CN203768318U - Fluidized bed distribution plate and fluidized bed reactor - Google Patents
Fluidized bed distribution plate and fluidized bed reactor Download PDFInfo
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- CN203768318U CN203768318U CN201420147222.1U CN201420147222U CN203768318U CN 203768318 U CN203768318 U CN 203768318U CN 201420147222 U CN201420147222 U CN 201420147222U CN 203768318 U CN203768318 U CN 203768318U
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- 238000009826 distribution Methods 0.000 title abstract description 31
- 239000002893 slag Substances 0.000 claims abstract description 14
- 238000005243 fluidization Methods 0.000 claims abstract description 13
- 239000000126 substance Substances 0.000 claims description 20
- 238000007599 discharging Methods 0.000 claims description 14
- 239000003245 coal Substances 0.000 abstract description 48
- 239000002245 particle Substances 0.000 abstract description 36
- 238000002309 gasification Methods 0.000 abstract description 20
- 238000005516 engineering process Methods 0.000 abstract description 6
- 230000015572 biosynthetic process Effects 0.000 abstract description 5
- 230000003197 catalytic effect Effects 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 26
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 23
- 239000001301 oxygen Substances 0.000 description 23
- 229910052760 oxygen Inorganic materials 0.000 description 23
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 16
- 238000002474 experimental method Methods 0.000 description 9
- 239000000203 mixture Substances 0.000 description 8
- 229910052757 nitrogen Inorganic materials 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 7
- 238000010586 diagram Methods 0.000 description 7
- 230000000052 comparative effect Effects 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 238000010926 purge Methods 0.000 description 4
- 239000010883 coal ash Substances 0.000 description 3
- 238000005070 sampling Methods 0.000 description 3
- 230000001464 adherent effect Effects 0.000 description 2
- 239000002817 coal dust Substances 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000007790 solid phase Substances 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000005094 computer simulation Methods 0.000 description 1
- 210000004907 gland Anatomy 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000003278 mimic effect Effects 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 238000003892 spreading Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Abstract
The embodiment of the utility model provides a fluidized bed distribution plate and a fluidized bed reactor, belonging to the technical field of coal gasification. The fluidized bed distribution plate and the fluidized bed reactor are used for avoiding the slag formation phenomenon caused by defluidization of large particles in a distribution plate area. The fluidized bed distribution plate is a cone-shaped barrel extending upwards and outwards; a rotary hole of which the incidence direction is consistent with the direction of a fluidization field inside a fluidized bed is formed in the side wall of the barrel. The fluidized bed distribution plate and the fluidized bed reactor can be used for coal catalytic gasification or pressurized coal gasification technologies using the fluidized bed reactor.
Description
Technical field
The utility model relates to Coal Gasification Technology field, relates in particular to a kind of distribuor of fluidized bed and fluidized-bed reactor.
Background technology
The energy feature of China is " rich coal, few oil, deficency ", it is the shortcut that is applicable to China's national situation and clean environment firendly that coal is converted into top quality fuel methane in the energy, be to adopt fluidization and coal is converted into one of common method of fuel methane, react with vaporized chemical from bottom to top and keep continuously boiling and suspended state to make it have good heat transfer property and reaction efficiency by coal.
In fluidized bed plant, topmost member is vaporized chemical distribution apparatus (being generally called " grid distributor "), plays the vital role of even gas distribution and support solid phase particles, and its shape and structure affect the production operation performances such as the heat and mass transfer of equipment greatly.The vaporized chemical grid distributor using in existing fluidized bed plant mostly is conical distribution plate, the angle of this grid distributor mostly is 45 degree, and be furnished with uniform aperture, can in grid distributor district, be formed with good gas-solid contact condition, thereby all particles are all kept in motion.
But in actual use, above-mentioned grid distributor to be used in normal, low pressure gasifying technology, at water coal ratio, oxygen coal than certain in the situation that, in fluidized-bed, gas speed is relatively high, can realize the active fluidization of grid distributor region particle, and be subject to the impact of feed coal size distribution less.If cannot be met fluidisation demand but be applied in the Coal Gasification Technology of middle high-pressure or catalytic coal gasifaction technology, particularly in wide particle diameter distributes or has the gasification that large particle diameter feed coal participates in especially easily because defluidization causes slagging scorification on grid distributor, finally cause the improper stoppage in transit of whole device.
