CN105199782A - Gasification agent, strong-rotating pulverized coal and fly ash mixed-burning gasifier device and method - Google Patents
Gasification agent, strong-rotating pulverized coal and fly ash mixed-burning gasifier device and method Download PDFInfo
- Publication number
- CN105199782A CN105199782A CN201510579057.6A CN201510579057A CN105199782A CN 105199782 A CN105199782 A CN 105199782A CN 201510579057 A CN201510579057 A CN 201510579057A CN 105199782 A CN105199782 A CN 105199782A
- Authority
- CN
- China
- Prior art keywords
- gasification
- flying dust
- dust
- slag
- vaporized chemical
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Abstract
The invention discloses a gasification agent, strong-rotating pulverized coal and fly ash mixed-burning gasifier device and method. The gasification agent, strong-rotating pulverized coal and fly ash mixed-burning gasifier device is characterized in that a gasification agent nozzle is inserted into a gasifier chamber along the tangential direction of the gasifier chamber; the axis of a fly ash nozzle and the axis of the gasification agent nozzle are located in the same horizontal plane; the lower part of a pulverized coal passage is provided with a rotational flow blade; a pulverized coal burner is arranged at the top part of a gasifier body; the axis of the pulverized coal burner is coincided with the axis of the gasifier chamber. The method comprises the steps of firstly, setting the pressure and the temperature in the gasifier chamber; secondly, sending dry pulverized coal which is carried by nitrogen or carbon dioxide into the gasifier chamber through the pulverized coal passage; thirdly, enabling mixed airflow of the dry pulverized coal and the gasification agent to be ignited by high-temperature synthesis gas; fourthly, spraying the fly ash which is carried by the nitrogen or the carbon dioxide into the gasifier chamber through the fly ash nozzle; fifthly, tangentially spraying the rest gasification agent into the gasifier chamber through the gasification agent nozzle; sixthly, enabling crude gas which is generated by gasifying to flow out of the gasifier chamber through a synthesis gas passage, and enabling generated liquid slag to flow into a slag bath along the wall. The gasification agent, strong-rotating pulverized coal and fly ash mixed-burning gasifier device and the method, disclosed by the invention, are applied to the field of coal gasification.
Description
Technical field
The present invention relates to a kind of vapourizing furnace and gasification process, be specifically related to a kind of vaporized chemical and rotate by force coal dust and flying dust and mix and burn gasifying furnace device and method.
Background technology
Coal Gasification Technology is the clean coal technology of high-efficiency cleaning.Current Coal Gasification Technology is mainly divided into moving-bed gasification, fluidized-bed gasification, entrained flow gasification and molten bath gasification four class.Wherein, entrained flow bed gasification technology because its gasification intensity is high, throughput is large, efficiency of carbon conversion advantages of higher has become present Coal Gasification Technology main development direction.Entrained flow gasification has two principal features, and one is that operating temperature is high, is about 1300 ~ 1600 DEG C, and the lime-ash formed in stove is liquid, and deslagging mode is slag tap; Another one feature adopts " with slag anti-slag " technology to protect furnace wall and to reduce thermosteresis.Airflow bed gasification furnace Problems existing is: (1), the easy scaling loss of gasification stove internal wall face.Gasification stove internal wall face burning problems causes vapourizing furnace often to stop, and vapourizing furnace is as the beginning of production of chemical enterprise, once stop, causes whole production line all to be stopped transport, and whole production line is stopped transport and once caused great economic loss to enterprise.Such as: the gasification production line of an a set of consumption of coal 1000t/d financial loss of stopping transport reaches more than 4,000 ten thousand yuan.(2), the flying dust amount that generates of vapourizing furnace is large, difficult treatment.The gasification production line of such as a set of consumption of coal 1000t/d, ature of coal ash content 10%, day generates flying dust about 50 tons, generates flying dust amount year about up to 1.65 ten thousand tons.According to the burying method process that enterprise is conventional, about 1.8 ten thousand steres need be digged pit for landfill flying dust by annual enterprise, and visible process cost is very big.(3), vapourizing furnace produce flying dust in combustible content high, the gasification production line of such as a set of consumption of coal 1000t/d, in flying dust, combustible content is 30%, every day generate flying dust carbon residue quality about 15 tons, waste the energy greatly.
Summary of the invention
The present invention is uneven for solving vapourizing furnace wall dross in prior art, the problems such as flying dust difficult treatment, and proposes a kind of vaporized chemical and rotate by force coal dust and flying dust and mix and burn gasifying furnace device and method.
The present invention be solve the problem adopt technical scheme be:
Device of the present invention comprises coal dust burner, gasification body of heater, water wall, synthetic gas passage, slag bath, vaporized chemical spout, flying dust spout and dust conveying system, water wall is arranged on the inner side-wall of gasification body of heater, water wall is made up of several Vertically tube, the solid of revolution inner chamber surrounded by water wall is gasification hearth, slag bath is positioned at gasification bottom of furnace body, synthetic gas channel setting is in gasification body of heater middle and lower part, and synthetic gas passage is communicated with gasification hearth, vaporized chemical spout and flying dust spout are all installed on body of heater column part top, vaporized chemical spout inserts in gasification hearth along the tangential direction of gasification hearth, the axis of flying dust spout and the axis of vaporized chemical spout are located in the same horizontal plane, the axis of flying dust spout is 5 ° ~ 30 ° with the angle of vapourizing furnace secant in the horizontal direction, vapourizing furnace secant is parallel to the axis of vaporized chemical spout, the described input terminus of flying dust spout is connected with the output terminal of dust conveying system, described coal dust burner comprises swirl vane and the coal dust channel of annular, the bottom of coal dust channel is provided with swirl vane, described coal dust burner is arranged on the top of gasification body of heater, and the axis of coal dust burner and the dead in line of gasification hearth.
