CN203002340U - Large-size ethynylation reactor - Google Patents
Large-size ethynylation reactor Download PDFInfo
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- CN203002340U CN203002340U CN 201220634654 CN201220634654U CN203002340U CN 203002340 U CN203002340 U CN 203002340U CN 201220634654 CN201220634654 CN 201220634654 CN 201220634654 U CN201220634654 U CN 201220634654U CN 203002340 U CN203002340 U CN 203002340U
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Abstract
The utility model relates to a large-size ethynylation reactor for producing butynediol by using ethyne and formaldehyde. The large-size ethynylation reactor is characterized by comprising a reactor cylinder body and a stirring device, wherein the cylinder body is provided with a feed port and an overflow type discharge port. The large-size ethynylation reactor is characterized in that the cylinder body is externally provided with an annular main air intake pipe, the annular main air intake pipe is connected with a branched pipe after annular air intake, and the branched pipe extends into the cylinder body; the stirring device comprises a stirring shaft and a stirrer; and a clamping sleeve is arranged outside the cylinder body. The large-size ethynylation reactor disclosed by the utility model ensures the sufficient mixing and contact of gas, liquid and solid phases in the reactor, can be used for uniformly distributing the continuous phases and the dispersed phases and keeping certain retention time of the continuous phases and the dispersed phases, enhances the production intensity and provides an ideal device for the production of the butynediol.
Description
Technical field
The utility model relates to a kind of large-scale ethynylation device by alkynes aldehyde method synthesizing butynediol technique, belongs to chemical machinery field.
Background technology
The type of reactor of tradition alkynes aldehyde method synthesizing butynediol process using is mainly two types of drip fixed bed and slurry bed.
In the drip fixed bed reactors, gas phase (acetylene) is continuous phase, reaction pressure higher (5 kg/cm2), so explosion hazard is larger.In addition, in trickle bed, catalyst is fixed, and the accessory substance carbene that generates in reaction is bonded together catalyst, bed resistance is increased, and make catalyst be difficult to draw off from reactor, brings very large difficulty for the replacing of catalyst.
In slurry bed reactor, react under low pressure operation the same as suspension bed, safety is guaranteed.But. solve catalyst very difficult with separating of reactant liquor in industrial production, need trouble of Special Equipment and operation.In addition. because catalyst particle size is little. deactivation rate is also fast, and the service life of catalyst is not long.
In addition, the bubble crushing method is adopted in traditional ethynylation device internals design, but the bubble crushing method is only applicable to the gas-solid two-phase reactor, and gas is dispersed in liquid fully.The acetylene bubble by reaction bed, has reduced time of contact fast, cause the acetylene conversion per pass lower, and acetylene tail gas can not reclaim (directly emptying), causes the raw material serious waste.Internals can not make catalyst stop on the other hand, and the suspension situation for keeping, causes unstable and skewness by internal circulating load, and the dead angle is many, causes the reaction useful space to dwindle, and catalyst is assembled easily caking simultaneously, causes potential safety hazard.
After adding the circulation fluid pipeline, traditional ethynylation device formaldehyde added in reactor by the inside reactor nozzle, because each nozzle is 8kg/cm at pump discharge pressure
2During pressure head, flow can reach 4m
3/ h left and right, and reactor bottom has 12 nozzles, will make soon the most of obstruction of nozzle after driving like this, only has 2～4 and works (because internal circulating load is 6 m
3About/h), cause like this formaldehyde charging skewness, simultaneously because gas, liquid two-phase enter reactor from diverse location respectively, mix inhomogeneously, also affect reaction yield.In addition, acetylene enters reactor by sintered plate, although bubble is little, bubble increases in uphill process, reach top after fragmentation, and top is without catalyst, so too part acetylene fails effectively to participate in reaction, discharge as tail gas, cause waste of raw materials, the reaction space-time yield reduces.
