CN205062002U - Fluidized bed gasifica tion stove - Google Patents
Fluidized bed gasifica tion stove Download PDFInfo
- Publication number
- CN205062002U CN205062002U CN201520805029.7U CN201520805029U CN205062002U CN 205062002 U CN205062002 U CN 205062002U CN 201520805029 U CN201520805029 U CN 201520805029U CN 205062002 U CN205062002 U CN 205062002U
- Authority
- CN
- China
- Prior art keywords
- fluidized
- bed
- gas distribution
- orifice plate
- distribution orifice
- 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.)
- Active
Links
Landscapes
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The utility model relates to a coal gasification field especially relates to a fluidized bed gasifica tion stove. Can forming in each laminarization bed in the fluidized bed gasifica tion stove and stabilizing the flow field, the back mixing of buggy flows in each laminarization bed of reinforcing upper portion, can improve methane content in the product gas, improves the efficiency of carbon con version of buggy, prevents that the material fluidization from causing the overflow pipe wearing and tearing and blockking up the maintenance and the maintenance of the overflow pipe of being convenient for. An embodiment of the utility model provides a fluidized bed gasifica tion stove, include: a housing, from the top down is provided with at least two -stage gas distribution orifice plate in the interval in proper order in the casing, and the gas distribution orifice plate except that the gas distribution orifice plate of bottommost will the space separation of the gas distribution orifice plate top of bottommost is at least two -layer fluidized bed, and except that the bottommost fluidized bed was bubbling fluidized bed, other each laminarization beds were the efflux fluidized bed, and from the top down is every two -layer adjacent the fluidized bed communicates through at least one overflow pipe respectively, and each the overflow pipe is located the outside of casing.
Description
Technical field
The utility model relates to gasification field, particularly relates to a kind of fluidized-bed gasification furnace.
Background technology
Catalytic coal gasifaction prepares a kind of important way that the clean energies such as methane have become Coal Clean efficiency utilization.In coal catalytic gasification technique, coal and vaporized chemical (mainly comprising water vapour, hydrogen, carbon monoxide etc.) issue raw catalytic coal gasification in the katalysis of catalyzer, generate and are rich in methane coal gas.
In order to improve the efficiency of carbon conversion of catalytic coal gasifaction, providing a kind of multistage gasifying process in prior art, namely adopting multiple vapourizing furnace to carry out classification gasification to coal, this technique, owing to adopting multiple vapourizing furnace, makes facility investment higher, operates more complicated.In order to reduce costs, improve operation efficiency, prior art additionally provides a kind of stratified carburation technique, namely layering is carried out to the space in fluidized-bed gasification furnace, and upflow tube is set in described vapourizing furnace inside, enter the coal dust in each sheaf space and issue soft coal gasification reaction in the rheomorphism of vaporized chemical, coal dust is in constantly kinestate, when the height of coal dust in each sheaf space is greater than the inlet height of described upflow tube, coal dust proceeds reaction in continuous reaction process in described upflow tube overflow to next sheaf space, therefore, the residence time of coal dust in vapourizing furnace can be improved, thus the comprehensive utilization ratio of coal dust can be improved.But in this stratified carburation technique, the flow field that every layer of material is formed is substantially identical, easily to be subject in next adjacent sheaf space generate the impact of fluidized gas, cause the abnormal operating state such as defluidization, ditch flow short-circuit, simultaneously due to violent flow and the shock of gas-solid particle in stove, in described stove, upflow tube is easily worn, and affects normal productive process.
Utility model content
Main purpose of the present utility model is, a kind of fluidized-bed gasification furnace is provided, uniform and stable flow field can be formed in each laminarization bed in described fluidized-bed gasification furnace, strengthen the back-mixing flowing of coal dust in each laminarization bed in top, methane content in gas product can be improved, improve the efficiency of carbon conversion of coal dust, prevent goods fluid from causing upflow tube to wear and tear and blocking, be convenient to maintenance and the maintenance of upflow tube.
For achieving the above object, the utility model adopts following technical scheme:
The utility model embodiment provides a kind of fluidized-bed gasification furnace, comprise: in described housing, be arranged at intervals with at least two-stage gas distribution orifice from top to bottom successively, separated by spaces above the gas distribution orifice plate of described bottommost is at least two-layer fluidized-bed by the gas distribution orifice plate except the gas distribution orifice plate of bottommost, every one-level gas distribution holes plate respectively one_to_one corresponding is arranged on the below of fluidized-bed described in every one deck, the housing of the fluidized-bed of top is provided with product gas outlet, the scum pipe gas distribution orifice plate of bottommost being provided with connected entrance and being communicated with described connected entrance, one end that described scum pipe stretches out described housing bottom is slag-drip opening, the middle part of the gas distribution orifice plate except the gas distribution orifice plate of described bottommost is provided with central jet pipe, every two-layer adjacent described fluidized-bed is communicated with respectively by least one upflow tube, and upflow tube described in each is positioned at the outside of described housing.
Optionally, fluidized-bed described in every one deck comprises freeboard of fluidized bed, top and bottom emulsion zone, and the import of upflow tube described in each is all arranged on emulsion zone with outlet.
Preferably, upflow tube described in each comprises the epimere and hypomere that are interconnected, and described epimere and the angle between described hypomere and horizontal direction are 30-75 degree, and the junction of described epimere and hypomere is arc-shaped transition district.
Further, upflow tube described in each also comprises the transition section being communicated with described epimere and hypomere, and described transition section is vertically arranged.
Preferably, described in every one-level, gas distribution orifice plate is all in back taper, and described connected entrance is arranged on the cone angle place of the gas distribution orifice plate of bottommost.Optionally, angle described in every one-level between gas distribution orifice plate and horizontal direction is 30-75 degree, and the angle described in every one-level except the gas distribution orifice plate of bottommost between gas distribution orifice plate and horizontal direction is greater than the angle between the gas distribution orifice plate of described bottommost and horizontal direction.