Utility model content
The purpose of this utility model is to provide a kind of distribuor of fluidized bed and fluidized-bed reactor, with the slagging scorification phenomenon of avoiding macrobead to cause because of defluidization in grid distributor region.
For achieving the above object, embodiment of the present utility model adopts following technical scheme:
On the one hand, the utility model provides a kind of distribuor of fluidized bed, and described distribuor of fluidized bed has upwards outward extending conical shell, on described cylinder lateral wall, offer the inner fluidisation field orientation of incident direction and fluidized-bed consistent revolve hole.
Optionally, the angle forming between the upper surface of described cylindrical shell and described sidewall is 50-80 °.
Optionally, described in, revolve hole and be opened in more than 1/3 region of described cylindrical shell.
Further, described in, revolve the incident direction in hole and the tangent line angle of its place flat circle is 0-60 °.
Optionally, described in revolve hole diameter be 2-10mm, percentage of open area is 0.2-0.5%.
Optionally, on described cylinder lateral wall, also offer straight hole.
Further, described straight hole is opened in the region of described cylindrical shell below 1/2.
Further, in the region of the described cylindrical shell of distance lower surface 5-20mm, do not offer straight hole.
Optionally, the diameter of described straight hole is 0.5-2mm, and percentage of open area is 0.1-0.5%.
On the other hand, the utility model provides a kind of fluidized-bed reactor, comprising: reactor body, feeding line, vaporized chemical pipeline, the pipeline of giving vent to anger, gas control slag discharging device and comprise the distribuor of fluidized bed that above-mentioned arbitrary technical scheme provides.
The utility model embodiment provides a kind of distribuor of fluidized bed and fluidized-bed reactor, compare from existing distribuor of fluidized bed and different be, on the sidewall of the distribuor of fluidized bed providing at embodiment, offer the inner fluidisation field orientation of incident direction and fluidized-bed consistent revolve hole, can strengthen grid distributor region oarse-grained mobile, and strengthen its back-mixing behavior in stove, thereby the slagging scorification phenomenon on grid distributor causing because having the flow dead of defluidizationization formation when effectively avoiding wide particle diameter to distribute or having large particle diameter feed coal to participate in gasification, particularly reduce aerobic in reaction process and have the slagging scorification risk in situation, and then be conducive to the carrying out of coal gasification course.
Brief description of the drawings
The schematic diagram of the distribuor of fluidized bed that Fig. 1 provides for the utility model embodiment;
The tangent line angle β schematic diagram that revolves hole and place flat circle of offering on distribuor of fluidized bed that Fig. 2 provides for the utility model embodiment;
The elevation angle gamma schematic diagram that revolves hole and place flat circle of offering on distribuor of fluidized bed that Fig. 3 provides for the utility model embodiment;
The schematic diagram of the fluidized-bed reactor that Fig. 4 provides for the utility model embodiment;
The CFD mimic diagram that the oxygen concn of the different angles grid distributor that Fig. 5 provides for the utility model embodiment distributes.
Embodiment
Below in conjunction with the accompanying drawing in the utility model embodiment, the technical scheme in the utility model embodiment is clearly and completely described, obviously, described embodiment is only the utility model part embodiment, instead of whole embodiment.Based on the embodiment in the utility model, those of ordinary skill in the art are not making the every other embodiment obtaining under creative work prerequisite, all belong to the scope of the utility model protection.
The distribuor of fluidized bed and the fluidized-bed reactor that the utility model embodiment are provided below in conjunction with accompanying drawing are described in detail.
The schematic diagram of the distribuor of fluidized bed that Fig. 1 provides for the utility model embodiment.Illustrated by Fig. 1, the utility model embodiment provides a kind of distribuor of fluidized bed, described distribuor of fluidized bed is for having upwards outward extending conical shell, on described cylinder lateral wall 2, offer incident direction consistent with the inner fluidisation field orientation of fluidized-bed revolve hole 3.
