CN1290603C - Reactor of fluidized bed - Google Patents
Reactor of fluidized bed Download PDFInfo
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- CN1290603C CN1290603C CN 200510049233 CN200510049233A CN1290603C CN 1290603 C CN1290603 C CN 1290603C CN 200510049233 CN200510049233 CN 200510049233 CN 200510049233 A CN200510049233 A CN 200510049233A CN 1290603 C CN1290603 C CN 1290603C
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- thimble tube
- gas
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- fluidized
- cone body
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- 238000005243 fluidization Methods 0.000 abstract description 16
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- 238000013461 design Methods 0.000 description 11
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 10
- 239000003054 catalyst Substances 0.000 description 10
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 8
- 239000000428 dust Substances 0.000 description 6
- 239000000178 monomer Substances 0.000 description 6
- 229910052710 silicon Inorganic materials 0.000 description 6
- 239000010703 silicon Substances 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 235000013312 flour Nutrition 0.000 description 5
- 239000000377 silicon dioxide Substances 0.000 description 5
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical group [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 4
- 230000008859 change Effects 0.000 description 4
- YGZSVWMBUCGDCV-UHFFFAOYSA-N chloro(methyl)silane Chemical compound C[SiH2]Cl YGZSVWMBUCGDCV-UHFFFAOYSA-N 0.000 description 4
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- LIKFHECYJZWXFJ-UHFFFAOYSA-N dimethyldichlorosilane Chemical compound C[Si](C)(Cl)Cl LIKFHECYJZWXFJ-UHFFFAOYSA-N 0.000 description 1
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The present invention discloses a fluidized bed reactor. A gas distributor is arranged between a lower cone and a gas predistribution chamber, and finger sleeve pipe bundles are symmetrically distributed on the distributor and are vertically arranged as a conical surface. The vertical finger sleeve pipe bundles are communicated with and inlet and an outlet of heat transfer media out of the lower cone, and solid feed inlets for returned stock and raw materials are also arranged out of the lower cone. A raw gas inlet is arranged out of the gas predistribution chamber, upper sealing heads are symmetrically distributed as conical surface dropping type finger sleeve pipe bundles, the upper cone is provided with a synthetic gas outlet and an inlet of the heat transfer media of the finger sleeve pipe bundles, and an outlet of the heat transfer media of the finger sleeve pipe bundles are arranged on the upper sealing heads. The conicity of the upper cone and the lower cone and the two finger sleeve pipe sections are axially distributed and are matched and changed according to material particle size distribution, so bottom gas speed in the reactor is high, and top gas speed is low. The reactor can effectively processes the fluidization of broad particle size distribution particles, adjust fluidization cross-sectional area and improve fluidization quality. The heat transfer media control temperature via sections and parts, so the present invention is easy to satisfy technical requirements.
Description
Technical field
The present invention relates to a kind of wide particle diameter distribution fluidisation granular system, strong heat release and the gas-solid of luming easily fluidized-bed reactor mutually that is applicable to.
Background technology
Fluidized-bed reactor relates to the system that solid material that a lot of wide particle diameters distribute or solid grain size reduce gradually with reaction, and is synthetic etc. such as the ore roast in industrial coal dust firing, the metallurgical industry, organic silicon monomer in the chemical industry.
For fluidized-bed combustion boiler, because distribution of the wide particle diameter of fuel (coal dust) granularity and operating air velocity have considerable influence to the operating mode of bubbling fluidized bed and recirculating fluidized bed, gas-solid flow process more complicated in the stove, particle phase concentration scope alters a great deal from high to low and (reaches 1～1000kg/Nm
3).And in combustion process, what often run into is the variable mass motion problems, and, fugitive constituent broken as the heat of coal grain after feeding fluid bed separated out, caught fire and combustion reaction weightlessness etc.
