CN1400289A - Powdered coal fluidized bed gasification method and gasification furnace - Google Patents
Powdered coal fluidized bed gasification method and gasification furnace Download PDFInfo
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- CN1400289A CN1400289A CN 01123960 CN01123960A CN1400289A CN 1400289 A CN1400289 A CN 1400289A CN 01123960 CN01123960 CN 01123960 CN 01123960 A CN01123960 A CN 01123960A CN 1400289 A CN1400289 A CN 1400289A
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Abstract
The present invention relates to a powdered coal fluidized gasification method and its gasification furnace, and is aimed at providing a tech chnique for effectively solving the "vomiting and diarrhea" problem of existent fluidized gasification furnace. Said invention is characterized by that it utilizes pneuamtic separation process to separate out fine powder from coal firstly, after the fine powder is formed, said fine powder can be fed into gasification furnace; gasification agent is fed into dense-phase section of gasification furance by means of combined nozzle, coal can be combusted in high-temp. combustion section, the ash can be agglomerated, discharged from throat-tube structure, cooled in heat exchanger, and first-level fly ash is combusted in combustor and fed into furance and second-level fly ash is combined with adhesive coal powder, dry-distilled and coked.
Description
The present invention relates to a kind of powdered coal fluidized bed gasification method and device.It belongs to the gasification of coal field.
Comparatively advanced at present powdered coal fluidized bed gasification stove is a raw material with fine coal (0-10mm), can adapt to multiple metamorphic grade coal and high grey low-quality coal gasification, gasification intensity occupies between fixed bed and the air flow bed, gasification does not have the tar pollution thing, gasification operation temperature moderate (900-1100 ℃) can adopt conventional equipment material and control techniques.Its shortcoming is still to have its distinctive " suffering from vomiting and diarrhoea " problem, and the gasification efficiency of its process is restricted.So-called " on tell " refers in gasification, a large amount of flying dusts leave vapourizing furnace with coal gas, though taked cyclone dust removal, the operation of flying dust round-robin at present, facts have proved that these methods can not thoroughly solve the flying dust problem, flying dust is recycled into stove, can not be transformed effectively as imagination ground, but be taken out of outside the stove again very soon, production process constantly produces fine powder, flying dust constantly accumulates, and causes the problems such as obstruction, wearing and tearing and pollution of the follow-up system of coal gas; So-called " dropping " refers in the lime-ash that vapourizing furnace discharges and contains a large amount of carbon.Because bed material intense mixing in the fluidized-bed gasification furnace, when adopting the ordinary method ash discharge, the solid in the discharge is formed may be similar to gasification siege material, thereby its carbon containing is very high; Existing development and the ash cohesive technology of using can make the high problem of ash discharge carbon containing be improved or solution to a certain extent, but existing inappropriate design can not guarantee to reduce reaching of ash discharge carbon containing purpose.Flying dust carbon containing height and lime-ash carbon containing height not only cause the gasification Energy efficiency low, and cause the environmental pollution of solid flying dust.The existence of these problems has influenced the development of fluidized-bed gasification technology greatly and has applied.