For feed coal can be contacted better with the state flowing with vaporized chemical in the process that participates in gasification, on the sidewall 2 of described cylindrical shell, offer incident direction and fluidized-bed inside fluidisation field orientation consistent revolve hole 3.Like this, the vaporized chemical that is delivered to air chamber by vaporized chemical pipeline just can by the hole 3 of revolving offered on sidewall 2, to enter reactor cavity indoor, so that the vaporized chemical entering can produce larger drag force upwards to particle in grid distributor region, can drive more feed coal to move upward, form more effective contact and back-mixing.Here it should be noted that, distribuor of fluidized bed be have certain thickness, the certain thickness here can determine according to the concrete application conditions of the selected material of reality and grid distributor, and in the present embodiment, the concrete thickness to distribuor of fluidized bed is not further qualified.
The embodiment of the present invention provides a kind of distribuor of fluidized bed, compare from existing distribuor of fluidized bed and different be, on the sidewall of the distribuor of fluidized bed being provided by the embodiment of the present invention, offer the inner fluidisation field orientation of incident direction and fluidized-bed consistent revolve hole, can strengthen grid distributor region oarse-grained mobile, and strengthen its back-mixing behavior in stove, thereby the slagging scorification phenomenon on grid distributor causing because having the flow dead of defluidizationization formation when effectively avoiding wide particle diameter to distribute or having large particle diameter feed coal to participate in gasification, particularly reduce aerobic in reaction process and have the slagging scorification risk in situation, and then be conducive to the carrying out of coal gasification course.
In the present embodiment, in order slowly to reduce the horizontal section variation tendency of grid distributor, reduce the gas speed variable gradient in grid distributor region, to avoid wide particle diameter or large particle diameter feed coal in the flow dead that participates in forming because of defluidization in gasification, the angle (α) forming between the upper surface 1 of described cylindrical shell and its sidewall 2 is 50-80 °, preferably, this α angle is 55-76 °, more preferably 65-72 °.Selection about the angular range of α angle can be determined according to the distribution situation of grain diameter, concrete, generally follows in the time of size distribution≤3mm, and the scope of α angle is 50-65 °, and in the time of size distribution≤6mm, the scope of α angle is the principle of 60-80 °.
In another embodiment provided by the invention, revolve hole 3 and can be opened in more than 1/3 region of described cylindrical shell, refer to from cylindrical shell upper surface herein to 2/3 of described cylindrical shell vertical height be line of delimitation, revolve hole 3 and can be opened in the upper area of the described cylindrical shell of being divided with this line of delimitation.It should be noted that, the position of revolving hole 3 can change the upwards starting point of impellent of eddy flow, and when revolving after hole site moves down, part eddy flow tolerance has been brought into play the effect of gas control deslagging, and the upwards drag force grid distributor region particle being produced strengthens, and bed drain purge is reduced.Therefore, the position distribution of revolving hole 3 is very crucial, and those skilled in the art can be as the case may be, considers grid distributor α angle and feed coal size distribution regulates in scope of the present invention.
In another embodiment of the present invention, as shown in Figure 2, on described cylinder lateral wall, offer the inner fluidisation field orientation of incident direction and fluidized-bed consistent revolve hole 3, revolving hole 3 is 0-60 ° with the tangent line angle (β) of its place flat circle.The vaporized chemical of being carried by air chamber enters in chamber of the reactor and drives feed coal motion by revolving hole 3 with this angle.Preferably, tangent line angle β is 0-45 °, preferred, and tangent line angle β is 0-25 °.This is because described distribuor of fluidized bed has upwards outward extending conical structure, by reasonable adjusting tangent line angle β, makes vaporized chemical effectively along revolving the adherent chamber of the reactor that enters in hole 3, farthest drives feed coal to move upward.
In another embodiment of the present invention, as shown in Figure 3, revolve hole 3 and also can be the elevation angle (γ) with place flat circle and enter, γ may be selected to be 0-30 °, and preferred, γ is 0-17 °, preferred, and γ is 0-10 °.Equally also can make vaporized chemical effectively along revolving the adherent chamber of the reactor that enters in hole 3, realize and farthest drive feed coal to move upward.
