CN2901210Y - Fine particle fluidized bed reactor - Google Patents
Fine particle fluidized bed reactor Download PDFInfo
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- CN2901210Y CN2901210Y CN 200620040527 CN200620040527U CN2901210Y CN 2901210 Y CN2901210 Y CN 2901210Y CN 200620040527 CN200620040527 CN 200620040527 CN 200620040527 U CN200620040527 U CN 200620040527U CN 2901210 Y CN2901210 Y CN 2901210Y
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- reactor
- heat exchange
- fine particles
- fluidized bed
- bed reactor
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Abstract
The utility model relates to a fine-grain fluidized-bed reactor mainly for solving the problem with strenuous oscillation of a heat transfer component, and the oscillation effects technical matter of durability, wherein a secondary cyclone or tertiary cyclone, a heat transfer component, a gas distributor, a dispersion plate are positioned in a reactor shell and the heat transfer component. The heat transfer component is a straight way type recuperator with a compensating ring on the upper end. The utility model adopts integral cannular transition in a joint of two ends of the heat transfer and a barrel to solve the problem with strenuous oscillation, and is applicable to ammoxidation industrial production.
Description
Technical field
The utility model relates to a kind of stream of fine particles fluidized bed reactor.
Background technology
Ammonia oxidation Synthin chemical products are a kind of simple, economic commercial runs, now are widely used.The stream of fine particles fluidized bed reactor is the key equipment of ammonia oxidation just, and it reasonably utilizes reacting gas to contact with the effective of catalyst, has not only removed reaction heat effectively, and the reactor resistance drop is met the demands.Therefore, the fluidization quality of stream of fine particles fluidized bed reactor will directly influence the yield of conversion of raw material and product; Secondly, the master of ammonia oxidation pays reaction and is generally strong exothermal reaction, must in time remove reaction heat, otherwise will cause the hurried rising of conversion zone temperature, thereby reduce the purpose product selectivity, and cause coking and inactivation easily.
At present, the heat exchanger tube of ammoxidation of hydrocarbons subtraction unit stream of fine particles fluidized bed reactor inside generally adopts U-shaped pipe or thimble tube.Both advantages are simple in structure, easy fixing, easy layouts, and shortcoming is that the U-shaped pipe is more at the inside reactor pad, and U-shaped pipe bottom is easy to wear, and the water pipe bend is many; The steam channel of thimble tube is narrower relatively, easily produces water hammer.So strong vibration easily takes place these two kinds of heat exchange structures, influence the service life of heat exchanger tube.In case and heat exchanger tube leaks, and will directly influence expensive catalyst, makes it inactivation, causes enormous economic loss.Secondly, after the heat exchanger tube of fluidized-bed reactor inside uses certain hour, need repairing or change, the perforate on cylindrical shell of at this moment having to, it is very inconvenient to operate.
A kind of fluidized-bed reactor is disclosed among the Chinese patent CN2494698Y, the heat exchange structure of this reactor is by the conduction oil distributor box that is arranged on upper end in the cylindrical shell, be connected and the tube bank of equally distributed droop suspension shape cover with the conduction oil distributor box, and resiliently mounted banded penstock dish is carried out in cover tube bank form, solved the inconvenience of heat-exchanging tube bundle installation, maintenance.But for the stream of fine particles fluidized bed reactor of built-in cyclone separator, the dipleg of cyclone separator directly inserts the concentrated phase area of fluidized-bed layer, so be not suitable for being provided with the conduction oil distributor box.
Summary of the invention
Technical problem to be solved in the utility model is that the heat exchange component vibration of stream of fine particles fluidized bed reactor in the prior art is violent, have a strong impact on its service life, thereby influence the control of reaction temperature, and the shortcoming of installation, maintenance inconvenience, a kind of new stream of fine particles fluidized bed reactor is provided.It has good effect of heat exchange, smooth operation, and fluidization quality is good, characteristics easy to maintenance.
For solving the problems of the technologies described above, the technical solution adopted in the utility model is as follows: a kind of stream of fine particles fluidized bed reactor, comprise reactor shell, upper cover, low head, feed(raw material)inlet and reactant outlet, be provided with secondary or three-stage cyclone separator, heat exchange component, gas distributor and dispersion plate in the reactor shell, wherein the upper end of cyclone separator is positioned on the fluidized-bed layer and with reacting product outlet and links to each other, and the lower end of cyclone separator is arranged on the concentrated phase area gas distributor of fluidized-bed layer; Dispersion plate is positioned under the gas distributor, on the low head; The upper end of heat exchange component is positioned on the fluidized-bed layer, the lower end of heat exchange component is arranged on the concentrated phase area, gas distributor of fluidized-bed layer, heat exchange component is the through-type heat exchanger tube of upper end band compensating ring, and the integral cannula transition is adopted in the junction of heat exchange component two ends and reactor shell.