Technical problem to be solved by this invention is exactly effectively to solve the powdered coal fluidized bed gasification method of " suffering from vomiting and diarrhoea " and the structure of vapourizing furnace thereof, and reach by following measure, the 10mm sieve is crossed in the broken back of feed coal [C0], coal less than 10mm is entered by air separator [E1] top, enter from the air [K0] of gas blower bottom by air separator [E1], air-flow from bottom to top contacts with coal facies, and the moisture of coal particle surface enters in the gas.Gas tangentially enters to be increased disturbance and prolongs solid retention time, and enhancement moisture enters the effect in the air-flow.Epimere at air separator [E1] also feeds an amount of air-flow, increases disturbance, makes to break away from adherent fine particle of large particle surface and macrobead, thereby guarantees high fine powder separating effect.Carried secretly by air-flow less than the 0.5mm coal charge and to leave air separator [E1], enter in the cyclonic separator [E18], solid is collected in tornado dust collector, and gas is thereafter washed back emptying.Entering on tornado dust collector [E18] pipeline before, an amount of water smoke of auxiliary sprinkling to improve the solid separation efficiency, also can make isolating fine powder material avoid airborne dust simultaneously, is easy to handle.The coal grain of being carried secretly by air-flow [C1] does not then fall in the coal bin, enters vapourizing furnace [E0] through feeder [E16].The solid of collecting in cyclonic separator send in the shaper [E2], adds binding agent [A1], cohesiveness fine coal [A2] and catalyzer [A3] and suitable quantity of water etc. in [E2] simultaneously, adopts extruded moulding machinery at this, finishes the moulding of powder.Before the moulding, coal dust and binding agent, cohesiveness fine coal and catalyzer uniform mixing in the kneading machine device.Binding agent adopts organic types such as spent pulping liquor class, also can adopt the mineral binder bond that contains Ca, Al etc.; Cohesiveness fine coal refers to the fine powder of coals such as the stronger bottle coal of cohesiveness, rich coal; Catalyzer is alkali, salt solid or the liquid substance that technical purity grade or industrial waste contain K, Na etc.The ratio of caking coal and coal dust is a scope between 1: 1 to 1: 4.The catalyzer usage quantity is 2% to 10% of a coal feed weight.Adding an amount of water, to make molding materials moisture be between 5 to 15%.The diameter of extrusion product selects 3 to 6mm.When vapourizing furnace was low voltage operated, extrusion machinery directly was connected with vapourizing furnace, and extruded product directly enters vapourizing furnace dilute phase section.Also can adopt roller forming machinery, add water this moment is 10-20%, and the balling-up particle diameter is 2-5mm, becomes ball particle to send in the moving-bed type drying, at this, adopts 200-250 ℃ stack gas and granular layer counter current drying.The coarse particles material of drying products and air separator output is mixed into vapourizing furnace.The air (or oxygen) of gas blower or compressor [E11] is divided into four the tunnel and enters vapourizing furnace, they are respectively: gas [G1] is the air-flow that carries out heat exchanging part with lime-ash, [G2] is then for entering the air-flow that heat is equipped with the ash-pan slit, lime-ash is blown off from pallet smoothly, and [G1] determined by Venturi control ash discharge speed with the total flux of [G2].Air-flow [G3] is supplied with the vaporized chemical of high temperature combustion zone, [G4] is the main vaporized chemical fluid of vapourizing furnace, it with mix after set of nozzles [E15] enters the close section mutually of vapourizing furnace from the steam [G5] of boiler, keep vapourizing furnace and reach stable fluidization, the ratio height of steam and air is then regulated according to the temperature of vapourizing furnace.Coal generates coal gas with vaporized chemical reaction back in vapourizing furnace, the carbon in the coal particle is progressively consumed simultaneously.Ash in the coal charge is by enrichment and adhesive aggregation, reunion, after the lime-ash that height contains ash is discharged by ash releasing tube [E6] selectivity, after heat is equipped with formula ash-pan [E7] and falls in the moving-bed type interchanger with cold air [G1] heat exchange from the bottom after, [H1] is expelled to [E10] by spiral ash ejector [E9].When leaving vapourizing furnace, still carries gasification gas the part flying dust secretly, isolated flying dust [H2] returns vapourizing furnace and delivers to high temperature combustion zone [E5] after dipleg is delivered to flying dust burner combustion [E17] in one-level tornado dust collector [E12], participate in reignition at this flying dust, and through with the collision of high temperature ash ball adhesive aggregation taking place.And the flying dust of collecting at second cyclone dust extractor [E13] [H3] does not directly enter vapourizing furnace, but deliver in the flying dust Fitz chilsonator [E14], at this, cohesiveness coal dust [A4] is tangentially sprayed into, with from last dispersion and under hot flying dust contact mixing, coal is heated the generation retort process, with the blended flying dust through stages such as softening, melt-flow, curing and contractions, the final semicoke small-particle [H4] with suitable intensity that forms, this part material is returned the raw material coal bin, enters the vapourizing furnace gasification once more.The flying dust granulation is according to following principle design: the cohesiveness fine coal generation retort process of being heated, and flying dust is participated in this process and is formed semicoke together, and destructive distillation institute heat requirement is provided by hot flying dust.The concrete enforcement of flying dust granulation is as follows: flying dust has the high temperature more than 800 ℃, its granularity is generally less than 0.1mm, participate in granulation for having more by force or the coal dust of the caking coal of strong cohesive property very, when in Fitz chilsonator, falling with hot flying dust, cohesiveness coal dust eddy flow sprays into, two kinds of fine powders mix, under 450-750 ℃ of temperature, the cohesiveness coal dust experience retort process of being heated, processes such as softening, the fusion of its generation, curing and semicoke contraction are included in flying dust to be finished together, has been generated the fine particle product thus by fine powder.Granulated deliver to gasified raw material or directly send vapourizing furnace back to gasify.The ratio of caking coal and flying dust is 1: 1 to 1: 2, is determined by the caking index of caking coal and the characteristic of flying dust.