In order to make vaporized chemical can effectively drive the feed coal particle of different-grain diameter size to move upward entering behind grid distributor region, optional, the diameter that revolves hole 3 is 2-10mm.Further preferred, diameter is 6-8mm.Selection about the diameter that revolves hole 3 can be selected according to the maximum particle diameter of used different material coal, is generally its 1-2 doubly.Offering the object of revolving hole 3 is that grid distributor region is oarse-grained flows in order to strengthen, and strengthens its back-mixing behavior in stove, has the slagging scorification risk of situation to reduce better in reaction process aerobic particularly.Under normal circumstances, revolve hole 3 and be uniformly distributed in the flat circle of grid distributor, and percentage of open area is 0.2-0.5%.It should be noted that, about offering concrete quantity and the position distribution of revolving hole 3, those skilled in the art can and be revolved under the definite prerequisite of bore dia at percentage of open area, specifically set according to the grain fluidized characteristic in grid distributor region.
In another embodiment of the present invention, optional, on described cylinder lateral wall 2, also can offer straight hole 4, its objective is in order to revolve hole to grid distributor below 3 and the particle at common factor position provides impellent, avoid particle packing, to ensure the unobstructed of deslagging.Further, straight hole 4 is opened in the region of described cylindrical shell below 1/2, it is more than 5 region between 1/2 in lower surface 5 and lower surface of distribuor of fluidized bed, 1/2 place that refers to described cylindrical shell vertical height is herein line of delimitation, straight hole 4 can be opened in the lower region of the described cylindrical shell of being divided with this line of delimitation, thereby can impellent be provided to better feed coal and the coal ash of grid distributor lower end, impel it to flow fully.It should be noted that, for fear of form sealing gland face in grid distributor bottom, also for the buffer zone of the bottom at grid distributor and scum pipe Link Port place formation gas speed, optional, in the region of the described cylindrical shell of distance lower surface 5-20mm, do not offer straight hole 4.Leave the buffer zone within the scope of this, can control preferably the discharge of coal ash.
In order to make vaporized chemical can effectively drive the feed coal of greater particle size and coal ash particle to move upward entering after chamber of the reactor's bottom section, optionally, the diameter of straight hole 4 is 0.5-2mm, and percentage of open area is 0.1-0.5%, and is uniformly distributed in the flat circle of grid distributor.It should be noted that, the quantity of straight hole 4 and position those skilled in the art can comprehensively determine according to the total percentage of open area of grid distributor and the needs that revolve hole area.
The schematic diagram of the fluidized-bed reactor that Fig. 4 provides for the utility model embodiment.As shown in Figure 4, the utility model provides a kind of fluidized-bed reactor, comprising:
Reactor body 41, its inside is formed with chamber;
Comprise the distribuor of fluidized bed 42 that above-mentioned arbitrary technical scheme provides, be positioned at described reactor body bottom, and be formed with air chamber between the wall of described reactor body bottom;
Feeding line (not shown), through the top of described reactor body, with described chamber in fluid communication, enters in described chamber for gasified raw material;
Vaporized chemical pipeline 43, through reactor body bottom, is opened on air chamber, enters in described chamber by described distribuor of fluidized bed for vaporized chemical;
The pipeline (not shown) of giving vent to anger, through reactor body top, with described chamber in fluid communication, discharges reactor for gaseous product;
Gas control slag discharging device 44, is positioned at reactor body bottom, is connected with described distribuor of fluidized bed, discharges reactor for solid product.
The embodiment of the present invention provides a kind of fluidized-bed reactor, in this fluidized-bed reactor, include the incident direction grid distributor consistent with the inner fluidisation field orientation of fluidized-bed that revolves hole that offer that the embodiment of the present invention provides, can strengthen grid distributor region oarse-grained mobile, and strengthen its back-mixing behavior in stove, thereby the slagging scorification phenomenon on grid distributor causing because having the flow dead of defluidizationization formation when effectively avoiding wide particle diameter to distribute or having large particle diameter feed coal to participate in gasification, particularly reduce aerobic in reaction process and have the slagging scorification risk in situation, and then be conducive to the carrying out of coal gasification course.