Method of the present invention is realized by following steps:
Step one: setting gasification hearth internal pressure is 0.1MPa ~ 4MPa, and the operating temperature of gasification hearth is 1250 ~ 1600 DEG C;
Step 2: temperature is that the dry pulverized coal of 25 DEG C ~ 100 DEG C carries with the coal dust channel feeding gasification hearth of cyclone mode on coal dust burner inner by nitrogen or carbonic acid gas, formed in furnace roof region and rotate downward breeze airflow, wherein dry pulverized coal accounts for 1% ~ 25% of dry pulverized coal and nitrogen mixture cumulative volume;
Step 3: dry coal powder airflow touches after Central backflow area entrainments the high-temperature synthesis gas of returning, and is lighted, form slag at gasification hearth top combustion by high-temperature synthesis gas;
Step 4: flying dust is stored in powder storehouse, after opening powder storehouse valve, flying dust leans on gravity fall in lock hopper, close powder storehouse valve, when lock hopper is forced into and is greater than flying dust to batch can internal pressure, open lock hopper valve, flying dust flows into flying dust in batch can, close lock hopper valve, after passing into high pressure nitrogen or carbonic acid gas by high-pressure delivery gas feed, temperature is that the flying dust of 25 DEG C ~ 100 DEG C is carried by nitrogen or carbonic acid gas and tangentially sprays in gasification hearth through flying dust spout, wherein flying dust accounts for 1% ~ 25% of flying dust and nitrogen mixture cumulative volume, under high temperature action, slag is formed after flying dust enters gasification hearth, the ratio of the described flying dust and quality of pc that pass into gasification hearth is 0 ~ 1:1,
Step 5: temperature is that the vaporized chemical of 20 DEG C ~ 400 DEG C tangentially sprays into gasification hearth by vaporized chemical spout with the speed of 100m/s ~ 200m/s, strong swirling eddy is formed after vaporized chemical air-flow at a high speed pours gasification hearth, under the influence of centrifugal force, the slag of 80% is thrown to face, furnace wall and forms thicker slag blanket, slag blanket is even, swirling eddy constantly washes away the slag blanket on burner hearth wall, and gasification reaction strong in its generation;
Step 6: the raw gas that gasification generates flows out gasification hearth by synthetic gas passage, and the liquid slag of generation flows into slag bath along wall, discharges gasification body of heater by bottom slag discharge after cooling.
The present invention has following beneficial effect compared with existing gasification installation and method:
1, in the present invention, slag blanket is formed by centrifugal action.In prior art (see Fig. 3), coal dust and vaporized chemical all spray into burner hearth from top of gasification furnace, and coal dust at high temperature forms slag after entering burner hearth, and slag general in the same way mode with direct current together with vaporized chemical air-flow flows to burner hearth bottom.In flow process, the slag of a small amount of near wall is only had to form slag film because gas adheres on wall; And in the present invention, coal dust sprays into from top of gasification furnace, flying dust tangentially sprays into, coal dust, flying dust at high temperature form slag after entering burner hearth, the vaporized chemical tangentially spraying into burner hearth with the speed of 100m/s ~ 200m/s forms strong swirling eddy in stove, slag flows downward near wall district high speed rotating together with vaporized chemical, and the slag of about 80% is constantly thrown on wall by the centrifugal action revolving by force generation and forms slag blanket.
2, the quantity of slag sticked in the present invention on furnace wall is many, and thickness of slag layer is large.In prior art, coal dust and vaporized chemical all spray into burner hearth from top of gasification furnace, and coal dust at high temperature forms slag after entering burner hearth, and slag general in the same way mode with direct current together with vaporized chemical air-flow flows to burner hearth bottom.In flow process, the slag of a small amount of near wall is only had to form slag film because gas adheres on wall, cannot adhere on wall from wall slag remotely, therefore only have an appointment about 10% slag can adhere to wall and form slag film, because the quantity of slag sticked on furnace wall is little, cause wall slag film thinner, general slag film thickness is 2mm ~ 3mm; The present invention relies on centrifugal force slag to be thrown to wall and forms slag blanket, vaporized chemical tangentially sprays in burner hearth 3 with the speed of 100m/s ~ 200m/s, form strong swirling eddy, the centrifugal force produced is enough to slag to be thrown on wall form slag blanket, the slag accounting for about 80% in gasification is all thrown on wall and forms slag blanket, because the quantity of slag sticked on furnace wall is many, therefore wall slag blanket is thicker, and thickness of slag layer can reach 5mm ~ 6mm.
3, in the present invention, wall thickness of slag layer is more even.In prior art, coal dust and vaporized chemical all spray into burner hearth from top of gasification furnace, and coal dust at high temperature forms slag after entering burner hearth, and slag general in the same way mode with direct current together with vaporized chemical air-flow flows to burner hearth bottom.In flow process, the slag of a small amount of near wall is only had to form slag film because gas adheres on wall, cannot adhere on wall from wall slag remotely, therefore only have an appointment about 10% slag can adhere to wall and form slag film, because the quantity of slag sticked on furnace wall is little, when along the tolerance skewness of vapourizing furnace circumferential direction, along the circumferential direction to adhere to situation uneven for wall slag, causes circumferential direction wall slag non-uniform film thickness even.And in the present invention, coal dust sprays into from top of gasification furnace, flying dust tangentially sprays into, coal dust, flying dust at high temperature form slag after entering burner hearth, the vaporized chemical sprayed into the tangential velocity of 100m/s ~ 200m/s forms strong swirling eddy in stove, and slag flows downward near wall district high speed rotating together with vaporized chemical.In the present invention, gas velocity is high, and turbulence intensity is large, is conducive to mixing of vaporized chemical and slag.Under the centrifugal action revolving by force generation, be thrown to wall after slag along the circumferential direction mixes with vaporized chemical form slag blanket, wall thickness of slag layer is more even.
4, the present invention can more available protecting gasification stove internal wall face.Wall slag blanket main component is silicon-dioxide, and silicon-dioxide thermal conductivity is about 7.6W/mk, and the thermal conductivity of conventional refractory brick is about 20W/mk ~ 28W/mk, and slag blanket thermal conductivity ratio refractory brick is much little, therefore the good heat-insulation effect of slag blanket.In prior art, wall slag film is thinner, slag film thickness is generally 2mm ~ 3mm, and along the circumferential direction slag non-uniform film thickness is even, easily occurs the problem that internal partial wall face does not have slag film and covers, gasification stove internal wall face is exposed in high-temperature flue gas environment, easily occurs overtemperature and is burnt.Containing the carbon monoxide of 60% ~ 70% in gasification furnace gas, the carbon monoxide of high temperature is corrosive gases, and gasification stove internal wall face is exposed to high temperature and under being rich in the environment of carbon monoxide, easily chemical corrosion occurs.In the present invention, wall slag blanket is thick, and thickness of slag layer, up to 5mm ~ 6mm, is 2 times ~ 3 times of prior art, and simultaneously thickness of slag layer is relatively more even, does not have gasification stove internal wall face to be exposed in high-temperature flue gas, more can available protecting gasification stove internal wall face not by high-temperature gas scaling loss; And gasification stove internal wall face and furnace gas (carbon monoxide containing 60% ~ 70%) separate by thicker slag blanket, gasification stove internal wall face can be protected not by the chemical corrosion of CO (carbon monoxide converter) gas.