Optionally, central jet pipe described in each is " L " type structure.
Preferably, described in each, the caliber of central jet pipe is less than the caliber of described scum pipe.
Preferably, the aspect ratio of the bottom emulsion zone of the fluidized-bed of bottommost is 5-10, and described in the every one deck except the fluidized-bed of described bottommost, the aspect ratio of the bottom emulsion zone of fluidized-bed is 2-5.
Further, described product gas outlet is arranged on the top shell of the fluidized-bed of described top, described vapourizing furnace also comprises gas-solid separating device, the import of described gas-solid separating device is communicated with described product gas outlet, and the solid outlet of described gas-solid separating device is communicated with at least one upflow tube of bottommost.
A kind of fluidized-bed gasification furnace that the utility model embodiment provides, by arranging at least two-stage gas distribution orifice in the housing of vapourizing furnace, separated by spaces above the gas distribution orifice plate of described bottommost is at least two-layer fluidized-bed by the gas distribution orifice plate except the gas distribution orifice plate of bottommost, the fluidized-bed of bottommost feeds oxygen-containing gas by the gas distribution orifice plate of described scum pipe and bottommost, described oxygen-containing gas is at least one of oxygen or air and the mixture of water vapour, regulates corresponding proportion according to oxygen concentration.
In the fluidized-bed of bottommost, coal dust and described oxygen-containing gas burn, gasification, the carbon monoxide that the reaction such as water-gas change generates, hydrogen, the high-temperature gas mixture body of carbonic acid gas and water vapor, enter as the fluidized-bed on top adjacent is with it as fluidizing agent by gas distribution orifice plate, and with the coal dust generation pyrolysis entered in the fluidized-bed on adjacent top, gasification reaction generates the coal gas being rich in methane, the like, the high-temperature gas mixture body being rich in methane that each laminarization bed generates is in the fluidized-bed that gas distribution orifice plate enters top adjacent with it, with the coal dust generation pyrolysis of fluidized-bed entering top, gasification reaction, the fluidized-bed generation coal gasification reaction of top generates the high-temperature gas mixture body being rich in methane and enters subsequent disposal through described product gas outlet, and the fluidized-bed of bottommost burns, the lime-ash that the reactions such as gasification produce is discharged by described slag-drip opening.
According to the fluidization characteristic of coal dust, in initial start up phase, when coal dust carries out in every laminarization bed in two-phase transportation mode, realized continuous flow and the reaction of coal dust material by the upflow tube being located at each laminarization bed.When the height of coal dust under rheomorphism specifically described in each fluidized-bed of fluidized-bed top being bottommost is greater than the inlet height of described upflow tube, in coal dust meeting overflow to described upflow tube, and get back to continuation generation coal gasification reaction in next adjacent with it laminarization bed through described upflow tube, the like, the coal dust being in fluidized state in the fluidized-bed adjacent with bottommost fluidized-bed continues generating gasification in the fluidized-bed that upflow tube enters bottommost, combustion reactions, the lime-ash generated can be discharged through slag-drip opening, in the process, the residence time of coal dust in vapourizing furnace can be improved, avoid the risk of high bed fluidized bed process, improve the comprehensive utilization ratio of coal dust, and be arranged on the outside of described housing due to described upflow tube, compared with being arranged in described housing with described upflow tube, goods fluid is avoided to cause upflow tube to wear and tear and blocking, be convenient to maintenance and the maintenance of upflow tube, further, because the middle part of the gas distribution orifice plate except the gas distribution orifice plate of described bottommost is provided with central jet pipe, oxygen-containing steam or vaporized chemical can be passed in the fluidized-bed on top through described central jet pipe, formed jet fluidized-bed, strengthen the back-mixing flowing of coal dust in each laminarization bed in top, guarantee bed temperature is even, improve the methane in each laminarization bed in top in gas product and tar light oil content.
Accompanying drawing explanation
In order to be illustrated more clearly in the utility model embodiment or technical scheme of the prior art, below the accompanying drawing used required in describing embodiment is briefly described, apparently, accompanying drawing in the following describes is only embodiments more of the present utility model, for those of ordinary skill in the art, under the prerequisite not paying creative work, other accompanying drawing can also be obtained according to these accompanying drawings.
The structural representation of a kind of fluidized-bed gasification furnace that Fig. 1 provides for the utility model embodiment;
The structural representation of the another kind of fluidized-bed gasification furnace that Fig. 2 provides for the utility model embodiment;
The structural representation of the another kind of fluidized-bed gasification furnace that Fig. 3 provides for the utility model embodiment;
The structural representation of another fluidized-bed gasification furnace that Fig. 4 provides for the utility model embodiment.
Embodiment
Below in conjunction with the accompanying drawing in the utility model embodiment, be clearly and completely described the technical scheme in the utility model embodiment, obviously, described embodiment is only the utility model part embodiment, instead of whole embodiments.Based on the embodiment in the utility model, those of ordinary skill in the art are not making the every other embodiment obtained under creative work prerequisite, all belong to the scope of the utility model protection.
In description of the present utility model, it will be appreciated that, term " " center ", " on ", D score, " front ", " afterwards ", " left side ", " right side ", " vertically ", " level ", " top ", " end ", " interior ", orientation or the position relationship of the instruction such as " outward " are based on orientation shown in the drawings or position relationship, only the utility model and simplified characterization for convenience of description, instead of indicate or imply that the device of indication or element must have specific orientation, with specific azimuth configuration and operation, therefore can not be interpreted as restriction of the present utility model.In description of the present utility model, except as otherwise noted, the implication of " multiple " is two or more.