The present invention can also reach by following measure, and the vapourizing furnace that is used for powdered coal fluidized bed gasification method is made up of close phase section [E4], high temperature combustion zone [E5], Venturi ash releasing tube [E6] and hot ash discharge controlling organization [E7], lime-ash aheat exchanger [E8], the ash discharge spiral [E9] etc. of being equipped with of conventional dilute phase section [E3], back taper type respectively from top to bottom.The dilute phase section is further gasification section, contains higher dust concentration in this section air-flow, and the high-temperature gas that leaves close phase section continues the generation coal gas that reacts with it; Close phase section is the low speed fluidization regions, it is the most important region of generating gasification reaction in the vapourizing furnace, the gasification furnace structure of this section adopts the back taper type, will be comprised that by set of nozzles the vaporized chemical of air (or oxygen) and steam is sent in the vapourizing furnace in proportion, and makes the good fluidization of formation in the fluidized-bed.In this section, low-speed mode is adopted in fluidization, and superfacial velocity is 0.5-1.0m/s.Burning of coal and reduction reaction are mainly carried out in this zone, and temperature of reaction is 900 to 1050 ℃, and gasification has produced H
2, CO, CH
4And CO
2Etc. gaseous fraction.
It is that the vapourizing furnace operation realizes ash cohesive, ash reunion that high temperature combustion zone and its combine with ash exhauster, and then reaches the basic assurance of the low target of ash discharge carbon containing.At high temperature combustion zone, when carrying out air gasification, a bubbling air is made fluidisation and gasifying medium; When carrying out pure oxygen or oxygen-rich gasification, also only be added into the steam of lower concentration.Mutually different with the low speed fluidization of close phase section, in this district, adopt medium fluidizing velocity, superfacial velocity is 0.8-1.5m/s.According to fluidization property, the solid particulate in this district will be macrobead bed material and the bigger particle of density.During flowing, the solid circulation of small-particle in bed mainly enter into the close phase section and even the dilute phase section in its outside; To have more at the heavier particle of close phase section, multimachine can enter this middling speed fluidization regions.Because the medial temperature that the temperature that makes in this district will be higher than vapourizing furnace is reacted in the rapid combustion of high oxygen concentration, the ash fusibility softening temperature of controlling this temperature and specific coal ash is close in this district.According to the difference of coal, this district's temperature can be at 1050-1250 ℃.With the carrying out of gasification, for specific particle, its carbon content progressively reduces, and ash content increases.When its ash content is lower than to a certain degree, in case this particle enters into the high-temperature atmosphere, softening, fusion tendency that particle surface occurs; And be between the particle of this state when having an opportunity to bump contact, its surface is bonding mutually; Granose gathering causes particulate " to be grown up ".The particle of growing up carries out ash content with reaction and improves, and pellet density increases; This particle tendency enters high temperature combustion zone, under this high temperature action, particle further take place molten poly-, reunite, strengthened more that particulate " is grown up " and " weightening finish " process.When this particle arrived to a certain degree greatly or heavily, particle was discharged by the control of selectivity dust removing system.
Venturi tube has been applied to selective control ash discharge technology, at this, takes high-speed upward air stream circulation operation.High gas flow speed will make little/light grains blow afloat and carry secretly upwards, and big/heavy particle can not oppositely be fallen with air-flow by picking-up, thereby leaves vapourizing furnace, reaches the purpose of selecting ash discharge.The big young pathbreaker of gas velocity according to vapourizing furnace scale, raw material granularity, coal ash is specific determines, generally in the 7-25m/s scope.