Summary of the invention
The purpose of this utility model is to provide a kind of suspended-bed reactor, and liquid phase is evenly distributed, and mixability is high; Reaction pressure is low, has avoided the danger of blast; Simultaneously, catalyst is kept in motion, and can not lump, and has made up the deficiencies in the prior art.
The technical solution adopted in the utility model is: large-scale ethynylation device, comprise reactor shell and agitating device, charging aperture and overflow-type discharging opening are arranged on cylindrical shell, it is characterized in that: cylindrical shell is outside equipped with annular inlet manifold, be connected with after the annular air inlet and be in charge of, be in charge of and stretch in cylindrical shell; Agitating device comprises shaft and agitator; Cylindrical shell has chuck outward.
Optimize, be provided with baffle plate in cylindrical shell, the quantity of baffle plate is 4, is 90 ° of distributions on circumference.
Optimize, the quantity of being in charge of is 36, is divided into 6 groups and enters in cylindrical shell uniformly.
Optimize, agitator is three layer of four leaf inclined paddle type agitator;
Optimize, be provided with spiral deflector in chuck.
Optimize, chuck is divided into top tubular chuck and bottom U-shaped chuck, forms two independently heat exchange circulating systems.
Optimize, stirrer diameter is 0.3 ~ 0.5 with the ratio of barrel diameter.
Optimize, the cylindrical shell volume is 25 ~ 150 m
3, ratio of height to diameter is 1.2 ~ 2.5, nominal diameter is 2.0 ~ 6.0m.
Good effect of the present utility model is: the large-scale ethynylation device that adopts the utility model to provide, effectively raise production capacity, heat-transfer capability and the mixing effect of reactor, liquid phase is evenly distributed, reaction pressure is low, avoided the danger of blast, simultaneously, catalyst is kept in motion, can lump.Because the draw ratio of this reactor is suitable, volume is large, so output is large, efficient is high.Outside the low head of reactor and cylindrical shell, U-shaped chuck and tubular chuck are set, spiral deflector is set in chuck, the reactor exchange capability of heat has been improved less than 1mm in the gap between spiral deflector and chuck, can control more accurately the ethynylation temperature; Gas is assigned to many laterals by ring main and enters evenly distribution in reactor, makes Gas distribution even, fully contacts with liquid phase; Agitator adopts three layer of four leaf inclined paddle type agitator, be equipped with strip-shaped baffle, mixing effect and heat-transfer effect have further been improved, guaranteed that the gas, liquid, solid three-phase fully mixes, contacts in reactor, evenly distribute and keep continuous phase and decentralized photo that certain time of staying is arranged, having improved production intensity and product quality; The production of butynediols of making a living provides ideal device.
Description of drawings
Fig. 1 is the structural representation of the utility model embodiment.
Fig. 2 is the agitating device structural representation.
Fig. 3 is overflow-type discharge hole structure schematic diagram.
Fig. 4 is annular inlet manifold's structural representation.
Fig. 5 is for being in charge of the arrangement schematic diagram.
The specific embodiment
Embodiment:
Large-scale ethynylation device is the continuous operation process, and in large-scale ethynylation device production process, liquid phase material formaldehyde and solid-phase material enter in cylindrical shell 5 from charging aperture 100; Gaseous phase materials acetylene enters from annular charging house steward 10, is in charge of 11 by equally distributed 36 and enters cylindrical shell 5 bottoms effusions, and react with formaldehyde and solid catalyst in cylindrical shell 5.
Start simultaneously agitating device, the power of motor 13 and reductor 14 is delivered to shaft 19 by shaft coupling 15,18, and shaft 19 and three layer of four leaf inclined paddle type agitator 21 are rotated, and carries out stirring action.The effect of baffle plate 22 is to coordinate with agitating device, changes the flow field, strengthens stirring and mixing effect.Guarantee that the gas, liquid, solid three-phase fully mixes and reacts.
