CN202823383U - Butane oxidation reactor - Google Patents
Butane oxidation reactor Download PDFInfo
- Publication number
- CN202823383U CN202823383U CN201220416994.1U CN201220416994U CN202823383U CN 202823383 U CN202823383 U CN 202823383U CN 201220416994 U CN201220416994 U CN 201220416994U CN 202823383 U CN202823383 U CN 202823383U
- Authority
- CN
- China
- Prior art keywords
- liquid
- gas
- reactive tank
- oxidation reactor
- cylindrical shell
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
The utility model discloses a butane oxidation reactor which comprises a barrel body, a liquid inlet and a gas outlet are formed in the upper portion of the barrel body, a liquid outlet and a gas inelt are formed in the lower portion of the barrel body, a plurality of reactive tanks are respectively formed in the upper portion and the lower portion inside the barrel body, liquid downcommers are arranged between the reactive tanks and the barrel body lateral wall, the upper and lower adjacent liquid downcomers are arranged in a stagger mode, gas ascending channels and gas distributors are arranged on the reactive tanks, external circulating pipelines are connected outside the barrel body, and a cooler and a circulating pump are installed on the external circulating pipelines. Liquid material enters the barrel body through the liquid inlet, and flows through the reactive tanks in sequence from top to bottom through overflow of the liquid downcomers; gas enters the gas distributors through the gas ascending channels, is mixed with the liquid material inside the reactive tanks in a bubbling mode, and reacts with the liquid material; and reaction heat is cooled and removed through the cooler installed on the external pipelines. The butane oxidation reactor is suitable for being used in a liquid phase oxidation process with low rate of reaction, and continuous operation is achieved easily. The oxygen-containing gas flows through the reactor from bottom to top in one time, and therefore power consumption is saved.
Description
Technical field
The utility model relates to a kind of chemical reaction device, particularly a kind of butane oxidation reactor that is applicable to the butane oxidation reaction.
Background technology
The butane oxidation reaction belongs to typical gas-liquid two-phase reaction, or gas-liquid-solid three phase catalytic reaction, and oxidation reaction mainly occurs in the liquid phase body.Current generally all using with churned mechanically blistering reaction still realized oxidation reaction, and this class reactor can speed up gas and liquid mixes, and reduces or eliminates resistance to mass tranfer between the gas-liquid two-phase, thereby play the effect of fast reaction speed.But this type of reactor operation energy consumption is large, and the repair and maintenance expense is high, and in addition, it is high that butane oxidation reacts required pressure, and the mechanical agitation reactor easily leaks, and has potential safety hazard.
Chinese patent ZL200410000231.9 discloses a kind of cyclohexane oxidation device, and it adopts the gas circulating compressor multistage feeding, and reaction zone is installed filler etc., makes every effort to reduce the gas-liquid mass transfer resistance, accelerates reaction rate, intermittently operated.This type of reactor obviously is not suitable for the butane oxidation process, because butane oxidation belongs to long reaction induction period, reaction rate is slower, and the oxygen-containing gas that the unit interval consumes is less, and the gas-liquid mass transfer resistance is not principal contradiction.
The utility model content
Based on above-mentioned technical problem, the utility model provides a kind of butane oxidation reactor, and this reactor undesirable gas recycle compressor is saved power consumption, is applicable to the slower liquid phase oxidation reaction process of reaction rate.
Its technical solution is:
A kind of butane oxidation reactor, comprise cylindrical shell, on cylindrical shell top liquid-inlet and gas vent are set, in the cylindrical shell bottom liquid outlet and gas feed are set, in cylindrical shell, set gradually up and down a plurality of reactive tanks, between reactive tank and cylinder lateral wall, downspout is set, neighbouring downspout shifts to install, at reactive tank gas rising passway and gas distributor are set, be externally connected with the outer circulation pipeline at cylindrical shell, cooler and circulating pump are installed on the circulating line outside, liquid material enters cylindrical shell through liquid-inlet, flow through successively reactive tank from top to bottom through the downspout overflow, the liquid material bubbling hybrid reaction of gas in the gas rising passway enters gas distributor and reactive tank, reaction heat removes by the cooling of the cooler on the outer circulation pipeline.
Further, aforesaid liquid outlet connects cooler through outlet, and the cooled partially liq of cooler is delivered in the pipe-line mixer with raw material liq after the preheater preheating through liquid circulation pump and mixes, and pipe-line mixer connects liquid-inlet by inlet tube.
Further, be provided with outer circulation liquid-inlet and the outer circulation liquid outlet that connects the outer circulation pipeline at cylinder lateral wall.
The height of above-mentioned cylindrical shell and the ratio of internal diameter are not less than 8, and preferred high/footpath is than being 30～50.
