CN101890325B - Fine solid particle recycling device and fluidized bed reactor comprising same - Google Patents
Fine solid particle recycling device and fluidized bed reactor comprising same Download PDFInfo
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- CN101890325B CN101890325B CN200910203552.1A CN200910203552A CN101890325B CN 101890325 B CN101890325 B CN 101890325B CN 200910203552 A CN200910203552 A CN 200910203552A CN 101890325 B CN101890325 B CN 101890325B
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Abstract
The invention provides a fine solid particle recycling device of a fluidized bed reactor, which comprises an injector connected with a dipleg, and the dipeg extends from a cyclone separator connected with the reactor, wherein fine solid particles are removed from the dipleg and mixed with injection gas for forming mixture of the injection gas-fine solid particles, thereby leading the fine solid particles to be recycled into the region of a fluidized bed, and further leading the fine solid particles to be reacted in the region of the fluidized bed for improving the reaction efficiency.
Description
Technical field
The present invention relates to a kind of fine solid particle to collect and recycle device and comprise its fluidized-bed reactor.
Background technology
Fluidized-bed reactor is generally used for making solid-phase reactant and vapor-phase reactant produce chemical reaction.The direct product of the fluidized bed region of this reactor is often called as exit flow, and it includes gaseous product and containing not producing the solid-phase reactant of chemical reaction or the solid particle of product (lime-ash).These solid particles are the particulate of various sizes.In order to improve the utilization ratio of solid-phase reactant, and in order to reduce the quantity of useless lime-ash, usually use the cyclone separator (multi-cyclone) of one-level or more level in a fluidized bed reactor.
In multi-cyclone builds, first order cyclone separator can be collected bulky grain and is recovered in fluid bed by solid particle by the coupling dipleg with various machinery or non-mechanical valves.But usual first order cyclone separator is insufficient or effective for removing fine solid particulate.Therefore, after first order cyclone separator, usually another primary cyclone also had at least to collect the fine particles leaked out from first order cyclone separator.If when fluid bed carries out work at lower than the temperature of 800 DEG C, Normal practice adopts cyclone dip-leg insert to be positioned in fluid bed, as used in fluid catalytic cracking unit; See the the 3rd, 652, No. 446, the 4th, 220, No. 623 and the 4th, 578, No. 183 United States Patent (USP)s.
When fluid bed is at higher than the temperature of 800 DEG C or when there is oxygen-containing gas in fluid bed and carrying out work, be difficult in fluid bed, adopt dipleg insert.This is because the material of fluid bed easily forms slag in the inside of dipleg and surface.
It is also vital for preventing gas from flowing backward to cyclone separator from fluid bed via cyclone dip-leg.Such as, in the fluid catalytic cracking (FCC) of refining industry, adopt various flapper valve to prevent in gas backflow feed back leg in one end of dipleg.Flapper valve can prevent it from flowing backwards by confining gas while permission solid particle flows out outside dipleg.The dipleg that one end has flapper valve can make this dipleg and this cyclone separator be installed on the inside of fluid bed.But because needs adopt resistant to elevated temperatures material when at high temperature using flapper valve, therefore price is surprisingly high.For fluidized bed combustion chamber or gasifier, the temperature of this fluid bed can reach 1050 DEG C, and most material can lost strength at such a temperature.In fact, flapper valve is adopted to be almost impossible.
Another kind of sealing dipleg prevents the method for gas backflow from being imbed disconnected for solid particle outlet in fluid bed.But, due to very strict to the requirement of manufactured materials, therefore need meticulous design to insert in this fluid bed to make dipleg.Therefore, Normal practice is incorporated into gasifier from outside by dipleg.In this approach, the interconnection of leading between the solid particle inlet of fluid bed and dipleg is furnished with heat proof material, and it can withstand higher temperatures.
One application-specific of fluid bed is that fluidized-bed gasifier is for being converted into fuel or synthesis gas by the carbonaceous material of such as coal etc.In this gasifier, after first order cyclone separator, the mean particle dia staying the solid particle in gas is less than about 100 microns usually, and it has the average diameter of about 15 to 20 microns.These particulates usually have coagulability and are difficult to be fluidized, and are recycled in gasifier to effectively be sent by solid particle, and those particulates are expected to flow as liquid as fine sand; But the agglomerated particles in the cyclone separator of the second level, but the spitting image of wheat flour, forms the caking and raceway groove that are not fluidized.Therefore, be difficult to solid particle to be recycled to gasifier.
