CN1171667C - Multistage circulation reactor - Google Patents
Multistage circulation reactor Download PDFInfo
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- CN1171667C CN1171667C CNB02100451XA CN02100451A CN1171667C CN 1171667 C CN1171667 C CN 1171667C CN B02100451X A CNB02100451X A CN B02100451XA CN 02100451 A CN02100451 A CN 02100451A CN 1171667 C CN1171667 C CN 1171667C
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- guide shell
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- liquid
- circular flow
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- 239000007788 liquid Substances 0.000 claims abstract description 13
- 238000004080 punching Methods 0.000 claims description 3
- 239000012295 chemical reaction liquid Substances 0.000 claims description 2
- 238000006243 chemical reaction Methods 0.000 abstract description 31
- 239000007787 solid Substances 0.000 abstract description 21
- 239000012530 fluid Substances 0.000 abstract description 19
- 238000000034 method Methods 0.000 abstract description 8
- 230000000694 effects Effects 0.000 abstract description 6
- 239000002245 particle Substances 0.000 abstract description 5
- 238000005984 hydrogenation reaction Methods 0.000 abstract description 4
- 238000007254 oxidation reaction Methods 0.000 abstract description 4
- 238000004517 catalytic hydrocracking Methods 0.000 abstract description 3
- 239000010865 sewage Substances 0.000 abstract description 3
- 239000010802 sludge Substances 0.000 abstract description 3
- 239000004215 Carbon black (E152) Substances 0.000 abstract description 2
- 238000009825 accumulation Methods 0.000 abstract description 2
- 239000003245 coal Substances 0.000 abstract description 2
- 230000008021 deposition Effects 0.000 abstract description 2
- 238000004090 dissolution Methods 0.000 abstract description 2
- 229930195733 hydrocarbon Natural products 0.000 abstract description 2
- 150000002430 hydrocarbons Chemical class 0.000 abstract description 2
- 239000000463 material Substances 0.000 abstract description 2
- 238000000855 fermentation Methods 0.000 abstract 1
- 230000004151 fermentation Effects 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 30
- 239000012071 phase Substances 0.000 description 6
- 230000005587 bubbling Effects 0.000 description 5
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 2
- 238000013019 agitation Methods 0.000 description 2
- JHIVVAPYMSGYDF-UHFFFAOYSA-N cyclohexanone Chemical compound O=C1CCCCC1 JHIVVAPYMSGYDF-UHFFFAOYSA-N 0.000 description 2
- 230000002950 deficient Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- PXWYZLWEKCMTEZ-UHFFFAOYSA-N 1-ethyl-2-nitrobenzene Chemical compound CCC1=CC=CC=C1[N+]([O-])=O PXWYZLWEKCMTEZ-UHFFFAOYSA-N 0.000 description 1
- LRWZZZWJMFNZIK-UHFFFAOYSA-N 2-chloro-3-methyloxirane Chemical compound CC1OC1Cl LRWZZZWJMFNZIK-UHFFFAOYSA-N 0.000 description 1
- YQYGPGKTNQNXMH-UHFFFAOYSA-N 4-nitroacetophenone Chemical compound CC(=O)C1=CC=C([N+]([O-])=O)C=C1 YQYGPGKTNQNXMH-UHFFFAOYSA-N 0.000 description 1
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 1
- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- WHNWPMSKXPGLAX-UHFFFAOYSA-N N-Vinyl-2-pyrrolidone Chemical compound C=CN1CCCC1=O WHNWPMSKXPGLAX-UHFFFAOYSA-N 0.000 description 1
- 241000772415 Neovison vison Species 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000005530 etching Methods 0.000 description 1
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- HFPZCAJZSCWRBC-UHFFFAOYSA-N p-cymene Chemical compound CC(C)C1=CC=C(C)C=C1 HFPZCAJZSCWRBC-UHFFFAOYSA-N 0.000 description 1
- HNJBEVLQSNELDL-UHFFFAOYSA-N pyrrolidin-2-one Chemical compound O=C1CCCN1 HNJBEVLQSNELDL-UHFFFAOYSA-N 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 210000004243 sweat Anatomy 0.000 description 1
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
A multi-stage circulation reactor for various gas-liquid two-phase and gas-liquid-solid three-phase chemical reactions comprises a tower body 1, a guide shell 2 and a gas distributor 3, wherein the guide shell 2 is arranged in the tower body 1, and the gas distributor 3 is arranged at the bottom of the guide shell 2. Once bubbles are generated at the bottom of the tower, the fluid in the guide shell moves upwards to form a flow state that the large circulation is sleeved with the small circulation; the gas-liquid contact in the reactor is full, the gas content is high, the local gas content is uniformly distributed, the mass transfer rate is high, and the gas dissolution speed is high; for a gas-liquid-solid three-phase reaction system, solid particles are uniformly distributed in the reactor, and local accumulation or deposition cannot occur; the heat transfer effect is good, the heat exchange speed between the fluid and the wall of the reactor is high, the temperature in the reaction system is uniformly distributed due to the full mixing of the materials in the reactor, and the temperature difference of different areas is very small, so that the reactor can be widely applied to various gas-liquid and gas-liquid-solid reaction processes such as an oxidation reaction process, a hydrogenation reaction process, a hydrocracking process, a coal liquefaction hydrogenation process, a fermentation process, a hydrocarbon processing reaction process, an activated sludge sewage treatment process and the like.