5, the consumption of oxygen of the present invention is few.In prior art, wall dross is thin and uneven, and slag film thickness is generally 2mm ~ 3mm; In the present invention, wall dross is thick and even, and thickness of slag layer is up to 5mm ~ 6mm, and be 2 times ~ 3 times of prior art, and slag blanket thermal conductivity is little, thermal insulation is good, and therefore the present invention can reduce wall thermosteresis.Carbon and oxygen reaction generate carbon monoxide heat release 112.1kJ/mol, and carbon and oxygen reaction generate carbonic acid gas heat release 395kJ/mol, and it is 3.52 times that generate carbon monoxide liberated heat that obvious carbon and oxygen reaction generate carbonic acid gas heat release.Coal dust gasification needs could react rapidly under comparatively high temps (1250 DEG C ~ 1600 DEG C), although expect that the gasification product obtained is carbon monoxide, but in order to maintain higher in-furnace temperature, excessive oxygen must be passed into and generate carbonic acid gas to improve temperature.In prior art, wall thermosteresis is comparatively large, and when during actual motion, the equivalence ratio of adjustment Sauerstoffatom and carbon atom is 1.05 ~ 1.1, the oxygen that is passing into 5% ~ 10% generates carbonic acid gas maintenance furnace temperature more.And slag blanket is thick in the present invention, wall thermosteresis is little, and adjustment Sauerstoffatom is 1.01 ~ 1.05 furnace high-temperatures that can remain same with the equivalence ratio of carbon atom, and compared with prior art the consumption of oxygen reduces about 5%.Oxygen is separated from air, and sepn process current consumption is large, and the present invention reduces the consumption of a large amount of oxygen, a large amount of electric energy of corresponding saving.
6, the viscosity-temperature characteristics of the present invention to coal ash are insensitive, and Suitability of Coals is strong, can be applicable to the coal that grey split pole is low.Slag gasification furnace wants the technological line protection water wall reaching " with slag anti-slag ", then must ensure that wall-cooling surface place exists thicker slag blanket.In prior art, the formation of wall-cooling surface place slag film only relies on the slag adhered near wall place, and its quantity of slag sticked on wall is few.Sticking under the few condition of the quantity of slag on wall, for reaching certain thickness slag blanket, then to the viscosity-temperature characteristics of coal ash, harsh requirement must be proposed: within the scope of gasification temperature, coal ash viscosity can not be too low or too high.The too low then slag fluidity of coal ash viscosity is good, and slag film is thinner, can not play the effect of protection water wall; Coal ash viscosity is too high, and slag fluidity weakens, and in slag notch flowing slowly, deslagging is not smooth.Require harsh to the viscosity-temperature characteristics of coal ash, then mean that existing vapourizing furnace Suitability of Coals is poor, suitable coal must be selected normally to run.In the present invention, the slag of 80% is got rid of to wall place, and wall-cooling surface forms certain thickness slag blanket, and the viscosity-temperature characteristics of thickness of slag layer to coal ash are insensitive, and therefore Suitability of Coals of the present invention is strong.For the invention " a kind of vaporized chemical rotates by force coal dust gasification device and gasification process " applied for the present invention simultaneously, although its Suitability of Coals compared with prior art strengthens greatly, but for the coal (as ash content is about the brown coal of 0.6%) that grey split pole is low, because in-furnace slag amount is few, thicker slag blanket cannot be formed, therefore cannot process.And during the coal that the present invention utilizes grey split pole low, can account for by sending in stove the flying dust that total amount is up to 50%, make have enough slags to exist in vapourizing furnace, a large amount of slags can be thrown on wall, form thicker slag blanket, realize the technological line of " with slag anti-slag ".Therefore Suitability of Coals of the present invention is extremely strong, can be applicable to the coal that grey split pole is low.
7, the present invention can process the flying dust that gasification produces.Airflow bed gasification furnace Japanese consumpting coal amount is large, and fly ash emission amount is large, and the particle size of fly ash simultaneously generated little (being less than 100 microns), flying dust air-flow Portability is good, and air storage dust pollution is serious.Conventional flyash treatment method is landfill disposal, and the method not only adds establishment expense but also waste valuable land resources.Such as: the gasification production line of a set of consumption of coal 1000t/d, in ature of coal, ash content is 10%, and day generates flying dust about 50 tons, and generate flying dust amount year up to 1.65 ten thousand tons, about 1.8 ten thousand steres need be digged pit for landfill disposal flying dust by enterprise.The flying dust that vapourizing furnace produces passes in stove by the present invention to gasify again, flying dust becomes slag under furnace high-temperature, got rid of on wall under the centrifugal action revolving by force generation after forming slag by the flying dust accounting for total amount 80%, flow downward along wall with the form of liquid slag inflow slag bath, in slag bath, cooling forms solid-state clinker.The solid-state clinker produced can be used for paving the way, and has both saved flying dust processing costs, can also be enterprise's extra earning, turn waste into wealth.
8, the present invention can utilize the carbon residue in flying dust, improves efficiency of carbon conversion, save energy.Fly ash combustible material (carbon residue) content of existing vapourizing furnace discharge is high, and existing airflow bed gasification furnace unburned combustible in fly ash of being on active service is up to 20% ~ 40%.Passed in stove by flying dust in the present invention and again gasify, discharge vapourizing furnace with the form of solid-state clinker after the flying dust gasification of 80%, the combustible content of solid-state clinker is about 8%.Compare the flying dust that existing vapourizing furnace produces, the combustible content of the solid-state clinker that the present invention produces is low, improves efficiency of carbon conversion, save energy.