Reactor body 41 has bearing capacity, can tolerate and maintain the temperature and pressure of reactor inner space, and be made up of pressure-resistant material.Described feeding line and vaporized chemical pipeline 43, for described material being introduced under certain pressure to inside reactor chamber, fully contact rear generating gasification reaction for the two.Wherein, in vaporized chemical pipeline 43, pass into by O
2, CO or H
2in the vaporized chemical that mixes of one or more and superheated vapour.The described pipeline of giving vent to anger is for discharging reactor by the gaseous product after gasification reaction.Gas control slag discharging device 44 can be connected with equipment, also can be one-body molded, control bed drain purge by the inert material in the threeway of adjusting gas control slag discharging device or the inlet of vaporized chemical.It should be noted that, in actual production process, those skilled in the art can determine according to practical situation the required number of above-mentioned respective lines, thereby realize better function separately, realize utility model object.By the grid distributor of larger α angle angle therewith deslagging mode combine, can ensure the flow problem of grid distributor region particle, can realize again accurate control bed drain purge.
For a kind of distribuor of fluidized bed, fluidized-bed reactor and gasification process thereof are described better, be elaborated with specific embodiment and comparative example below.
The feed coal that employing has certain grain size distribution carries out catalytic coal gasifaction experiment, experimental installation is the fluidized-bed of internal diameter 0.2m, high 4m, on the vertical height of bed body wall face, every 25cm is provided with point for measuring temperature, pressure tap, gas-solid sampling spot, take grid distributor upper surface as height zero reference level, raw materials used coal load 10wt% catalyzer, size distribution is as table 1, table 2, table 3.
Table 1 wide particle diameter feed coal size distribution (4mm is following)
| Particle diameter/mm | Per-cent/% |
| 2-4 | 19.44 |
| 0.9-2 | 33.43 |
| 0.15-0.9 | 29.19 |
| <0.15 | 17.94 |
Particle diameter feed coal size distribution in table 2 (2mm is following)
| Particle diameter/mm | Per-cent/% |
| 0.85-2 | 4.63 |
| 0.425-0.85 | 45.99 |
| 0.18-0.425 | 10.79 |
| 0.096-0.18 | 11.17 |
| <0.096 | 27.42 |
The narrow particle diameter feed coal of table 3 size distribution (0.425mm is following)
| Particle diameter/mm | Per-cent/% |
| 0.25-0.425 | 34.68 |
| 0.18-0.25 | 20.49 |
| 0.125-0.18 | 19.79 |
| 0.096-0.125 | 7.76 |
| <0.096 | 17.28 |
Embodiment 1
Vapourizing furnace is installed 80 ° of grid distributors, and grid distributor upper surface is evenly distributed the hole of revolving that diameter is 2mm in following 1/2 region, and revolving hole incident direction is the tangential direction of place elevation plane circle, and revolving hole percentage of open area is 0.5%.In more than grid distributor lower surface 5mm region below 1/4, be evenly covered with the straight hole that diameter is 0.5mm, direction is horizontal direction, and percentage of open area is 0.1%, and the threeway gas control slag discharging device that grid distributor lower end is 25mm with internal diameter is connected.
Experiment adopts wide particle diameter distribution feed coal, and as table 1, grid distributor passes into the gas mixture 50kg/h of superheated vapour and oxygen, and oxygen concn is 15mol%, and center scum pipe passes into nitrogen 10Nm
3/ h, experimental temperature is 700 °, and pressure is 3.5MPa, and feeding rate is 20kg/h, in the time that bed is stabilized in 2m left and right, collects related data, in table 4.
Embodiment 2
Vapourizing furnace is installed 50 ° of grid distributors, and grid distributor upper surface is evenly distributed the hole of revolving that diameter is 4mm in following 1/2 region, and incident direction becomes 60 ° of angles with the tangential direction of place elevation plane circle, and revolving hole percentage of open area is 0.2%.In more than grid distributor lower surface 10mm region below 1/3, be evenly covered with the straight hole that diameter is 1mm, direction is horizontal direction, and percentage of open area is 0.3%, and the threeway gas control slag discharging device that grid distributor lower end is 25mm with internal diameter is connected.