Adopt heat to be equipped with the formula structure in the bottom of control ash releasing tube, this structure is former disc type design, and two up-small and down-big concentric arranged superposed of disk leave slit therebetween.The diameter of bottom disk is by the characteristic decision of stopping of thermal material, and the slope of repose can be got by measuring.Air-flow [G2] sprays at a high speed from slit between two-layer dish after the disc centre inflow of lower floor again.When vapourizing furnace normally moved, the particle ash that is fallen by ash releasing tube dropped on earlier on the upper strata disk [E7], behind spout place between its landing to two dish, was blown out the chassis scope by high velocity air and fell, and no longer rested on the disk.When vapourizing furnace needed blowing out or heat to stop fully, the air-flow in the central row ash pipe stopped, and material flows down by pipe core in the bed; Because disk slit airless, the particulate material of whereabouts will stop on the disk, and particulate material is after filling the set solid ash pipe, and furnace charge no longer falls; Be equipped with to stop need to start once more when driving in heat, only need start each road air-flow respectively, after the ash releasing tube air-flow recovered, solid materials was excluded and returns to normal in the pipe.
Vapourizing furnace when operation, be equipped with the grey solid impurity particle that ash-pan [E7] falls from heat and be in the scorching hot state of high temperature.Moving-bed type heat-exchanger rig [E8] is set in its underpart; Freezing air or oxygen and part steam and high-temperature ash are carried out countercurrent flow, and ash temperature is reduced to below 300 ℃ and sent to ash bin [E10] after ash discharge spiral [E9] is got rid of; Behind the gas heating of grieshoch heat exchange, be equipped with the ash-pan air-flow and enter vapourizing furnace as ash releasing tube gas with heat.The carbon containing that may exist in the lime-ash will with air or oxygen heat exchange contact process in further reaction transform, therefore, the carbon containing of getting rid of lime-ash at last will be very low, generally can reach below the 4-8%.
Leave the coal gas of vapourizing furnace and may carry part flying dust dust secretly, after in one-level tornado dust collector [E12], separating, fine powder [H2] enters the flying dust burner [E17] that its bottom is provided with through primary dipleg, air (or oxygen) is used for combustion-supporting, in [E17], be provided with the coal gas burner noz(zle) on duty that stable burning is used, flying dust after the burning is recycled to the high temperature combustion zone [E5] of vapourizing furnace bottom, when the fine powder dust collides ash cohesive state particle and stick on it, no longer fly out, further reaction makes carbon containing wherein reach the conversion of maximum possible.Avoid the flying dust accumulation thereby reach, reduce the purpose that flying dust is taken out of.
The present invention compared with prior art has following advantage:
1 adopts the strength isolation technique to carry out fine powder separates, and good separating effect, processing power are greatly, granularity control is flexible, process is continuous, environmental influence is little; And that mechanical grading particularly has a screening that necessarily contains wet coal charge to the 0.5mm granularity is very difficult.To in the water capacity, low feed coal carries out after strength separates, fine powder is separated, and more coarse grained surface-moisture is evaporated in the air-flow and is dried, and coal charge can not need further dry and directly add vapourizing furnace through charging system, thereby the simplification Production Flow Chart reduces the baking needed energy consumption.
2 moulding add an amount of cohesiveness coal dust, make moulding product not drying and directly into behind the stove because the effect of cohesiveness coal carbonization causes semicoke intensity height, can efflorescence.This moment, powdered coal formation was simple, and production cost is low.Add catalyzer during the fine powder moulding, the speed of response when catalytic gasification reacts than catalyst-free improves 5 to 10 times.The adding of catalyzer not only improves the throughput of vapourizing furnace greatly, but also can reduce the required service temperature of gasification, raising gas quality; Simultaneously, catalyzer also significantly promotes grey aggregation procedure and ash to absorb the efficient of sulfide in the coal gas.These characteristics are very useful to fluidized-bed gasification old, the low activity coal especially.