9, under same volume, pressure, in the present invention, coal dust residing time in furnace is long, and vaporization time is long, and gasification rate is high.(1), under identical furnace volume, pressure, vapourizing furnace compared to existing technology, in the present invention, coal dust is long at residing time in furnace, and vaporization time is long.Coal dust and vaporized chemical running orbit in prior art, as shown in Figure 3, vaporized chemical carries coal dust and directly flows to bottom from vapourizing furnace top, because pulverized coal particle is generally less than 75 microns, the carrying capacity of air-flow to coal dust is extremely strong, namely coal dust carries coal dust vaporized chemical at residing time in furnace is flowed directly to the time of bottom from vapourizing furnace top, the residence time is very short, about 4s ~ 6s; In the present invention, slag under the influence of centrifugal force, and the slag of about 80% is thrown on wall and forms slag blanket, and the residence time of coal dust in stove is that molten slag is from top of gasification furnace along wall sluggish flow to the time of bottom.Because vaporized chemical tangentially sprays in stove, rotational flow is done in stove, vaporized chemical is more weak to the molten slag carrying capacity flowed downward along wall, and molten slag viscosity is larger, slowly flow downward along wall, this just substantially prolongs coal dust at gasification residing time in furnace, and the residence time is about 12s ~ 16s, and under identical furnace volume, pressure, the coal dust residence time is 2 times ~ 4 times of prior art.(2), gasification reaction speed of the present invention is high.Gasification in-furnace temperature is higher, and gasification reaction belongs to diffusion control district, and described diffusion control district refers to that at relatively high temperatures, speed of reaction is exceedingly fast, so that any gas one arrives Coal Char Particles surface, exhausts rapidly with regard to reacting with carbon immediately.At this moment the diffusion through frictional belt just becomes controlling factor, and is determined by the speed of relative movement of coal dust and vaporized chemical through the diffusion in frictional belt, and therefore in vapourizing furnace, the speed of relative movement of coal dust and vaporized chemical decides the speed of gasification reaction.After in prior art, coal dust and vaporized chemical are sprayed by burner, the slag accounting for total amount 10% sticks to wall place and forms slag film, and remaining slag is coflow together with vaporized chemical.The slag accounting for total amount 90% together with vaporized chemical with comparatively lower velocity coflow, velocity of flow is about 0.4m/s ~ 0.6m/s, both speed of relative movement are lower, be about 0.08m/s ~ 0.12m/s, the slag forming slag film at wall place reacts with the vaporized chemical air-flow generating gasification of pressing close to wall, and both speed of relative movement are similar to the velocity of flow of vaporized chemical air-flow, be about 0.4m/s ~ 0.6m/s, speed of relative movement is lower, and it is slow that gas is diffused into particle surface, and gasification reaction speed is low.Due to the effect of strong rotational gas flow in the present invention, the slag accounting for total amount 80% forms slag blanket on wall, and remaining slag is with vaporized chemical rotational flow in stove.Slag blanket flows downward along wall, vaporized chemical then high speed rotating washes away slag blanket, gasification agent inlet place vaporized chemical air-flow tangential velocity is 100m/s ~ 200m/s, along with flow process is decayed gradually, syngas outlet place vaporized chemical air-flow tangential velocity decays to 50m/s ~ 100m/s, and the average tangential velocity of vaporized chemical is about 75m/s ~ 150m/s.Slag on wall and the speed of relative movement of vaporized chemical are similar to the tangential velocity of vaporized chemical, average out to 75m/s ~ 150m/s, are 900 times ~ 1200 times of prior art.The slag accounting for total amount 20% does rotational flow with vaporized chemical in stove, and vaporized chemical V-bar is 75m/s ~ 150m/s, and vaporized chemical speed is large, and turbulence intensity is large, and gasification reaction speed is high.In the present invention, vaporized chemical speed is large as can be seen here, and the speed of relative movement of coal dust and vaporized chemical is large, and the speed that gas is diffused into particle surface is large, so gasification efficiency of the present invention is far above the vapourizing furnace of prior art.
10, rely on the high-temperature synthesis gas of backflow to light a fire in the present invention, catch fire stable.In prior art, coal dust flows downward after spraying into burner hearth together with vaporized chemical, and in the process of flowing downward, coal dust is constantly subject to the radiation of high-temperature synthesis gas, and temperature raises gradually, is just lighted higher than during its burning-point when its temperature is elevated to.Due to reasons such as the disturbance of burner hearth flow field and the fluctuations in temperature field, fluctuate coal powder ignition position, ignition time thereupon, instability of catching fire.The present invention is flowed near wall district due to swirling eddy, burner hearth center pressure is lower, the high-temperature synthesis gas of burner hearth bottom is entrainmented to burner hearth central upward flow, form stable high temperature center recirculating zone, in high temperature center recirculating zone, high-temperature synthesis gas is back to coal dust burner root, mix with breeze airflow, firing coal-dust, coal dust stable ignition can be ensured.
11, the present invention reduces investment outlay.From advantage 9, coal dust of the present invention is in residing time in furnace, gasification reaction speed all far above prior art, and gasification intensity is large.Therefore, when uniform pressure, identical gas making amount, in the present invention, vapourizing furnace equipment is much smaller than the vapourizing furnace equipment of prior art, and gasification intensity and prior art are quite even better than prior art.Thus save great deal of investment.
Accompanying drawing explanation
Fig. 1 be the specific embodiment of the invention one one-piece construction front view (in gasification hearth 3, the curve of band arrow is air trajectory, border of refluxing centered by the synthetic gas that mark 17 be breeze airflow, mark 18 be slag blanket, mark 19 be backflow, mark 20, mark 21 be the defeated powder gas of high pressure of input, mark 22 is input fine coal+nitrogen or carbonic acid gas, mark 23 is input vaporized chemical, mark 24 be input flying dust+nitrogen or carbonic acid gas, mark 25 is slag-drip opening);
Fig. 2 is the A-A sectional view of Fig. 1;
Fig. 3 is existing vapourizing furnace (mark 26 is vaporized chemical and coal dust).
Embodiment
Embodiment one: composition graphs 1 and Fig. 2 illustrate present embodiment, present embodiment comprises coal dust burner 1, gasification body of heater 2, water wall 4, synthetic gas passage 5, slag bath 6, vaporized chemical spout 7, flying dust spout 8 and dust conveying system, water wall 4 is arranged on the inner side-wall of gasification body of heater 2, water wall 4 is made up of several Vertically tube, the solid of revolution inner chamber surrounded by water wall 4 is gasification hearth 3, slag bath 6 is positioned at bottom gasification body of heater 2, synthetic gas passage 5 is arranged on gasification body of heater 2 middle and lower part, and synthetic gas passage 5 is communicated with gasification hearth 3, vaporized chemical spout 7 and flying dust spout 8 are all installed on body of heater column part top, vaporized chemical spout 7 inserts in gasification hearth 3 along the tangential direction of gasification hearth 3, the axis of flying dust spout 8 and the axis of vaporized chemical spout 7 are located in the same horizontal plane, the axis of flying dust spout 8 is 5 ° ~ 30 ° with the angle α of vapourizing furnace secant M in the horizontal direction, vapourizing furnace secant M is parallel to the axis of vaporized chemical spout 7, the input terminus of flying dust spout 8 is connected with the output terminal of dust conveying system, described coal dust burner 1 comprises swirl vane 9 and the coal dust channel 10 of annular, the bottom (nearly fire end) of coal dust channel 10 is provided with swirl vane 9, described coal dust burner 1 is arranged on the top of gasification body of heater 2, and the dead in line of the axis of coal dust burner 1 and gasification hearth 3.