In the technique scheme, preferred version is that heat exchange component evenly distributes according to the needs of removing heat in the reactor; The heat exchanger tube preferred version is for to fix with support.The radius of compensating ring is 1.5～10.0 times of heat exchanger tube nominal diameter, and the number of turns of compensating ring is 1/4～2 circle.The gas distributor preferred version is a multi-tube structure; The dispersion plate preferred version is the gas distribution grid of band honeycomb duct type.
In the technique scheme, the preferred version of heat exchange component is for being evenly distributed in cylindrical shell according to the needs of removing heat in the reactor, and the integral cannula transition is adopted in the junction of heat exchange component two ends and reactor shell.This heat exchange component has two effects in reactor: the one, remove the heat that reaction produces, and keep suitable reaction temperature; The 2nd, the vertical inner member as reactor reaches reinforcement fluidization quality, optimizes the effect of reaction.This heat exchange component enters from reactor lower part with a thinner seamless steel pipe, zoom into the required heat exchanger tube of calculating by a reduced pipe, refute thinner pipe equally in the heat exchanger tube upper end, and this pipe is designed to a compensating ring, the radius of this compensating ring is 1.5～10.0 times of heat exchanger tube nominal diameter; The number of turns of compensating ring is 1/4～2.Because the wall thickness δ t of heat exchanger tube often differs bigger with reactor shell wall thickness δ s, general δ t＜1/2 δ s, secondly, in the heat exchanger tube with reactor shell in the temperature difference also bigger, can reach about 350 ℃.So the import and export of heat exchanger tube are taken over simplified junction and had the stress concentration phenomenon, this junction is the weakest link of heat exchanger tube, and we have adopted the technical scheme of integral cannula transition, have solved this problem preferably.Concrete grammar is: the short tube of welding one segment length about 120～200mm on reactor shell, short tube one end is concordant with cylinder inboard wall, the other end refute into caliber than the about 2mm of heat exchanger tube than small takeover, and weld with heat exchanger tube.This sleeve pipe can be made with the method for whole punching press, and low cost of manufacture is even the transformation of old device also can be implemented this method.Fixedly the support of heat exchange component is divided into two groups up and down, a gripper shoe is welded in every heat exchanger tube lower end, and fix by U bolt and support, the heat exchanger tube upper end directly adopts U bolt and support to fix, the both sides of this U bolt connect a nut respectively, making between pipe and the bolt has certain clearance, to guarantee heat exchanger tube level of freedom is arranged, and the compensating ring of upper end is played one's part to the full.This support preferentially adopts angle steel to manufacture, and the top of angle steel is the umbrella shape lid that a band steel is welded into, and can effectively prevent the accumulation of catalyst.
In the utility model, because after adopting this heat exchange component, steam channel is unimpeded, water hammer has also been eliminated, and the stress concentration phenomenon of the junction of heat exchange component two ends and reactor shell obtains bigger alleviation simultaneously.Thereby significantly reduced the oscillation phenomenon of heat exchange component, and reactor is operated steadily, prolonged the service life of heat exchange component, obtained better technical effect.
Description of drawings
Fig. 1 is a stream of fine particles fluidized bed reactor structural representation.
Fig. 2 is the heat exchanger tube layout drawing.
Fig. 3 is the heat exchange tube structure schematic diagram.
Fig. 4 is heat exchanger tube and reactor barrel connection diagram.
In Fig. 1,1 is tasty and refreshing for putting, and 2 is the lower cone end socket, 3 is air intlet, and 4 is support, and 5 is reactor shell, 6 is heat exchanger tube, and 7 is charge door, and 8 is reacting product outlet, 9 is upper cover, and 10 is venting, and 11 for measuring mouth, 12 is cyclone separator, and 13 for purging mouth, and 14 is combi inlet port, 15 is the multitube distributor, and 16 are band honeycomb duct type dispersion plate.
Below by embodiment the utility model is further elaborated.
