CN2121988U - Fluidized bed plant for pyrolysis preparation of oxide using salt solution - Google Patents
Fluidized bed plant for pyrolysis preparation of oxide using salt solution Download PDFInfo
- Publication number
- CN2121988U CN2121988U CN 92224073 CN92224073U CN2121988U CN 2121988 U CN2121988 U CN 2121988U CN 92224073 CN92224073 CN 92224073 CN 92224073 U CN92224073 U CN 92224073U CN 2121988 U CN2121988 U CN 2121988U
- Authority
- CN
- China
- Prior art keywords
- bed
- fluidization
- concentrated phase
- composite
- regions
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The utility model belongs to the technical field of fluidization, designing a composite fluidized bed apparatus which is formed by the superposition of a dense-phase fluidized bed and a rapid cycle fluidized bed. The utility model with simple devices can be used for salt water solutions to prepare superfine and highly active oxide products with pyrolysis, avoid the trouble of bonded beds and substantially raise productivity and product quality.
Description
The utility model belongs to the fluidization technology field.Specifically, be to have designed a kind of composite fluidization bed apparatus that salts solution drying and pyrolysis can be prepared oxide.
In the prior art, United States Patent (USP) 3251650 is to adopt spouted bed to produce magnesia powder from magnesium chloride brine, and the advantage of this method is not want distribution grid, shortcoming is that material handling easily bonds, and grain fluidized height is lower, and residence time of material is shorter, and unit are production capacity is low.United States Patent (USP) 3447901 is to adopt common fluidized bed pyrolysis to produce magnesia, its advantage is a uniformity of temperature profile in the bed, shortcoming is the particle time of staying of fluidization regions to distribute very inhomogeneous, some particle has little time pyrolysis and just discharges from outlet fully, the magnesia powder and the fluidizing agent magnesia of discharging mix, and still need and further separate, for keeping fluidized bed height constant, need constantly in bed, to replenish magnesia, increased thermal loss.In addition, because hot gas speed can not surpass the carrying velocity of particle, limited the exchange capability of heat of unit fluidized volume, bed also is prone to bonding simultaneously.
The utility model has been created the composite fluidization bed apparatus at the shortcoming of prior art, makes when the salts solution pyrolysis prepares its oxide powder, greatly improve production capacity, and has avoided adhesion problem thorny in the fluidization technology.
The utility model composite fluidization bed is formed by stacking by concentrated phase fluid bed and rapid circulating fluidized bed.Add in the fluid bed and contain a certain amount of coarse grained fine grained fluidisation medium, the speed of control fluidizing gas can make the coarse granule fluidizing agent be in the concentrated phase fluidized state in the fluid bed bottom, forms the concentrated phase fluid bed; And fine grained fluidisation medium is carried upwards rapid movement by gas, leave fluid bed from the outlet of fluid bed top and enter gas-solid separating device, fine grained fluidisation medium after separated from the gas comes back to the fluid bed bottom through straight tube and material returning device, drive through air-flow again and make progress again, make shuttling movement, form rapid circulating fluidized bed.
Referring now to accompanying drawing, the utility model is elaborated.
Fig. 1 is a composite fluidization bed schematic diagram.
Fig. 2 is the schematic diagram of conical bed for the concentrated phase fluidization regions.
Fig. 3 is the schematic diagram of spouted bed for the concentrated phase fluidization regions.
Fig. 4 chews schematic diagram in the heat supply of concentrated phase fluidization regions internal combustion for part of fuel by burning.
Fig. 5 chews schematic diagram in the heat supply of concentrated phase fluidization regions internal combustion for whole fuel by burning.
Wherein: (1)-composite fluidization bed
(2)-distribution grid
(3)-the coarse granule fluidizing agent
(4)-the concentrated phase fluidization regions
(5)-the material liquid import
(6)-nozzle
(7)-hot air intake
(8)-quick ciculation fluidized district
(9)-composite fluidization bed top exit
(10)-the level gas-solid separating device
(11)-straight tube
(12)-material returning device
(13)-air intlet
(14)-the secondary gas-solid separating device
(15)-the oxide product outlet
(16)-the tail gas outlet
(17)-burn and chew
The bottom of composite fluidize bed (1) is concentrated phase fluidization regions (4), top is Rapid Circulation fluidization regions (8), composite fluidize bed top exit (9) links to each other with one-level gas-solid separating device (10) import, one-level gas-solid separating device (10) lower end links to each other with material returning device (12) by straight tube (11), and material returning device (12) other end links to each other with concentrated phase fluidization regions (4) sidewall of composite fluidize bed (1); Material liquid nozzle (6) is positioned at concentrated phase fluidization regions (4); The fluidizing agent of thick, thin two kinds of particles is housed in the bed, and coarse granule is the fluidizing agent of concentrated phase fluidization regions, and fine grained is the fluidizing agent of Rapid Circulation fluidization regions.
