CN207463192U - Fluid bed reaction apparatus - Google Patents
Fluid bed reaction apparatus Download PDFInfo
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- CN207463192U CN207463192U CN201721265109.3U CN201721265109U CN207463192U CN 207463192 U CN207463192 U CN 207463192U CN 201721265109 U CN201721265109 U CN 201721265109U CN 207463192 U CN207463192 U CN 207463192U
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Abstract
The utility model is related to a kind of fluid bed reaction apparatus, including housing, dense-phase fluidized bed and Disengagement zone；The dense-phase fluidized bed and the Disengagement zone delivery pipe in fluid communication by way of be connected；The delivery pipe extends upward into the Disengagement zone；The dense-phase fluidized bed is configured at the lower part of the fluid bed reaction apparatus, from bottom to top including the first flow distribution device, the second flow distribution device and removes heat pipe；The Disengagement zone is configured at the top of the fluid bed reaction apparatus, including fast gas-solid separation device, cyclone separator and collection chamber；The entrance of the fast gas-solid separation device is connected with the delivery pipe, and outlet is communicated with the Disengagement zone；The entrance of the cyclone separator is communicated with the Disengagement zone, and outlet is connected with collection chamber；The collection chamber is configured at below product gas outlet and in communication.
Description
Technical field
The utility model is related to a kind of fluid bed reaction apparatus.
Background technology
Glyoxylic ester has the chemical property of aldehyde and ester concurrently, and a variety of reactions can occur, and particularly hydrolysis can prepare glyoxalic acid.
And glyoxalic acid is the organic intermediates such as synthetic perfume, medicine, food, varnish raw material, dyestuff, plastic additive, available for producing
Oral penicillin, vanillic aldehyde, mandelic acid and allantoin etc., so both at home and abroad to the consumption figure of glyoxalic acid also becoming into rising always
Gesture.
Domestic and international glyoxalic acid preparation method is mainly included with raw material point：Oxidation of glyoxal, acid by electrolytic reduction of oxalic method, dichloro
Acetic acid or dibromoacetic acid Hydrolyze method, maleic anhydride Ozonation, glycolic enzymatic oxidation method, in addition with ethylene oxy
Change method and acetaldehyde oxidation etc..Wherein, oxidation of glyoxal is the main production process of current glyoxalic acid, but the main of this method is asked
Topic have glyoxalic acid yield is low, environmental pollution weight, equipment corrosion are fast, reaction condition acutely and product separation difficulty etc..In above-mentioned second
In the various production technologies of aldehydic acid, cost of material height and product isolation technics complexity are main bottlenecks.At present, domestic glyoxalic acid life
Production technology generally relatively falls behind, and particularly product impurity content is high, limits its scope of application, so as to serious influence
The market development of glyoxalic acid and its downstream product, thus improve oxoacetic acid product quality, reduce production cost, find it is suitable
Vanguard technology has important practical significance.
Coal-ethylene glycol technique obtains fast development in recent years, and domestic industry production technology is increasingly ripe at present, number
A coal-ethylene glycol commercialized devices have been gone into operation or just in the Large scale construction stage, the thing followed can generate a large amount of technique pair
Product ethanol acid esters.The utilization of methyl glycollate are also increasingly paid attention to by researchers in recent years, rationally efficiently sharp
It makes good use of methyl glycollate to be of great significance to improving coal-ethylene glycol process efficiency and reducing glyoxalic acid production cost, thus opens
Hair with ethyl glycolate catalysis oxidation glyoxylic ester, then through catalyzing hydrolysis be made glyoxalic acid process route be it is very necessary and tool
There is the market competitiveness.
It is well known that methyl glycollate is in the presence of a catalyst, it is one to generate glyoxalic acid methylester by oxidative dehydrogenation
Exothermal reaction process, the complete oxidation occurred with side reaction or subsequent reactions act on, and generate CO2And water, it can also release big
The heat of amount.Thus to inhibit worthless subsequent reactions, the yield of purpose product is improved, heat must be enable preferably timely
It removes.But the prior art is concentrated mainly on catalyst and the technique research and development side of methyl glycollate catalysis oxidation production glyoxalic acid methylester
Face, type of reactor generally use tubular reactor.For example, document US4340748 discloses one kind using ethyl glycolate as raw material,
In tubular reactor, under the conditions of 100~600 DEG C carrying out catalytic gas phase oxidation to it with oxygen-containing gas obtains glyoxylic ester
Method, the yield of glyoxylic ester is up to 88.3% in liquid product, and the yield of glyoxylic ester only has 43.5% under the conditions of some.