The specific embodiment
[embodiment 1]
2000 tons of/year isophthalodinitrile devices, adopt stream of fine particles fluidized bed reactor shown in Figure 1, the reactor shell diameter is 2400 millimeters, 19000 millimeters of height, 108 millimeters of heat exchanger tube external diameters, are concentric circles and evenly distribute by totally 32 in cylindrical shell, its tubule diameter is that 45 millimeters, compensating ring radius are that 175 millimeters, the number of turns are 11/2, and the integral cannula external diameter of heat exchange component two ends and reactor shell junction is 76 millimeters.Equipment operates steadily, and does not have the high vibration phenomenon.Drive continuously to check not occur leaking after half a year.
[comparative example 1]
The process conditions of certain isophthalodinitrile device are all identical with embodiment 1 with the structure of reactor parameter, and difference is that heat exchange tube structure adopts the thimble tube form, and heat exchanger tube is imported and exported the direct and cylindrical shell welding of the mouth of pipe.Equipment when operation, send continuous metal bump sound, operation occurred leaking less than two months, checked and found have 4 microcrack to occur, and the quality of catalyst in reactor is exerted a certain influence.
[embodiment 2]
2000 tons of/year benzonitrile devices, adopt stream of fine particles fluidized bed reactor shown in Figure 1, the reactor shell diameter is 2400 millimeters, 19000 millimeters of height, 108 millimeters of heat exchanger tube external diameters, are concentric circles and evenly distribute by totally 32 in cylindrical shell, its tubule diameter is that 45 millimeters, compensating ring radius are that 175 millimeters, the number of turns are 1, and the integral cannula external diameter of heat exchange component two ends and reactor shell junction is 76 millimeters.Equipment operates steadily, and does not have the high vibration phenomenon.
[embodiment 3]
1000 tons of/year itrile group arsenic heavy stone used as an anchor devices, adopt stream of fine particles fluidized bed reactor shown in Figure 1, the reactor shell diameter is 1600 millimeters, 20300 millimeters of height, 89 millimeters of heat exchanger tube external diameters, are matrix and evenly distribute by totally 17 in cylindrical shell, its tubule diameter is that 32 millimeters, compensating ring radius are that 200 millimeters, the number of turns are 1 and 1,1/2 two kind, and the integral cannula external diameter of heat exchange component two ends and reactor shell junction is 57 millimeters.Equipment operates steadily, and does not have the high vibration phenomenon.
Claims (6)
1, a kind of stream of fine particles fluidized bed reactor, comprise reactor shell, upper cover, low head, feed(raw material)inlet and reactant outlet, be provided with secondary or three-stage cyclone separator, heat exchange component, gas distributor and dispersion plate in the reactor shell, wherein the upper end of cyclone separator is positioned on the fluidized-bed layer and with reacting product outlet and links to each other, and the lower end of cyclone separator is arranged on the concentrated phase area gas distributor of fluidized-bed layer; Dispersion plate is positioned under the gas distributor, on the low head; The upper end of heat exchange component is positioned on the fluidized-bed layer, the lower end of heat exchange component is arranged on the concentrated phase area, gas distributor of fluidized-bed layer, it is characterized in that heat exchange component is the through-type heat exchanger tube of upper end band compensating ring, the integral cannula transition is adopted in the junction of heat exchange component two ends and reactor shell.
2,, it is characterized in that heat exchange component evenly distributes according to the needs of removing heat in the reactor according to the described stream of fine particles fluidized bed reactor of claim 1.
3,, it is characterized in that heat exchanger tube fixes with support according to the described stream of fine particles fluidized bed reactor of claim 1.
4, according to the described stream of fine particles fluidized bed reactor of claim 1, the radius that it is characterized in that compensating ring is 1.5～10.0 times of heat exchanger tube nominal diameter, and the number of turns of compensating ring is 1/4～2 circle.
5,, it is characterized in that gas distributor is a multi-tube structure according to the described stream of fine particles fluidized bed reactor of claim 1.
6,, it is characterized in that dispersion plate is the gas distribution grid of band honeycomb duct type according to the described stream of fine particles fluidized bed reactor of claim 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200620040527 CN2901210Y (en) | 2006-03-27 | 2006-03-27 | Fine particle fluidized bed reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200620040527 CN2901210Y (en) | 2006-03-27 | 2006-03-27 | Fine particle fluidized bed reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN2901210Y true CN2901210Y (en) | 2007-05-16 |
Family
ID=38085375
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200620040527 Expired - Lifetime CN2901210Y (en) | 2006-03-27 | 2006-03-27 | Fine particle fluidized bed reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN2901210Y (en) |
-
2006
- 2006-03-27 CN CN 200620040527 patent/CN2901210Y/en not_active Expired - Lifetime
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20070516 |
|
| EXPY | Termination of patent right or utility model |