Organic silicon monomer (methylchlorosilane) adopts the Rochow direct method synthetic usually, solid material in the synthetic reaction is a silicon powder particle, catalyst is a copper powder particle, and chloromethanes and gaseous reaction products play the effect of fluidizing agent, Gu Gu course of reaction be gas--reaction.The methylchlorosilane of unreacted chloromethanes, gaseous state, the byproduct of gaseous state, catalyst component and fine dust leave reactor.Silica flour and copper powder fully contact and effectively withdraw from reaction heat to reaction important influence, the therefore industrial production of all adopting the continuous fluid bed bioreactor to realize the methylchlorosilane monomer.In order to obtain the selectivity of high as far as possible target product (dimethyldichlorosilane), not only need high as far as possible productive rate (the formed silane quantity of time per unit and reaction volume), and need the reliable and elastic operation of high as far as possible silicon conversion ratio and whole factory.Silicon powder particle itself just has very wide particle diameter and distributes, and in process of production, silica flour is constantly consumed, and particle diameter changes, and constantly replenishes fresh silica flour to reactor simultaneously.In addition, the particle diameter of catalyst copper powder is less relatively, has than big-difference with the silica flour particle diameter.Therefore, it is wide to be in the principal character of organic silicon monomer fluidized bed reactor that solid grain size distributes, and contains more fine powder, needs to realize the abundant mixing of different-grain diameter particle.Key is to need to solve the heat transfer problem of reaction and the fluidisation problem of wide distributed granule.
The direct method synthesizing methyl-chloro-silane is a strong exothermal reaction, for in time discharging the reaction liberated heat, U type pipe or thimble tube generally all are set as heat exchange structure in fluid bed, the every pipe that present U type pipe that uses or thimble tube have is connected with outer tube separately, what have organizes with several Guan Weiyi, is connected with outer tube then.But, because reaction is lumpd easily, cause fluidized state to worsen, product quality descends, and reaction selectivity reduces.Can luming by dust stratification in U type pipe bottom, causes the problem of hot-spot fever, and adopt the thimble tube type heat exchanger.But because it is arranged on the fluid bed top, thimble tube is very long, causes that heat exchange is irregular up and down, bottom heat transfer intensity height, and heat exchange of top part intensity is low.
Patent CN 2456835Y has introduced two kinds of existing organic silicon monomer resultant current fluidized bed reactors, a kind of half cone bed bioreactor for water evaporation heat-obtaining; Another kind is the cylindrical bed reactor of simple oil heat-obtaining.The no heat-obtaining face conversion zone of suitable thickness is arranged at the half cone bed bottom of the half cone bed bioreactor of water evaporation heat-obtaining.It is to adopt to add water to finger-type nest of tubes bottom intermittence (or inhomogeneous), boiled water evaporation in very short zone, and the end of water evaporating area is cooled to contact (catalyst+silica flour) material below the reaction temperature.Bed particle up all is lower than reaction temperature again, and synthetic reaction does not take place these contacts.This class reactor production capacity is low, and bed end temperature fluctuation is frequent, and the steam flow of generation is extremely unstable, so be difficult to this part heat energy of comprehensive utilization.
The bottom section of general fluid bed adopts conical bed, improve all abundant fluidisation of material that fluidizing velocity makes different-grain diameter, and section is amplified in the top employing, make the gas prompt drop low, thereby make material be easy to deposit, be difficult for being taken out of, reduce the load of piece-rate system thereafter by gas.But dozens or even hundreds of heat exchanger tube arranged for very big large-scale fluidized bed of exothermic heat of reaction amount, the adding of heating surface bank, for equal cylinder fluid beds straight, can significantly reduce bed body net sectional area, cause empty tower gas velocity too high, thereby the little particle of granularity is blown easily, particularly for the organic silicon monomer production process, because the granularity of catalyst copper powder is very little, makes catalyst be blown a body easily, thereby influences course of reaction.
Patent CN 1425494A has introduced a kind of large-scale fluidized bed reactor that is applicable to the wide-size distribution fluidized particles, it is made up of main bed, conical bed, dactylethrae heat exchange inner member, gas distributor, it is characterized in that on the gas distributor of conical bed bottom, introducing the up-small and down-big body structure of falling the female cone, its semi-cone angle 5～13 degree.After in conical bed, introducing the body structure of falling the female cone, under the certain situation of throughput, can effectively change fluidizing cross-section area, just relative bigger in the gas speed of bed bottom, be beneficial to the initial fluidisation of particle, thus raising fluidization quality.Another advantage of introducing the body structure of falling the female cone is exactly the amplification design that helps such reactor.If the simple conical bed structure that in design, only adopts, if the scale of fluidized-bed reactor further enlarges so, for half inclination angle that guarantees conical bed within the specific limits, the height of conical bed part will inevitably be very big, bring difficulty so just for the appropriate design and the processing of whole reactor, even can not satisfy the chemical technology condition.By introducing the female cone body structure, just the height of conical bed can well be controlled within the specific limits.