Document CN85101409A discloses a kind of method that hydrated glyoxylate is prepared using glyoxylic ester as raw material, using tubular reactor
Device, catalyst support have done the arrangement mode of monomer stringent limitation at least by a cylindrical type monomer composition, liquid phase production
The yield of glyoxylic ester is up to 82.1% in object.It can be seen that for calandria type fixed bed reactor, going for reaction heat is improved
Except efficiency is always problem to be solved, when particularly reaction temperature is higher, the salt bath of used complexity removes hot systems meeting
Cause the inconvenience of control and checking maintenance.Hot-spot easily occurs in catalyst bed, so as to cause reaction temperature control
System is difficult, and then is prone to the side reactions such as deep oxidation, so as to cause the reduction of purpose product yield and the sintering of catalyst
Inactivation etc..
The current present situation of the prior art is to be still required for a kind of material mixing fully, and reaction temperature is easily controllable, so as to carry
The consersion unit of high purpose product yield.
Invention content
The utility model is related to a kind of fluid bed reaction apparatus.The fluid bed reaction apparatus, including housing, dense fluidized
Bed and Disengagement zone；It is characterized in that,
The dense-phase fluidized bed and the Disengagement zone delivery pipe in fluid communication by way of be connected；The delivery pipe to
On extend into the Disengagement zone；
The dense-phase fluidized bed is configured at the lower part of the fluid bed reaction apparatus, from bottom to top including the first flow distribution
Device, the second flow distribution device and remove heat pipe；
The Disengagement zone is configured at the top of the fluid bed reaction apparatus, including fast gas-solid separation device, cyclone separator
And collection chamber；The entrance of the fast gas-solid separation device is connected with the delivery pipe, and outlet is communicated with the Disengagement zone；The whirlwind
The entrance of separator is communicated with the Disengagement zone, and outlet is connected with collection chamber；The collection chamber is configured under product gas outlet
It is square and in communication.
According to an aspect of the present invention, the first flow distribution device is distributed for pipe distributor or multiaperture-type
Device, the second flow distribution device are pipe distributor.
According to an aspect of the present invention, it is configured with nozzle on the second flow distribution device.
According to an aspect of the present invention, the heat pipe of removing is U-tube or straight tube.
According to an aspect of the present invention, outer cover is configured on the outside of the fast gas-solid separation device, is configured above the outer cover
There is outlet, the fast gas-solid separation device is communicated by the outlet with the Disengagement zone.
According to an aspect of the present invention, the dense-phase fluidized bed is connected part with the delivery pipe using conical section mistake
It crosses；The conical section bottom is tightly connected with the case inside wall；It is configured with above the conical section and loosens gas distribution dress
It puts.
According to an aspect of the present invention, the fluid bed reaction apparatus further include be configured at the hull outside, from
The Disengagement zone to the dense-phase fluidized bed catalyst circulation standpipe；Guiding valve is configured on the catalyst circulation standpipe.
According to an aspect of the present invention, the fluid bed reaction apparatus is further included communicates with the dense-phase fluidized bed top
Regenerative agent add in pipe and the spent agent efferent duct that is communicated with the dense-phase fluidized bed lower part.
According to an aspect of the present invention, the quantity of the cyclone separator is 1 to 20.
Beneficial effects of the present invention：The utility model is sufficiently mixed reactant and catalyst, shortens the reaction time, reaction
Generated heat is removed by the heat pipe of removing in reactor, and reaction temperature is easily controllable, improves the yield of purpose product.
Description of the drawings
Fig. 1 is the schematic diagram of the utility model fluid bed reaction apparatus.Wherein, the first flow distribution device is distributed for tubular type
Device.
Fig. 2 is the schematic diagram of the utility model fluid bed reaction apparatus.Wherein, the first flow distribution device is multiaperture-type
Distributor.