The hot formula ash discharge structure fully of the disc type of 3 designs is equipped with startup, the heat of vapourizing furnace and stops, blowing out is very convenient.This structure design is installed simply, regulation and control are flexible, operation is reliable.And existing vapourizing furnace adopts the high-temperature machinery valve, its high-temperature operation, and material requirements height, price are expensive, complicated operation, maintenance capacity are big.Set up the lime-ash heat exchange and burn system, the Energy efficiency of process is further enhanced.
4 ash cohesive, ash reunion controls efficiently, but the ash content of coal of the bed material in the steady decrease fluidized-bed, thus vapourizing furnace is had ready conditions than general vapourizing furnace raising service temperature, last effect is that vaporization ability increases, gas quality improves.
5 vapourizing furnace technology of the present invention will change weakness such as the big and flying dust carbon containing height of ash discharge carbon containing height, flying dust amount that existing vapourizing furnace still exists, and ash will be mainly reunited by discharging the vapourizing furnace bottom through ash cohesive and ash in the coal, and the lime-ash carbon containing is very low, is 4%-8%.Total efficiency of carbon conversion of vapourizing furnace will be increased to 95-99% by present 85-90%.A large amount of flying dusts cause problems such as wearing and tearing, Energy efficiency are low, environmental pollution to be expected to be solved preferably
Fig. 1 is the powdered coal fluidized bed gasification process flow diagram.
Fig. 2 is a powdered coal fluidized bed gasification furnace structure synoptic diagram.
The invention will be further described below in conjunction with accompanying drawing 1.Process system mainly is made up of following components: the air separator E1 of feed coal, fine powder shaper E2, vapourizing furnace gasification section E4, combustion zone E5, heat are equipped with structure E7, ash cooling E8, coal gas dust removal and flying dust burning E17 and cohering of secondary cyclone dust removal flying dust made ball device E14 etc.
Technological process is made up of main following process: the burning of the heat exchange of the separation of raw coal strength, fine powder moulding, vapourizing furnace high-temperature gasification, the high-temp combustion of bed material, the hot control fully of ash discharge, heat ash and cold air, the one-level cyclone dust removal of coal gas and flying dust, the two-stage dust removal of coal gas and flying dust granulation etc.
Feed coal after the fragmentation [C0] is crossed the 10mm sieve, wherein the part less than 10mm enters air separator [E1] top, air [K0] from gas blower enters air separator [E1] bottom, contact with the coal facies that fall from bottom to top, carried secretly by air-flow less than the 0.5mm fine powder material and to leave air separator [E1], collect through gas-solid separator, gas is washed back emptying.The moisture of coal particle surface with the gas contact process in enter gas, gas tangentially enters to be increased disturbance and prolongs solid retention time, promotes moisture and enters effect in the air-flow.The coal grain of not carried secretly by air-flow in air separator [C1] then falls in the coal bin, enters vapourizing furnace [E0] through feeder [E16] and directly participates in gasification reaction.The solid of collecting in gas-solid separator is delivered in the shaper [E2], adds binding agent [A1], cohesiveness fine coal [A2] and catalyzer [A3] and suitable quantity of water etc. in [E2] simultaneously, adopts extruded moulding machinery to carry out the moulding of powder.Before the moulding, coal dust and binding agent, cohesiveness fine coal and catalyzer uniform mixing in the kneading machine device.The ratio of caking coal and coal dust is a scope between 1: 1 to 1: 4.The catalyzer usage quantity is 2% to 10% of a coal feed weight.Adding an amount of water, to make molding materials moisture be between 5 to 15%.The diameter of extrusion product selects 3 to 6mm.When vapourizing furnace was low voltage operated, extrusion machinery directly was connected with vapourizing furnace, and extruded product directly enters vapourizing furnace dilute phase section.Also can adopt the roller forming scheme, add water this moment is 10-20%, and the balling-up particle diameter is 2-5mm, becomes ball particle to send in the moving-bed type drying, at this, adopts 200-250 ℃ stack gas and granular layer counter current drying.After mixing, the coarse particles material of drying products and air separator output enters vapourizing furnace.