Description
Technical field
A kind of reactor that is used for all kinds of solution-air two-phases and gas-liquid-solid three-phase chemical reaction belongs to field of chemical engineering, specifically, is multi-stage circular flow reactor.
Background technology
Solution-air or gas-liquid-solid reactor are widely used in chemical industry, petrochemical industry and other industrial process at present.Usually, solution-air or gas-liquid-solid reaction are all adopted bubbling style reactor or stirred-tank reactor.This two quasi-traditions reactor efficiency is low, the energy consumption height, and application is subjected to the restriction of reaction system.Solution-air or gas-liquid-solid effective mixing, gas and solid particle are the important performances of reactor at the fine dispersion of liquid phase, the high speed directed flow and the higher mass transfer rate of fluid in these courses of reaction.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, energy consumption height not only, and for the reaction system of high temperature, high pressure, deep-etching, be difficult to realize.
The common loop reactor that grows up based on bubbling style reactor is to introduce guide shell in bubbling style reactor, fluid is produced in reactor to circulate, thereby strengthened solution-air or gas-liquid-solid mixed effect, the overall mass transfer rate of reactor also is higher than traditional bubbling style reactor.
But, there is a serious defective in traditional common loop reactor, promptly in the annular space zone between guide shell and reactor wall, because the suffered buoyancy of bigger bubble is greater than suffered drag force, therefore the drag force that liquid circulation produced can not be pulled bigger bubble get off, cause the annular space gas holdup little, the reactor utilization rate is low, and the overall efficiency of reactor is low.
Summary of the invention
The objective of the invention is to: on the basis of traditional bubbling style reactor, propose and developed a kind of multi-stage circular flow reactor.This multi-stage circular flow reactor adopts the multilevel deflector tube and the inner member of different structure, solved the defective that traditional common loop reactor annular space gas holdup is little, reaction efficiency is low fully, its hydrodynamic performance is good, solution-air or gas-liquid-solid good mixing, total mass transfer rate height, reactor temperature is evenly distributed, and can be widely used at all kinds of solution-airs or gas-liquid-solid chemical reaction process.
The present invention is achieved in that
Comprise body of the tower 1, guide shell 2, gas distributor 3, guide shell 2 is arranged in the body of the tower 1, gas distributor 3 is arranged at the bottom of guide shell 2.
The present invention also adopts following technical scheme:
Body of the tower 1 height overall is 3-12 with the ratio of reactor inside diameter, and guide shell 2 diameters are 0.3-0.9 with the ratio of reactor inside diameter.
Guide shell 2 is an integral body, can be one section, also can be more than two sections; 5～50 centimetres of intersegmental distances link to each other with the rigidity rib; The intersegmental deflection plate that adds, punching on every section guide shell 2.
Guide shell 2 is provided with aperture area vertically.
Perforate on the guide shell 2 can be a place, also can be more than the place.
Inner member 4 is arranged on the guide shell 2.
The distance of the following end distance reactor bottom of guide shell 2 is 10-100 centimetre; The liquid level 10-200 of the last end distance reaction liquid of guide shell centimetre.
Reactor is built-in with multilevel deflector tube 2, and is mutually coaxial fixing between the guide shells at different levels, between leave the space.
Guide shell 2 can have the 1-6 root, and each guide shell 2 axis is parallel, places in the reactor, and every guide shell all is equipped with gas distributor 32 times.