In the accompanying drawings, identical component uses identical reference numeral.Attached drawing is not according to practical ratio.
Reference sign：
1 housing
2 catalyst circulation standpipes
3 guiding valves
4 dense-phase fluidized beds
5 first flow distribution devices
6 first logistics inlet tubes
7 spent agent efferent ducts
8 second logistics inlet tubes
9 second flow distribution devices
10 regenerative agents add in pipe
11 remove heat pipe
12 conical sections
13 loosen distribution device in gas-fluid
14 delivery pipes
15 fast gas-solid separation devices
16 fast gas-solid separation device outer covers
17 cyclone separators
18 collection chambers
19 product gas export
20 Disengagement zone
The present invention is described in detail below in conjunction with the accompanying drawings, it should be noted however that protection scope of the present invention is simultaneously
By this, this is not limited, and but is determined by the appended claims.
All publications, patent application, patent and the other bibliography that this specification is mentioned all draw in this for reference.
Unless otherwise defined, all technical and scientific terms used herein all contains with what those skilled in the art routinely understood
Justice.In case of conflict, it is subject to the definition of this specification.
When this specification with prefix " well known to those skilled in the art ", " prior art " or its export material similar to term
Whens material, substance, method, step, device or component etc., object derived from the prefix is covered this field when the application proposes and is routinely made
Those, but also include also being of little use at present, will but become art-recognized is suitable for those similar to purpose.
It should be strongly noted that disclosed two or more aspects (or embodiment) in the context of the present specification
It can arbitrarily combine each other, the technical solution formed therefrom belongs to a part for this specification original disclosure, while
It falls under the scope of the present invention.
The present invention relates to a kind of fluid bed reaction apparatus.The fluid bed reaction apparatus includes housing 1, dense-phase fluidized bed 4
With Disengagement zone 20.Enclosure interior space, top are Disengagement zone 20, and lower part is dense-phase fluidized bed 4.
According to the present invention, dense-phase fluidized bed 4 and Disengagement zone 20 delivery pipe 14 in fluid communication by way of be connected；Conveying
Pipe 14 extends upward into Disengagement zone 20.
According to the present invention, dense-phase fluidized bed 4 is configured at the lower part of fluid bed reaction apparatus, from bottom to top including the first logistics
Distribution apparatus 5, the second flow distribution device 9 and remove heat pipe 11.
According to the present invention, Disengagement zone 20 is configured at the top of fluid bed reaction apparatus, including fast gas-solid separation device 15, whirlwind
Separator 17 and collection chamber 18.The entrance of fast gas-solid separation device 15 is connected with delivery pipe 14, and outlet is communicated with Disengagement zone 20.Whirlwind
The entrance of separator 17 is communicated with Disengagement zone 20, and outlet is connected with collection chamber 18.Collection chamber 18 is configured at product gas outlet 19
Lower section is simultaneously in communication.
According to the present invention, the first flow distribution device 5 is pipe distributor or multiaperture-type distributor.
According to the present invention, the second flow distribution device 9 is pipe distributor, and spray is configured on the second flow distribution device 9
Mouth.
According to the present invention, heat pipe 11 is removed as U-tube or straight tube.
According to the present invention, 15 outside of fast gas-solid separation device is configured with outer cover 16, and 16 top of outer cover is configured with outlet, and gas-solid is fast
Separating device 15 is communicated by exporting with Disengagement zone 20.
According to the present invention, dense-phase fluidized bed 4 is connected part with delivery pipe 14 using 12 transition of conical section.12 bottom of conical section
It is tightly connected with 1 madial wall of housing, 12 top of conical section, which is configured with, loosens distribution device in gas-fluid 13.
According to the present invention, fluid bed reaction apparatus further include be configured at the outside of housing 1, from Disengagement zone 20 to dense fluidized
The catalyst circulation standpipe 2 of bed 4 is configured with guiding valve 3 on catalyst circulation standpipe 2.
According to the present invention, fluid bed reaction apparatus further includes the regenerative agent communicated with 4 top of dense-phase fluidized bed and adds in pipe 10,
With the spent agent efferent duct 7 communicated with 4 lower part of dense-phase fluidized bed.
According to the present invention, the quantity of the cyclone separator is 1 to 20.