The coagulability of solid particle creates another difficulty of solid particle recycling.Normally, the solid particle being collected in cyclone separator makes freely falling body downwards along dipleg, bottom dipleg, form an intensive post.Can form a hydrostatic head (static head) when solid particle close is fluidized mutually, it is very important from the relatively low pressure region bottom cyclone dip-leg to the movement of the fluidized bed region in relatively high pressure region for solid particle.Owing to there is the intensive post of solid particle, the flowing of solid particle also maintains the sealing of system.But the solia particle condensed in cyclone dip-leg can not produce hydrostatic head.Particularly for the fine particle be collected in the cyclone separator of the second level.Therefore the particulate owing to condensing in dipleg, the solid particle of second level cyclone collection easily can not be recovered utilization.
There is above-mentioned difficulties owing to being recovered in gasifier by fine-particle solid particle, coml fluidized-bed gasifier does not adopt second level cyclone separator usually.Therefore, in the solid particle at first order Cyclone outlet place, the solid reactant such as such as carbon can not be utilized, and result in lower gasifier efficiency of carbon con version.Such as, utilizing the gasifier efficiency of carbon con version of prior art to be only approximately 80-85%, is the contour reaction coal of such as brown coal and subbituminous coal even if used.Carbon loss is a significant deficiency economically, and threatens because the lime-ash discharged in a large number also produces environment.Further, the fine solid particle of carbon containing is also comparatively light, and in usual per unit mass, its volume is 4-5 times of water, makes be difficult to process and utilize further.Utilized more fully once the carbon in solid particle, final solia particle will have higher volume density, more easily by humidifying and process.
Therefore, need a kind of new device solid particle can be recovered to area of low pressure from high-pressure area, thus improve the efficiency of carbon con version of fluid bed.
Summary of the invention
The invention provides a kind of innovative solution about recycling fine particle from the unstrpped gas of fluidized-bed reactor.In one embodiment, the invention provides a kind of fine particle recycle device of fluidized-bed reactor, wherein this fluidized-bed reactor comprises one and surrounds by reaction tube the fluidized bed region formed, at least one cyclone separator is communicated with fluidized bed region fluid, the first gas-solid mixture of fine solid particle is contained for receiving package, this cyclone separator is connected for the dipleg collecting isolated fine solid particle from the gas-solid mixture of cyclone separator with one, this device comprises an injector be connected with this dipleg, wherein fine solid particle is removed from this dipleg, and be mixed with ejection gas to form ejection gas-fine solid particle mixture, fine solid particle is recovered in fluidized bed region by it.Although injector is generally used for the transmission of solid particle, be unknown at downstream pressure before making the present invention higher than adopting injector when downstream pressure.Better ejection gas of the present invention or motive gas can be N
2, CO
2, air, steam, O
2or its mist.
In another embodiment, in fine solid particle recycling device of the present invention, dipleg is sit upright, and dipleg is connected with the solid particle import of injector by a horizontal leg.Horizontal leg flows to injector to prevent gas backflow injector to cyclone separator for controlling gas and solid particle stream from dipleg.
Horizontal leg comprises the first end that is connected with dipleg and the second end away from this dipleg.In one embodiment, in fine solid particle recycling device of the present invention, a vertical component effect is arranged between the second end of horizontal leg and the solid particle import of injector further.This vertical component effect controls gas better further and solid particle stream flows with the direction expected.
Fine solid particle recycling device in another embodiment can comprise one or more ventilating opening being arranged at this injector downstream further to promote that ejection gas-fine solid particle mixture is recovered to fluidized bed region.
The present invention is particularly useful for collecting or recycling to have the fine solid particle being less than about 100 micron-scales, especially has the fine solid particle of the mass mean diameter of about 15 to 20 microns.
The present invention further provides the fluidized-bed reactor that comprises above-mentioned fine solid particle recycling device.In the preferred embodiment, be fluid bed coal-gasification device according to fluidized-bed reactor of the present invention.
In the preferred embodiment, fluidized-bed reactor of the present invention comprises secondary or multi-cyclone, and wherein every grade of cyclone separator is provided with an injector.In another embodiment, fluidized-bed reactor of the present invention comprises secondary or multi-cyclone, and wherein an injector is arranged at second level cyclone separator, or is arranged at arbitrary cyclone separator after this second level cyclone separator.