The air (or oxygen) of gas blower or compressor [E11] is divided into four the tunnel and enters vapourizing furnace.Gas [G1] is the air-flow that carries out heat exchanging part with lime-ash, and air-flow [G2] enters when heat is equipped with ash-pan slit assurance normal running lime-ash is blown off from pallet smoothly, and the total flux of [G1] and [G2] enters the Venturi ash releasing tube and controls ash discharge speed; Air-flow [G3] is a vaporized chemical of supplying with high temperature combustion zone; [G4] is the main vaporized chemical fluid of vapourizing furnace, it with mix after set of nozzles [E15] enters the close section mutually of vapourizing furnace from the steam [G5] of boiler, keep vapourizing furnace and reach stable fluidization.
Coal generates coal gas with the vaporized chemical pyroreaction in vapourizing furnace, carbon in the coal particle is progressively consumed, ash in the coal charge is by enrichment and adhesive aggregation, reunion, height contains the lime-ash of ash and is discharged by ash releasing tube [E6] selectivity, after heat is equipped with formula ash-pan [E7] and falls in the moving-bed type interchanger with cold air [G1] heat exchange, lime-ash is expelled to ash bin by spiral ash ejector [E9].Gasification gas leaves vapourizing furnace and carry out gas solid separation in one-level tornado dust collector [E12], flying dust [H2] is delivered to flying dust burner combustion [E17] (wherein the value of setting companion nozzle guarantees that combustion processes is stable) through dipleg, participate in reignition with the high temperature combustion zone [E5] that returns vapourizing furnace after the combustion air burning and deliver to vapourizing furnace, and adhesive aggregation takes place with the collision of high temperature ash ball.And deliver in the flying dust Fitz chilsonator [E14] at the flying dust [H3] that second cyclone dust extractor [E13] is collected, cohesiveness coal dust [A4] is tangentially sprayed into wherein, from last dispersion and under hot flying dust contact mixing with coal dust, coal is heated the generation retort process, experience the stages such as softening, melt-flow, curing and contraction with the blended flying dust, the final semicoke small-particle [H4] with suitable intensity that forms, it is returned the raw material coal bin, enters the vapourizing furnace gasification once more.The ratio of caking coal and flying dust is 1: 1 to 1: 2 according to the caking index of coal and the characteristic of flying dust.
Further specify the structure of fluidized-bed gasification furnace below in conjunction with Fig. 2.Vapourizing furnace is made up of close phase section [E4], high temperature combustion zone [E5], Venturi ash releasing tube [E6] and hot ash discharge controlling organization [E7], lime-ash aheat exchanger [E8], the ash discharge spiral [E9] etc. of being equipped with of dilute phase section [E3], back taper type respectively from top to bottom.Coal and vaporized chemical carry out high-temp combustion and gasification reduction reaction production coal gas in vapourizing furnace, and lime-ash is discharged from vapourizing furnace.Vaporized chemical divides four the tunnel to enter vapourizing furnace, and coal gas is left by top of gasification furnace.
Dilute phase section E3 is columnar structured, gas links to each other with the close section mutually of bottom, carry higher fine particle flying dust concentration in the high-temperature gas from close phase section secretly, fine particle and gas continue to take place gas-solid mutually or the gas gas-phase reaction in this section, and feed coal is from dilute phase section adding vapourizing furnace; Close phase section E4 comprises the cylinder and the inverted cone part of dilute phase pars infrasegmentalis, comprise air G4 (or oxygen) and steam G5 vaporized chemical that the built up nozzle E15 that evenly arranges along the cone segments circumference will be mixed in proportion are sent in the vapourizing furnace, and make the fluidized-bed main body form good fluidization.The superfacial velocity of this section is 0.5-1.0m/s.In temperature is that burning of coal and reduction reaction have produced H under 900 to 1050 ℃ of conditions
2, CO, CH
4And CO
2Etc. gaseous fraction.
