CN201006419Y - Bubbling type heterogemeous reactor - Google Patents
Bubbling type heterogemeous reactor Download PDFInfo
- Publication number
- CN201006419Y CN201006419Y CNU2007200031113U CN200720003111U CN201006419Y CN 201006419 Y CN201006419 Y CN 201006419Y CN U2007200031113 U CNU2007200031113 U CN U2007200031113U CN 200720003111 U CN200720003111 U CN 200720003111U CN 201006419 Y CN201006419 Y CN 201006419Y
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- Prior art keywords
- tower
- reactor
- gas
- riser
- tray
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- 230000005587 bubbling Effects 0.000 title claims description 34
- 241000282326 Felis catus Species 0.000 claims description 4
- 230000001788 irregular Effects 0.000 claims description 3
- 241001235022 Aplysia punctata Species 0.000 claims description 2
- 229910003460 diamond Inorganic materials 0.000 claims description 2
- 239000010432 diamond Substances 0.000 claims description 2
- 238000006243 chemical reaction Methods 0.000 abstract description 20
- 239000007787 solid Substances 0.000 abstract description 15
- 230000000694 effects Effects 0.000 abstract description 6
- 239000007788 liquid Substances 0.000 abstract description 5
- 230000005540 biological transmission Effects 0.000 abstract 1
- 230000007547 defect Effects 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 29
- 239000012071 phase Substances 0.000 description 22
- 238000012546 transfer Methods 0.000 description 11
- 230000016507 interphase Effects 0.000 description 5
- 239000007791 liquid phase Substances 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- 239000007790 solid phase Substances 0.000 description 4
- 238000013019 agitation Methods 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 239000003245 coal Substances 0.000 description 2
- 239000003250 coal slurry Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 230000008021 deposition Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 238000009423 ventilation Methods 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000011978 dissolution method Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000002787 reinforcement Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 210000004243 sweat Anatomy 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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Abstract
The utility model relates to a bubble multi-phase reactor, comprising a tower, 2-8000 tower discs, and a gas distributor, wherein the tower discs are equally or non-equally arranged in the tower, each tower disc is provided with 10-200 boost tubes regularly or irregularly and 1-5 down spouts at the edge of the tower disc, the hole rate of the boost tube is 5-50%, each boost tube is provided with 1-30 air holes regularly or irregularly, which aperture is 0.5-10mm. The utility model can resolve the defects of traditional bubble reactor as low air rate and low reaction efficiency, with better dynamic property, better mixing effect of gas-liquid or gas-liquid-solid, high transmission efficiency and wide application for kinds of gas-liquid or gas-liquid-solid reaction.
Description
Technical field
The utility model relates to the chemical engineering equipment field, specifically, relates to multi-phase bubbling reactor.
Technical background
Solution-air or gas-liquid-solid phase reactor are widely used in fields such as chemical industry, the energy, environment and biochemistry.Usually solution-air or gas-liquid-solid reaction are all adopted bubble type or mechanical agitation tank reactor.The reactor efficiency of this two quasi-tradition is low, energy consumption is high, and application is subjected to the restriction of reaction system.In the multiphase flow reactor, interphase mass transfer, mixing and heat transfer are the important technology indexs of decision reactor performance, the response intensity that directly has influence on, conversion ratio and product quality.For solution-air or gas-liquid-solid reaction system, interphase mass transfer determines the key factor of reactor effect often.Be overall reaction control step and the course of reaction that relates to liquid phase or solid-phase catalyst particularly,, just must adopt the mechanical agitation of certain form, to improve mass transfer rate and alternate mixing for accelerating overall process for mass transfer.Adopt mechanical agitation, not only the energy consumption height is difficult for sealing, causes environmental pollution, when particularly volume of industrial production is big, often adopts many same stirred tanks, has not only increased equipment investment, and the quality of stability of product and uniformity also are affected.Though it is simple in structure that general bubbling bed has, alternate contact is advantage preferably, and very big leeway is being arranged aspect the interphase mass transfer reinforcement.In this class reactor, with the increase of superficial gas velocity, generally from even bubbling area, transition region to stirring turbulence district (inhomogeneous bubbling area), in the bed footpath hour, also the plunger district can appear, all can form the ball cap shape air pocket of some.Because ball cap shape air pocket is compared with minute bubbles, its specific area is very little, has a strong impact on alternate contact effect, and because the air pocket rate of climb is very fast, cause portion gas short circuit to a certain degree, these all make the conversion ratio of interphase mass transfer and reactant reduce greatly.