See Fig. 1, for the utility model embodiment provides a kind of fluidized-bed gasification furnace, comprise: housing 1, be arranged at intervals with successively from top to bottom in described housing 1 at least two-stage gas distribution orifice (for three grades of gas distribution orifice plates, be respectively 2, 3 and 4), separated by spaces above the gas distribution orifice plate 4 of described bottommost is at least two-layer fluidized-bed (in this case three laminarization beds by the gas distribution orifice plate (2 and 3) except the gas distribution orifice plate 4 of bottommost, be respectively 21, 31 and 41), every one-level gas distribution holes plate (2, 3 and 4) correspondence is arranged on fluidized-bed (21 described in every one deck respectively, 31 and 41) below (such as, first step gas distribution orifice plate 2 is arranged on the below of the first layer fluidized-bed 21, second stage gas distribution orifice plate 3 is arranged on the below of second layer fluidized-bed 31, third stage gas distribution orifice plate 4 is arranged on the below of third layer fluidized-bed 41), the housing of the fluidized-bed 21 of top is provided with product gas outlet 5, the gas distribution orifice plate of bottommost is (at this, refer to third stage gas distribution orifice plate 4) on the scum pipe 11 that is provided with connected entrance and is communicated with described connected entrance, described scum pipe 11 one end of stretching out bottom described housing 1 is slag-drip opening (not shown), the middle part of the gas distribution orifice plate (2 and 3) except the gas distribution orifice plate 4 of described bottommost is provided with central jet pipe 13, every two adjacent described fluidized-bed (the first layer fluidized-bed 21 and second layer fluidized-beds 31 from top to bottom, second layer fluidized-bed 31 and third layer fluidized-bed 41) between be communicated with respectively by least one upflow tube (being designated as 6 at this), upflow tube 6 described in each is positioned at the outside of described housing 1.
Wherein, in the utility model embodiment, the specific works process of described fluidized-bed gasification furnace and principle of work as follows:
By arranging at least two-stage gas distribution orifice (being followed successively by 2,3 and 4 from top to bottom) in the housing 1 of vapourizing furnace, separated by spaces above the gas distribution orifice plate 4 of described bottommost is at least two-layer fluidized-bed (21,31 and 41) by the gas distribution orifice plate (2 and 3) except the gas distribution orifice plate 4 of bottommost, described oxygen-containing gas is at least one of oxygen or air and the mixture of water vapour, regulates corresponding proportion according to oxygen concentration.
In the fluidized-bed 41 of bottommost, coal dust and described oxygen-containing gas burn, gasification, the carbon monoxide that the reaction such as water-gas change generates, hydrogen, the high-temperature gas mixture body of carbonic acid gas and water vapor, the fluidized-bed 31 on top adjacent is with it entered as fluidizing agent by gas distribution orifice plate 3, and with the coal dust generation pyrolysis entered in the fluidized-bed 31 on adjacent top, gasification reaction generates the coal gas being rich in methane, the like, the high-temperature gas mixture body being rich in methane that each laminarization bed generates is in the fluidized-bed that gas distribution orifice plate enters top adjacent with it, with the coal dust generation pyrolysis of fluidized-bed entering top, gasification reaction, the fluidized-bed generation coal gasification reaction of top generates the high-temperature gas mixture body being rich in methane and enters subsequent disposal through described product gas outlet 5, and the fluidized-bed 41 of bottommost burns, the lime-ash that the reactions such as gasification produce is discharged by described slag-drip opening.
According to the fluidization characteristic of coal dust, in initial start up phase, when coal dust carries out in every laminarization bed in two-phase transportation mode, realized continuous flow and the reaction of coal dust material by the upflow tube 6 being located at each laminarization bed.When the height of coal dust under rheomorphism specifically described in each fluidized-bed of fluidized-bed 41 top (21 and 31) being bottommost is greater than the inlet height of described upflow tube, in coal dust meeting overflow to described upflow tube 6, and get back to continuation generation coal gasification reaction in next adjacent with it laminarization bed through described upflow tube 6, the like, the coal dust being in fluidized state in the fluidized-bed 31 adjacent with bottommost fluidized-bed 41 enters in the fluidized-bed 41 of bottommost through upflow tube 6 and continues to burn, the reactions such as gasification, the lime-ash generated can be discharged through slag-drip opening, in the process, the residence time of coal dust in vapourizing furnace can be improved, avoid the risk of high bed fluidized bed process, thus improve the comprehensive utilization ratio of coal dust.
A kind of fluidized-bed gasification furnace that the utility model embodiment provides, by described upflow tube 6 being arranged on the outside of described housing 1, compared with being arranged in described housing 1 with described upflow tube 6, goods fluid is avoided to cause upflow tube to wear and tear and blocking, be convenient to maintenance and the maintenance of upflow tube 6, further, because the middle part of described gas distribution orifice plate (2 and 3) except the gas distribution orifice plate 4 of described bottommost is provided with central jet pipe 13, oxygen-containing steam or vaporized chemical can be passed in the fluidized-bed (2 or/and 3) on top through described central jet pipe 13, formed jet fluidized-bed, strengthen the back-mixing flowing of coal dust in each laminarization bed in top, guarantee bed temperature is even, improve the methane in each laminarization bed in top in gas product and tar light oil content.
Wherein, it should be noted that, fluidized-bed 21 described in every one deck is entered in the mode of two-phase transportation at coal dust, time in 31 and 41, at every one-level gas distribution holes plate 2, fluidized-bed layer is formed under the rheomorphism of the vaporized chemical of 3 and 4 distributions, in each laminarization bed, usually, pellet density is larger, the coal dust that median size is also larger is positioned at the lower region of described fluidized-bed layer, be called emulsion zone, and pellet density is less, the coal dust that mean particle size is less is arranged in the upper area of described fluidized-bed layer, be called freeboard of fluidized bed, can learn thus, each laminarization bed 21, 31 and 41 comprise freeboard of fluidized bed, top A and bottom emulsion zone B, see Fig. 1, Fig. 2 and Fig. 3, it should be noted that, it is only a kind of method for expressing to two regions that freeboard of fluidized bed, top A wherein and bottom emulsion zone B encloses all by a dotted line, this does not cause restriction to described top freeboard of fluidized bed A and bottom emulsion zone B.