The characteristics of multi-stage circular flow reactor of the present invention are:
1. multi-stage circular flow reactor of the present invention is made of body of the tower, guide shell, inner member and gas distributor.Guide shell is single hop or multistage, intersegmental employing various ways combination and/or interpolation inner member;
2. reacting gas enters aeration tower through gas distributor.Once generation, because the jet power and the density contrast of gas, bubble group will drive surrounding liquid and move upward bubble at the bottom of tower, and totally carry out circulation movement fast round each section of guide shell and guide shell, form the flow regime that big circulation overlaps little circulation;
3. because the solution-air full contact, the gas holdup height, local gas holdup is evenly distributed, so the mass transfer rate height, the gas dissolution velocity is fast; To gas-liquid-solid three-phase reaction system, solid particle is evenly distributed in reactor, local accumulation or deposition can not take place.
4. heat transfer effect is good: because fluid does slewing campaign at the reactor annular space, and the wall exchange rate height of fluid and reactor, simultaneously because the abundant mixing of the interior material of reactor, the interior uniformity of temperature profile of reaction system, the temperature difference of zones of different is very little.
Description of drawings
Accompanying drawing 1 is one of structure chart of multi-stage circulating aerating tower of the present invention;
Accompanying drawing 2 be multi-stage circulating aerating tower of the present invention structure chart two;
Accompanying drawing 3 be multi-stage circulating aerating tower of the present invention structure chart three;
Accompanying drawing 4 be multi-stage circulating aerating tower of the present invention structure chart four;
Accompanying drawing 5 is structure charts of the inner member (deflection plate) between guide shell of the present invention;
Accompanying drawing 6 is the fluid flow state figure in the structure of reactor shown in Figure 1;
Accompanying drawing 7 is the fluid flow state figure in the structure of reactor shown in Figure 2;
Accompanying drawing 8 is the fluid flow state figure in the structure of reactor shown in Figure 3;
Accompanying drawing 9 is the fluid flow state figure in the structure of reactor shown in Figure 4;
Accompanying drawing 10 is the structure and the flow regime figure of many guide shell multi-stage circular flow reactors.
Concrete enforcement
Describe the present invention below in conjunction with accompanying drawing:
As shown in Figure 1, form by three parts such as body of the tower 1, guide shell 2 and gas distributors 3.Guide shell can be one section, two sections or multistage, and is intersegmental continuous with the rigidity rib.
As shown in Figure 2: form by four parts such as body of the tower, guide shell, inner member 4 and gas distributors.Guide shell can be one section, two sections or multistage.
As shown in Figure 3: form by three parts such as body of the tower, the guide shell 2 of being with perforate and gas distributors.Along guide shell one place, two places or many places aperture area can be arranged axially.
As shown in Figure 4, form by four parts such as body of the tower, guide shell, inner member and gas distributors.Guide shell can be one section, two sections or multistage, and certain position on every section guide shell is provided with aperture area.
As Fig. 6, fluid carries out directed movement fast round every section guide shell and whole guide shell in tower, form the motor pattern that big circulation overlaps little circulation.
In multi-stage circular flow reactor of the present invention, reacting gas is entered through gas distributor 3 by the multi-stage circular flow reactor bottom, and produce a large amount of bubbles on every side at gas distributor 3 immediately, also promptly around gas distributor 3, form dilute-phase zone, the density of dilute-phase zone is less than surrounding liquid, under density contrast and gas enter momentum effect in the reactor, bubble is together with liquid upwards motion in guide shell of dilute-phase zone, and the liquid in the annular space district can flow to gas distributor immediately and sentences and replenish between guide shell 2 and reactor wall, forms quick circulation movement thus.During the top of upward fluid to the first section guide shell 2, under the effect of deflection plate and/or differential static pressure, a part of fluid can flow to annular space by the space between first and second guide shells, and with annular space in the fluid bout that flows downward; Part fluid still can move upward and enter in second guide shell, and continues to move upward.So continue, up to the top of fluid motion to a last guide shell, turning back then moves downward along annular space.
Obviously, in above-mentioned the flowing in reactor, form some little circulation, form big circulation, promptly form the flow regime that big circulation overlaps little circulation along whole guide shell along every section guide shell 2.Like this, the less turbulence difference is little everywhere at inside reactor, and gas holdup is evenly distributed, and is evenly distributed along the axial bubble of reactor; To the gas-liquid-solid reaction system, solid particulate distributions is even.Because gas is done the multi-stage circulating motion in reactor, though mean residence time remains unchanged, the distance that gas was flowed through before the effusion reactor is longer, and solution-air fully contacts mixing simultaneously, so gas is at the solubility height of liquid phase.