Accompanying drawing explanation
Fig. 1 is the schematic diagram that display one gasifier is equipped with for the first order and second level cyclone separator solid particle being recycled to gasifier;
Fig. 2 is the schematic diagram of display one embodiment of the invention; And
Fig. 3 is the structural representation that be furnished with the injector of heat proof material of display for high temperature.
Detailed description of the invention
The invention provides a kind of fine solid particle to collect and recycle device and comprise its fluidized-bed reactor.
Fig. 1 gives the relative position of the various main elements of the fluidized bed reactor system including fine solid particle recycling device of the present invention.
As shown in Figure 1, this fluidized bed reactor system comprises gasifier 10, first order cyclone separator 20 and second level cyclone separator 30.
This gasifier 10 comprises gas feed 11, solid particle import 12 and gas and solid particle outlet 13.This gas feed 11 is positioned at the below of gasifier 10, inputs air-flow and oxygen for the inside to gasifier 10.This solid particle import 12 is positioned at the sidewall of gasifier 10, for the inside input coal solid particle to gasifier 10.As previously mentioned, can chemical reaction be there is in the inside of gasifier 10, and produce the product containing gas and solid particle.This gas and solid particle outlet 13 are for exporting gas and solid particle stream to the first cyclone separator 20.This first order cyclone separator 20 comprise gas and solid particle inlet 21, superposed gas and solid particle outlet 22 and be positioned at bottom solid particle outlet 23.This gas and solid particle inlet 21 are for receiving the gas and solid particle stream that are transmitted by gasifier 10 to carry out cyclonic separation.This gas and solid particle outlet 22 are for exporting the gas comprising less solid particle and solid particle stream that obtain after being separated to second level cyclone separator 30.This solid particle outlet 23 for exporting by a ring seal wind structure coal solid particle obtained after cyclonic separation to gasifier 10, and again utilizes with the air-flow of its inside and oxygen generation chemical reaction again in gasifier 10.This second level cyclone separator 30 comprises the gas that is positioned at sidewall and solid particle import 31, is positioned at the gas vent 32 of top and is positioned at the solid particle outlet 33 of below.This gas and solid particle import 31 are for receiving the gas and solid particle stream that are transmitted by first order cyclone separator 20 to carry out cyclonic separation again.This gas vent 32 is for exporting synthesis gas.The outlet of this solid particle 33 for exporting the solid particle obtained after cyclonic separation, and makes solid particle be sent in gasifier 10 by an injector 50 (as shown in Figure 2) again to utilize.Its specific implementation process will specifically describe below in conjunction with Fig. 2 and Fig. 3.
In one embodiment, the invention provides a kind of device being less than the fine solid particle of about 100 microns from cyclone collector recovery size, it is recovered in fluidized bed region under the air pressure slightly lower than the fluidized bed region of fluidized-bed reactor.
In one embodiment, the cyclone separator 30, that fine solid particle retracting device of the present invention comprises the solid particle that a collection air-flow carries as shown in Figure 2 receives solid particle and the dipleg 40 be preferably positioned at below cyclone separator; And the injector 50 that is communicated with dipleg outlet fluid.
Cyclone separator 30 is one utilize centrifugal force by fluid and the device being carried on the separation of particles in fluid.Conventional cyclone in fluidized-bed reactor is used for gas to be separated with solid particle.Cyclone separator 30 have at least one solid particle carrying air-flow tangential inlet 31, have less solid particle carrying gas vent 32 and another collect solid particle outlet 33.As shown in Figure 2, for most of conventional cyclone 30, gas and solid particle 31 import are usually located at sidewall, and gas vent 32 is positioned at top, and solid particle outlet 33 is positioned at bottom.
This cyclone separator can comprise cylindrical portion 34 and the conus portion 35 be connected with this cylindrical portion 34.The top (solid particle import) of dipleg 40 is connected with the narrow end (solid particle exports) of cyclone separator 30 conus portion 35.
In another embodiment, dipleg 40 of the present invention is the body of a coupling, and it has and exports 33 imports be connected 41 with cyclone separator 30 solid particle, and the outlet 42 be connected with a horizontal 43.This horizontal 43 the most at last solid particle is sent to an injector 50, and it is connected with the solid particle outlet (i.e. injector 50) of fluidized bed region solid particle being recycled to reactor.Because the pressure of fluidized bed region is higher than the fluid pressure in cyclone separator 30, therefore when not having injector 50, the pressure of the import 41 of dipleg 40 is by the pressure of the outlet 42 lower than dipleg 40.