Wherein, pellet density is comparatively large, median size is also comparatively large is comparatively speaking with pellet density is less, median size is also less, at this, does not affect the realization of the utility model embodiment object.
In an embodiment of the present utility model, the upper body 1 of fluidized-bed 21,31 and 41 described in every one deck is provided with obliquely at least two symmetrical coal powder entrances 12.When coal dust is entered in fluidized-bed 21,31 and 41 described in every one deck by described coal powder entrance 12 in two-phase transportation mode, because the incident direction of coal powder entrance 12 is symmetrical arranged, make coal dust can to carry out dispersed to spray mode, and described coal dust fully contacts in a counter-current fashion with vaporized chemical, make gas-solid mixing more abundant and even, thus make the reaction of coal dust and vaporized chemical more abundant.
Wherein, it should be noted that, fluidized-bed 21 described in every one deck is entered in two-phase transportation mode at coal dust, in 31 and 41, entering fluidized-bed 21 described in every one deck, continuous kinestate is under the rheomorphism of the vaporized chemical in 31 and 41, when the fluidizing velocity of vaporized chemical is certain, fluidized-bed 21 described in every one deck, in 31 and 41, macrobead coal dust is in the relatively low position of fluidized-bed described in every one deck for small-particle coal dust, fluidized-bed 21 described in every one deck, the coal gas meeting entrainment portions small-particle coal dust being rich in methane generated in 31 and 41 or unreacted completely coal dust enter in last layer fluidized-bed adjacent with it.
Wherein, the coal dust being in fluidized state of the fluidized-bed that two adjacent (21 and 31 or 31 and 41) fluidized-bed 21 or 31 at the middle and upper levels the entrance of upflow tube described in each 6 and the setting position of outlet do not limited, as long as can enter lower floor's fluidized-bed 31 or 41 by described upflow tube 6 when overflowing to certain altitude.
In an embodiment of the present utility model, see Fig. 2, fluidized-bed described in every one deck (21,31 and 41) comprises freeboard of fluidized bed, top A and bottom emulsion zone B, and the import of upflow tube 6 described in each is all arranged on emulsion zone B with outlet.
Wherein, the concrete structure of upflow tube described in each 6 is not limited.Preferably, see Fig. 4, upflow tube 6 described in each comprises the epimere 61 and hypomere 62 that are interconnected, and described epimere 61 and the angle between hypomere 62 and horizontal direction are 30-75 degree, and the junction of described epimere and hypomere is arc-shaped transition district.Thus make coal dust smoothly by described upflow tube 6, to prevent coal dust from accumulating and blockage phenomenon in upflow tube 6.
Wherein, do not limit the mode of communicating between described epimere 61 and hypomere 62, for be interconnected at angle, also can arrange transition section 63 between described epimere 62 and hypomere 62, wherein, described transition section 63 can be circular arc.
Preferably, see Fig. 3 and Fig. 4, upflow tube 6 described in each also comprises the transition section 63 being communicated with described epimere 61 and hypomere 62, and described transition section 63 is vertically arranged.Adopt this structure, the smoothness of described upflow tube 6 blanking can be improved further, prevent blocking.
Wherein, it should be noted that, under normal conditions, the material being in fluidized state in upper strata fluidized-bed 21 overflows to the upper inlet place of described upflow tube 6, and upper strata fluidized-bed 21 and lower floor's fluidized-bed 31 meet certain pressure reduction time, material overflow in described upflow tube 6, and can complete returning charge by described upflow tube 6 voluntarily.But, under special circumstances, the putty phenomenon in upflow tube 6 may be there is, such as, when the build up of material in described upflow tube 6 is too much, putty phenomenon may occur.
In an embodiment of the present utility model, the lower curved zone of transition of described upflow tube 6 offers air inlet port, the angle between the airintake direction of described air inlet port and the flow direction of material is acute angle.Blown to the material in described upflow tube 6 by described air inlet port, mass transport can be accelerated further, reduce solid accumulation, prevent putty.
Wherein, connected entrance on the gas distribution orifice plate 4 of described bottommost and the setting position of scum pipe 11 that is communicated with described connected entrance are not limited, in a preferred embodiment of the present utility model, see Fig. 1 and Fig. 4, gas distribution orifice plate described in every one-level (2,3 and 4) is all in back taper, and described connected entrance is arranged on the cone angle place of the gas distribution orifice plate 4 of bottommost.Adopt this structure, described scum pipe 11 is positioned at the middle part of the fluidized-bed 41 of bottommost, when the fluidized-bed 41 of described bottommost burn, the reaction such as gasification time, the lime-ash of generation can be discharged by described scum pipe 11 in time.
Wherein, the gas speed of the oxygen-containing gas passing into described scum pipe 11 not being limited, in the utility model embodiment, conservative control can be carried out to bed drain purge by regulating the gas velocity of described oxygen-containing gas.
In an embodiment of the present utility model, see Fig. 1 and Fig. 4, central jet pipe 13 described in each is " L " type structure.Adopt this structure, vaporized chemical or oxygen-containing steam can be passed into from the export-oriented each laminarization bed (21 and 31) except the fluidized-bed 4 of bottommost of vapourizing furnace by described central jet pipe 13, to strengthen top fluidisation, simultaneously, when passing into oxygen-containing steam, can also regulate by regulating the gasification temperature of content to each laminarization bed of oxygen in oxygen-containing steam.