Embodiment two: composition graphs 1 and Fig. 2 illustrate present embodiment, the axis of the flying dust spout 8 of present embodiment is 10 ° with the angle α of vapourizing furnace secant M in the horizontal direction, and vapourizing furnace secant M is parallel to the axis of vaporized chemical spout 7.Other composition and annexation identical with embodiment one.
Embodiment three: composition graphs 1 and Fig. 2 illustrate present embodiment, the axis of the flying dust spout 8 of present embodiment is 20 ° with the angle α of vapourizing furnace secant M in the horizontal direction, and vapourizing furnace secant M is parallel to the axis of vaporized chemical spout 7.Other composition and annexation identical with embodiment one.
Embodiment four: composition graphs 1 and Fig. 2 illustrate present embodiment, the dust conveying system of present embodiment comprises powder storehouse 11, powder storehouse valve 12, lock hopper 13, lock hopper valve 14, flying dust to batch can 15 and flying dust feed tank valve 16, and powder storehouse 11, powder storehouse valve 12, lock hopper 13, lock hopper valve 14, flying dust are connected with flying dust feed tank valve 16 from top to bottom successively to batch can 15.Other composition and annexation identical with embodiment one.
Embodiment five: composition graphs 1 and Fig. 2 illustrate present embodiment, and present embodiment is realized by following steps:
Step one: setting gasification hearth 3 internal pressure is 0.1MPa ~ 4MPa, and the operating temperature of gasification hearth 3 is 1250 ~ 1600 DEG C;
Step 2: temperature is that the dry pulverized coal of 25 DEG C ~ 100 DEG C is carried by nitrogen or carbonic acid gas that to send into gasification hearth 3 with the coal dust channel 10 of cyclone mode on coal dust burner 1 inner, formed in furnace roof region and rotate downward breeze airflow, wherein dry pulverized coal accounts for 1% ~ 25% of dry pulverized coal and nitrogen mixture cumulative volume;
Step 3: dry coal powder airflow touches after Central backflow area entrainments the high-temperature synthesis gas of returning, and is lighted, form slag at gasification hearth 3 top combustion by high-temperature synthesis gas;
Step 4: flying dust is stored in powder storehouse 11, after opening powder storehouse valve 12, flying dust leans on gravity fall in lock hopper 13, close powder storehouse valve 12, when lock hopper 13 is forced into and is greater than flying dust to batch can 15 internal pressure, open lock hopper valve 14, flying dust flows into flying dust in batch can 15, close lock hopper valve 14, after passing into high pressure nitrogen or carbonic acid gas by high-pressure delivery gas feed 15-1, temperature is that the flying dust of 25 DEG C ~ 100 DEG C is carried by nitrogen or carbonic acid gas and tangentially sprays in gasification hearth 3 through flying dust spout 8, wherein flying dust accounts for 1% ~ 25% of flying dust and nitrogen mixture cumulative volume, under high temperature action, slag is formed after flying dust enters gasification hearth 3, the ratio of the described flying dust and quality of pc that pass into gasification hearth 3 is 0 ~ 1:1,
Step 5: temperature is that the vaporized chemical (oxygen and water vapour) of 20 DEG C ~ 400 DEG C tangentially sprays into gasification hearth 3 by vaporized chemical spout 7 with the speed of 100m/s ~ 200m/s, vaporized chemical air-flow at a high speed forms strong swirling eddy after pouring gasification hearth 3, under the influence of centrifugal force, the slag of 80% is thrown to face, furnace wall and forms thicker slag blanket, slag blanket is even, swirling eddy constantly washes away the slag blanket on burner hearth wall, and gasification reaction strong in its generation;
Step 6: the raw gas that gasification generates flows out gasification hearth 3 by synthetic gas passage 5, the liquid slag of generation flows into slag bath 6 along wall, discharges gasification body of heater 2 after cooling by bottom slag discharge.
Embodiment six: composition graphs 1 illustrates present embodiment, present embodiment is that to set gasification hearth 3 internal pressure in step one be 2.5MPa, and the operating temperature of gasification hearth 3 is 1500 DEG C.Other step is identical with embodiment five.
Embodiment seven: composition graphs 1 illustrates present embodiment, present embodiment be that in step 2, dry pulverized coal accounts for dry pulverized coal and nitrogen mixture cumulative volume 10%.Other step is identical with embodiment five.
Embodiment eight: composition graphs 1 illustrates present embodiment, present embodiment be that in step 2, dry pulverized coal accounts for dry pulverized coal and nitrogen mixture cumulative volume 20%.Other step is identical with embodiment five.
Embodiment nine: composition graphs 1 illustrates present embodiment, present embodiment be that in step 4, flying dust accounts for defeated powder gas and fly ash mixture cumulative volume 10%, described in pass into gasification hearth 3 the ratio of flying dust and quality of pc be 0.5:1.Other step is identical with embodiment five.
Embodiment ten: composition graphs 1 illustrates present embodiment, present embodiment is that in step 5, temperature is that the vaporized chemical (oxygen and water vapour) of 300 DEG C tangentially sprays into gasification hearth 3 by vaporized chemical spout 7 with the speed of 150m/s.Other step is identical with embodiment five.
Principle of work of the present invention:
In vapourizing furnace, principle of work as shown in Figure 1, and nitrogen or carbonic acid gas carry coal dust and blow into coal dust channel 10 in coal dust burner 1, rotates and spray into gasification hearth 3 after flowing through swirl vane 9, formed rotate downward breeze airflow on gasification hearth 3 top.Breeze airflow and Central backflow area entrainment after the high-temperature synthesis gas of returning mixes, and lighted, form slag at gasification hearth 3 top combustion by it.Nitrogen or carbonic acid gas carry flying dust (mass ratio of the flying dust and coal dust that pass into gasification hearth 3 is 0 ~ 1:4) and tangentially spray into gasification hearth 3 by flying dust spout 8, form slag after entering burner hearth under high temperature.Vaporized chemical after preheating tangentially sprays into gasification hearth 3 at a high speed through vaporized chemical spout 7, is subject to the restriction of furnace wall in gasification hearth 3, forms the strong vaporized chemical air-flow rotated.Under the injection of this strand of strong rotary pneumatic agent air-flow, the slag that the slag that flying dust is formed, coal dust firing are formed, the high-temperature synthesis gas of entrainmenting rotate near wall district and flow downward together with vaporized chemical air-flow; Be subject to the strong effect rotating the centrifugal force produced, the slag of about 80% is thrown on wall, forms the uniform thicker liquid slag blanket of one deck.The remaining slag of about 20%, the high-temperature synthesis gas of entrainmenting and vaporized chemical air-flow mix and continue to rotate near wall district to flow downward.Slag blanket slowly flows downward along wall, and the strong mixed airflow rotated then constantly washes away wall slag blanket, and in the process, the vaporized chemical in mixed airflow constantly with the slag in wall slag blanket, mixed airflow, strong gasification reaction occurs.Reacted wall slag blanket continues to flow downward along wall, is discharged after entering slag bath cooling by slag-drip opening.Rotate the continuous generating gasification reaction of downward mixed airflow, when arriving vapourizing furnace bottom, become the synthesis gas flow of high temperature.Because mixed airflow is in nearly furnace wall district rotational flow, the pressure at burner hearth center is relatively low, and the synthetic gas of vapourizing furnace bottom is subject to Involving velocity, at burner hearth central upward flow, forms stable high temperature center recirculating zone.The high-temperature synthesis gas that high temperature center recirculating zone is entrainmented is back to vapourizing furnace top, lights the breeze airflow sprayed into by coal dust burner 1, and then enter near wall region rotate move downward.Finally, the synthetic gas of generation flows out from synthetic gas passage 5.