This reactor is made up of four parts such as body of the tower 1, inner member 4, guide shell 2 and bottom gas distributors 3.No mechanical mixing component in the reactor of the present invention, fluid is slewing circulation in reactor, solution-air or gas-liquid-solid good mixing, reactor does not have the dead angle, the mass transfer rate height; By the effect of guide shell and inner member, in reactor, form the rapid movement pattern that circulation or big circulation overlap little circulation, bubble and solid particle evenly distribute, and gas holdup and solid holdup uniformity, solid particle can not accumulate at any position; Because at the quick circulation movement of reactor inner fluid, reactor temperature is evenly distributed, fluid and reactor wall heat exchange are good.The present invention can be widely used in oxidation reaction process, hydrogenation process, and hydrocracking process, coal liquefaction hydrogenation process, sweat is in all kinds of solution-airs such as hydrocarbon processing course of reaction and activated sludge sewage disposal process and the gas-liquid-solid reaction process.
The multilevel deflector tube can be divided into secondary, three grades or some levels according to the height of reactor.The multilevel deflector tube can have different forms, comprising: guide shell is divided into multistage, and is intersegmental apart from 5-50 centimetre; Guide shell is divided into multistage, and the intersegmental deflection plate that adds punches at different parts on every section guide shell; Guide shell is one section, and in the different parts punching, percent opening is determined by the guide shell length overall.
Gas distributor is equipped with in the bottom of the inherent guide shell of reactor.
Introduce several specific embodiment of the present invention below.
Embodiment 1: gas-liquid reaction
Reactor: primary circulation reactor; Volume: 50 liters
Chemical reaction: alpha-pyrrolidone+acetylene → vinyl pyrrolidone
Reaction temperature: 170 ℃; Reaction pressure: 12atm; Catalyst: KOH
Continued operation, liquid air speed: 0.25h
-1
Embodiment 2: oxidation reaction
Reactor: secondary circulation reactor; Volume: 1m
3
Chemical reaction: to nitro ethylbenzene+air → p-nitroacetophenone
Reaction temperature: 140 ℃; Reaction pressure: 5atm; Catalyst: acetate
Intermittently operated, the reaction time: 11h
Embodiment 3: oxidation reaction
Reactor: secondary circulation reactor; Volume: 20 liters
Chemical reaction: isopropyl toluene+oxygen → CHP
Reaction temperature: 106 ℃; Reaction pressure: 5.6atm
Intermittently operated, reaction time 4h
Embodiment 4: the mink cell focus catalytic hydrocracking
Reactor: secondary circulation reactor; Reactor volume: 20m
3
Reaction temperature: 450 ℃; Reaction pressure: 130atm
Continued operation, liquid air speed 1h
-1
Embodiment 5: trade effluent is handled
Reactor: the secondary circulation reactor, body of the tower is made by carbon steel; Volume: 25m
3
Sewage is the petrochemical industry comprehensive wastewater, mainly contain benzene, toluene, styrene, epoxychloropropane and cyclohexanone etc., COD is 960-1020mg/l, adopt continued operation, environment temperature is 6-20 ℃, and water temperature is 18-25 ℃ in the tower, the time of staying of waste water in tower is 6 hours, day output is 100 tons of waste water/days, and concentration of activated sludge is 3-6g/l, and the COD of water reduces to 80-140 after treatment.The COD clearance is 86.2-91.6%.
Claims (9)
1. multi-stage circular flow reactor comprises body of the tower (1), guide shell (2), gas distributor (3), it is characterized in that: guide shell (2) is arranged in the body of the tower (1), and gas distributor (3) is arranged at the bottom of guide shell (2).
2. multi-stage circular flow reactor according to claim 1 is characterized in that: body of the tower (1) height overall is 3-12 with the ratio of reactor inside diameter, and guide shell (2) diameter is 0.3-0.9 with the ratio of reactor inside diameter.
3. multi-stage circular flow reactor according to claim 1 is characterized in that: guide shell (2) is an integral body, can be one section, also can be more than two sections, 5～50 centimetres of intersegmental distances link to each other with the rigidity rib, the intersegmental deflection plate that adds can be gone up punching at every section guide shell (2).
