustion zone, like this, the molten slag that produces in the combustion zone has enough low viscosity, make molten slag can get rid of in the combustion zone in the mode of relative low viscosity stream and gas combustion product press separate mode mobile.
21, by the described combustion method of claim 12, its feature also be to flow through temperature of gaseous product of slag recovery area is maintained at the molten grey temperature that is higher than the non-combustion component of carbon-containing fuel substantially.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 86108138 CN86108138A (en) | 1986-12-01 | 1986-12-01 | Slagging conbustion system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 86108138 CN86108138A (en) | 1986-12-01 | 1986-12-01 | Slagging conbustion system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN86108138A true CN86108138A (en) | 1988-07-20 |
Family
ID=4803813
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 86108138 Pending CN86108138A (en) | 1986-12-01 | 1986-12-01 | Slagging conbustion system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN86108138A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1320305C (en) * | 2002-05-29 | 2007-06-06 | Tps特密斯卡加工处理股份有限公司 | Control of cyclone burner |
| CN102344834A (en) * | 2010-07-29 | 2012-02-08 | 气体产品与化学公司 | Method for gasification and a gasifier |
| CN104879747A (en) * | 2015-04-17 | 2015-09-02 | 石家庄新华能源环保科技股份有限公司 | Clean combustion device |
-
1986
- 1986-12-01 CN CN 86108138 patent/CN86108138A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1320305C (en) * | 2002-05-29 | 2007-06-06 | Tps特密斯卡加工处理股份有限公司 | Control of cyclone burner |
| CN102344834A (en) * | 2010-07-29 | 2012-02-08 | 气体产品与化学公司 | Method for gasification and a gasifier |
| CN104879747A (en) * | 2015-04-17 | 2015-09-02 | 石家庄新华能源环保科技股份有限公司 | Clean combustion device |
| CN104879747B (en) * | 2015-04-17 | 2018-05-01 | 石家庄新华能源环保科技股份有限公司 | A kind of clean combustion equipment |
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