Summary of the invention
The object of the present invention is to provide and be applicable to wide particle diameter distribution fluidisation granular system, strong heat release and a kind of gas-solid of luming easily fluidized-bed reactor mutually, the broad particle distribution that is particularly useful for solid particle, or solid particle is participated in reaction, the gas-solid reaction system that its granularity diminishes gradually along with course of reaction.
The technical solution adopted for the present invention to solve the technical problems is:
The present invention includes successively and constitute by top end socket, up big and down small upper cone body, cylinder, up big and down small pre-distributing chamber of lower cone body, gas and bottom head; Between lower cone body and the pre-distributing chamber of gas gas distributor is set, vertical thimble tube bundle is installed in the gas distributor top, be multilayer equidistantly or equidistant concentric circles distribute, or it is uniform to be equilateral triangle; The terminal middle height low taper seat all around that forms of the vertical thimble tube bunchy top portion of different length, heat transferring medium import that vertical thimble tube bundle is external with being contained in lower cone and heat transferring medium outlet are communicated with, external feed back charge door and the raw material solid charge door of also being equipped with of lower cone, the pre-outdoor raw material gas inlet that is equipped with that distributes of gas, the top end socket is equipped with the droop thimble tube bundle of different length, low high taper seat all around in the middle of droop thimble tube bundle lower end forms, the upper cone body have syngas outlet and with the thimble tube heat transferring medium import of droop thimble tube Shu Liantong, the outlet of thimble tube heat transferring medium is housed on the end socket of top.
The vertical thimble tube bundle of symmetrical distribution different length on the described gas distributor, low taper seat around the height in the middle of the terminal formation of vertical thimble tube bunchy top portion, its cone angle scope is 30～150 degree.
Described droop thimble tube bundle subregion is arranged, according to interlacing subregion or concentric circles subregion or angle subregion, be divided into 1 subregion, 2 subregions, 3 subregions or 4 subregions according to cylinder diameter and heat exchanger tube number, the number of partitions is identical with thimble tube heat transferring medium import number.
Described top end socket is equipped with the droop thimble tube bundle of different length, low high taper seat all around in the middle of the lower end of droop thimble tube bundle forms, and its cone angle scope is 30～150 degree.
The cylinder height of described reactor is 5～15 meters, and the cylinder diameter is 0.5～6 meter, and the angle of taper of reactor upper cone body and lower cone body is 5～30 degree.
The upper cone body of this fluidized-bed reactor and the angle of taper of lower cone body, the length of droop thimble tube bundle and vertical thimble tube bundle is in axial distribution, can distribute according to material particular diameter cooperate variation, makes that fluid bed inner bottom part gas speed is big and top gas speed is little.Under the certain situation of throughput, can effectively change the cross-sectional area of fluidized-bed reactor bed body.Want big in the gas speed of reactor lower part cone with respect to cylindrical bed and common conical bed, help oarse-grained initial fluidisation in the wide distribution material of initial fluidisation, especially particle diameter of particle, thus raising fluidization quality.And in reactor head, adopt the conical bed body of small-angle, under the prerequisite of avoiding the dust stratification caking, can significantly improve the cross-sectional area of a body, reduce empty tower gas velocity, make granule (catalyst or solid reactant) to fall as much as possible and get back to cylinder and lower cone body, reduce the outside Cyclonic separating apparatus of fluidized-bed reactor or the load of filter plant.Make reaction formed and, can be used again effectively by fine catalyst dust and raw material dust that product is carried outside.Advantage is exactly to help prolonging the thin reaction raw materials and the time of staying of catalyst fines in reactor.
Heat transferring medium can enter droop from the fluidized-bed reactor top and hang the thimble tube bundle, can advance simultaneously
Go into the vertical thimble tube bundle on the gas distributor of fluid bed bottom, realize the sectional temperature-controlled up and down of fluid bedreactors inside.Reaction generally concentrates on gas distributor top near zone, this regional thermal discharge is big, therefore adopts the vertical finger-type heat exchange sleeve bundle of reactor bottom effectively to remove heat of reaction, and reacting balance is carried out, avoid hot-spot, produce charing and agglomeration problems.