Experiment adopts wide particle diameter distribution feed coal, and as table 1, grid distributor passes into the gas mixture 50kg/h of superheated vapour and oxygen, and oxygen concn is 15mol%, and center scum pipe passes into nitrogen 10Nm
3/ h, experimental temperature is 700 °, and pressure is 3.5MPa, and feeding rate is 20kg/h, in the time that bed is stabilized in 2m left and right, collects related data, in table 4.
Embodiment 3
Vapourizing furnace is installed 60 ° of grid distributors, and grid distributor upper surface is evenly distributed the hole of revolving that diameter is 10mm in following 2/3 region, and incident direction becomes 30 ° of angles with the tangential direction of place elevation plane circle, and revolving hole percentage of open area is 0.4%.In more than grid distributor lower surface 20mm region below 1/2, be evenly covered with the straight hole that diameter is 2mm, direction is horizontal direction, and percentage of open area is 0.5%, and the threeway gas control slag discharging device that grid distributor lower end is 25mm with internal diameter is connected.
Experiment adopts wide particle diameter distribution feed coal, and as table 1, grid distributor passes into the gas mixture 50kg/h of superheated vapour and oxygen, and oxygen concn is 15mol%, and center scum pipe passes into nitrogen 10Nm
3/ h, experimental temperature is 700 °, and pressure is 3.5MPa, and feeding rate is 20kg/h, in the time that bed is stabilized in 2m left and right, collects related data, in table 4.
Embodiment 4
Vapourizing furnace is installed 70 ° of grid distributors, and grid distributor upper surface is evenly distributed the hole of revolving that diameter is 5mm in following 1/3 region, and incident direction becomes 20 ° of angles with the tangential direction of place elevation plane circle, and revolving hole percentage of open area is 0.3%.Grid distributor lower surface is evenly covered with the straight hole that diameter is 1.5mm in above 1/2 region, and direction is horizontal direction, and percentage of open area is 0.4%, and the threeway gas control slag discharging device that grid distributor lower end is 25mm with internal diameter is connected.
Size distribution feed coal during experiment adopts, as table 2, grid distributor passes into the gas mixture 35kg/h of superheated vapour and oxygen, and oxygen concn is 15mol%, and center scum pipe passes into nitrogen 5Nm
3/ h, experimental temperature is 700 °, and pressure is 3.5MPa, and feeding rate is 20kg/h, in the time that bed is stabilized in 2m left and right, collects related data, in table 4.
Embodiment 5
Vapourizing furnace is installed 65 ° of grid distributors, and grid distributor upper surface is evenly distributed the hole of revolving that diameter is 2mm in following 2/3 region, and incident direction becomes 10 ° of angles with the tangential direction of place elevation plane circle, and revolving hole percentage of open area is 0.3%.Grid distributor lower surface is evenly covered with the straight hole that diameter is 0.5mm in above 1/3 region, and direction is horizontal direction, and percentage of open area is 0.5%, and the threeway gas control slag discharging device that grid distributor lower end is 25mm with internal diameter is connected.
Experiment adopts narrow size distribution feed coal, and as table 3, grid distributor passes into the gas mixture 35kg/h of superheated vapour and oxygen, and oxygen concn is 15mol%, and center scum pipe passes into nitrogen 5Nm
3/ h, experimental temperature is 700 °, and pressure is 3.5MPa, and feeding rate is 20kg/h, in the time that bed is stabilized in 2m left and right, collects related data, in table 4.
Embodiment 6
Vapourizing furnace is installed 75 ° of grid distributors, and grid distributor upper surface is evenly distributed the hole of revolving that diameter is 6mm in following 2/3 region, and incident direction becomes 0 ° of angle with the tangential direction of place elevation plane circle, and revolving hole percentage of open area is 0.5%.In more than grid distributor lower surface 8mm region below 1/3, be evenly covered with the straight hole that diameter is 0.5mm, direction is horizontal direction, and percentage of open area is 0.2%, and the threeway gas control slag discharging device that grid distributor lower end is 25mm with internal diameter is connected.
Size distribution feed coal during experiment adopts, as table 2, grid distributor passes into the gas mixture 50kg/h of superheated vapour and oxygen, and oxygen concn is 10mol%, and center scum pipe passes into nitrogen 10Nm
3/ h, experimental temperature is 700 °, and pressure is 2.0MPa, and feeding rate is 20kg/h, in the time that bed is stabilized in 2m left and right, collects related data, in table 4.