The utility model content
The purpose of this utility model is to overcome the deficiency that bubbling style reactor traditional in the above-mentioned prior art exists, be engaged in the developmental research and the suitability for industrialized production practice of reactor apparatus for many years through the utility model people, exploitation provides a kind of structure unique novel, good, the good mixing of hydrodynamic performance, total high multi-phase bubbling reactor of mass-transfer efficiency.
The multi-phase bubbling reactor that the utility model provides is characterized in that comprising tower body 9 (cylindrical shell) 1, and cat head 6 at the bottom of the tower 7, all is a hemispherical at the bottom of cat head and the tower, and the tower body draw ratio is 3-12, is preferably 5-10; Tower tray 2 is 1 to 50 tower tray, and every tower tray equidistantly or not equidistantly is arranged in the tower body and is 90 ° of angles with tower body, and the diameter of tower tray equals the tower body internal diameter, by support or be weldingly fixed on the tower body; Gas distributor 3 is located at place, top at the bottom of the tower body bottom column; Described tower tray upwards is provided with 10 to 8000 riseies 4 thereon, be preferably 3000 to 7000 riseies, and under tower tray to having 1 to 5 downspout 5, riser on each tower tray is rule or irregular alignment for example is equilateral triangle, concentric circles, aplysia punctata, diamond shaped, quadrangle or square etc., be preferably respectively to arrange and adjacent staggering of riser be the equilateral triangle arrangement, wherein the riser percent opening is (each tray area) 5-50%, the high 5-100mm of each riser, be preferably 10-40mm, internal diameter 2-50mm, be preferably 2-30mm, (on every side and/or top) rule or irregularly have a 1-30 passage 8 on the riser body, its aperture is 0.5-10mm, and percent opening is the 0.1-30% of (riser) body area, is preferably 1-10%; Downspout is located at the tower tray marginal zone.
Reactor is generally tower reaction or other form reactor described in the multi-phase bubbling reactor that provides according to the utility model, along with reaction mass, solution-air or gas-liquid-solid different in kind, the difference of reaction condition and course, and the difference of flow rate, select tower body draw ratio, tray structure, quantity size of tray riser, and the number of passage especially and size make reaction system reach optimization.The percent opening of riser is meant the total area ratio tower tray area of a circle of riser perforate on the tower tray, if percent opening is below 5%, 50% above gas-liquid or gas-liquid-solid reaction system are moved bad in reactor, skewness, loose contact, plunger district and inhomogeneous bubble district can occur, produce air pocket and rise rapidly, have a strong impact on alternate contact effect and cause short circuit.
In multi-phase bubbling reactor of the present utility model, because device structure, special tray structure uniqueness, reacting gas enters through gas distributor 3 from the multi-phase bubbling reactor bottom, and produce a large amount of bubbles on every side at gas distributor 3 immediately, enter under the momentum effect of reactor at density contrast and gas, gas rises, carry out multistage distribution through the riser layer by layer 4 on the multistage tower tray, bubble distributes very evenly, liquid or liquid-solid two-phase enter from the bubbling style reactor top, flow downward by the downspout on the multistage tower tray 5, carry out adverse current with gas and contact with cross-flow on tower tray.Because gas evenly is scattered in minute bubbles, little in inside reactor turbulence difference everywhere, gas holdup is evenly distributed.When gas passes through every layer of tower tray in reactor, all evenly be scattered in minute bubbles and fully contact, thereby improve the solubility of gas in liquid phase, improve the interphase mass transfer effect, thereby improved reaction efficiency, shorten the reaction time with liquid phase or liquid-solid phase.
The characteristics of the multi-phase bubbling reactor that the utility model provides are:
1. the utility model multi-phase bubbling reactor is made of tower body, tower tray and gas distributor, and is simple in structure, tray structure uniqueness particularly, and it is little to have overcome traditional bubbling reactor gas holdup fully, the defective that reaction efficiency is low.
2. reacting gas is after gas distributor enters reactor, and bubble is after producing at the bottom of the tower, because the jet power and the density contrast of gas, bubble can move upward; Distribute through multistage tower tray, make bubble close and little, the solution-air full contact is complete, the gas holdup height, and local gas holdup is evenly distributed, so the mass transfer rate height, the gas dissolution velocity is fast; For gas-liquid-solid three-phase reaction system, solid particle is evenly distributed in reactor, and local accumulation and deposition do not take place, and shortens the reaction time, constant product quality.