Consersion unit shown in FIG. 1 is operated in the following manner.
First logistics is introduced by the first logistics inlet tube 6, and dense-phase flow is entered after the first flow distribution device 5 is uniformly distributed
Change bed 4 bottom, with being introduced by the second logistics inlet tube 8, the second logistics after the second flow distribution device 9 is uniformly distributed is close
It is flowed up after uniformly being mixed in phase fluid bed 4, reacts under catalyst action, generate the gas gas-phase objects containing target product
Stream, the heat and remove the cooling medium progress heat exchange in heat pipe 11, the gas containing target product of output that simultaneous reactions are released
Phase logistics entrainment portions catalyst solid particle continues up flowing, and as gas rises, part large granular catalyst gradually sinks
It lowers, after the free space of 4 top of dense-phase fluidized bed, enters fast gas-solid separation device through conical section 12 and delivery pipe 14
15, since the flow velocity of gas in delivery pipe 14 is much larger than the stream of 4 top dilute phase free space gas of dense-phase fluidized bed in housing 1
Speed so that output gas residence time in consersion unit is greatly shortened, so as to reduce the generation of side reaction.Carry portion
The gaseous stream containing target product of divided catalyst solid particle enters the fast gas-solid separation device of its end by delivery pipe 14
15, gas-solid mixture does high speed rotary motion in fast gas-solid separation device 15, carries out gas-solid under the influence of centrifugal force and quickly divides
From most of catalyst solid particle, which separates, to be discharged between fast gas-solid separation device outer cover 16 and delivery pipe 14, falls into taper
Upper space between the top of section 12 and housing 1, then, catalyst solid particle passes through catalyst circulation under the effect of gravity
Standpipe 2 returns to dense-phase fluidized bed 4, while guiding valve 3 is set on catalyst circulation standpipe 2, and guiding valve 3 ensure that 12 top of conical section
Catalyst solid particle from top to bottom unidirectionally flow into lower section dense-phase fluidized bed 4, avoid the unstripped gas in dense-phase fluidized bed 4
Body enters 12 top of conical section and is mixed into output gas.Meanwhile in order to ensure that catalyst solid particle smoothly enters catalysis
Agent circulating solid tube 2 is avoided overstocking above conical section 12, be entered above conical section 12 with the catalyst of catalyst circulation standpipe 2
Position between below mouthful, which is provided with, loosens gas distribution tube 13.That is separated from fast gas-solid separation device 15 contains target product
Logistics carry fraction catalyst granules exported from fast separation device outer cover 16 above discharge after, into cyclone separator 17
Further gas solid separation is carried out, the catalyst solid particle isolated falls into upper between the top of conical section 12 and housing 1
Then portion space returns to dense-phase fluidized bed 4 through catalyst circulation standpipe 2, the warp of the gaseous stream containing target product separated
It crosses collection chamber 18 to be drawn by product gas outlet 19, into later separation device.Wherein, it is urged from the to be generated of dense-phase fluidized bed 4
Agent solid particle is delivered to regenerator regeneration by spent agent efferent duct 7, and the catalyst solid particle after regeneration is added by regenerative agent
Enter pipe 10 and be recycled back into dense-phase fluidized bed 4 to be reacted.
The utility model fluid bed reaction apparatus can be used for methyl glycollate catalytic oxidative dehydrogenation and prepare glyoxalic acid methylester.