Distribution grid (2) in the composite fluidize bed (1) can adopt various ways, as long as can form stable fluid bed.
On the basis of Fig. 1, the version of concentrated phase fluidization regions can further change, shown in Fig. 2,3. When spouted hot air intake speed was enough high, the coarse granule fluidizing agent can fall, and the gas distribution grid of spouted bed can save.
The bed footpath in quick ciculation fluidized district (8) can be identical with the bed footpath of concentrated phase fluidization regions (4), also can be that the bed footpath of concentrated phase fluidization regions (4) is a bit larger tham the bed footpath of fast fluidization (8), decides according to the character of processing material.
The effect of material returning device (12) is that the circulation fine grained fluidisation medium that allows to get off from straight tube (11) at the uniform velocity returns the concentrated phase fluidization regions (4) of composite fluidization bed (1), but does not allow the hot gas short circuit in the composite fluidization bed (1).Material returning device (12) can be V-shaped valve, rotary valve, star valve or screw feeder etc.Material returning device shown in Fig. 1 (12) is a V-shaped valve.Solid circulating rate can change by ratio and the gas-operated linear speed that adds fine grained fluidisation medium in the composite fluidization bed.
Material liquid nozzle (6) can be provided with one, two or three, along composite fluidization bed axial distribution.Compare with a nozzle, a plurality of nozzles have the advantage of strengthening unit fluid bed volume pyrolysis ability.
Coarse granule fluidizing agent (3) in the concentrated phase fluidization regions (4), its granularity should be controlled in the scope of not taken away by hot gas and seething with excitement.Because the granule density height of concentrated phase fluidization regions, thermal capacity is big, is in the high speed fluidized state again, after salts solution sprays into, can dewater rapidly, and crystallization and drying can not produce because of local temperature and cross the low phenomenon that bonds.
Have a large amount of fine grained media to make shuttling movement in the composite fluidization bed, its direction of motion is shown in the arrow among Fig. 1.The temperature that this part ciculation fluidized medium enters concentrated phase fluidization regions (4) when bottom equals or is lower than temperature when leaving fast fluidization top (9) slightly, has very big thermal capacity, make the Temperature Distribution of composite fluidization bed very even, guarantee that salting liquid all is in the required optimum temperature range in whole pyrolytic process.
The pyrolysis material rises with gas and stream in the composite fluidization bed, and the time of staying distributes more even.Height according to the needed pyrolysis time design of pyrolytic reaction composite fluidization bed can guarantee that material obtains abundant pyrolysis.
The hot gas that enters in the composite fluidization bed can be supplied with by fuel such as heavy oil, diesel oil, coal gas or the natural gas back of burning outside bed.Also can chew (17) directly in composite fluidization bed concentrated phase fluidization regions (4) internal combustion heat supply, as shown in Figure 4 by burning by a part of fuel.When whole fuel and air were all chewed (17) in composite fluidization bed concentrated phase fluidization regions (4) internal combustion heat supply by burning, the distribution grid of composite fluidization bed can omit, as shown in Figure 5.
Compared with prior art, major advantage of the present utility model is:
1, the salting liquid thermal decomposition is very complete.In the composite fluidization bed, material and hot gas also flow to upward motion, and the time of staying of material in bed distributes more even.
2, the pyrolysis product quality can guarantee.The composite fluidization bed tempertaure is evenly distributed, and temperature can be controlled in the needed optimum temperature range of salting liquid pyrolysis exactly, thereby guarantee product quality.
3, production capacity is big, and in the composite fluidization bed, hot gas is carrying solid material and moving upward, and the rate of climb of hot gas can be very high.Thereby the gas-solid relative velocity is big, mass transfer, heat transfer efficiency height, and the production capacity of composite fluidization sheet position sectional area improves greatly than prior art.
4, because the thermal capacity in the composite fluidization bed is big, heat transfer, mass transfer velocity height, and under high speed turbulence effect, salting liquid is non-caked in pyrolytic process, has guaranteed the normal running of pyrolysis.