Producing reaction heat in course of reaction is taken away by ethylene glycol and water in top tubular chuck 7 and bottom U-shaped chuck 6, spiral deflectors 8 in top tubular chuck 7 and bottom U-shaped chuck 6 make ethylene glycol and the water can short circuit in flow process, guaranteed the stable of reaction temperature, reduce the generation of side reaction, improved product quality.And the design of two independent chucks makes heat transfer effect better.
The material that reaction is completed continuously outflows from the overflow-type discharging opening 20 on cylindrical shell 5 tops, and new material constantly enters again and participates in reaction in reaction.
Claims (8)
1. large-scale ethynylation device, comprise reactor shell and agitating device, and charging aperture and overflow-type discharging opening are arranged on cylindrical shell, and it is characterized in that: cylindrical shell is outside equipped with annular inlet manifold, is connected with after annular air inlet and is in charge of, and is in charge of and stretches in cylindrical shell; Agitating device comprises shaft and agitator; Cylindrical shell has chuck outward.
2. large-scale ethynylation device as claimed in claim 1, it is characterized in that: be provided with baffle plate in cylindrical shell, the quantity of baffle plate is 4, is 90 ° of distributions on circumference.
3. large-scale ethynylation device as claimed in claim 1, it is characterized in that: the quantity of being in charge of is 36, is divided into 6 groups and enters in cylindrical shell uniformly.
4. large-scale ethynylation device as claimed in claim 1, it is characterized in that: agitator is three layer of four leaf inclined paddle type agitator.
5. large-scale ethynylation device as claimed in claim 1, is characterized in that: be provided with spiral deflector in chuck.
6. large-scale ethynylation device as claimed in claim 1, it is characterized in that: chuck is divided into top tubular chuck and bottom U-shaped chuck, forms two independently heat exchange circulating systems.
7. large-scale ethynylation device as claimed in claim 1, it is characterized in that: stirrer diameter is 0.3 ~ 0.5 with the ratio of barrel diameter.
8. large-scale ethynylation device as claimed in claim 1, it is characterized in that: the cylindrical shell volume is 25 ~ 150m
3, ratio of height to diameter is 1.2 ~ 2.5, nominal diameter is 2.0 ~ 6.0m.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220634654 CN203002340U (en) | 2012-11-27 | 2012-11-27 | Large-size ethynylation reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220634654 CN203002340U (en) | 2012-11-27 | 2012-11-27 | Large-size ethynylation reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203002340U true CN203002340U (en) | 2013-06-19 |
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ID=48593976
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220634654 Expired - Lifetime CN203002340U (en) | 2012-11-27 | 2012-11-27 | Large-size ethynylation reactor |
Country Status (1)
| Country | Link |
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| CN (1) | CN203002340U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103464083A (en) * | 2013-01-31 | 2013-12-25 | 宜昌三峡中润纳米材料有限公司 | Reaction vessel for producing nanometer powder |
| CN104007225A (en) * | 2014-05-29 | 2014-08-27 | 新疆美克化工股份有限公司 | B3D reaction catalyst evaluation experimental device |
-
2012
- 2012-11-27 CN CN 201220634654 patent/CN203002340U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103464083A (en) * | 2013-01-31 | 2013-12-25 | 宜昌三峡中润纳米材料有限公司 | Reaction vessel for producing nanometer powder |
| CN103464083B (en) * | 2013-01-31 | 2016-01-06 | 宜昌三峡中润纳米材料有限公司 | A kind of reactor for the production of nano-powder |
| CN104007225A (en) * | 2014-05-29 | 2014-08-27 | 新疆美克化工股份有限公司 | B3D reaction catalyst evaluation experimental device |
| CN104007225B (en) * | 2014-05-29 | 2016-02-03 | 新疆美克化工股份有限公司 | A kind of B3D catalysts evaluation experimental device |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20130619 |
|
| CX01 | Expiry of patent term |