In an embodiment of the present utility model, the caliber of central jet pipe 13 described in each is less than the caliber of described scum pipe 11.Adopt this structure, when passing into oxygen-containing steam in the fluidized-bed 41 of described bottommost, when passing into oxygen-containing steam or steam or carbonic acid gas in each laminarization bed 21 and 31 in top, when by described central jet pipe 13 with certain by the tolerance of described scum pipe 11, comparatively high by the gas velocity of described scum pipe 11 by the gas velocity of the oxygen-containing steam of described central jet pipe 13, such as, usually be by the 10-40 of the gas velocity of described scum pipe 11 doubly by the gas velocity of central jet pipe 13, therefore, the fluidisation of coal dust in each laminarization bed 21 and 31 in top can be strengthened, coal dust is made fully to react the coal gas generating and be rich in methane, and coal dust in the fluidized-bed 41 of bottommost due to fluidisation degree less, the residence time of coal dust in the fluidized-bed 41 of described bottommost can be extended, thus improve the utilization ratio of coal dust further, when carrying out coal gasification reaction by this gasification furnace of fluidized bed, the methane content in gas product can be improved, improve utilization ratio and the efficiency of carbon conversion of coal dust on the whole.
Wherein, do not limit the percentage of open area of gas distribution orifice plate described in each (2,3 and 4), the percentage of open area of described gas distribution orifice plate rationally can be arranged according to the flow velocity of coal, pulverized coal particle size and required vaporized chemical.Preferably, the percentage of open area of gas distribution orifice plate described in each (2,3 and 4) is 0.1%-2%.
In an embodiment of the present utility model, see Fig. 1 and Fig. 2, angle between gas distribution orifice plate described in every one-level (2,3 and 4) and horizontal direction is 30-75 degree, and described in every one-level except the gas distribution orifice plate 4 of bottommost, gas distribution orifice plate 2 and the angle between 3 and horizontal direction are greater than the angle between the gas distribution orifice plate 4 of described bottommost and horizontal direction.
Adopt this structure, to comprise two-stage gas distribution orifice (such as 2 and 3) in described housing 1, see Fig. 2, wherein, separated by spaces above described next stage gas distribution orifice plate 3 is upper strata fluidized-bed 21 and lower floor's fluidized-bed 31 by upper level gas distribution orifice plate 2, angle between upper level gas distribution orifice plate 2 and horizontal direction is greater than the angle between next stage gas distribution orifice plate 3 and horizontal direction, like this, the coal gas being rich in methane generated in the fluidized-bed 31 of bottommost is when upper level gas distribution orifice plate 2 is distributed in described last layer fluidized-bed 21, when the percentage of open area of every one-level gas distribution holes plate is certain, angle between gas distribution orifice plate and horizontal direction is larger, angle between described gas distribution orifice plate and the inwall of described housing is larger, thus make coal dust not easily form defluidization, prevent from forming fluidisation dead band, therefore, the fluidisation degree of the coal dust in last layer fluidized-bed 2 can be increased, thus raising spillover efficiency, improve the residence time of coal dust in fluidized-bed described in every one deck, and generating gasification in final overflow to the fluidized-bed 41 of bottommost, combustion reactions, improve the efficiency of carbon conversion of coal dust, see Fig. 1, when comprising the gas distribution orifice plate (respectively for 2,3 and 4) of more than three grades in described housing 1, described in every one-level except the gas distribution orifice plate 4 of bottommost, gas distribution orifice plate 2 and the angle between 3 and horizontal direction are greater than the angle between the gas distribution orifice plate 4 of described bottommost and horizontal direction, like this, the object strengthening top each laminarization bed fluidisation can be played equally.
Wherein, described in the every one-level except the gas distribution orifice plate 4 of bottommost, gas distribution orifice plate 2 and the angle between 3 with horizontal direction can be equal, also can be unequal, do not limit at this.
Wherein, it should be noted that, in whole fluidized-bed gasification furnace, when the flow velocity of passed into vaporized chemical is less, is unfavorable for the fluidisation of each fluidized-bed layer, thus affects reaction effect, and the flow velocity of working as passed into vaporized chemical larger time, part small-particle coal dust is easily carried secretly by described vaporized chemical and is taken described vapourizing furnace out of through described product gas outlet 5, can reduce the utilization ratio of coal dust like this, be unfavorable for making full use of of the energy.In an embodiment of the present utility model, see Fig. 3 and Fig. 4, described product gas outlet 5 is arranged on the top shell of fluidized-bed 21 of described top, described vapourizing furnace also comprises gas-solid separating device 7, the import of described gas-solid separating device 7 is communicated with described product gas outlet 5, and the solid outlet of described gas-solid separating device 7 is communicated with at least one upflow tube 6 of bottommost.Adopt this structure, when part small-particle coal dust generate in each laminarization bed be rich in the carrying secretly of the coal gas of methane under move upward, and finally enter in described gas-solid separating device 7 through product gas outlet 5 in the fluidized-bed of top, the coal gas that described gas-solid separating device 7 is rich in methane to described and small-particle coal dust carry out gas solid separation and obtain clean gas and small-particle coal dust and fraction solids semicoke, described small-particle coal dust and fraction solids semicoke enter at least one upflow tube 6 of bottommost through the solid outlet of described gas-solid separating device 7, and proceed combustion reactions by the fluidized-bed that described upflow tube 7 is back to bottommost, the utilization ratio of coal dust can be improved, thus improve the efficiency of carbon conversion of coal dust further.
Wherein, do not limit the volume of fluidized-bed described in every one deck (21,31 and 41), described in every one deck, the volume of fluidized-bed 21,31 and 41 can be equal, also can not wait.
In an embodiment of the present utility model, see Fig. 1 and Fig. 4, the aspect ratio of the bottom emulsion zone B of the fluidized-bed 41 of described bottommost is 5-10, and described in the every one deck except the fluidized-bed 41 of bottommost, the aspect ratio of the bottom emulsion zone B of fluidized-bed (21,31) is 2-5.