As everyone knows, fluid can not flow to high-pressure area from area of low pressure, therefore needs a kind of special design.As mentioned above, dipleg 40 is realized gas solids granulate mixture for the hydrostatic head produced by fluidized mass in dipleg 40 and flows to high-pressure area from area of low pressure.But, for the particulate in second level cyclone dip-leg 40, as previously mentioned because the particulate of cohesion can not, by traditional method institute fluidisation, therefore be difficult to set up hydrostatic head.Because solid particle post requires that fluidisation is to set up hydrostatic head, in the dipleg 40 of therefore second level cyclone separator 30, particulate can not produce hydrostatic head, thus does not have outside help just can not flow out from dipleg 40.
In one embodiment, the present invention utilizes an injector 50 to overcome above-mentioned difficulties.Injector is have the first import 51 (" former dynamic fluid inlet ") that a high-pressure fluid is also called as former dynamic fluid; Second import 52 (" solid particle import ") of one release solid particle; And one discharges the device being mixed with the outlet 53 of the former dynamic fluid of solid particle.According to Bernoulli principle, the kinetic energy rejection of motive gas will produce low pressure thus be introduced in injector 50 by solid particle in solid particle import 52 region, so be pushed out outlet under the air pressure injecting at motive gas and produce.
As shown in Figures 2 and 3, in a preferred embodiment, injector 50 comprises a narrow portion 54, and it is narrower than the body downstream portion leading to outlet.The caliber increase in narrow portion 54 downstream to reduce in body air-flow from narrow portion to the speed of release, thus decreases the atmospheric pressure lost because frictional force produces, and meeting motive gas needs more hypobaric requirement.
According to one embodiment of present invention, when gas solids granulate mixture tangentially enters cyclone separator 30 from sidewall, solid particle can promote to sidewall by centrifugal force.Acceleration due to centrifugal force approximate inlet line speed square divided by the radius of cyclone separator, the centrifugal force therefore acting on identical particulate is compared to the gravitational high 100 times for identical particle mass usually.Therefore, the little particulate to 5 microns can rotate towards sidewall.In sidewall areas, the speed of fluid is lower and solid particle is collected in sidewall areas, flows towards outlet at bottom 33 so downward under gravity.
In another embodiment, the bottom in cyclone separator 30 tapering 35 is connected with dipleg 40 as shown in Figure 2.The solid particle on dipleg 40 top is in diluted state (dilute phase) and can falls along sidewall under gravity.Because solid particle is collected in direction, dipleg 40 bottom, solid particle slows down and engages with the close of dipleg.Although the close phase of fine particle oneself can not form hydrostatic head, can not only be moved to outside dipleg at gravity but also in the effect of injector 50 attraction according to the present invention.
Have less solid particle carrying gas can to the central flows of cyclone separator 30 and the final low pressure due to exit flow to the outlet 32 at top.
Motive gas: motive gas can be N
2, CO
2, air, steam, O
2or its mist.Preferably, motive gas is that a kind of gasifying agent that is used as in gasifier 10 is to generate the gas of synthesis gas.The former dynamic fluid source of high pressure draught is produced by compressor or pumping usually.The N that nitrogen compressor produces
2can be used for fluidized-bed gasifier 10 injection solid particle.Negative pressure that is that produce or that expect can calculate with well-known method in prior art (for example, see Parker, J., Boggs, J., Blick, E., hydrodynamics and heat transfer are introduced, Addison-Wesley, 1970, pp163).In another embodiment, preferably gravitation is about 20-30kPa and release pressure is 35-70kPa.Preferably motive gas pressure ratio gasifier 10 operating pressure height 400-600kPa.
As previously mentioned, due to the coagulability of solid particle, the solid particle in dipleg 40 can not produce hydrostatic head and with traditional dipleg 40, it can not be recovered to high-pressure area from area of low pressure separately.According to the present invention, the effect of injector 50 produces low pressure in import 52 region of injector 50 thus at the local pressure of the import 52 of injector 50 lower than dipleg 40 base pressure be connected with cyclone separator 30 due to Venturi effect.Therefore, flow to injector 50 from dipleg 40 because solid particle stream facilitates solid particle stream from the flowing of relatively high pressure field flow orientation relatively low pressure region.