Droop hangs the design form that thimble tube bundle and two sections heat-exchanging tube bundles of vertical finger-type heat exchange sleeve bundle all can adopt the subregion adding.Heat transferring medium enters the dactylethrae heat exchange component from reactor head by several different subregions, discharges after heat exchange.Number of partitions can be 1～4 according to fluid bed cylinder diameter, and the discharge of heat transferring medium (steam or heat exchange oil) concentrates on an outlet.By such zoning design, heat transferring medium evenly can be distributed, also made things convenient for the amplification design of reactor simultaneously.
Can reach optimized mode of operation by above design and the concrete parameter of local adjustment.
The useful effect that the present invention has is: the length of the upper cone body of fluid bed and the tapering of lower cone body and two sections finger-type heat exchanger tubes is in axial distribution, distribution cooperates variation according to material particular diameter, make that fluid bed inner bottom part gas speed is big and top gas speed is little, so fluidized-bed reactor of the present invention can effectively be handled the fluidisation of wide particle diameter distributed granule, adjust fluidizing cross-section area, improve fluidization quality.Because the design form that heat transferring medium takes segmentation and subregion to add carries out temperature control, technological requirement is content with very little simultaneously.Fluidized-bed reactor of the present invention is applicable to the gas-solid phase reaction that fluidized particles system, thermal discharge are big and reactant easily lumps that wide particle diameter distributes.
Description of drawings
Fig. 1 is a change cone fluidized-bed reactor structural representation of the present invention;
Fig. 2 is gas distributor of the present invention and bottom vertical heat-exchanging tube bundle distribution schematic diagram;
Fig. 3 is a thimble tube bundle heat exchanger tube subregion schematic diagram of the present invention;
Fig. 4 is the empty tower gas velocity comparison diagram of fluidized-bed reactor of the present invention and the straight tube of traditional half cone bed bioreactor.
Among the figure: 1, thimble tube heat transferring medium outlet, 2, the import of thimble tube heat transferring medium, 3, droop thimble tube bundle, 4, half-pipe jacket, 5, the upper cone body, 6, cylinder, 7, lower cone body, 8, the feed back charge door, 9, vertical thimble tube bundle, 10, gas distributor, 11, the heat transferring medium import, 12, the pre-distributing chamber of gas, 13, bottom head, 14, raw material gas inlet, 15, the heat transferring medium outlet, 16, raw material solid charge door, 17, syngas outlet, 18 top end sockets.
The specific embodiment
The invention will be further described below in conjunction with drawings and Examples.
As shown in Figure 1, the present invention is made of top end socket 18, up big and down small upper cone body 5, cylinder 6, up big and down small pre-distributing chamber 12 of lower cone body 7, gas and bottom head 13 successively; At lower cone body 7 and 12 of the pre-distributing chamber of gas gas distributor 10 is set, vertical thimble tube bundle 9 is installed in gas distributor 10 tops, be multilayer equidistantly or equidistant concentric circles distribute, or it is uniform to be equilateral triangle; High low taper seat all around in the middle of vertical thimble tube bundle 9 top end of different length form, heat transferring medium import 11 that vertical thimble tube bundle 9 is outer with being contained in lower cone body 7 and heat transferring medium export 15 and are communicated with, lower cone body 7 outer feed back charge door 8 and the raw material solid charge doors 16 of also being equipped with, the pre-distributing chamber of the gas 12 outer raw material gas inlet 14 that are equipped with, top end socket 18 is equipped with the droop thimble tube bundle 3 of different length, low high taper seat all around in the middle of droop thimble tube bundle 3 lower end form, thimble tube heat transferring medium outlet 1 is equipped with in the thimble tube heat transferring medium import 2 that upper cone body 5 has syngas outlet 17 and is communicated with droop thimble tube bundle 3 on the top end socket 18.
The vertical thimble tube bundle 9 of the different length that is symmetrically distributed on the described gas distributor 10, high low taper seat all around in the middle of vertical thimble tube bundle 9 top end form, its cone angle scope is 30～150 degree.
As shown in Figure 2, described vertical thimble tube bundle 9 is installed in gas distributor 10 tops, be equidistantly or the equidistant concentric circles of multilayer and distribute, or it is uniform to be equilateral triangle.
As shown in Figure 3, described droop thimble tube bundle 3 subregions are arranged, according to interlacing subregion (shown in Fig. 3 a) or concentric circles subregion (shown in Fig. 3 b) or angle subregion (shown in Fig. 3 c), can be divided into 1 subregion, 2 subregions, 3 subregions or 4 subregions according to cylinder 6 diameters and heat exchanger tube number, the number of partitions is identical with thimble tube heat transferring medium import 2 numbers.