The quantity of above-mentioned reactive tank is no less than 6, and the quantity of preferred reaction groove is 20～30.
The degree of depth of above-mentioned reactive tank is not less than 80mm, and the degree of depth of preferred reaction groove is 80～120mm.
Offer drain hole on the base plate of above-mentioned reactive tank, the diameter of drain hole is 2～6mm.
The cross-sectional area of above-mentioned downspout accounts for more than 5% of cylindrical shell cross-sectional area, and preferred 5%～10%.
Leave the gap of passing through for liquid between above-mentioned downspout bottom and the below adjacent reaction trough floor, above-mentioned reactive tank base plate downspout adjacent with the below leaves the gas compartment between the top, wherein reserves the preferred 40～60mm of height of the gas compartment between the adjacent downspout in reactive tank base plate and the below top.
Above-mentioned cylindrical shell and be positioned at the reactive tank of inner barrel and the member such as downspout is made by stainless steel material.
Useful technique effect of the present utility model is:
1, in the utility model reactor a plurality of reactive tanks are set, in each reactive tank, liquid material contacts mixing with from bottom to top oxygen-containing gas bubbling, fully reaction; It is longer that this reactor is applicable to induction period, and reaction rate is slower, and the reaction that the oxygen-containing gas of unit interval internal consumption is less is particularly useful for the oxidation reaction of butane, and production efficiency is high, and is easy to realize continued operation;
2, the external circulating line of the utility model reactor is equipped with the equipment such as cooler, liquid circulation pump, by the control of one or more snippets external liquid circulation cooling heat transferring realization response temperature at circulating line;
3, in the utility model reactor, the reactive tank base plate and above between the adjacent downcomer bottom and the reactive tank base plate and below all leave gap or the gas compartment of suitable distance between the adjacent downspout top, be convenient on the one hand liquid material in the reactive tank through the smooth overflow of downspout to next reactive tank, make again on the other hand from the upper strata reactive tank and have certain flow velocity through the liquid that downcomer bottom flows into lower floor's reactive tank, liquid flow in the reactive tank mixes, liquid level upgrades to be accelerated, impel the again mass transfer between liquid level and the gas, continue the oxygen in the reaction consumption gas, oxidation reaction is more abundant, make simultaneously that oxygen content further reduces in the tail gas of outflow reactor, improved the security of oxidation reaction;
4, in the utility model reactor, the ratio of the cross-sectional area of downspout and cylindrical shell cross-sectional area is not less than 5%, guarantees to exist all the time in the downspout fluid-tight; Offer the drain hole of diameter 2～6mm at the base plate of reactive tank, be used for emitting after reactor is stopped using the liquid material of cylindrical shell;
5, the utility model reactor machinery-free stirs facility, has eliminated the potential safety hazards such as leakage, has reduced running cost, and oxygen-containing gas once-through reactor from bottom to top, and the undesirable gas recycle compressor has been saved power consumption.
Description of drawings
Fig. 1 is the structural principle schematic diagram of oxidation reactor among the embodiment 1;
Fig. 2 is the layout drawing of gas distributor among the embodiment 1;
Fig. 3 is the structural principle schematic diagram of gas distributor among the embodiment 2;
Fig. 4 is the layout drawing of gas distributor among the embodiment 2.
Among the figure: 1-cylindrical shell, a liquid-inlet, b gas feed, c gas vent, d liquid outlet, 2-reactive tank, 3-gas rising passway, 4-gas distributor, the 5-gas passage that turns back, 6-drain hole, 7-downspout, the 8-cooler, 9-liquid circulation pump, 10-pipe-line mixer, 11-preheater, 21～27 pipelines.
The specific embodiment
Embodiment 1
As shown in Figure 1, a kind of butane oxidation reactor comprises cylindrical shell 1, the height of cylindrical shell 1 and the ratio of internal diameter are 40, on cylindrical shell 1 top liquid-inlet a and gas vent c are set, in cylindrical shell 1 bottom liquid outlet d and gas feed b are set, in cylindrical shell 1, set gradually up and down 20 reactive tanks 2.Reactive tank 2 is crowded around by base plate, side plate and cylinder lateral wall and is formed, depth H=the 120mm of reactive tank 2, base plate at reactive tank 2 is installed a gas rising passway 3, gas rising passway 3 be shaped as cylindrical shape, arranged outside gas distributor 4 at gas rising passway 3, gas distributor 4 is blister-type, as shown in Figure 2, between gas rising passway 3 and gas distributor 4, form the gas passage 5 that turns back, gas rises to the top through gas rising passway 3, enter in the reactive tank with the passage 5 that turns back by gas, mix with liquid bubbling in the reactive tank.The drain hole 6 that also to offer a diameter on the base plate of reactive tank 2 be 2mm.Downspout 7 is set between reactive tank 2 and cylinder lateral wall, and neighbouring downspout shifts to install, and the cross-sectional area of downspout 7 accounts for 7% of cylindrical shell cross-sectional area.The gas compartment is left between the adjacent downspout top in the base plate of reactive tank 2 and below, gas compartment height h=50mm, the reactive tank base plate and above leave the gap between the adjacent downcomer bottom, to pass through for liquid.