Comparative example 1
Vapourizing furnace is installed conventional 45 ° of shape grid distributors, and grid distributor is evenly covered with the straight hole that diameter is 1mm, and direction is horizontal direction, and percentage of open area is 0.5%, and the threeway gas control slag discharging device that grid distributor lower end is 25mm with internal diameter is connected.
Size distribution feed coal during experiment adopts, as table 2, grid distributor passes into the gas mixture 50kg/h of superheated vapour and oxygen, and oxygen concn is 15mol%, and center scum pipe passes into nitrogen 10Nm
3/ h, experimental temperature is 700 °, and pressure is 3.5MPa, and feeding rate is 20kg/h, in the time that bed is stabilized in 2m left and right, collects related data, in table 4.
Comparative example 2
Vapourizing furnace is installed 70 ° of grid distributors, and grid distributor is evenly covered with the straight hole that diameter is 2mm, and direction is horizontal direction, and percentage of open area is 0.8%, and the threeway gas control slag discharging device that grid distributor lower end is 25mm with internal diameter is connected.
Experiment adopts wide particle diameter distribution feed coal, and as table 1, grid distributor passes into the gas mixture 50kg/h of superheated vapour and oxygen, and oxygen concn is 15mol%, and center scum pipe passes into nitrogen 10Nm
3/ h, experimental temperature is 700 °, and pressure is 3.5MPa, and feeding rate is 20kg/h, in the time that bed is stabilized in 2m left and right, collects related data, in table 4.
Table 4 embodiment effect comparison data
With reference to the analysis of table 4 correlation data, the gasification that distributes or have macrobead feed coal to participate in for wide particle diameter, 80 ° of angles of data presentation are more even than 50 ° of angle bed temperatures, same sampling spot grain diameter is all less than 50 ° of cone angle grid distributors, this is that the impellent straight up that grid distributor region produces is larger, is beneficial to macrobead coal dust fluidisation and bed back-mixing due to after angle change greatly, oxygen concn is uniformly dispersed, and bed temperature is basicly stable.
Move down and on grid distributor, revolve hole site, change the starting point of eddy flow impellent, before gasification index and change, difference is little, but bed drain purge slightly reduces, analyze reason and be and revolve after hole moves down, part eddy flow tolerance has been brought into play the effect of scum pipe gas control deslagging, therefore can be by reducing the stability of scum pipe tolerance control deslagging.
Comparative example has adopted 70 ° of grid distributors described in common 45 ° of grid distributors and the present invention, all be arranged as 1mm straight hole, feed coal to greater particle size gasifies, all there is grid distributor slagging scorification in result, find by the solid phase sample of checking different sampling spots, grid distributor region macrobead ratio is very large, there is flow dead and caused oxygen concn to assemble spreading, cause grid distributor district overtemperature, coal dust sintering, as seen revolves the effect in hole for wide particle diameter distribution feed coal gasification grid distributor very big; If it is larger that grid distributor all adopts Xuan Kongze grid distributor district to rotate up impellent, data as shown in comparative example 3, deslagging is not easy to be controlled.
Embodiment 7
In order to understand more intuitively the impact of grid distributor on situation in stove, utilizing CFD computer modeling technique (Fluent software) is that 200mm fluidized-bed is simulated to 45 ° and 70 ° of grid distributors, internal diameters, investigate oxygen concn distribution situation under the certain oxygen-supply quantity of grid distributor, calculation result as shown in Figure 5.
From figure, can find, 70 ° of grid distributor fluidized-beds more easily disperse oxygen than 45 ° of grid distributor fluidized-beds, and minimizing oxygen gathers a certain position, and combustion zone is effectively promoted, and has avoided because of the grain fluidized not good enough violent burning generation slagging scorification that causes in grid distributor region.
Obviously, above-described embodiment is only for example is clearly described, and the not restriction to embodiment.For those of ordinary skill in the field, can also make other changes in different forms on the basis of the above description.Here without also giving exhaustive to all embodiments.And the apparent variation of being extended out thus or the still protection domain in the invention of variation.