High temperature combustion zone E5 is little cylindrical structure, and its top links to each other with cone E4, and bottom and ash releasing tube E6 join, and its inside is provided with air distribution plate, and flying dust round-robin inlet is arranged in the side of cylindrical shell.When carrying out air gasification, air G3 enters this district by air distribution plate and makes fluidizing medium; When carrying out pure oxygen or oxygen-rich gasification, also only be added into the steam of lower concentration.Distinguishing apparent fluidizing velocity at this is 0.8-1.5m/s, compares with emulsion zone, and the solid particulate in this district will be mainly macrobead bed material and the bigger particle of density.In this district, the rapid combustion reaction of high oxygen concentration makes the temperature in this district will be higher than the medial temperature of vapourizing furnace, and bed is expected coal ash generation adhesive aggregation or reunion, and carbon is further burnt cinder in the lime-ash.The high temperature flying dust circulation that comes from one-level flying dust burner E17 enters local area and participates in further combustion reactions, and flying dust and high-temperature particle collide and participate in adhesive aggregation, and flying dust is no longer taken out of with gas with particulate form alone.According to the difference of coal, this district's temperature can be at 1050-1250 ℃.
Ash releasing tube E6 with throat tubular construction is used to carry out selectivity ash discharge control, joins with high temperature combustion zone E5 on it, and the bottom connects ash discharge heat and is equipped with structure and lime-ash cooling structure.Cross ash releasing tube from the air communication of its underpart and enter vapourizing furnace, take high gas flow velocity range (generally at 7-25m/s) operation.When high velocity air entered vapourizing furnace, small and light particle was blown afloat and is carried secretly upwards, and big and heavy particle can not oppositely fall by picking-up and with air-flow and leave vapourizing furnace.
It is former disc type design that the heat that is connected with control ash releasing tube E6 is equipped with the formula structure, and two up-small and down-big concentric arranged superposed of disk leave slit therebetween.The diameter of bottom disk is by the characteristic decision of stopping of thermal material.Air-flow [G2] sprays at a high speed from slit between two-layer dish after the disc centre inflow of lower floor again.When vapourizing furnace normally moved, the particle ash that is fallen by ash releasing tube dropped on earlier on the upper strata disk [E7], behind spout place between its landing to two dish, was blown out the chassis scope by high velocity air and fell, and no longer rested on the disk.When vapourizing furnace needed blowing out or heat to stop fully, the air-flow in the central row ash pipe stopped, and material flows down by pipe core in the bed; Because disk slit airless, the particulate material of whereabouts will stop on the disk, and particulate material is after filling the set solid ash pipe, and furnace charge no longer falls; Be equipped with to stop need to start once more when driving in heat, only need start each road air-flow respectively, after the ash releasing tube air-flow recovered, solid materials was excluded and returns to normal in the pipe.
The bottom that is equipped with structure in heat is provided with moving-bed type heat-exchanger rig [E8]; Freezing air or oxygen and part steam and high-temperature ash are carried out countercurrent flow, and ash temperature is reduced to below 300 ℃ and sent to ash bin [E10] after ash discharge spiral [E9] is got rid of; Be equipped with the ash-pan air-flow with heat behind the gas heating of grieshoch heat exchange and mix as ash releasing tube gas and enter vapourizing furnace.The carbon containing that may exist in the lime-ash will with air or oxygen heat exchange contact process in further reaction transform.
The coal gas that gasification produces leaves from top of gasification furnace, carries out gas solid separation in one-level tornado dust collector [E12], and fine powder is recycled into stove after burning in flying dust burner [E17].