Liquid outlet d connects cooler 8 through pipeline 21, cooler 8 cooled partially liqs are delivered in the pipe-line mixer 10 with raw material liq after preheater 11 preheatings through liquid circulation pump 9, pipeline 22 and mix, cooler 8 cooled all the other liquid are delivered to downstream unit through circulating pump 9 and pipeline 23, and pipe-line mixer 10 connects liquid-inlet a by pipeline 24.Preheater links to each other with the pipeline 25 of carrying the fresh liquid material.
The below describes specific works process of the present utility model:
Fresh butane material pumps into preheater 11 with the 960.0ml/h flow rate through pipeline 25 and is preheated to 110 ℃, with enter in the lump pipe-line mixer 10 from the outer circulation material of pipeline 22 (flow rate of outer circulation material with the flow rate of fresh feed than being 1:1) and mix by inlet tube 24, liquid-inlet a sends into reactor, under action of gravitation, flow through successively each reactive tank, downspout, until reactor bottom, flow out through liquid outlet d, enter cooler 8 coolings, enter subsequently liquid circulation pump 9, part loops back reactor through pipeline 22, all the other send into downstream unit through pipeline 23, and the control reaction pressure is 3.2MPa.Oxygen-enriched air enters reactor through gas feed b, and the gas rising passway that then passes each reactive tank from bottom to top contacts with the interior liquid material bubbling of gas distributor and reactive tank, the top of through reactor, and reacted tail gas is discharged through gas vent c.Product is through chromatography, and the conversion ratio of iso-butane is 24.6%, the product tert-butyl alcohol be 82.7% selectively, realized purpose of the present invention.
The structure of butane oxidation reactor is substantially with embodiment 1, the difference part is: increase by two sections outer circulation pipelines 26,27 outside cylindrical shell, cooler 8 and liquid circulation pump 9 all are installed outside, better to remove oxidation reaction heat, as shown in Figure 3 on the circulating line 26,27; Depth H=the 80mm of reactive tank, the quantity of reactive tank is 30; The gas distributor annular that adopt to distribute, as shown in Figure 4, so that liquid better mixes in gas and the reactive tank; The remainder physical dimension is constant.
In the specific works process, the flow rate of outer circulation material is 0.5:1 with the flow rate of fresh feed ratio, and all the other process conditions are with embodiment one.Product is through chromatography, and the conversion ratio of iso-butane reaches 41.8%, the product tert-butyl alcohol be 82.3% selectively, realized purpose of the present invention.
Outer circulation pipeline in above-described embodiment 2 also can add in the relevant position as required, with the control of reaction temperature in the better realization response device.
Need to prove, under the instruction of this specification, any equivalents that those skilled in the art have done, or obvious variant all should be within protection domains of the present utility model.
Claims (10)
1. butane oxidation reactor, comprise cylindrical shell, it is characterized in that: on cylindrical shell top liquid-inlet and gas vent are set, in the cylindrical shell bottom liquid outlet and gas feed are set, in cylindrical shell, set gradually up and down a plurality of reactive tanks, between reactive tank and cylinder lateral wall, downspout is set, neighbouring downspout shifts to install, at reactive tank gas rising passway and gas distributor are set, be externally connected with the outer circulation pipeline at cylindrical shell, cooler and circulating pump are installed on the circulating line outside, liquid material enters cylindrical shell through liquid-inlet, flow through successively reactive tank from top to bottom through the downspout overflow, the liquid material bubbling hybrid reaction of gas in the gas rising passway enters gas distributor and reactive tank, reaction heat removes by the cooling of the cooler on the outer circulation pipeline.
2. a kind of butane oxidation reactor according to claim 1, it is characterized in that: liquid outlet connects cooler through outlet, the cooled partially liq of cooler is delivered in the pipe-line mixer with raw material liq after the preheater preheating through circulating pump and mixes, and pipe-line mixer connects liquid-inlet by inlet tube.
3. a kind of butane oxidation reactor according to claim 2 is characterized in that: be provided with outer circulation liquid-inlet and the outer circulation liquid outlet that connects the outer circulation pipeline at cylinder lateral wall.
4. a kind of butane oxidation reactor according to claim 1, it is characterized in that: the height of described cylindrical shell and the ratio of internal diameter are not less than 8.