3. do not have machinery in the reactor of the present utility model and stir parts, solution-air or fluid good mixing in reactor such as gas-liquid-solid, no dead angle, mass transfer rate height.Bubble and solid particle evenly distribute on tower tray, and gas holdup and solid holdup uniformity, solid particle can not deposit at any position.
The multi-phase bubbling reactor that the utility model provides can be widely used in oxidation reaction process, in all kinds of solution-airs such as sweat and the gas-liquid-solid reaction process.
Description of drawings
The structural representation of Fig. 1 multi-phase bubbling reactor
Fig. 2 is the structural representation of tower tray
The specific embodiment
The utility model further specifies the utility model with the following example, but protection domain of the present utility model is not limited to the following example.
Embodiment 1 and comparative example 1
At the gas-liquid system, be gas medium with the atmospheric air, liquid phase medium is a water.Experiment is bubbling bed reactor (comparative example 1) and multi-phase bubbling reactor (embodiment 1) with reactor.Wherein bubbling bed reactor urceolus internal diameter is 0.30m, and total reactor height 3.0m, reactor bottom are spherical, and gas distributor is housed.Multi-phase bubbling reactor (tower body 1) internal diameter is 0.30m, total reactor height 3.0m, and 7 is spherical at the bottom of the reactor column, near the tower bottom gas distributor 3 is being housed.Six tower trays 2 are housed in the multi-phase bubbling reactor, tray spacing 0.3m, on tower tray, upwards establish 50 riseies 4, riser is equilateral triangle and arranges, the high 10mm of riser, internal diameter 8mm, opening 2 apertures on each riser body is 1.5mm passage 8, and 1 downspout 5, be located at place, tower tray border area downwards.
In the ventilation scope is under the condition of 1cm/s-8cm/s, and the top number of bubbles of bubbling bed reactor is more, and the bottom number of bubbles is less, and it is very inhomogeneous that bubble distributes, bubble in tower by the time have from the phenomenon of tower center line short circuit and take place; And in the multi-phase bubbling reactor, bubble is evenly distributed, and full contact is complete, and bubble has long motion path in reactor, and the time of staying is long.Judge that from nowed forming multi-phase bubbling reactor obviously is better than bubbling bed reactor.
Adopt the gas holdup of bed expansion method assaying reaction device, oxygen dissolution method assaying reaction body amasss average mass tranfer coefficient.Multi-phase bubbling reactor is compared with bubbling bed reactor, and average gas holdup improves 10-30%, and reactor average external volume mass tranfer coefficient improves 10%-40%.
Embodiment 2:
At gas-liquid-solid three-phase system, be gas medium with the atmospheric air, concentration is that 20% water-coal-slurry is a liquid-solid phase.The granularity of coal is less than 0.15mm, and experiment is a multi-phase bubbling reactor with reactor, and multi-phase bubbling reactor tower body 1 internal diameter is 0.30m, total reactor height 3.0m, and 7 is spherical at the bottom of the reactor column, near the tower bottom gas distributor 3 is being housed.Six tower trays 2 are housed in the reactor, tray spacing 3.0m, on tower tray, upwards establish 50 riseies 4, long air pipe is concentric circles and arranges, the high 10mm of riser, internal diameter 8mm, to open 4 apertures be 1.5mm passage 8 to rule on each riser body, and 2 downspout 5 symmetries are located at tower tray two border areas downwards.Under the condition of ventilation scope 5cm/s-8cm/s, the water-coal-slurry continuous feed, inlet amount is 80kg/h.Test after 24 hours, check every layer of tower tray, do not find the coal particle deposition on the tower tray.
Claims (3)
1. a multi-phase bubbling reactor is characterized in that comprising tower body (1), and cat head (6) at the bottom of the tower (7), is hemispherical at the bottom of cat head and the tower, and the tower body draw ratio is 3-12; Tower tray (2) is 1 to 50 tower tray, and every tower tray equidistantly or not equidistantly is arranged in the tower body and is 90 ° of angles with tower body, and the diameter of tower tray equals the tower body internal diameter, by support or be weldingly fixed on the tower body; Gas distributor (3) is located at place, top at the bottom of the tower body bottom column; Described tower tray upwards is provided with 10 to 8000 riseies (4) thereon, and under tower tray to having 1 to 5 downspout (5), riser on each tower tray is rule or irregular alignment, wherein the riser percent opening is 5-50%, and each riser high 5 is to 100mm, and internal diameter 2 is to 50mm, rule or irregular 1 to 30 passage (8) that has on the riser body, its aperture is 0.5 to 10mm, and percent opening is 0.1-30%, and downspout is located at the tower tray marginal zone.