5, the composite fluidization bed structure is simple, and equipment investment is few, can significantly reduce the investment cost of unit product.
Now producing magnesia equipment with this device as the magnesium chloride brine pyrolysis is example, further specifies the utility model in conjunction with the accompanying drawings.
0.2 meter of composite fluidization bed (1) diameter, 6 meters of height overalls, returning charge mouth are positioned between nozzle (6) and the distribution grid (2).
Adopt thick, fine-grained two kinds of magnesia as fluidizing agent.3400 kilograms/meter of crude magnesium sand density
3, granularity 1-3 millimeter, 20 kilograms of additions; 3400 kilograms/meter of thin magnesia density
3, granularity 0.4-1 millimeter, 20 kilograms of additions.Thick, thin magnesia is placed composite fluidization bed (1), feed the thermal current of 1100 ℃ of temperature from hot air intake (7), flow is 180 standard meters
3/ hour, thermal current passes distribution grid (2), enters concentrated phase fluidization regions (4) and rises, and makes coarse granule magnesia (3) boiling, and provides heat for the magnesium chloride brine pyrolysis.The magnesium chloride brine concentration that adds is 450 grams per liters, and temperature is 30 ℃, and flow is 39 liters/hour, from the water-soluble stream of vaporific magnesium chloride of nozzle (6) ejection at first in concentrated phase fluidization regions (4) dehydration, crystallization, drying.Control hot gas speed make thin magnesia and dry granular material bring fast fluidization (8) into, and coarse granule magnesia (3) is still stayed concentrated phase fluidization regions (4) boiling.Material finally generates magnesium oxide powder and hydrogen chloride gas in fast fluidization (8) Bian Shangsheng, limit pyrolysis.React as follows:
The magnesium chloride pyrolysis temperature is controlled at about 700 ℃.
Magnesium oxide powder that generates and thin magnesia carry down at gas, enter one-level gas-solid separating device (10) from top exit (9), through separating, the small amounts magnesium dust falls through straight tube (11) under the gravity effect with thin magnesia, send back in the bed by material returning device (12), make shuttling movement.Overwhelming majority oxide powder passes through secondary gas-solid separating device (14) again with gas to be separated, and finally obtains magnesium oxide product.
Result of implementation: magnesium chloride resolution ratio 99.6%, pyrolysis product content of magnesia 94.1%, composite fluidization sheet position sectional area is produced 240 kilograms/meter of magnesia abilities
2Hour, 1.2 microns of magnesium oxide product particle mean sizes, density 3.58 gram per centimeters
3, 1.45 meters of specific areas
2/ gram.
The utility model is applicable to the chloride of metals such as iron, aluminium, nickel, chromium, cobalt, titanium, copper, barium, zirconium, cerium, strontium, and the drying of solution such as fluoride, sulfate and pyrolysis also are applicable to the physical process of no chemical reaction such as drying etc.
Claims (7)
1, a kind of pyrolysis salting liquid is produced the fluid bed of oxide, comprise fluid bed (1), gas-solid separating device (10) and material liquid nozzle (6), it is characterized in that fluid bed (1) is the composite fluidization bed (1) that is formed by stacking by concentrated phase fluid bed and rapid circulating fluidized bed, the bottom of composite fluidization bed (1) is concentrated phase fluidization regions (4), top is quick ciculation fluidized district (8), composite fluidization bed top exit (9) links to each other with one-level gas-solid separating device (10) import, one-level gas-solid separating device (10) lower end links to each other with material returning device (12) by straight tube (11), and material returning device (12) other end links to each other with concentrated phase fluidization regions (4) sidewall of composite fluidization bed (1); Material liquid nozzle (6) is positioned at concentrated phase fluidization regions (4); In the bed thick, fine grain fluidizing agent is housed, coarse granule is the fluidizing agent of concentrated phase fluidization regions, and fine grained is the fluidizing agent in quick ciculation fluidized district.
2, device according to claim 1, the structure that it is characterized in that the bottom concentrated phase fluidization regions (4) of composite fluidization bed (1) can be common fluid bed or conical fluidized bed or spouted fluidized bed.
3, according to claim 1,2 described devices, it is characterized in that the bed footpath in quick ciculation fluidized district (8) and the bed footpath of concentrated phase fluidization regions (4) can be identical, also can be that the bed footpath of concentrated phase fluidization regions (4) is a bit larger tham the bed footpath of fast fluidization (8).