5. a kind of butane oxidation reactor according to claim 1, it is characterized in that: the quantity of described reactive tank is no less than 6.
6. a kind of butane oxidation reactor according to claim 1, it is characterized in that: the degree of depth of described reactive tank is not less than 80mm.
7. a kind of butane oxidation reactor according to claim 1, it is characterized in that: offer drain hole on the base plate of described reactive tank, the diameter of drain hole is 2～6mm.
8. a kind of butane oxidation reactor according to claim 1, it is characterized in that: the cross-sectional area of described downspout accounts for more than 5% of cylindrical shell cross-sectional area.
9. a kind of butane oxidation reactor according to claim 1 is characterized in that: the downspout bottom and below leave the gap of passing through for liquid between the adjacent reaction trough floor, the reactive tank base plate and below leave the gas compartment between the adjacent downspout top.
10. a kind of butane oxidation reactor according to claim 1 is characterized in that: described cylindrical shell and the reactive tank and the downspout that are positioned at inner barrel are made by stainless steel material.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201220416994.1U CN202823383U (en) | 2012-08-22 | 2012-08-22 | Butane oxidation reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201220416994.1U CN202823383U (en) | 2012-08-22 | 2012-08-22 | Butane oxidation reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202823383U true CN202823383U (en) | 2013-03-27 |
Family
ID=47935183
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201220416994.1U Expired - Lifetime CN202823383U (en) | 2012-08-22 | 2012-08-22 | Butane oxidation reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202823383U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102806061A (en) * | 2012-08-22 | 2012-12-05 | 山东科技大学 | Butane oxidation reactor |
| CN115282918A (en) * | 2021-12-24 | 2022-11-04 | 衢州学院 | Tubular reactor |
-
2012
- 2012-08-22 CN CN201220416994.1U patent/CN202823383U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN115282918A (en) * | 2021-12-24 | 2022-11-04 | 衢州学院 | Tubular reactor |
| CN115282918B (en) * | 2021-12-24 | 2024-06-11 | 衢州学院 | Tubular reactor |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103801242B (en) | Reactor and the alkylation reaction method utilizing this reactor | |
| US11628415B2 (en) | Built-in micro interfacial enhanced reaction system and process for PTA production with PX | |
| CN202410629U (en) | Air-lift-type circulation flow reactor | |
| CN100427198C (en) | Staged reactor | |
| CN202823383U (en) | Butane oxidation reactor | |
| CN102806061B (en) | Butane oxidation reactor | |
| WO2020155505A1 (en) | Low-pressure gas-liquid enhanced emulsifying bed reaction device and method | |
| CN104759228A (en) | Gas push type self-mixing combined purifying tank | |
| CN104152275A (en) | Gas-phase methanol esterification reaction device | |
| CN204656509U (en) | Airlift circulating reactor | |
| CN106732200A (en) | A kind of turbine type cold hydrogen box | |
| CN111151201A (en) | Reaction device and system and method for synthesizing acetic acid by methanol carbonylation | |
| CN201969546U (en) | Multiphase chemical reactor | |
| CN105413590B (en) | A kind of catalyzed butane oxidation reaction unit | |
| CN100522897C (en) | Cyclohexane oxidation reactor | |
| CN212595615U (en) | Reaction unit and system for synthesizing acetic acid by methanol carbonyl | |
| CN203227485U (en) | Gas-liquid reaction kettle | |
| CN202199146U (en) | External circular reaction side-discharge rectification apparatus in composite structure | |
| CN202860529U (en) | Reaction device for producing cyclohexene by partial hydrogenation of benzene | |
| CN101244996B (en) | Vertical type bubbling oxidation reaction device for synthesizing naphthalic acid | |
| CN101704742B (en) | Reactor for producing aromatic carboxylic acid | |
| CN102181047B (en) | Polyethylene terephthalate (PET) esterification reaction kettle | |
| CN104478698B (en) | A kind of method of continuous seepage stearyl chloride | |
| CN201593047U (en) | Liquid continuous impinging stream multi-phase reaction and aerobic fermentation technical equipment | |
| CN201598320U (en) | Gold-containing copper pyrite reaction device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20191104 Address after: 266590 No. 579, Bay Road, Huangdao District, Shandong, Qingdao Co-patentee after: CNNOOC TAIZHOU PETROCHEMICAL CO.,LTD. Patentee after: SHANDONG University OF SCIENCE AND TECHNOLOGY Address before: 266590 Qingdao economic and Technological Development Zone, Shandong, former Bay Road, No. 579 Co-patentee before: TAIZHOU DONGLIAN CHEMICAL Co.,Ltd. Patentee before: Shandong University of Science and Technology |
|
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20130327 |