The reaction mechanism of glyoxalic acid methylester is generated it is found that methyl glycollate depositing in catalyst according to methyl glycollate catalytic oxidative dehydrogenation
Under, it is an exothermal reaction process to generate glyoxalic acid methylester by oxidative dehydrogenation, is occurred with side reaction or subsequent reactions
Complete oxidation acts on, and generates CO2And water, it can also release a large amount of heat.Thus to inhibit worthless subsequent reactions, mesh is improved
Product yield, heat must be enable preferably to remove in time.Research shows that it is reacted in oxygen with methyl glycollate catalysis
In the process, the excessive oxidation of glyoxalic acid methylester and decomposition are to cause to react the low main original of purpose product glyoxalic acid methylester yield
Because, and the excessive oxidation of glyoxalic acid methylester and the temperature of decomposition and reactor bed, reaction time are closely related, temperature is got over
The high and reaction time is longer, and the excessive oxidation and decomposition probability of glyoxalic acid methylester are higher.Thus the control of reaction temperature is it
In difficult point and one of key.It is well known that for calandria type fixed bed reactor, the removal efficiency for improving reaction heat is always
Problem to be solved, when particularly reaction temperature is higher, the salt bath of used complexity, which removes hot systems, can cause to control and examine
The inconvenience of repair.Hot-spot easily occurs in catalyst bed, difficult, Jin Eryi is controlled so as to cause reaction temperature
In the side reactions such as deep oxidation occur, so as to cause sintering deactivation of the reduction of purpose product yield and catalyst etc..For this purpose, it adopts
It is a kind of preferable solution with fluidized-bed reactor, fluidized-bed reactor can make gas-solid good contact, so as to fulfill temperature
Degree is evenly distributed and effectively removes heat, the good controlling reaction temperature of energy in strong exothermal reaction, and then ensures reaction raw materials
High conversion and purpose product are in high yield.The technical solution of the utility model is fully combining methyl glycollate catalytic oxidation
On the basis of feature and fluidized-bed reactor design feature, first, glyoxalic acid first is produced in methyl glycollate catalytic oxidative dehydrogenation
The consersion unit bottom of ester sets the first flow distribution device and the second flow distribution device, it is ensured that feed product is in reactor
It is interior to be evenly distributed and material and catalyst are sufficiently mixed, while by removing heat pipe in Mi Xiangfanyingqu settings, ensure that anti-
The timely removal of heat is answered, and then improves the homogeneity of equipment inner radial temperature, improves the yield of target product.Secondly,
By the way that settling section traditional in fluidized-bed reactor is changed to delivery pipe, while use fast gas-solid separation device, by product gas with
Catalyst quickly detaches so that the gas of output quickly draws equipment, reduces reactor product in the stop of free space
Between, so as to reduce the generation of byproduct, improve the yield of target product.Again, it is separated by fast gas-solid separation device
Gas-solid mixture in most of catalyst solid particle separate and fall into underlying space, pass through catalyst circulation standpipe
The catalyst separated quickly returns to dense-phase fluidized bed, improves the service efficiency of catalyst.It is produced using the utility model
Glyoxalic acid methylester is 0.6 in oxygen and methyl glycollate molar ratio:1~3:1, the weight space velocity of methyl glycollate is 0.1h-1~
5.0h-1, reaction temperature is 200 DEG C~400 DEG C, and reaction pressure contacts under conditions of being 0~1.0MPa with containing vanadium and silver catalyst
Reaction generation glyoxalic acid methylester, yield >=88.5% of glyoxalic acid methylester achieve preferable technique effect.
The present invention will be further described below by way of examples.
Specific embodiment
【Embodiment 1】
Glyoxalic acid methylester is produced using consersion unit as shown in Figure 1.Setting Straight removes heat in the fluidized-bed reactor
Pipe, cooling medium are vapor, and oxygen-containing gas distributor is pipe distributor, and methyl glycollate distributor is the pipe with nozzle
Formula distributor, the number of cyclone separator is 20.
Liquid charging stock containing methyl glycollate is methyl glycollate and the mixture of water, and the content of methyl glycollate is
80%, remaining is water；Oxygen-containing gas is air；The molar ratio of oxygen and methyl glycollate into reactor is 3:1, glycolic
The weight space velocity of methyl esters is 5.0h-1, reaction temperature is 400 DEG C, pressure 1.0MPa, and catalyst is the catalyst containing vanadium and silver.
In the above conditions, the yield of glyoxalic acid methylester is 88.5%.
【Embodiment 2】
Glyoxalic acid methylester is produced using consersion unit as shown in Figure 1.Setting U-tube removes heat in the fluidized-bed reactor
Pipe, cooling medium are water, and oxygen-containing gas distributor is pipe distributor, and methyl glycollate distributor is the tubular type with nozzle point
Cloth device, the number of cyclone separator is 12.
Liquid charging stock containing methyl glycollate is methyl glycollate and the mixture of methanol, and the content of methyl glycollate is
70%, remaining is methanol；Mixture of the oxygen-containing gas for oxygen and nitrogen, oxygen content 1%, nitrogen content 99%；Into
The molar ratio of oxygen and methyl glycollate for entering reactor is 2:1, the weight space velocity of methyl glycollate is 2.5h-1, reaction temperature
It it is 350 DEG C, pressure 0.8MPa, catalyst is the catalyst containing vanadium and silver.
In the above conditions, the yield of glyoxalic acid methylester is 89.8%.
【Embodiment 3】
Glyoxalic acid methylester is produced using consersion unit as shown in Figure 2.Setting U-tube removes heat in the fluidized-bed reactor
Pipe, cooling medium are water, and oxygen-containing gas distributor is distribution plate type distributor, and methyl glycollate distributor is the pipe with nozzle
Formula distributor, the number of cyclone separator is 10.
Liquid charging stock containing methyl glycollate is methyl glycollate and the mixture of methanol, and the content of methyl glycollate is
60%, remaining is methanol；Mixture of the oxygen-containing gas for oxygen and nitrogen, oxygen content 15%, nitrogen content 85%；Into
The molar ratio of oxygen and methyl glycollate for entering reactor is 1:1, the weight space velocity of methyl glycollate is 1.5h-1, reaction temperature
It it is 320 DEG C, pressure is normal pressure, and catalyst is the catalyst containing vanadium and silver.
In the above conditions, the yield of glyoxalic acid methylester is 90.2%.
【Embodiment 4】
Glyoxalic acid methylester is produced using consersion unit as shown in Figure 2.Setting U-tube removes heat in the fluidized-bed reactor
Pipe, cooling medium are water, and oxygen-containing gas distributor is distribution plate type distributor, and methyl glycollate distributor is the pipe with nozzle
Formula distributor, the number of cyclone separator is 1.
Liquid charging stock containing methyl glycollate is straight alcohol acid methyl esters；Oxygen-containing gas is air；Into the oxygen of reactor
Molar ratio with methyl glycollate is 0.6:1, the weight space velocity of methyl glycollate is 0.1h-1, reaction temperature is 200 DEG C, pressure
For 0.5MPa, catalyst is the catalyst containing vanadium and silver.
In the above conditions, the yield of glyoxalic acid methylester is 89.6%.
【Embodiment 5】
Glyoxalic acid methylester is produced using consersion unit as shown in Figure 2.Setting U-tube removes heat in the fluidized-bed reactor
Pipe, cooling medium are water, and oxygen-containing gas distributor is distribution plate type distributor, and methyl glycollate distributor is the pipe with nozzle
Formula distributor, the number of cyclone separator is 6.
Liquid charging stock containing methyl glycollate is methyl glycollate and water, and the content of methyl glycollate is 85%, remaining is
Water；Mixture of the oxygen-containing gas for oxygen and nitrogen, oxygen content 20%, nitrogen content 80%；Into the oxygen of reactor
The molar ratio of gas and methyl glycollate is 1:1, the weight space velocity of methyl glycollate is 0.5h-1, reaction temperature is 250 DEG C, pressure
For 0.3MPa, catalyst is the catalyst containing vanadium and silver.
In the above conditions, the yield of glyoxalic acid methylester is 90.5%.
【Embodiment 6】
Glyoxalic acid methylester is produced using consersion unit as shown in Figure 2.Setting U-tube removes heat in the fluidized-bed reactor
Pipe, cooling medium are water, and oxygen-containing gas distributor is distribution plate type distributor, and methyl glycollate distributor is the pipe with nozzle
Formula distributor, the number of cyclone separator is 8.
Liquid charging stock containing methyl glycollate is methyl glycollate and the mixture of water, and the content of methyl glycollate is
80%, remaining is water；Mixture of the oxygen-containing gas for oxygen and nitrogen, oxygen content 20%, nitrogen content 80%；Into
The oxygen of reactor and the molar ratio of methyl glycollate are 0.8:1, the weight space velocity of methyl glycollate is 1h-1, reaction temperature is
280 DEG C, pressure 0.4MPa, catalyst is the catalyst containing vanadium and silver.
In the above conditions, the yield of glyoxalic acid methylester is 91.5%.
【Comparative example 1】
According to【Embodiment 3】Identical condition and reaction raw materials, type of reactor is identical with document CN85101409A, second
The yield of aldehydic acid methyl esters is 79.6%.
【Comparative example 2】
According to【Embodiment 6】Identical condition and reaction raw materials, type of reactor is identical with document CN85101409A, second
The yield of aldehydic acid methyl esters is 82.5%.
Claims (9)
1. a kind of fluid bed reaction apparatus, including housing, dense-phase fluidized bed and Disengagement zone；It is characterized in that,
The dense-phase fluidized bed and the Disengagement zone delivery pipe in fluid communication by way of be connected；The delivery pipe is prolonged upwards
Extend into the Disengagement zone；
The dense-phase fluidized bed is configured at the lower part of the fluid bed reaction apparatus, is from bottom to top filled including the first flow distribution
It puts, the second flow distribution device and remove heat pipe；
The Disengagement zone is configured at the top of the fluid bed reaction apparatus, including fast gas-solid separation device, cyclone separator sum aggregate
Gas chamber；The entrance of the fast gas-solid separation device is connected with the delivery pipe, and outlet is communicated with the Disengagement zone；The cyclonic separation
The entrance of device is communicated with the Disengagement zone, and outlet is connected with collection chamber；The collection chamber is configured at product gas outlet lower section simultaneously
It is in communication.
2. fluid bed reaction apparatus according to claim 1, which is characterized in that the first flow distribution device is tubular type point
Cloth device or multiaperture-type distributor, the second flow distribution device are pipe distributor.
3. fluid bed reaction apparatus according to claim 2, which is characterized in that be configured on the second flow distribution device
Nozzle.
4. fluid bed reaction apparatus according to claim 1, which is characterized in that the heat pipe of removing is U-tube or straight tube.
5. fluid bed reaction apparatus according to claim 1, which is characterized in that be configured on the outside of the fast gas-solid separation device outer
Cover, the outer cover top are configured with outlet, and the fast gas-solid separation device is communicated by the outlet with the Disengagement zone.
6. fluid bed reaction apparatus according to claim 1, which is characterized in that the dense-phase fluidized bed and the delivery pipe phase
Even part uses conical section transition；The conical section bottom is tightly connected with the case inside wall；Match above the conical section
It is equipped with loosening distribution device in gas-fluid.
7. fluid bed reaction apparatus according to claim 1, which is characterized in that the fluid bed reaction apparatus further includes configuration
In the hull outside, from the Disengagement zone to the catalyst circulation standpipe of the dense-phase fluidized bed；The catalyst circulation
Guiding valve is configured on standpipe.
8. fluid bed reaction apparatus according to claim 1, which is characterized in that the fluid bed reaction apparatus further includes and institute
It states the regenerative agent that dense-phase fluidized bed top communicates and adds in pipe and the spent agent efferent duct communicated with the dense-phase fluidized bed lower part.
9. fluid bed reaction apparatus according to claim 1, which is characterized in that the quantity of the cyclone separator is 1 to 20
Platform.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721265109.3U CN207463192U (en) | 2017-09-29 | 2017-09-29 | Fluid bed reaction apparatus |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721265109.3U CN207463192U (en) | 2017-09-29 | 2017-09-29 | Fluid bed reaction apparatus |
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| CN207463192U true CN207463192U (en) | 2018-06-08 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111715154A (en) * | 2019-03-18 | 2020-09-29 | 上海卓然工程技术股份有限公司 | Circulating fluidized bed reaction device |
| US11473019B2 (en) | 2018-09-27 | 2022-10-18 | Shanghai Supezet Engineering Technology Co., Ltd. | Naphtha catalytic cracking catalyst, catalytic cracking method and reaction device |
-
2017
- 2017-09-29 CN CN201721265109.3U patent/CN207463192U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US11473019B2 (en) | 2018-09-27 | 2022-10-18 | Shanghai Supezet Engineering Technology Co., Ltd. | Naphtha catalytic cracking catalyst, catalytic cracking method and reaction device |
| CN111715154A (en) * | 2019-03-18 | 2020-09-29 | 上海卓然工程技术股份有限公司 | Circulating fluidized bed reaction device |
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