Claims (10)
1. a distribuor of fluidized bed, is characterized in that, described distribuor of fluidized bed has upwards outward extending conical shell, on described cylinder lateral wall, offer the inner fluidisation field orientation of incident direction and fluidized-bed consistent revolve hole.
2. distribuor of fluidized bed according to claim 1, is characterized in that, the angle forming between the upper surface of described cylindrical shell and described sidewall is 50-80 °.
3. distribuor of fluidized bed according to claim 1, is characterized in that, described in revolve hole and be opened in more than 1/3 region of described cylindrical shell.
4. according to the distribuor of fluidized bed described in claim 1 or 3, it is characterized in that, described in revolve the incident direction in hole and the tangent line angle of its place flat circle is 0-60 °.
5. according to the distribuor of fluidized bed described in claim 1 or 3, it is characterized in that, described in revolve hole diameter be 2-10mm, percentage of open area is 0.2-0.5%.
6. distribuor of fluidized bed according to claim 1, is characterized in that, also offers straight hole on described cylinder lateral wall.
7. distribuor of fluidized bed according to claim 6, is characterized in that, described straight hole is opened in the region of described cylindrical shell below 1/2.
8. according to the distribuor of fluidized bed described in claim 6 or 7, it is characterized in that, in the region of the described cylindrical shell of distance lower surface 5-20mm, do not offer straight hole.
9. according to the distribuor of fluidized bed described in claim 6 or 7, it is characterized in that, the diameter of described straight hole is 0.5-2mm, and percentage of open area is 0.1-0.5%.
10. a fluidized-bed reactor, is characterized in that, comprising: reactor body, feeding line, vaporized chemical pipeline, the pipeline of giving vent to anger, gas control slag discharging device and the distribuor of fluidized bed as described in claim 1-9 any one.
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| CN201420147222.1U CN203768318U (en) | 2014-03-28 | 2014-03-28 | Fluidized bed distribution plate and fluidized bed reactor |
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| CN201420147222.1U CN203768318U (en) | 2014-03-28 | 2014-03-28 | Fluidized bed distribution plate and fluidized bed reactor |
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| CN104673397A (en) * | 2015-01-26 | 2015-06-03 | 新奥科技发展有限公司 | Fluidized bed gas distributor and gasifier |
| CN105930585A (en) * | 2016-04-21 | 2016-09-07 | 厦门大学 | CFD-based simulation method for flow field and temperature field of Shell gasifier |
| CN111603890A (en) * | 2019-02-26 | 2020-09-01 | 中国石化工程建设有限公司 | Adsorption tower for preventing dust deposition in air chamber and method for treating flue gas by using adsorption tower |
| CN112552962A (en) * | 2020-12-04 | 2021-03-26 | 陕西延长石油（集团）有限责任公司 | Multi-stage circulating gasification device and method for carbon-containing solid particles |
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2014
- 2014-03-28 CN CN201420147222.1U patent/CN203768318U/en not_active Expired - Lifetime
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104673397A (en) * | 2015-01-26 | 2015-06-03 | 新奥科技发展有限公司 | Fluidized bed gas distributor and gasifier |
| CN104673397B (en) * | 2015-01-26 | 2017-03-01 | 新奥科技发展有限公司 | A kind of gas distributor of fludized bed and gasification furnace |
| CN105930585A (en) * | 2016-04-21 | 2016-09-07 | 厦门大学 | CFD-based simulation method for flow field and temperature field of Shell gasifier |
| CN105930585B (en) * | 2016-04-21 | 2019-05-24 | 厦门大学 | The analogy method of Shell gasification furnace Flow and heat flux based on CFD |
| CN111603890A (en) * | 2019-02-26 | 2020-09-01 | 中国石化工程建设有限公司 | Adsorption tower for preventing dust deposition in air chamber and method for treating flue gas by using adsorption tower |
| CN111603890B (en) * | 2019-02-26 | 2022-06-17 | 中国石化工程建设有限公司 | Adsorption tower for preventing dust deposition in air chamber and method for treating flue gas by using adsorption tower |
| CN112552962A (en) * | 2020-12-04 | 2021-03-26 | 陕西延长石油（集团）有限责任公司 | Multi-stage circulating gasification device and method for carbon-containing solid particles |
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