Adopt this structure, when comprising two-stage gas distribution orifice in described housing 1, see Fig. 2 and Fig. 3, separated by spaces in described housing 1 is upper strata fluidized-bed 21 and lower floor's fluidized-bed 31 by described two-stage gas distribution orifice (for 2 and 3), at this moment, aspect ratio due to described upper strata fluidized-bed 21 is less than the aspect ratio of described lower floor fluidized-bed 31, described upper strata fluidized-bed 21 is surface bed reaction zone, described lower floor fluidized-bed 31 is dark bed reaction zone, when upper strata fluidized-bed 21 reacts, the residence time of coal dust in described surface bed reaction zone can be reduced, thus the methane content improved in the coal gas in upper strata fluidized-bed 21, and the coal dust in upper strata fluidized-bed 21 can continue reaction in described upflow tube 6 overflow to lower floor's fluidized-bed 31, and due to lower floor's fluidized-bed 31 be dark bed reaction zone, when the coal dust of the non-complete reaction in upper strata fluidized-bed 21 is when being back in described lower floor fluidized-bed 31 through described upflow tube 6, the residence time of coal dust in dark bed reaction zone can be improved, improve the utilization ratio of coal dust, thus improve efficiency of carbon conversion further.See Fig. 1 and Fig. 4, when comprising gas distribution orifice plate (for 2,3 and 4) of more than three grades in described housing 1, the aspect ratio of the bottom emulsion zone B of fluidized-bed 21 and 31 described in the every one deck except the fluidized-bed 41 of bottommost is 2-5, be less than the aspect ratio of the bottom emulsion zone B of the fluidized-bed 41 of described bottommost, can play equally and improve the methane content of coal gas that upper fluid-bed 21 and 31 reacts gained, and increase the effect of the residence time of coal dust in the fluidized-bed 41 of described bottommost of the non-complete reaction returned by upflow tube 6.
Wherein, described in described every one deck except the fluidized-bed 41 of bottommost, the aspect ratio of the bottom emulsion zone B of fluidized-bed 21 and 31 can be equal, also can not wait, not limit at this.
Embodiment
Below, the utility model embodiment is described technique effect of the present utility model respectively by embodiment.These embodiments are only the examples proposed to illustrate the utility model, and those skilled in the art are not it is appreciated that scope of the present utility model is subject to the restriction of these embodiments and test example.
Embodiment 1
See Fig. 3, in described embodiment 1 in housing from top to bottom a minor tick two-stage gas distribution orifice be set be described.
When being gasified to coal by described vapourizing furnace fluidized-bed, the temperature of lower floor's fluidized-bed 31 is made to control at 800-1000 DEG C by regulating the mass ratio of oxygen-containing steam and coal dust, pressure-controlling is at 0-5Mpa, the aspect ratio of emulsion zone controls 5, by described by feed coal in the mode of two-phase transportation through the coal powder entrance 12 of every one deck to enter in upper strata fluidized-bed 21 and lower floor's fluidized-bed 31 respectively to spray mode, wherein, the gas distribution orifice plate 3 of lower floor's fluidized-bed 31 through bottom and slag-drip opening pass into oxygen-containing gas, described oxygen-containing gas contacts with the coal dust entered in lower floor's fluidized-bed 31 is reverse, coal dust burns, gasification reaction generates vaporized chemical and solid semicoke, the gas distribution orifice plate 2 of vaporized chemical through top generated enters upper strata fluidized-bed 21, with the coal dust entered in described upper strata fluidized-bed 21 reverse contact, pyrolysis occurs, gasification reaction generates vaporized chemical and solid semicoke, in described upper strata fluidized-bed 21, oxygen-containing steam or steam is passed into by central jet pipe 13, the temperature in upper strata fluidized-bed 21 is made to control at 500-800 DEG C, pressure-controlling is at 0-5Mpa, the aspect ratio of emulsion zone controls 2, wherein, the speed being maintained by the oxygen-containing steam in described central jet pipe 13 is 20 times of the speed of oxygen-containing steam by scum pipe 11, coal dust in upper strata fluidized-bed 21 and solid semicoke fully react under the rheomorphism of vaporized chemical, part coal dust and solid semicoke enter in described lower floor fluidized-bed 31 through described upflow tube 6 and burn under rheomorphism, gasification reaction, the gas product generated enters gas-solid separating device 7 through product gas outlet 5, in the gas product that gas-solid separating device 7 is separated, the content of methane and tar light oil is higher, fraction solids semicoke enters in lower floor's fluidized-bed 31 through upflow tube 6 and burns, gasification reaction.
Conclusion: when adopting this fluidized-bed gasification furnace to gasify to each coal, the efficiency of carbon conversion of final obtained coal dust is more than 95%, and in the gas product generated, the volume content of methane is more than 20%.
Embodiment 2
See Fig. 4, in described embodiment 2 in housing from top to bottom a minor tick three grades of gas distribution orifice plates be set be described.