Application example 1:
The vapourizing furnace of an application consumption of coal 1000t/d of the present invention, there is not scaling loss in predicted operation 4 years water wall, can ensure that lasting operation is not stopped for 4 years, compare other technology, reduces financial loss 1.6 hundred million yuan.Numerical evaluation checking is learnt: this TV station vapourizing furnace wall thickness of slag layer is 6mm, slag blanket is thicker and even, coal dust residing time in furnace is 14s, the residence time is longer, and gasification agent inlet place coal dust and vaporized chemical speed of relative movement are about 150m/s, and syngas outlet place coal dust and vaporized chemical speed of relative movement are about 75m/s, coal dust and vaporized chemical average relative are about 115m/s, coal dust and vaporized chemical speed of relative movement high, it is rapid that gas is diffused into particle surface, and speed of reaction is high.This vapourizing furnace day process flying dust amount is up to 500t/d, can save the expense of a large amount of process flying dust, effectively make use of the carbon residue in flying dust simultaneously, improve the effective rate of utilization of the energy.
Certain chemical plant adopts the vapourizing furnace of a consumption of coal 1000t/d of general technology, coal dust is about 5s at residing time in furnace, the speed of relative movement of vaporized chemical and slag is about 0.1m/s, wall-cooling surface slag film thickness is thinner, about 2mm, and slag non-uniform film thickness is even, internal partial wall face is exposed in high-temperature flue gas environment, the easy scaling loss of inner-wall surface, stops once because of inner-wall surface scaling loss every year on average, often stops and once cause total financial loss about 4,000 ten thousand yuan.This vapourizing furnace day generates flying dust about 50 tons, and generate flying dust amount year up to 1.65 ten thousand tons, about 1.8 ten thousand steres need be digged pit for landfill disposal flying dust by annual enterprise.
Claims (10)
1. a vaporized chemical rotates by force coal dust and flying dust mixes burning gasifying furnace device, described a kind of vaporized chemical rotates by force coal dust and flying dust and mixes and burn gasifying furnace device and comprise coal dust burner (1), gasification body of heater (2), water wall (4), synthetic gas passage (5) and slag bath (6), water wall (4) is arranged on the inner side-wall of gasification body of heater (2), water wall (4) is made up of several Vertically tube, the solid of revolution inner chamber surrounded by water wall (4) is gasification hearth (3), slag bath (6) is positioned at gasification body of heater (2) bottom, synthetic gas passage (5) is arranged on gasification body of heater (2) middle and lower part, and synthetic gas passage (5) is communicated with gasification hearth (3), it is characterized in that: described a kind of vaporized chemical rotates by force coal dust and flying dust and mixes and burn gasifying furnace device and also comprise vaporized chemical spout (7), flying dust spout (8) and dust conveying system, vaporized chemical spout (7) and flying dust spout (8) are all installed on body of heater column part top, vaporized chemical spout (7) inserts in gasification hearth (3) along the tangential direction of gasification hearth (3), the axis of flying dust spout (8) and the axis of vaporized chemical spout (7) are located in the same horizontal plane, the axis of flying dust spout (8) is 5 ° ~ 30 ° with the angle (α) of vapourizing furnace secant (M) in the horizontal direction, vapourizing furnace secant (M) is parallel to the axis of vaporized chemical spout (7), the input terminus of described flying dust spout (8) is connected with the output terminal of dust conveying system, described coal dust burner (1) comprises swirl vane (9) and the coal dust channel 10 of annular, the bottom of coal dust channel 10 is provided with swirl vane (9), described coal dust burner (1) is arranged on the top of gasification body of heater (2), and the dead in line of the axis of coal dust burner (1) and gasification hearth (3).
2. a kind of vaporized chemical according to claim 1 rotates by force coal dust and flying dust mixes burning gasifying furnace device, it is characterized in that: the axis of described flying dust spout (8) is 10 ° with the angle (α) of vapourizing furnace secant (M) in the horizontal direction.
3. a kind of vaporized chemical according to claim 1 rotates by force coal dust and flying dust mixes burning gasifying furnace device, it is characterized in that: the axis of described flying dust spout (8) is 20 ° with the angle (α) of vapourizing furnace secant (M) in the horizontal direction.
4. a kind of vaporized chemical according to claim 1 rotates by force coal dust and flying dust mixes burning gasifying furnace device, it is characterized in that: described dust conveying system comprises powder storehouse (11), powder storehouse valve (12), lock hopper (13), lock hopper valve (14), flying dust to batch can (15) and flying dust feed tank valve (16), and powder storehouse (11), powder storehouse valve (12), lock hopper (13), lock hopper valve (14), flying dust are connected with flying dust feed tank valve (16) from top to bottom successively to batch can (15).