On the other hand, the high pressure of motive gas ensure that the pressure of pressure higher than fluidized bed region at outlet 53 place of injector 50.Solid particle is sent to fluidized bed region by the high pressure with motive gas kinetic energy.
In one embodiment, fine solid particle recycling device of the present invention comprises horizontal leg 43 further, and it is by injector 50, and the import 52 of injector 50 is connected with dipleg 40 specifically.The additional drag that this horizontal leg 43 adds gas and solid particle stream is sent to gasifier 10 to prevent a large amount of gas from cyclone separator 30.
This horizontal leg 43 can also prevent motive gas from upwards blowing back (refluence) in the dipleg 40 of cyclone separator 30, thus prevents in fluid bed, have unexpected pressure oscillation to upset the operation of cyclone separator 30.Due to the additional drag that horizontal leg 43 produces, the solid particle in horizontal leg 43 prevents gas to flow back to cyclone separator 30 from injector 50.When not having horizontal leg 43, diluent gas also can directly be drawn onto gasifier 10 from cyclone separator 30 by the negative inlet pressure that injector 50 produces.
Preferably horizontal leg 43 length reaches 4-12 times that is about horizontal diameter, and it is close to the comparatively low side of dipleg 40.If the very large motive gas air pressure of needs it is easily understood that horizontal leg 43 is oversize, can be made solid particle flow forward by those skilled in the art; When horizontal leg 43 too in short-term, horizontal leg 43 can not prevent gas from upwards flowing back in cyclone separator 30 fully.
In another embodiment, as shown in Figure 2 in solids inlet 52 place of injector 50, described dipleg 40 comprises vertical component effect 44 further, and it is connected with above-mentioned horizontal leg 43.Preferably the height of vertical component effect 44 is about the 6-8 of import 52 internal diameter of tube body of injector 50 doubly.
In certain embodiments of the present invention, ventilating opening (not shown) can be used for promoting that solid particle stream is from cyclone separator 30 to fluidized bed flow.Ventilating opening is arranged according to the bed of the fluid bed that the solids flow rate degree of precognition and solid particle turn back to.
In another embodiment, the ventilating opening of the vertical component effect 44 of dipleg 40 about spaced 1.5 to 2 meters usually, the internal diameter of ventilating opening is about 10-30 millimeter usually.Those ventilating openings are about that 30 to 60 directions spending angle tilt towards flow direction and with horizontal direction.Spaced 0.3 to 0.5 meter and identical with the ventilating opening diameter of vertical component effect 44 of the ventilating opening of horizontal part 43.Gas velocity in ventilating opening is between 2.5 to 5 meter per seconds.Internal diameter is less than to the dipleg 40 of 0.5 meter, a ventilating opening of the ad-hoc location of usual whole circumference is just enough.If when the internal diameter of dipleg 40 is greater than 0.5 meter, so at least one ventilating opening circumferentially can be arranged with certain height or position.
The present invention can realize high carbon conversions and reduce the flying dust quantity of gasifier 10 generation.
The present invention is applicable to fluidized-bed gasifier 10 and other require multi-cyclone and to need trickle condensed material to be recycled under high pressure and high temperature in the fluidization system of fluid bed any second or third-stage cyclone separator.The combustion chamber of such as fluid bed can adopt an injector 50 that solid particle is recycled to fluid bed, and can adopt a catalytic cracking regenerator.
Claims (11)
1. the fine solid particle recycling device of a fluidized-bed reactor; it is characterized in that; this fluidized-bed reactor comprises and surrounds by reaction tube the fluidized bed region formed; at least one cyclone separator is communicated with fluidized bed region fluid; the first gas-solid mixture of fine solid particle is contained for receiving package; this cyclone separator is connected for the dipleg collecting isolated fine solid particle from the gas-solid mixture of cyclone separator with one, and described dipleg is sit upright, and this device comprises:
One injector be connected with this dipleg, described injector has former dynamic fluid inlet and solid particle import, wherein, fine solid particle is removed from this dipleg, and with former dynamic fluid inlet gas and vapor permeation to form ejection gas-fine solid particle mixture, it makes fine solid particle be recovered in fluidized bed region;
One horizontal leg, the bottom of described dipleg is connected with the solid particle import of injector by described horizontal leg, thus controls gas and solid particle stream and flow to injector to prevent gas backflow injector to cyclone separator from dipleg.