Claims (2)
1, a kind of powdered coal fluidized bed gasification method, it is characterized in that sending in the air separator [E1] through the feed coal [C0] that broken and 10mm sieve, air [K0] from gas blower is entered by [E1] bottom, gas is accelerated at the epimere of [E1], contact with [C0] material, being carried secretly by air-flow less than the 0.5mm coal charge in [C0] sent in the shaper [E2] after separating, and rest materials [C1] then falls to coal bin and adds vapourizing furnace through the metered charge device; In [E2], add binding agent [A1], cohesiveness fine coal [A2] and catalyzer [A3] and suitable quantity of water etc. simultaneously, directly clamp-on in the vapourizing furnace through the material of moulding; Be divided into four the tunnel from the air (or oxygen) of gas blower/compressor [E11] and enter vapourizing furnace respectively, they are respectively: gas [G1] is the air that carries out heat exchanging part with lime-ash, [G2] is then for entering the air-flow that heat is equipped with the ash-pan slit, [G1] enters vapourizing furnace with the mixed gas of [G2] by the Venturi control tube, air-flow [G3] is supplied with high temperature combustion zone, [G4] is the main vaporized chemical fluid of vapourizing furnace, it with mix after set of nozzles [E15] enters the close section mutually of vapourizing furnace from the steam [G5] of boiler, keep vapourizing furnace and reach stable fluidization; High temperature combustion zone [E5] adopts middling speed fluidization operation, ash in gasification is protected in the coal charge is by enrichment and adhesive aggregation, reunion, after the lime-ash that height contains ash is discharged by ash releasing tube [E6] selectivity, after heat is equipped with formula ash-pan [E7] and falls in the moving-bed type interchanger with cold air [G1] heat exchange from the bottom after, [H1] is expelled to [E10] by the spiral ash ejector; When leaving vapourizing furnace, still carries gasification gas the part flying dust secretly, isolated flying dust [H2] send flying dust burner [E17] in one-level tornado dust collector [E12], after the burning of this and combustion air, return vapourizing furnace and deliver to high temperature combustion zone [E5], participate in reignition at this flying dust, and through with the collision of high temperature ash ball adhesive aggregation taking place; And deliver in the flying dust Fitz chilsonator [E14] at the flying dust [H3] that second cyclone dust extractor [E13] is collected, at this, cohesiveness coal dust [A4] is tangentially sprayed into, with from last dispersion and under the mixing that contacts of hot flying dust, coal is heated the generation retort process, through stages such as softening, melt-flow, curing and contractions, finally forms the semicoke small-particle [H4] with suitable intensity with the blended flying dust, this part material is returned the raw material coal bin, enters the vapourizing furnace gasification once more.
2 one kinds of vapourizing furnaces that are used for claim 1 powdered coal fluidized bed gasification method is characterized in that being made up of close phase section [E4], high temperature combustion zone [E5], Venturi ash releasing tube [E6] and hot ash discharge controlling organization [E7], lime-ash aheat exchanger [E8], the ash discharge spiral [E9] etc. of being equipped with of conventional dilute phase section [E3], back taper type respectively from bottom to top; Dilute phase section E3 is columnar structured, continues to react from the high-temperature gas of close phase section and the fine particle flying dust of carrying secretly; Close phase section [E4] comprises the cylinder and the inverted cone part of dilute phase pars infrasegmentalis, and comprise air [G4] (or oxygen) and steam [G5] vaporized chemical that the built up nozzle of evenly arranging along the cone segments circumference [E15] will be mixed in proportion are sent in the vapourizing furnace; High temperature combustion zone [E5] is little cylindrical structure, its top links to each other with cone [E4], the bottom joins with ash releasing tube [E6], its inside is provided with air distribution plate, flying dust round-robin inlet is arranged in the side of cylindrical shell, air [G3] enters this district by air distribution plate and makes fluidizing medium and carry out combustion reactions, and the high temperature flying dust circulation that comes from one-level flying dust burner [E17] enters this district; Ash releasing tube [E6] with throat tubular construction carries out selectivity ash discharge control, the bottom connects ash discharge heat and is equipped with structure and lime-ash cooling structure, cross ash releasing tube from the air communication of its underpart and enter vapourizing furnace, when high velocity air enters vapourizing furnace, in the stove in the material big and heavy particle can not be fallen by picking-up and leave vapourizing furnace; It is former disc type design that the heat that is connected in control ash releasing tube [E6] bottom is equipped with the formula structure, and two up-small and down-big concentric arranged superposed of disk leave slit therebetween, and air-flow [G2] sprays at a high speed from slit between two-layer dish after the disc centre inflow of lower floor again; The bottom that is equipped with structure in heat is moving-bed type heat-exchanger rig [E8]; Freezing air [G1] (or oxygen and part steam) carries out countercurrent flow with high-temperature ash, and the carbon residue that may exist in the lime-ash will further react with oxygen, and ash temperature is reduced to below 300 ℃ and sent to ash bin [E10] after ash discharge spiral [E9] is got rid of; Be equipped with the ash-pan air-flow with heat behind the gas heating of grieshoch heat exchange and mix as ash releasing tube gas and enter vapourizing furnace.
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