Described top end socket 18 is equipped with the droop thimble tube bundle 3 of different length, high taper seat around the centre that the lower end of droop thimble tube bundle 3 forms is low, and its cone angle scope is 30～150 degree.
The cylinder 6 of described reactor highly is 5～15 meters, and cylinder 6 diameters are 0.5～6 meter, and the angle of taper of reactor upper cone body 5 and lower cone body 7 is 5～30 degree.
Operation principle of the present invention is as follows:
Unstripped gas process raw material gas inlet 14 backs to distributing, enter gas distributor 10 all around then in the pre-distributing chamber 12 of gas, distribution of gas is more even.The percent opening of gas distributor 10, perforate number, nozzle angle degree and aperture, the parameter and the bed pressure drop of association reaction device and vertical thimble tube bundle 9 come optimal design, guarantee that fluidized-bed reactor is in optimized mode of operation.
The reactant solid material adds reactor in advance, reacts by bringing into after gas fluidized in lower cone body 7 and the cylinder 6.The gas-phase reaction product is discharged from syngas outlet 17.Need the raw material solid that replenishes in reaction, enter lower cone body 7 from raw material solid charge door 16, the fine grained from the reactor external separator reclaims need return lower cone body 7 from feed back charge door 8.
Described fluidized-bed reactor inside is equipped with many droop thimble tube bundles 3 and vertical thimble tube bundle 9 vertically arranged, is used to shift out reaction heat.The introducing of thimble tube bundle can be so that this fluidized-bed reactor be specially adapted to the reaction system of those strong heat releases.And do not have horizontal heat exchange and fluidisation member, therefore can avoid dust stratification and caking.The distribution mode of thimble tube bundle can adopt equidistantly or the equidistant concentric circles of multilayer to distribute, or adopts equilateral triangle uniform.Heat transferring medium can adopt the mode of desalted water vaporization, perhaps adopts the mode of conduction oil heat exchange.Can adjust the number of heat exchange component according to actual exchange capability of heat.The heat exchange structure that is arranged in the body comprises: be arranged on the equally distributed droop thimble tube bundle 3 in upper cone body 5, cylinder 6 and the lower cone body 7; Be arranged in the lower cone body 7 the equally distributed vertical thimble tube bundle 9 on gas distributor 10 tops; With the half-pipe jacket 4 that is provided with in fluidized-bed reactor bed external body.The present invention adopts two sections heat-exchanging tube bundle modes, carries out sectional temperature-controlled.Top droop thimble tube bundle 3 is evenly flowed in the every thimble tube chuck from thimble tube heat transferring medium import 2 by heat transferring medium, imports heat transferring medium outlet 1 from the thimble tube centre bore after heat exchange, flows out fluid bed again; The bottom heat-exchanging tube bundle is evenly flowed in the every thimble tube chuck by heat transferring medium import 11, imports heat transferring medium outlet 15 from the thimble tube centre bore after heat exchange, flows out fluid bed again; In the present invention, droop thimble tube bundle 3 can further be taked the form of zoning design, as shown in Figure 3, according to interlacing subregion (shown in Fig. 3 a, being divided into 2 districts) or concentric circles subregion (shown in Fig. 3 b, being divided into 2 districts) or angle subregion (shown in Fig. 3 c, being divided into 3 districts), be divided into 1 subregion, 2 subregions, 3 subregions or 4 subregions according to cylinder 6 diameters and finger-type heat exchanger tube number, the number of partitions is identical with thimble tube heat transferring medium import 2 numbers.This design can effectively be controlled reaction and remove heat.
Embodiment: Fig. 4 is the empty tower gas velocity comparison diagram of fluidized-bed reactor of the present invention and the straight tube of traditional half cone bed bioreactor.The abscissa of Fig. 4 is the fluidized-bed reactor height H, and the ordinate of Fig. 4 is empty tower gas velocity V.Compare with half cone straight tube fluidized-bed reactor (1.6 meters of diameters) commonly used, change conical bed body of the present invention and finger-type heat-exchanging tube bundle cooperate, and the cross-sectional area of formation is littler at reactor bottom, and empty tower gas velocity V is higher, helps oarse-grained fluidisation; The cross-sectional area of reactor head is bigger relatively, and empty tower gas velocity significantly reduces, and helps the falling of granule or catalyst fines, alleviates the load of separation and filter.Reaction temperature control is stable more and convenient.