2. fine solid particle recycling device as claimed in claim 1; it is characterized in that; described horizontal leg comprises the first end that is connected with dipleg and the second end away from this dipleg, and a vertical component is arranged between the second end of horizontal leg and the solid particle import of injector.
3. fine solid particle recycling device as claimed in claim 1, it is characterized in that, one or more ventilating opening is arranged at the downstream of this injector, to promote that ejection gas-fine solid particle mixture is recovered to fluidized bed region.
4. fine solid particle recycling device as claimed in claim 1, it is characterized in that, described ejection gas is N
2, CO
2, steam, O
2or its mist.
5. fine solid particle recycling device as claimed in claim 1, it is characterized in that, the diameter of described fine solid particle is less than 100 microns.
6. fine solid particle recycling device as claimed in claim 5, it is characterized in that, the average diameter of described fine solid particle tool is the fine solid particle of 15 to 20 microns.
7. one kind comprises the fluidized-bed reactor of fine solid particle recycling device as claimed in claim 1.
8. fluidized-bed reactor as claimed in claim 7, it is characterized in that, described fluidized-bed reactor is fluid bed coal-gasification device.
9. fluidized-bed reactor as claimed in claim 7, it is characterized in that, described fluidized-bed reactor comprises secondary or multi-cyclone.
10. fluidized-bed reactor as claimed in claim 9, it is characterized in that, described every grade of cyclone separator is provided with an injector.
11. fluidized-bed reactors as claimed in claim 9, it is characterized in that, an injector is arranged at second level cyclone separator, or is arranged at the cyclone separator after this second level cyclone separator.
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| CN200910203552.1A CN101890325B (en) | 2009-05-20 | 2009-05-20 | Fine solid particle recycling device and fluidized bed reactor comprising same |
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|---|---|---|---|
| CN200910203552.1A CN101890325B (en) | 2009-05-20 | 2009-05-20 | Fine solid particle recycling device and fluidized bed reactor comprising same |
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| CN101890325A CN101890325A (en) | 2010-11-24 |
| CN101890325B true CN101890325B (en) | 2015-05-13 |
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| CN104053753B (en) * | 2011-06-24 | 2016-01-20 | 综合能源有限公司 | Catch and recycle the system and method for particulate |
| CN110606175B (en) * | 2018-06-15 | 2021-03-30 | 北京航空航天大学 | Mixed working medium for passenger escape rapid injection inflation system |
| CN112387434A (en) * | 2020-10-29 | 2021-02-23 | 西安热工研究院有限公司 | Cyclone separator suitable for boiler dust removal and feed back |
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| US4931260A (en) * | 1987-01-31 | 1990-06-05 | Rheinische Braunkohlenwerke Ag | Process and apparatus for the treatment of granular solid materials in a fluidized layer |
| CN1054302A (en) * | 1990-02-21 | 1991-09-04 | 中国科学院工程热物理研究所 | Fluidized bed combustion apparatus with graded circulation |
| US6488901B1 (en) * | 1997-05-07 | 2002-12-03 | Metallgesellschaft Ag | Method of adjusting a circulating fluidized bed and use of the method |
| CN101261010A (en) * | 2008-04-22 | 2008-09-10 | 青岛科技大学 | Double distribution plate coal-base serial fluidized-bed chemical chain combustion apparatus |
| CN201225613Y (en) * | 2008-06-23 | 2009-04-22 | 中国华电工程(集团)有限公司 | Circulating fluid bed boiler of stalk biomass for combustion |
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2009
- 2009-05-20 CN CN200910203552.1A patent/CN101890325B/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4931260A (en) * | 1987-01-31 | 1990-06-05 | Rheinische Braunkohlenwerke Ag | Process and apparatus for the treatment of granular solid materials in a fluidized layer |
| CN1054302A (en) * | 1990-02-21 | 1991-09-04 | 中国科学院工程热物理研究所 | Fluidized bed combustion apparatus with graded circulation |
| US6488901B1 (en) * | 1997-05-07 | 2002-12-03 | Metallgesellschaft Ag | Method of adjusting a circulating fluidized bed and use of the method |
| CN101261010A (en) * | 2008-04-22 | 2008-09-10 | 青岛科技大学 | Double distribution plate coal-base serial fluidized-bed chemical chain combustion apparatus |
| CN201225613Y (en) * | 2008-06-23 | 2009-04-22 | 中国华电工程(集团)有限公司 | Circulating fluid bed boiler of stalk biomass for combustion |
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