5. utilize the device described in claim 1 to realize vaporized chemical and rotate by force coal dust and flying dust mixes a burning gasification process, it is characterized in that: described method is realized by following steps:
Step one: setting gasification hearth (3) internal pressure is 0.1MPa ~ 4MPa, and the operating temperature of gasification hearth 3 is 1250 ~ 1600 DEG C;
Step 2: temperature is that the dry pulverized coal of 25 DEG C ~ 100 DEG C carries with the coal dust channel (10) feeding gasification hearth (3) of cyclone mode on coal dust burner (1) inner by nitrogen or carbonic acid gas, formed in furnace roof region and rotate downward breeze airflow, wherein dry pulverized coal accounts for 1% ~ 25% of dry pulverized coal and nitrogen mixture cumulative volume;
Step 3: dry coal powder airflow touches after Central backflow area entrainments the high-temperature synthesis gas of returning, and is lighted, form slag at gasification hearth (3) top combustion by high-temperature synthesis gas;
Step 4: flying dust is stored in powder storehouse (11), open powder storehouse valve (12) afterwards flying dust by gravity fall in lock hopper (13), close powder storehouse valve (12), when lock hopper (13) is forced into and is greater than flying dust to batch can (15) internal pressure, open lock hopper valve (14), flying dust flows into flying dust in batch can (15), close lock hopper valve (14), after passing into high pressure nitrogen or carbonic acid gas by high-pressure delivery gas feed (15-1), temperature is that the flying dust of 25 DEG C ~ 100 DEG C is carried by nitrogen or carbonic acid gas and tangentially sprays in gasification hearth (3) through flying dust spout (8), wherein flying dust accounts for 1% ~ 25% of flying dust and nitrogen mixture cumulative volume, flying dust forms slag after entering gasification hearth (3) under high temperature action, the ratio of the described flying dust and quality of pc that pass into gasification hearth (3) is 0 ~ 1:1,
Step 5: temperature is that the vaporized chemical of 20 DEG C ~ 400 DEG C tangentially sprays into gasification hearth (3) by vaporized chemical spout (7) with the speed of 100m/s ~ 200m/s, vaporized chemical air-flow at a high speed pours gasification hearth (3) and forms strong swirling eddy afterwards, under the influence of centrifugal force, the slag of 80% is thrown to face, furnace wall and forms thicker slag blanket, slag blanket is even, swirling eddy constantly washes away the slag blanket on burner hearth wall, and gasification reaction strong in its generation;
Step 6: the raw gas that gasification generates flows out gasification hearth (3) by synthetic gas passage (5), the liquid slag generated flows into slag bath (6) along wall, discharges gasification body of heater (2) after cooling by bottom slag discharge.
6. a kind of vaporized chemical according to claim 5 rotates by force coal dust and flying dust mixes burning gasification process, it is characterized in that: setting gasification hearth (3) internal pressure in described step one is 2.5MPa, the operating temperature of gasification hearth (3) is 1500 DEG C.
7. a kind of vaporized chemical according to claim 5 rotates by force coal dust and flying dust mixes burning gasification process, it is characterized in that: in described step 2, dry pulverized coal accounts for 10% of dry pulverized coal and nitrogen mixture cumulative volume.
8. a kind of vaporized chemical according to claim 5 rotates by force coal dust and flying dust mixes burning gasification process, it is characterized in that: in described step 2, dry pulverized coal accounts for 20% of dry pulverized coal and nitrogen mixture cumulative volume.
9. a kind of vaporized chemical according to claim 5 rotates by force coal dust and flying dust mixes burning gasification process, it is characterized in that: in described step 4, flying dust accounts for 10% of defeated powder gas and fly ash mixture cumulative volume, described in pass into gasification hearth (3) the ratio of flying dust and quality of pc be 0.5:1.
10. a kind of vaporized chemical according to claim 5 rotates by force coal dust and flying dust mixes burning gasification process, it is characterized in that: in described step 5, temperature is that the vaporized chemical of 300 DEG C tangentially sprays into gasification hearth (3) by vaporized chemical spout (7) with the speed of 150m/s.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510579057.6A CN105199782A (en) | 2015-09-11 | 2015-09-11 | Gasification agent, strong-rotating pulverized coal and fly ash mixed-burning gasifier device and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510579057.6A CN105199782A (en) | 2015-09-11 | 2015-09-11 | Gasification agent, strong-rotating pulverized coal and fly ash mixed-burning gasifier device and method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105199782A true CN105199782A (en) | 2015-12-30 |
Family
ID=54947745
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510579057.6A Pending CN105199782A (en) | 2015-09-11 | 2015-09-11 | Gasification agent, strong-rotating pulverized coal and fly ash mixed-burning gasifier device and method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105199782A (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105542866A (en) * | 2016-01-25 | 2016-05-04 | 新疆心连心能源化工有限公司 | Pulverized gas technology |
| CN105602625A (en) * | 2016-03-14 | 2016-05-25 | 鲁西化工集团股份有限公司煤化工分公司 | Novel technique for recycling fly ash |
| CN105950221A (en) * | 2016-07-14 | 2016-09-21 | 哈尔滨工业大学 | Gasification agent strong-rotation pulverized coal gasifier and gasification method |
| CN106221813A (en) * | 2016-07-14 | 2016-12-14 | 哈尔滨工业大学 | A kind of " water bag oxygen " preventing furnace wall scaling loss rotates by force powder coal gasification furnace |
| CN107267219A (en) * | 2017-08-01 | 2017-10-20 | 中国科学院工程热物理研究所 | The circulating fluidized bed gasification device and gasification process of tangential air distribution |
| WO2022121108A1 (en) * | 2020-12-07 | 2022-06-16 | 中国华能集团清洁能源技术研究院有限公司 | Fly ash recycling gasifier having fly ash burner and operating method therefor |
| CN114653717A (en) * | 2022-03-31 | 2022-06-24 | 西安热工研究院有限公司 | Device and method for harmlessly treating waste incineration fly ash |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60173092A (en) * | 1984-02-20 | 1985-09-06 | Hitachi Ltd | Coal gasifying oven |
| US4773917A (en) * | 1983-03-28 | 1988-09-27 | Babcock-Hitachi Kabushiki Kaisha | Coal gasifier |
| CN101712891A (en) * | 2008-10-07 | 2010-05-26 | 顾鸣海 | Solid fuel combustion and gasification device of fluidized bed or jetting bed with flying ash multiple coal gasification device |
| CN102796567A (en) * | 2012-08-24 | 2012-11-28 | 清华大学 | Coal water slurry cyclone entrained flow gasifier and gasification method thereof |
| CN102796566A (en) * | 2012-08-24 | 2012-11-28 | 清华大学 | Dry pulverized coal cyclone entrained flow bed gasification furnace and gasification method thereof |