2. according to the multi-phase bubbling reactor of claim 1, it is characterized in that described tower body draw ratio is 5 to 10; Riser on the described tower tray (4) is 3000 to 7000 riseies, triangular in shape, concentric circles, aplysia punctata, diamond shaped, quadrangle or square arrangement, and the high 10-40mm of each riser, internal diameter 2 is to 30mm; The percent opening of described passage (8) is 1 to 10%.
3. according to the multi-phase bubbling reactor of claim 2, it is characterized in that on the described tower tray that riser is and adjacent staggering be equilateral triangle and arrange.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007200031113U CN201006419Y (en) | 2007-01-29 | 2007-01-29 | Bubbling type heterogemeous reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007200031113U CN201006419Y (en) | 2007-01-29 | 2007-01-29 | Bubbling type heterogemeous reactor |
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| Publication Number | Publication Date |
|---|---|
| CN201006419Y true CN201006419Y (en) | 2008-01-16 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNU2007200031113U Expired - Lifetime CN201006419Y (en) | 2007-01-29 | 2007-01-29 | Bubbling type heterogemeous reactor |
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| Country | Link |
|---|---|
| CN (1) | CN201006419Y (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100528322C (en) * | 2007-01-29 | 2009-08-19 | 煤炭科学研究总院 | Multi-phase bubbling reactor |
| CN102806061A (en) * | 2012-08-22 | 2012-12-05 | 山东科技大学 | Butane oxidation reactor |
| CN104275132A (en) * | 2014-10-21 | 2015-01-14 | 武汉江汉化工设计有限公司 | Thioether oxidation tower for producing dimethyl sulfoxide |
| CN105709450A (en) * | 2014-12-19 | 2016-06-29 | Ifp新能源公司 | Dispenser tray for material and/or heat exchange column comprising bubbling means |
| CN108525614A (en) * | 2018-06-24 | 2018-09-14 | 唐山三友硅业有限责任公司 | Reactor for the experiment of silicon bronze body contacts reactivity worth |
-
2007
- 2007-01-29 CN CNU2007200031113U patent/CN201006419Y/en not_active Expired - Lifetime
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100528322C (en) * | 2007-01-29 | 2009-08-19 | 煤炭科学研究总院 | Multi-phase bubbling reactor |
| CN102806061A (en) * | 2012-08-22 | 2012-12-05 | 山东科技大学 | Butane oxidation reactor |
| CN102806061B (en) * | 2012-08-22 | 2014-04-16 | 山东科技大学 | Butane oxidation reactor |
| CN104275132A (en) * | 2014-10-21 | 2015-01-14 | 武汉江汉化工设计有限公司 | Thioether oxidation tower for producing dimethyl sulfoxide |
| CN105709450A (en) * | 2014-12-19 | 2016-06-29 | Ifp新能源公司 | Dispenser tray for material and/or heat exchange column comprising bubbling means |
| CN108525614A (en) * | 2018-06-24 | 2018-09-14 | 唐山三友硅业有限责任公司 | Reactor for the experiment of silicon bronze body contacts reactivity worth |
| CN108525614B (en) * | 2018-06-24 | 2024-04-26 | 唐山三友硅业股份有限公司 | Reactor for silicon-copper contact reaction performance test |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| COR | Change of bibliographic data |
Free format text: CORRECT: CO-PATENTEE TO: DONGHUA ENGINEERING TECHNOLOGY CO., LTD. ^ |
|
| CU01 | Correction of utility model patent |
Correction item: Co-patentee Correct: Donghua engineering Polytron Technologies Inc Number: 03 Page: The title page Volume: 24 |
|
| CU03 | Correction of utility model patent gazette |
Correction item: Co-patentee Correct: Donghua engineering Polytron Technologies Inc Number: 03 Volume: 24 |
|
| ERR | Gazette correction |
Free format text: CORRECT: CO-PATENTEE; FROM: NONE ^ TO: DONGHUA ENGINEERING TECHNOLOGY CO., LTD. ^ |
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| AV01 | Patent right actively abandoned |
Effective date of abandoning: 20070129 |
|
| C25 | Abandonment of patent right or utility model to avoid double patenting |