When being gasified to coal by described vapourizing furnace fluidized-bed, the temperature of lower floor's fluidized-bed 41 is made to control at 800-1000 DEG C by regulating the mass ratio of oxygen-containing steam and coal dust, pressure-controlling is at 0-5Mpa, the aspect ratio of emulsion zone controls 10, by feed coal in the mode of two-phase transportation through the coal powder entrance of every one deck to enter in each laminarization bed respectively to spray mode, wherein, the gas distribution orifice plate 4 of lower floor's fluidized-bed 41 through bottom and slag-drip opening pass into oxygen-containing gas, described oxygen-containing gas contacts with the coal dust entered in lower floor's fluidized-bed 41 is reverse, coal dust burns, gasification reaction generates vaporized chemical and solid semicoke, the gas distribution orifice plate 3 of vaporized chemical through middle part generated enters middle level fluidized-bed 31, with the coal dust entered in described middle level fluidized-bed 31 reverse contact, pyrolysis occurs, gasification reaction, in described middle level fluidized-bed 31, oxygen-containing steam or steam is passed into by central jet pipe 13, the temperature in middle level fluidized-bed 31 is made to control at 500-800 DEG C, pressure-controlling is at 0-5Mpa, the aspect ratio of emulsion zone controls 5, generate vaporized chemical and solid semicoke, coal dust in middle level fluidized-bed 31 and solid semicoke fully react under the rheomorphism of vaporized chemical, and part coal dust and solid semicoke enter in described lower floor fluidized-bed 41 through described upflow tube 6 under rheomorphism and proceed burning, gasification reaction generates vaporized chemical and solid semicoke, the vaporized chemical generated enters upper strata fluidized-bed 21, with the coal dust entered in described upper strata fluidized-bed 21 reverse contact, pyrolysis occurs, gasification reaction, in described upper strata fluidized-bed 21, oxygen-containing steam or steam is passed into by central jet pipe 13, the temperature in upper strata fluidized-bed 21 is made to control at 500-800 DEG C, pressure-controlling is at 0-5Mpa, the aspect ratio of emulsion zone controls 5, wherein, the speed being maintained by the oxygen-containing steam of described central jet pipe 13 is 40 times of the speed of the oxygen-containing steam of scum pipe 11, coal dust in upper strata fluidized-bed 21 and fraction solids semicoke fully react under the rheomorphism of vaporized chemical, and part coal dust and solid semicoke enter in described middle level fluidized-bed 31 through described upflow tube 6 and proceed pyrolysis under rheomorphism, gasification reaction, the gas product generated in described upper strata fluidized-bed 21 enters gas-solid separating device 7 through product gas outlet 5, in the gas product that gas-solid separating device 7 is separated, the content of methane and tar light oil is higher, the upflow tube 6 of fraction solids semicoke through bottom enters in lower floor's fluidized-bed 41 and burns, gasification reaction.
Conclusion: when adopting this fluidized-bed gasification furnace to gasify to each coal, the efficiency of carbon conversion of final obtained coal dust is more than 97%, and in the gas product generated, the volume content of methane is more than 25%.
Embodiment 3
Described embodiment 3 is substantially the same manner as Example 2, unlike, the aspect ratio of the emulsion zone of bottommost fluidized-bed 41 is 8, the aspect ratio of the emulsion zone of each laminarization bed on bottommost fluidized-bed 41 top is 4, and the speed being maintained by the oxygen-containing steam of described central jet pipe 13 is 30 times of the speed of oxygen-containing steam by described scum pipe 11.
Conclusion: when adopting this fluidized-bed gasification furnace to gasify to each coal, the efficiency of carbon conversion of final obtained coal dust is more than 97%, and in the gas product generated, the volume content of methane is more than 25%.
Comprehensive above-mentioned experiment conclusion is known: by improving fluidized-bed gasification furnace, make the fluidized-bed layer generation coal dust firing of bottommost, gasification reaction is the coal dust generation pyrolysis in each laminarization bed in top, gasification reaction provides heat, simultaneously, coal dust in each laminarization bed of top generates the coal gas being rich in methane and tar light oil under abundant rheomorphism, and by reacting layer by layer, improve the utilization ratio of coal dust and the efficiency of carbon conversion of coal dust, further, the fluidized-bed of bottommost is deep fluidized bed, the residence time of coal dust can be improved, thus improve utilization ratio and the efficiency of carbon conversion of coal dust further, wherein, upflow tube is arranged on the outside of described fluidized-bed gasification furnace, in raising gas product quality, while coal utilization and efficiency of carbon conversion, compared with being arranged in described housing with described upflow tube, goods fluid is avoided to cause upflow tube to wear and tear and blocking, be convenient to maintenance and the maintenance of upflow tube.
The above; be only embodiment of the present utility model; but protection domain of the present utility model is not limited thereto; anyly be familiar with those skilled in the art in the technical scope that the utility model discloses; change can be expected easily or replace, all should be encompassed within protection domain of the present utility model.Therefore, protection domain of the present utility model should be as the criterion with the protection domain of described claim.
Claims (10)
1. a fluidized-bed gasification furnace, it is characterized in that, comprise: housing, at least two-stage gas distribution orifice is arranged at intervals with from top to bottom successively in described housing, separated by spaces above the gas distribution orifice plate of described bottommost is at least two-layer fluidized-bed by the gas distribution orifice plate except the gas distribution orifice plate of bottommost, the housing of the fluidized-bed of top is provided with product gas outlet, the scum pipe gas distribution orifice plate of bottommost being provided with connected entrance and being communicated with described connected entrance, one end that described scum pipe stretches out described housing bottom is slag-drip opening, the middle part of the gas distribution orifice plate except the gas distribution orifice plate of described bottommost is provided with central jet pipe, every two-layer adjacent described fluidized-bed is communicated with respectively by least one upflow tube from top to bottom, and upflow tube described in each is positioned at the outside of described housing.
2. fluidized-bed gasification furnace according to claim 1, is characterized in that, fluidized-bed described in every one deck comprises freeboard of fluidized bed, top and bottom emulsion zone, and the import of upflow tube described in each is all arranged on emulsion zone with outlet.
3. fluidized-bed gasification furnace according to claim 2, it is characterized in that, upflow tube described in each comprises the epimere and hypomere that are interconnected, and described epimere and the angle between described hypomere and horizontal direction are 30-75 degree, and the junction of described epimere and hypomere is arc-shaped transition district.
4. fluidized-bed gasification furnace according to claim 3, is characterized in that, upflow tube described in each also comprises the transition section being communicated with described epimere and hypomere, and described transition section is vertically arranged.
5. fluidized-bed gasification furnace according to claim 1, is characterized in that, described in every one-level, gas distribution orifice plate is all in back taper, and described connected entrance is arranged on the cone angle place of the gas distribution orifice plate of bottommost.