| CN102911740A (en) * | 2012-09-28 | 2013-02-06 | 上海锅炉厂有限公司 | Two-section gasifying device of entrained-flow bed and gasifying method of two-section gasifying device |
| CN102942964A (en) * | 2012-10-29 | 2013-02-27 | 哈尔滨工业大学 | Apparatus and method for coal powder cyclone entrained flow gasification |
| CN103224813A (en) * | 2013-04-15 | 2013-07-31 | 中国五环工程有限公司 | Pressurized fluidized bed technology for coal gasification and pressurized fluidized bed system |
| CN104531219A (en) * | 2014-12-16 | 2015-04-22 | 中石化宁波工程有限公司 | Pressure gasification process for simultaneously gasifying powdered coal and coal water slurry |
| CN104593086A (en) * | 2015-01-30 | 2015-05-06 | 哈尔滨工业大学 | Undok pulverized coal gasification furnace with nitrogen, water vapor and synthesis gas-driven material return mechanism |
-
2015
- 2015-09-11 CN CN201510579057.6A patent/CN105199782A/en active Pending
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4773917A (en) * | 1983-03-28 | 1988-09-27 | Babcock-Hitachi Kabushiki Kaisha | Coal gasifier |
| JPS60173092A (en) * | 1984-02-20 | 1985-09-06 | Hitachi Ltd | Coal gasifying oven |
| CN101712891A (en) * | 2008-10-07 | 2010-05-26 | 顾鸣海 | Solid fuel combustion and gasification device of fluidized bed or jetting bed with flying ash multiple coal gasification device |
| CN102796567A (en) * | 2012-08-24 | 2012-11-28 | 清华大学 | Coal water slurry cyclone entrained flow gasifier and gasification method thereof |
| CN102796566A (en) * | 2012-08-24 | 2012-11-28 | 清华大学 | Dry pulverized coal cyclone entrained flow bed gasification furnace and gasification method thereof |
| CN102911740A (en) * | 2012-09-28 | 2013-02-06 | 上海锅炉厂有限公司 | Two-section gasifying device of entrained-flow bed and gasifying method of two-section gasifying device |
| CN102942964A (en) * | 2012-10-29 | 2013-02-27 | 哈尔滨工业大学 | Apparatus and method for coal powder cyclone entrained flow gasification |
| CN103224813A (en) * | 2013-04-15 | 2013-07-31 | 中国五环工程有限公司 | Pressurized fluidized bed technology for coal gasification and pressurized fluidized bed system |
| CN104531219A (en) * | 2014-12-16 | 2015-04-22 | 中石化宁波工程有限公司 | Pressure gasification process for simultaneously gasifying powdered coal and coal water slurry |
| CN104593086A (en) * | 2015-01-30 | 2015-05-06 | 哈尔滨工业大学 | Undok pulverized coal gasification furnace with nitrogen, water vapor and synthesis gas-driven material return mechanism |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105542866A (en) * | 2016-01-25 | 2016-05-04 | 新疆心连心能源化工有限公司 | Pulverized gas technology |
| CN105602625A (en) * | 2016-03-14 | 2016-05-25 | 鲁西化工集团股份有限公司煤化工分公司 | Novel technique for recycling fly ash |
| CN105950221A (en) * | 2016-07-14 | 2016-09-21 | 哈尔滨工业大学 | Gasification agent strong-rotation pulverized coal gasifier and gasification method |
| CN106221813A (en) * | 2016-07-14 | 2016-12-14 | 哈尔滨工业大学 | A kind of " water bag oxygen " preventing furnace wall scaling loss rotates by force powder coal gasification furnace |
| CN105950221B (en) * | 2016-07-14 | 2018-09-11 | 哈尔滨工业大学 | A kind of gasifying agent rotates by force powder coal gasification furnace and gasification process |
| CN106221813B (en) * | 2016-07-14 | 2018-10-02 | 哈尔滨工业大学 | A kind of " the water packet oxygen " preventing furnace wall scaling loss rotates by force powder coal gasification furnace |
| CN107267219A (en) * | 2017-08-01 | 2017-10-20 | 中国科学院工程热物理研究所 | The circulating fluidized bed gasification device and gasification process of tangential air distribution |
| CN107267219B (en) * | 2017-08-01 | 2023-05-23 | 中国科学院工程热物理研究所 | Tangential air distribution circulating fluidized bed gasification device and gasification method |
| WO2022121108A1 (en) * | 2020-12-07 | 2022-06-16 | 中国华能集团清洁能源技术研究院有限公司 | Fly ash recycling gasifier having fly ash burner and operating method therefor |
| CN114653717A (en) * | 2022-03-31 | 2022-06-24 | 西安热工研究院有限公司 | Device and method for harmlessly treating waste incineration fly ash |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105199782A (en) | Gasification agent, strong-rotating pulverized coal and fly ash mixed-burning gasifier device and method | |
| CN100366710C (en) | Multi-nozzle coal water mixture or fine coal gasifying furnace and its industrial application | |
| CN101985568B (en) | Two-stage oxygen supply dry slag removal pressurized gas flow bed gasification furnace | |
| CN101220299B (en) | Device and method for production synthesis gas energy conservation and emission reduction of static bed gas making furnace | |
| CN102134512B (en) | Staged powder spraying entrained bed gasification furnace and gasification method thereof | |
| CN1328356C (en) | Gasification of dry-powder solid fuel | |
| WO2017041338A1 (en) | Intensified rotating coal dust gasification apparatus having multi-stage gasification agent provision and gasification method | |
| CN104629807A (en) | Chilling process gasifier with high-temperature heat recovery unit | |
| CN203360394U (en) | Coal gasification device utilizing waste heat of high-temperature molten slag | |
| CN105087074A (en) | Gasifier device and method for gasifying pulverized coal by simultaneously feeding gasifying agents from top burner and furnace body layer by layer and strongly rotating gasifying agents | |
| CN103232860B (en) | High-intensity gasification reactor | |
| CN102816605A (en) | Two-section type multi-nozzle gasifying furnace with hierarchical oxygen supplying function and gasifying method of gasifying furnace | |
| CN105087835A (en) | System and method for recycling high-temperature slag waste heat in coal gasification manner | |
| CN204756903U (en) | Living beings combustion apparatus that partly gasifies | |
| CN104593083A (en) | Novel biomass step-by-step gasification method and device | |
| CN201850256U (en) | Process burner and system for gasifying water coal slurry | |
| CN105087075A (en) | Device and method for gasifying pulverized coal through stratified strong rotation of gasifying agents along furnace height | |
| CN105087073A (en) | Device and method for gasifying pulverized coal through multistage feeding and strong rotation of gasifying agents | |
| CN101570699B (en) | Gasification device for solid fuel and method for producing synthetic gas | |
| CN104879746A (en) | Biomass semi-gasification combustion equipment | |
| CN102517088A (en) | Novel gasification furnace of pressurized aerated bed | |
| CN203960148U (en) | A kind of airflow bed gasification furnace | |
| CN204417437U (en) | A kind of novel biomass substep gasification installation | |
| CN105219442A (en) | Top and body of heater feed vaporized chemical simultaneously and rotate by force pulverized coal gasification furnace device and method | |
| CN105176592A (en) | Strong-rotation pulverized coal gasification device with gasifying agents arranged in circumferential direction in staggered manner and gasification method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20151230 |
|
| RJ01 | Rejection of invention patent application after publication |