Claims (5)
1, a kind of fluidized-bed reactor is characterized in that: be made of top end socket (18), up big and down small upper cone body (5), cylinder (6), up big and down small lower cone body (7), the pre-distributing chamber of gas (12) and bottom head (13) successively; Between lower cone body (7) and the pre-distributing chamber of gas (12) gas distributor (10) is set, vertical thimble tube bundle (9) is installed in gas distributor (10) top, be multilayer equidistantly or equidistant concentric circles distribute, or it is uniform to be equilateral triangle; High low taper seat all around in the middle of vertical thimble tube bundle (9) top end of different length forms, heat transferring medium import (11) and heat transferring medium outlet (15) that vertical thimble tube bundle (9) is outer with being contained in lower cone body (7) are communicated with, outer feed back charge door (8) and the raw material solid charge door (16) of also being equipped with of lower cone body (7), the outer raw material gas inlet (14) that is equipped with of the pre-distributing chamber of gas (12), top end socket (18) is equipped with the droop thimble tube bundle (3) of different length, low high taper seat all around in the middle of droop thimble tube bundle (3) lower end forms, thimble tube heat transferring medium outlet (1) is equipped with in the thimble tube heat transferring medium import (2) that upper cone body (5) has syngas outlet (17) and is communicated with droop thimble tube bundle (3) on the top end socket (18).
2, a kind of fluidized-bed reactor according to claim 1, it is characterized in that: described gas distributor (10) is gone up the vertical thimble tube bundle (9) of the different length that is symmetrically distributed, high low taper seat all around in the middle of vertical thimble tube bundle (9) top end forms, its cone angle scope is 30～150 degree.
3, a kind of fluidized-bed reactor according to claim 1, it is characterized in that: described droop thimble tube bundle (3) subregion is arranged, according to interlacing subregion or concentric circles subregion or angle subregion, be divided into 1 subregion, 2 subregions, 3 subregions or 4 subregions according to cylinder (6) diameter and heat exchanger tube number, the number of partitions is identical with thimble tube heat transferring medium import (2) number.
4, a kind of fluidized-bed reactor according to claim 1, it is characterized in that: described top end socket (18) is equipped with the droop thimble tube bundle (3) of different length, low high taper seat all around in the middle of the lower end of droop thimble tube bundle (3) forms, its cone angle scope is 30～150 degree.
5, a kind of fluidized-bed reactor according to claim 1, it is characterized in that: the cylinder of described reactor (6) highly is 5～15 meters, cylinder (6) diameter is 0.5～6 meter, and the angle of taper of reactor upper cone body (5) and lower cone body (7) is 5～30 degree.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200510049233 CN1290603C (en) | 2005-01-26 | 2005-01-26 | Reactor of fluidized bed |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200510049233 CN1290603C (en) | 2005-01-26 | 2005-01-26 | Reactor of fluidized bed |
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| Publication Number | Publication Date |
|---|---|
| CN1680012A CN1680012A (en) | 2005-10-12 |
| CN1290603C true CN1290603C (en) | 2006-12-20 |
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| CN 200510049233 Expired - Fee Related CN1290603C (en) | 2005-01-26 | 2005-01-26 | Reactor of fluidized bed |
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Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101912752B (en) * | 2010-08-20 | 2012-05-23 | 中国航天空气动力技术研究院 | Solid particle player |
| CN101985092B (en) * | 2010-10-26 | 2012-07-04 | 周洪山 | Fluidized bed reactor with wear-resistant gas distributor |
| FR3029802B1 (en) * | 2014-12-11 | 2022-01-07 | Axens | DEVICE FOR LIMITING THE ENTRANCE OF SOLID PARTICLES AT THE OUTLET OF A THREE-PHASE FLUIDIZED BED |
| CN108800096B (en) * | 2018-08-01 | 2024-04-16 | 四川科新机电股份有限公司 | Waste heat boiler with fluidization gas distributor |
| CN115875980B (en) * | 2023-01-05 | 2023-05-16 | 唐山精研实业有限责任公司 | Air inlet and discharging structure for hydrogen-rich reduction large-speed difference fluidized bed |
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2005
- 2005-01-26 CN CN 200510049233 patent/CN1290603C/en not_active Expired - Fee Related
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