6. fluidized-bed gasification furnace according to claim 5, it is characterized in that, angle described in every one-level between gas distribution orifice plate and horizontal direction is 30-75 degree, and the angle described in every one-level except the gas distribution orifice plate of bottommost between gas distribution orifice plate and horizontal direction is greater than the angle between the gas distribution orifice plate of described bottommost and horizontal direction.
7. fluidized-bed gasification furnace according to claim 1, is characterized in that, central jet pipe described in each is " L " type structure.
8. fluidized-bed gasification furnace according to claim 1, is characterized in that, described in each, the caliber of central jet pipe is less than the caliber of described scum pipe.
9. fluidized-bed gasification furnace according to claim 2, is characterized in that, the aspect ratio of the bottom emulsion zone of the fluidized-bed of bottommost is 5-10, and described in the every one deck except the fluidized-bed of described bottommost, the aspect ratio of the bottom emulsion zone of fluidized-bed is 2-5.
10. fluidized-bed gasification furnace according to claim 1, it is characterized in that, described product gas outlet is arranged on the top shell of the fluidized-bed of described top, described vapourizing furnace also comprises gas-solid separating device, the import of described gas-solid separating device is communicated with described product gas outlet, and the solid outlet of described gas-solid separating device is communicated with at least one upflow tube of bottommost.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520805029.7U CN205062002U (en) | 2015-10-16 | 2015-10-16 | Fluidized bed gasifica tion stove |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520805029.7U CN205062002U (en) | 2015-10-16 | 2015-10-16 | Fluidized bed gasifica tion stove |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205062002U true CN205062002U (en) | 2016-03-02 |
Family
ID=55388582
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520805029.7U Active CN205062002U (en) | 2015-10-16 | 2015-10-16 | Fluidized bed gasifica tion stove |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205062002U (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107377968A (en) * | 2017-09-08 | 2017-11-24 | 安徽工业大学 | A kind of preparation facilities and preparation method of the Heterogeneous Composite powder based on injection fluidisation |
| CN108179032A (en) * | 2018-01-09 | 2018-06-19 | 新奥科技发展有限公司 | A kind of fluidized-bed gasification furnace, gasification system and method |
| CN109974003A (en) * | 2019-03-07 | 2019-07-05 | 张波 | A kind of townhouse formula refuse pyrolysis gasification furnace |
| CN111854477A (en) * | 2019-04-28 | 2020-10-30 | 航天长征化学工程股份有限公司 | Cooling device |
| CN115282886A (en) * | 2022-07-18 | 2022-11-04 | 湖南中蓝新材料科技有限公司 | Particle flow control method and control system for overflow cup blanking of multilayer fluidized bed |
-
2015
- 2015-10-16 CN CN201520805029.7U patent/CN205062002U/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107377968A (en) * | 2017-09-08 | 2017-11-24 | 安徽工业大学 | A kind of preparation facilities and preparation method of the Heterogeneous Composite powder based on injection fluidisation |
| CN108179032A (en) * | 2018-01-09 | 2018-06-19 | 新奥科技发展有限公司 | A kind of fluidized-bed gasification furnace, gasification system and method |
| CN109974003A (en) * | 2019-03-07 | 2019-07-05 | 张波 | A kind of townhouse formula refuse pyrolysis gasification furnace |
| CN111854477A (en) * | 2019-04-28 | 2020-10-30 | 航天长征化学工程股份有限公司 | Cooling device |
| CN115282886A (en) * | 2022-07-18 | 2022-11-04 | 湖南中蓝新材料科技有限公司 | Particle flow control method and control system for overflow cup blanking of multilayer fluidized bed |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN205062002U (en) | Fluidized bed gasifica tion stove | |
| CA2696246C (en) | Fluidized bed reactor system | |
| US9920267B2 (en) | Solids circulation system and method for capture and conversion of reactive solids with fluidized bed temperature control | |
| CN107286993B (en) | Variable cross-section circulating fluidized bed gasification device and gasification method | |
| CN107208882B (en) | With multiple fuel reaction areas and gravity for the burning chemistry chains method of the particle of oxidizing | |
| CN106221814B (en) | A kind of colm water cooling fireplace segmented couples gasification installation and gasification process | |
| CN107177384A (en) | A kind of catalytic gasification device, system and method | |
| CN106590761A (en) | Fluidized bed reaction device and reaction method for coal catalytic gasification for producing methane-rich synthetic gas | |
| CN106675658A (en) | Device and method for high-flux circulating fluidized bed low-rank coal gasifying | |
| CN107760377A (en) | Fluid bed and fixed bed combined type catalytic coal gasification devices and methods therefor | |
| CN108085063A (en) | A kind of low tar double bed gasification process and device | |
| CN103087778B (en) | Jet pipe, fluidized bed reactor with jet pipe and coal catalyzing and gasifying method | |
| CN107312575B (en) | Circulating fluidized bed gasification device with graded air distribution and gasification method | |
| CN101712891A (en) | Solid fuel combustion and gasification device of fluidized bed or jetting bed with flying ash multiple coal gasification device | |
| CN111054272A (en) | Fluidized bed gasification reaction apparatus and method | |
| CN2319410Y (en) | Cooperative prodn. Unit for two-stage gasifying fluidized bed coke loaded hot gas and steam | |
| CN102399595B (en) | Multilayer fluidized bed gasification furnace | |
| CN107267218A (en) | The method and system of solid fuel pyrolysis gasification | |
| CN107267219B (en) | Tangential air distribution circulating fluidized bed gasification device and gasification method | |
| CN207987121U (en) | A kind of biomass gasification device | |
| CN107760379A (en) | Fluid bed and melting bed combined type catalytic coal gasification devices and methods therefor | |
| CA2852763C (en) | Seal pot design | |
| CN107964427A (en) | A kind of device and technique of biomass production high-grade synthesis gas | |
| CN207727036U (en) | A kind of device of biomass production high-grade synthesis gas | |
| CN110205164A (en) | Circulating fluidized bed gasification device and ciculation fluidized bed gasification method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |