CN103521141B - A kind of continuous multi-stage radial reactor - Google Patents
A kind of continuous multi-stage radial reactor Download PDFInfo
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- CN103521141B CN103521141B CN201310270584.XA CN201310270584A CN103521141B CN 103521141 B CN103521141 B CN 103521141B CN 201310270584 A CN201310270584 A CN 201310270584A CN 103521141 B CN103521141 B CN 103521141B
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Abstract
The invention belongs to petroleum refining and chemical field, is related to a kind of continuous multi-stage radial reactor.It is characterized in that it is divided into inner cylinder from inside to outside in a reactor（2）, middle cylinder（3）And outer barrel（4）, catalyst is between inner cylinder and middle cylinder；Inner cylinder and middle cylinder barrel perforation, inner cylinder and outer barrel are divided into multistage, are spaced between each section；Reactor head sets catalyst shot tank（1）；Reactor bottom sets catalyst receiving tank（11）Receive the catalyst for needing to regenerate；Catalyst continuously enters in reactor from feed pot, is moved down between inner cylinder and middle cylinder, catalyst receiving tank is exited into from reactor bottom；Reaction mass（9）Into one section in inner cylinder or outer barrel, then enter radially across catalyst layer in outer barrel or the corresponding section of inner cylinder, entered back into after drawing heated or cooling by pipeline in other conversion zones.Necking passage can be set between section and section.
Description
Technical field
The invention belongs to petroleum refining and chemical field, is related to a kind of continuous multi-stage radial reactor.International monopoly point
Class belongs to C10G.
Background technology
In PETROLEUM PROCESSING and other chemical processes, radial reactor is often used, and frequently encounter strong endothermic reaction
Or strong exothermal reaction, such as dehydrogenating low-carbon alkane reaction, naphtha catalytic reforming reaction, petroleum distillate hydrogenation reaction, these are anti-
The characteristics of answering one obvious is exactly fuel factor height, if dehydrogenating low-carbon alkane reaction and naphtha catalytic reforming reaction are highly endothermic
Reaction, and petroleum distillate hydrogenation reaction is exothermic reaction, it is anti-to make because there is substantial amounts of fuel factor in these courses of reaction
It should be normally carried out, it is necessary to heat or remove reaction heat, the general reaction heat that removes is easier to, such as petroleum distillate hydrogenation reaction, typically
Hydrogen circulation amount can be increased in the reactor can take reaction heat out of, and some strong endothermic reactions are then not easy, especially instead
In the case of answering temperature very high.Need to carry out between 500-650 DEG C as propane, dehydrogenation of isobutane react, naphtha catalysis weight
Whole reaction is needed to carry out between 480-530 DEG C, and so high reaction temperature can only typically be carried out with heating furnace outside reactor
Heating.And the catalyst activity cycle of these reactions is shorter, catalyst needs often regeneration to keep activity, anti-answering pressure
Sensitivity, high pressure are unfavorable for reaction and carried out, therefore the radial reactor small typically using pressure drop.In general radial reactor can only be carried out
One section of reaction, for for example above-mentioned dehydrogenating low-carbon alkane of process and catalytic reforming reaction for needing multistage to react, turn to reach high
Rate could complete primary first-order equation task, it is necessary to which multiple reactors are connected, general between reactor to use pipeline connection with convenient
Catalyst circulates.Catalytic reforming process and propane dehydrogenation of isobutane technique such as Uop Inc. of the U.S. use multiple independent footpaths
Connected up and down to reactor, catalyst flows into second reactor from first, top reactor, enters back into the 3rd reactor；
Reaction mass after heat stove heat enters back into second reactor after being come out from first reactor, from second reactor out after
It is heated again to enter the 3rd reactor afterwards.French Inst Francais Du Petrole be then using three it is independent be positioned over conplane reactor,
Catalyst enters from first reactor head, after being come out from bottom with gas lift into second reactor top tank, then
Into second reactor, the catalyst gas lift that second reactor bottom comes out is into the 3rd reactor head tank, and the 3rd
The catalyst that reactor bottom comes out goes to regenerate.These technical process are connected using single reactor, reactor
Catalyst transfer between reactor is relatively difficult, and reactor complex designing, space-consuming is big, easily blocks, high energy consumption, mill
Damage is big.
Patent of the present invention provides a kind of new radial reactor, and catalyst can flow between each conversion zone, reacts
Material can also draw heating and be then back in reactor, and structure of reactor is simple, is not easily blocked, and energy consumption is low, and reaction efficiency is high.
The content of the invention
Reactor design and manufacture method with reference to example and the brief description of the drawings present invention is as follows：
A kind of continuous multi-stage radial reactor, it is characterized in that being divided into inner cylinder from inside to outside in a reactor（2）, middle cylinder
（3）And outer barrel（4）, catalyst between inner cylinder and middle cylinder, up and down it is continuously coupled；Inner cylinder and middle cylinder barrel perforation, inner cylinder and
Outer barrel is divided into 2 or multiple sections, is spaced between each section, and each section together with the catalyst between inner cylinder and middle cylinder reaction
Section；Reactor head sets a catalyst shot tank, is connected by pipeline and valve with reactor；Reactor bottom sets a catalyst
Receiving tank receives the catalyst for needing to regenerate；Catalyst continuously enters in reactor from catalyst shot tank, in inner cylinder with
Moved down between cylinder, catalyst receiving tank is exited into from reactor bottom；Reaction mass can enter in inner cylinder or outer barrel
One section, then enter radially across the catalyst layer between inner cylinder and middle cylinder in outer barrel or the corresponding section of inner cylinder, by pipeline
Entered back into after drawing heated or cooling in the inner cylinder or outer barrel of other conversion zones.
In fig. 1, reaction mass（9）Heated stove（8）Enter after heating in the first paragraph of inner cylinder bottom, pass through internal barrel
The catalyst layer reaction that the eyelet of wall enters between inner cylinder and middle cylinder, temperature reduces after reaction, into outer barrel bottom first paragraph, from
The section exits into heating furnace（7）Entered back into after middle heating in inner cylinder second segment, catalyst is exited into from internal barrel cinclides eye
Enter after layer in outer barrel second segment, enter back into heating furnace（6）Returned after middle heating in the 3rd section of inner cylinder, then it is laggard through catalyst layer
Enter the 3rd section of outer barrel, go out reactor from this.Catalyst can be between inner cylinder and middle cylinder catalyst layer slowly move from up to down
It is dynamic, catalyst collection tank is entered by the outlet of reactor lower part, the catalyst tank at the top of Returning reactor, is entered back into after regeneration
Reactor.Material is thus formed the circulation of catalyst, course of reaction is uninterruptedly carried out.Conversion zone is according to specific
Depending on reaction property, 3 sections are may generally be, can also 2-4 sections.
In actual moving process, because reaction mass can be directly entered reactor outlet through beds, this
Sample can cause the reaction time inadequate, the problems such as reaction conversion ratio is low, therefore necking passage can be set between section and section（5）,
Increase reaction mass is directed through the resistance of beds between conversion zone, reduces reaction mass and walks " short circuit ".Necking passage
It can use and install the baffle plate tilted down additional between inner cylinder and middle cylinder in a manner of reducing aisle spare, can also use by
The mode of multiple funnels is closed and then installed additional between cylinder and middle cylinder.
Brief description of the drawings：
Accompanying drawing 1：1. catalyst shot tank；2. inner cylinder；Cylinder in 3.；4. outer barrel；5. necking passage；6th, 7,8. heating furnace；9.
Reaction raw materials；10. reaction product；11. catalyst collection tank；12. dividing plate
Accompanying drawing 2：1. catalyst shot tank；2. inner cylinder；Cylinder in 3.；4. outer barrel；5. necking passage；6th, 7,8. flowmeter；9.
Reaction raw materials；10. reaction product；11. catalyst collection tank；12. dividing plate
Embodiment
The method that the present invention is further illustrated with reference to embodiment.
Embodiment：
It is simulated in the lab, as shown in Figure 2, in a transparent reactor model, reactor outer barrel
（4）Diameter 20cm, inner cylinder（2）Diameter 5cm, middle cylinder（3）Diameter 15cm, inner cylinder and middle cylinder screen making, inner cylinder and middle cylinder it
Between equipped with a diameter of 1-2mm alumina balls replace catalyst, up to reactor head is equipped with alumina balls；Reactor inner cylinder
Be divided into three sections with outer barrel, 70cm every section high, be bottom first paragraph, be followed successively by second segment, the 3rd section.Compressed air（Instead of
Reaction mass）First paragraph inner cylinder is initially entered, is connected into second segment inner cylinder from first paragraph outer barrel, then the 3rd is connected into from second segment outer barrel
Section inner cylinder, discharged from the 3rd section of outer barrel.6th, 7,8 be gas flowmeter.
Air-output pressure is adjusted, when air pressure is 0.3kgf/cm2When, the reading that flowmeter 6,7,8 is shown is respectively
35L/min, 36L/min, 38L/min, it is more or less the same, the amount for the gas for illustrating to walk " short circuit " by beds is seldom.When
Air pressure rises to 0.5kgf/cm2When, the reading that flowmeter 6,7,8 is shown is respectively 48L/min, 56L/min, 67L/min,
Differ larger, the amount for the gas for illustrating to walk " short circuit " by beds is more.
Necking is set up between inner cylinder and middle cylinder section, the gap between inner cylinder and middle cylinder is reduced into 2cm by 10cm, again
Experiment.Air pressure still sets 0.5kgf/cm2, flowmeter 6,7,8 show reading be respectively 63L/min, 65L/min,
67L/min, it is more or less the same, the amount for the gas for illustrating to walk " short circuit " by beds is seldom, increases between this explanation section and section
If necking is effective.
It should be noted that after using necking mode, catalyst can form clear area below necking, and Ji Gai areas do not have
There is catalyst, therefore inner cylinder and the corresponding part of middle cylinder cannot use aperture plate, be walked " short circuit " to prevent reaction mass.Perforation
Part must be contact catalyst.
Load alumina balls in reactor head tank, open the valve of reactor bottom, alumina balls slowly flow into instead
In the collecting tank for answering device bottom, correspondingly the alumina balls in the tank of top, which are also flowed into reactor, supplements, in flowmeter 6,7,8
Reading is basically unchanged, and illustrates that reactor fluidization process is very stable.
This is the pattern for simulating industrial reactor, and for industrial reactor, above design is equally applicable.
Certainly, described above is only one embodiment of the present invention, it should be pointed out that to the ordinary skill of this area
For personnel, under the premise without departing from the principles of the invention, some improvements and modifications can also be made, these improvements and modifications are equal
Belong within the protection domain of the claims in the present invention.
Claims (4)
1. a kind of continuous multi-stage radial reactor, it is characterized in that being divided into inner cylinder, middle cylinder and outer from inside to outside in a reactor
Cylinder, catalyst is between inner cylinder and middle cylinder, up and down continuously；Inner cylinder and middle cylinder barrel perforation, inner cylinder and outer barrel are divided into 2
Or be spaced between multiple sections, each section, each section together with the catalyst between inner cylinder and middle cylinder conversion zone；Reactor head is set
One catalyst shot tank, is connected by pipeline and valve with reactor；Reactor bottom sets a catalyst receiving tank and receives needs
The catalyst of regeneration；Catalyst continuously enters in reactor from catalyst shot tank, is moved down between inner cylinder and middle cylinder,
Catalyst receiving tank is exited into from reactor bottom；Enter in inner cylinder or outer barrel one section of reaction mass, then radially across
Catalyst layer between inner cylinder and middle cylinder enters in outer barrel or the corresponding section of inner cylinder, is drawn by pipeline after heated or cooling again
Into in the inner cylinder or outer barrel of other conversion zones.
2. continuous multi-stage radial reactor according to claim 1, it is characterised in that inner cylinder and outer barrel are divided into multistage, section
It is spaced between section.
3. continuous multi-stage radial reactor according to claim 1, it is characterised in that catalyst is continuously distributed in reaction
Between section, and it can move from up to down.
4. continuous multi-stage radial reactor according to claim 1, it is characterised in that necking passage is set between section and section.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201310270584.XA CN103521141B (en) | 2013-07-01 | 2013-07-01 | A kind of continuous multi-stage radial reactor |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201310270584.XA CN103521141B (en) | 2013-07-01 | 2013-07-01 | A kind of continuous multi-stage radial reactor |
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| CN103521141A CN103521141A (en) | 2014-01-22 |
| CN103521141B true CN103521141B (en) | 2017-12-19 |
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Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| US10882037B2 (en) * | 2016-10-28 | 2021-01-05 | Uop Llc | Apparatus and process for contacting catalyst with a gas and reduction |
| CN109250687B (en) * | 2017-07-14 | 2021-07-09 | 中国石油化工股份有限公司 | Radial reactor and chemical chain reaction process |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN200955019Y (en) * | 2006-04-21 | 2007-10-03 | 中国石油天然气股份有限公司 | Synthesized multi-sectional radial cold-exciting type reactor |
| CN101653710A (en) * | 2009-09-10 | 2010-02-24 | 惠生工程（中国）有限公司 | Multistage multi-channel radial adiabatic reactor |
| CN202506374U (en) * | 2012-02-29 | 2012-10-31 | 南京天华化学工程有限公司 | Uniform moving bed radial reactor |
-
2013
- 2013-07-01 CN CN201310270584.XA patent/CN103521141B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN200955019Y (en) * | 2006-04-21 | 2007-10-03 | 中国石油天然气股份有限公司 | Synthesized multi-sectional radial cold-exciting type reactor |
| CN101653710A (en) * | 2009-09-10 | 2010-02-24 | 惠生工程（中国）有限公司 | Multistage multi-channel radial adiabatic reactor |
| CN202506374U (en) * | 2012-02-29 | 2012-10-31 | 南京天华化学工程有限公司 | Uniform moving bed radial reactor |
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Effective date of registration: 20190221 Address after: 210048 No. 1 Puge Road, Nanjing Chemical Industrial Park, Nanjing, Jiangsu Province Patentee after: Jiangsu Jintong Surfactant Co., Ltd. Address before: 266580 No. 66 Changjiang West Road, Qingdao economic and Technological Development Zone, Shandong Patentee before: China Petroleum University (East China) |