4. according to claim 1 or 3 described multi-stage circular flow reactors, it is characterized in that: guide shell (2) is provided with aperture area vertically.
5. according to claim 1 or 4 described multi-stage circular flow reactors, it is characterized in that: the perforate on the guide shell (2) can be a place, also can be more than the place.
6. multi-stage circular flow reactor according to claim 1 is characterized in that: inner member (4) is arranged on the guide shell (2).
7. multi-stage circular flow reactor according to claim 1 is characterized in that: the distance of the following end distance reactor bottom of guide shell (2) is 10-100 centimetre; The liquid level 10-200 of the last end distance reaction liquid of guide shell (2) centimetre.
8. multi-stage circular flow reactor according to claim 1 is characterized in that: this device is built-in with multilevel deflector tube (2), and is mutually coaxial fixing between the guide shells at different levels, between leave the space.
9. multi-stage circular flow reactor according to claim 1 is characterized in that: guide shell (2) can have 1～6, and the axis of each guide shell (2) is parallel to each other, places in the reactor, all is equipped with gas distributor (3) under the every guide shell (2).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB02100451XA CN1171667C (en) | 2002-02-01 | 2002-02-01 | Multistage circulation reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB02100451XA CN1171667C (en) | 2002-02-01 | 2002-02-01 | Multistage circulation reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1435275A CN1435275A (en) | 2003-08-13 |
| CN1171667C true CN1171667C (en) | 2004-10-20 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB02100451XA Expired - Fee Related CN1171667C (en) | 2002-02-01 | 2002-02-01 | Multistage circulation reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1171667C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1332748C (en) * | 2005-09-16 | 2007-08-22 | 清华大学 | Self circulated cascade gas lift type internal-loop reactor system |
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| CN2836903Y (en) * | 2005-10-18 | 2006-11-15 | 浙江仁恒化工有限公司 | Diversion barrel type dissolver |
| CN100338179C (en) * | 2005-12-28 | 2007-09-19 | 煤炭科学研究总院 | Magnetic scraper loop reactor for coal direct liquefaction and coal direct liquefaction method thereof |
| US7358389B2 (en) * | 2006-01-04 | 2008-04-15 | Eastman Chemical Company | Oxidation system employing internal structure for enhanced hydrodynamics |
| CN100427198C (en) * | 2006-09-01 | 2008-10-22 | 清华大学 | Staged reactor |
| DE102008041652A1 (en) * | 2008-08-28 | 2010-03-04 | Evonik Oxeno Gmbh | Apparatus and method for the continuous reaction of a liquid with a gas |
| CN103043746B (en) * | 2011-10-17 | 2014-02-05 | 中国石油天然气股份有限公司 | Degreasing method for super heavy oil wastewater |
| CN103043847A (en) * | 2011-10-17 | 2013-04-17 | 中国石油天然气股份有限公司 | Air floatation-biochemical treatment method and equipment for super-heavy oil sewage |
| CN103880180B (en) * | 2014-03-05 | 2016-01-20 | 大连民族学院 | Industrial park high-concentration hardly-degradable waste water intelligent integral treatment unit |
| CN105727845B (en) * | 2016-02-03 | 2017-12-19 | 浙江大学 | A kind of double solid suspension bed reactors and its application for hydrocracking heavy oil |
| CN108479646A (en) * | 2018-03-30 | 2018-09-04 | 青岛理工大学 | Pneumatic mixing arrangement of spent acid reduction |
| CN111054278A (en) * | 2019-12-02 | 2020-04-24 | 河南金鹏化工有限公司 | Continuous production process and device for thiodicarb synthesis reaction |
| CN112808181B (en) * | 2021-01-19 | 2022-04-08 | 山西潞安化工有限公司 | Jet loop reactor for preparing ethylene by oxidative coupling of methane |
| CN112619566B (en) * | 2021-01-19 | 2022-04-12 | 山西潞安化工有限公司 | Multistage jet loop reactor for preparing ethylene by oxidative coupling of methane |
-
2002
- 2002-02-01 CN CNB02100451XA patent/CN1171667C/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1332748C (en) * | 2005-09-16 | 2007-08-22 | 清华大学 | Self circulated cascade gas lift type internal-loop reactor system |
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| CN1435275A (en) | 2003-08-13 |
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