4,, it is characterized in that material returning device (12) can be V-shaped valve or rotary valve or star valve or screw feeder according to claim 1,2 described devices.
5,, it is characterized in that material liquid nozzle (6) can have one, 2 or three according to claim 1,2 described devices.
6, according to claim 1,2 described devices, the sidewall that it is characterized in that concentrated phase fluidization regions (4) can be provided with a fuel and burn and chew (17), or fuel burns and chews the bottom that (17) are arranged at composite fluidization bed (1).
7,, it is characterized in that the returning charge mouth of material returning device (12) is positioned between distribution grid (2) and the material liquid nozzle (6) according to claim 1,2 described devices.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 92224073 CN2121988U (en) | 1992-06-10 | 1992-06-10 | Fluidized bed plant for pyrolysis preparation of oxide using salt solution |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 92224073 CN2121988U (en) | 1992-06-10 | 1992-06-10 | Fluidized bed plant for pyrolysis preparation of oxide using salt solution |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN2121988U true CN2121988U (en) | 1992-11-18 |
Family
ID=4966623
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 92224073 Granted CN2121988U (en) | 1992-06-10 | 1992-06-10 | Fluidized bed plant for pyrolysis preparation of oxide using salt solution |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN2121988U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101977675A (en) * | 2008-03-17 | 2011-02-16 | 犹德有限公司 | Method and device for metered removal of a fine-grained to coarse-grained solid material or solid material mixture from a storage container |
| CN103771344A (en) * | 2014-01-03 | 2014-05-07 | 东北大学 | Device for preparing metallic oxide by jetting and pyrolyzing metal chloride solution |
-
1992
- 1992-06-10 CN CN 92224073 patent/CN2121988U/en active Granted
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101977675A (en) * | 2008-03-17 | 2011-02-16 | 犹德有限公司 | Method and device for metered removal of a fine-grained to coarse-grained solid material or solid material mixture from a storage container |
| CN101977675B (en) * | 2008-03-17 | 2013-07-17 | 犹德有限公司 | Method and device for metered removal of a fine-grained to coarse-grained solid material or solid material mixture from a storage container |
| CN103771344A (en) * | 2014-01-03 | 2014-05-07 | 东北大学 | Device for preparing metallic oxide by jetting and pyrolyzing metal chloride solution |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109277057A (en) | A kind of reactor assembly producing granular materials and method | |
| KR101260519B1 (en) | Granulated animal feedstuffs additives | |
| CN101676203A (en) | Reactor for producing high purity granular silicon and method thereof | |
| CN102671584A (en) | Reactor and method for preparing particle material | |
| CN1729046A (en) | Method and apparatus for heat treatment in a fluidised bed | |
| CN2815487Y (en) | Internal back streaming tower fluidized_bed reactor with habyrinth helical fin diversion baffle | |
| CN1680013A (en) | Reactor of organic silicon fluidized bed with cyclone separator | |
| CN102849799B (en) | Device and method for synthesizing fullerene structure nanometer WS2 and application of fullerene structure nanometer WS2 | |
| CN217979522U (en) | Energy-saving continuous fluidized bed capable of prolonging retention time and achieving uniform drying | |
| CN1551797A (en) | Fluid bed granulation process | |
| CN201189461Y (en) | Granulation system of organic products | |
| CN1290603C (en) | Reactor of fluidized bed | |
| CN103344093A (en) | Vertical type continuous fluidized bed pelleting drying device and method | |
| CN101249401B (en) | Granulator | |
| CN2121988U (en) | Fluidized bed plant for pyrolysis preparation of oxide using salt solution | |
| CN2766949Y (en) | Fluidized bed reactor | |
| CN102051287A (en) | Method and equipment for preparing washing powder | |
| CN109626395A (en) | The preparation facilities and preparation method of ammonia | |
| CN1111444C (en) | Circulating fluidizing-system | |
| CN85106397A (en) | Light-burned processing method of magnesite gas suspension and device thereof | |
| CN1019074B (en) | Compartmented gas injection device | |
| CN1845783A (en) | Method for production of enzyme granules and enzyme granules produced thus | |
| CN2766950Y (en) | Organosilicon fluidized bed reactor with cyclone separator | |
| CN209890262U (en) | Ammonia gas preparation device | |
| CN201454507U (en) | Gas-solid phase deposition reactor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |