CN204294211U - Hexanediamine reactor - Google Patents
Hexanediamine reactor Download PDFInfo
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- CN204294211U CN204294211U CN201420482481.XU CN201420482481U CN204294211U CN 204294211 U CN204294211 U CN 204294211U CN 201420482481 U CN201420482481 U CN 201420482481U CN 204294211 U CN204294211 U CN 204294211U
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- circulation tube
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Abstract
The utility model relates to a kind of hexanediamine reactor, comprise tower body and circulation tube, described tower body is divided into cyclonic separation section under upper, supernatant section and precipitating phase, the cyclonic separation section of described tower body is cylindrical, top is provided with pneumatic outlet, the supernatant section of described tower body is cylindrical, the precipitating phase of described tower body conically, bottom is provided with throw out outlet, described circulation tube is divided into and rises liquid section and fall liquid section, the upper end rising liquid section of described circulation tube connects the cyclonic separation section of described tower body with tangential direction, the upper end falling liquid section of described circulation tube connects the cyclonic separation section of described tower body, the upper end falling liquid section of the described circulation tube link position in the cyclonic separation section of described tower body is lower than the link position rising the upper end of liquid section of described circulation tube.In the utility model, fully, speed of response is fast, and efficiency is high in various composition contact, and solid-liquid separation is effective simultaneously, and containing in the mixed solution of hexanediamine of output is substantially free of solid catalyst.
Description
Technical field
The utility model relates to a kind of hexanediamine reactor, belongs to chemical technology field.
Background technology
Hexanediamine reactor is for reacting generation hexanediamine, various compositions (comprising adiponitrile, caustic soda, ethanol, hydrogen and solid catalyst etc.) needed for reaction are sent in reactor and carries out hybrid reaction, the mixing being realized each composition by modes such as ebullated beds with fully contact, to realize the hydrogenation reaction of adiponitrile under the effect of catalyzer, generate hexanediamine, the composition of multiple gas-liquid-solid three kinds of different shapes is contained in reaction system, after three-phase is carried out preliminary separation, the mixed solution containing hexanediamine enters follow-up treatment process.Pre-existing reactors has multiple different internal structure, and major defect is that the contact of gas-liquid-solid composition in reaction system is abundant not, have impact on speed of response and reaction effect, and the separation of solid catalyst is thorough not, have impact on subsequent technique.
Utility model content
In order to overcome the above-mentioned defect of prior art, the utility model provides a kind of hexanediamine reactor, and in this reactor, various composition contact fully, speed of response is fast, efficiency is high, and solid-liquid separation is effective simultaneously, and containing in the mixed solution of hexanediamine of output is substantially free of solid catalyst.
The technical scheme that the utility model adopts: a kind of hexanediamine reactor, comprise tower body and circulation tube, described tower body is divided into cyclonic separation section under upper, supernatant section and precipitating phase, the cyclonic separation section of described tower body is cylindrical, top is provided with pneumatic outlet, the supernatant section of described tower body is cylindrical, the precipitating phase of described tower body conically, bottom is provided with throw out outlet, described circulation tube is divided into and rises liquid section and fall liquid section, described circulation tube rise liquid section and the bottom that falls liquid section is the bend pipe linkage section both linked together, the upper end rising liquid section of described circulation tube connects the cyclonic separation section of described tower body with tangential direction, the upper end falling liquid section of described circulation tube connects the cyclonic separation section of described tower body, the height of the link position of the upper end falling liquid section in the cyclonic separation section of described tower body of described circulation tube is lower than the height of the link position of the upper end rising liquid section in the cyclonic separation section of described tower body of described circulation tube.
The beneficial effects of the utility model: add reaction mass and hydrogen bottom circulation tube, rely on the gas lift effect of hydrogen, very medium flow is formed naturally in circulation tube, form tubular type ebullated bed state, oneself liquid two cured, caustic soda, ethanol, gaseous state hydrogen have maximum contact with solid catalyst in suspension, equipment, making gas, liquid emulsification contact without any operation under mechanism well, reacts completely, and is conducive to the productive rate improving speed of response and hexanediamine; Mixture carries out precipitating and supernatant in tower, and tower body profile design is reasonable, makes fine grain nickel catalyzator borrow gravity settling, therefore obtains reactant nickeliferous hardly on the top of settling vessel.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model.
Embodiment
See Fig. 1, the utility model provides a kind of hexanediamine reactor, comprise tower body 10 and circulation tube 20, described tower body is divided into cyclonic separation section 11 under upper, supernatant section 12 and precipitating phase 13, the cyclonic separation section of described tower body is cylindrical, top is provided with pneumatic outlet 14, the supernatant section of described tower body is cylindrical, the precipitating phase of described tower body conically, bottom is provided with throw out outlet 15, described circulation tube is divided into and rises liquid section 21 and fall liquid section 22, described circulation tube rise liquid section and the bottom that falls liquid section is the bend pipe linkage section both linked together, the upper end rising liquid section of described circulation tube connects the cyclonic separation section of described tower body with tangential direction, the upper end falling liquid section of described circulation tube connects the cyclonic separation section of described tower body, the height of the link position of the upper end falling liquid section in the cyclonic separation section of described tower body of described circulation tube is lower than the height of the link position of the upper end rising liquid section in the cyclonic separation section of described tower body of described circulation tube.Rely on the gas lift effect of hydrogen, the boiling-like body risen is formed in the liquid section that rises of circulation tube, various composition is fully contacted, catalyzed reaction needed for realization, mixed solution with solid catalyst enters cyclonic separation section with tangential direction and forms eddy flow, and gas rises through pneumatic outlet and exports, and liquid is to dirty, make entrained solid in liquid get rid of Xiang Tabi under the action of the centrifugal simultaneously, be beneficial to follow-up precipitation and supernatant.The cyclonic separation section that the upper end falling liquid section of described circulation tube connects described tower body also can be that tangential direction connects or connects (be referred to as and connect with tangential direction) close to tangential direction, but opening should facing to the direction of medium flow in tower body, so that medium can flow in circulation tube, usually can be arranged by suitable connection, to make the medium under certain proportion requirement enter circulation tube participate in reaction.
Usually, the bottom rising liquid section of described circulation tube can be provided with hydrogen inlet, described hydrogen inlet connects hydrogen inlet manifold, described hydrogen inlet manifold connects the outlet of compressor, thus by hydrogen with certain pressure send into circulation tube rise liquid section, be understandable that, hydrogen inlet should towards the medium flow direction in circulation tube.
Usually, described circulation tube can be connected with feeder sleeve, and the connecting portion of described feeder sleeve and described circulation tube is positioned at after the connecting portion of described hydrogen inlet manifold and described circulation tube, relies on the suction function that hydrogen produces thus, drives material flow forward.
Preferably, the tube wall of described circulation tube is jacket structured, centre is cooling medium pass, described jacket structured circulation tube tube wall is connected with the heat-eliminating medium input tube and heat-eliminating medium output tube that are communicated with described cooling medium pass, arranging of described heat-eliminating medium input tube and heat-eliminating medium output tube can according to prior art, to form the effective cooling to circulation tube.
Such as, described circulation tube rise middle part or the middle and lower part that the connecting portion of liquid section in the cyclonic separation section of described tower body can be positioned at the cyclonic separation section of described tower body usually, described circulation tube the bottom that the connecting portion of liquid section in the cyclonic separation section of described tower body can be positioned at the cyclonic separation section of described tower body usually falls.
Preferably, the main part rising liquid section of described circulation tube is vertically arranged, and the main part of falling liquid section of described circulation tube is obliquely installed, and thus when the one-piece construction realizing circulation tube requires, has maximally utilised the gas lift effect of hydrogen.
Preferably, guiding device 16 can be provided with in described tower body, the entrance end of described guiding device is positioned at the cyclonic separation section of described tower body, the exit end of described guiding device is positioned at the supernatant section of described tower body and the position that is connected of precipitating phase, described guiding device can adopt prior art or the other technologies of any suitable, the streams of the cyclonic separation section of described tower body is made partly to enter guiding device from the upper end of guiding device, flow out from the lower end of guiding device again, such as funnel-form can be adopted, thrust-augmenting nozzle is extended downwards in the lower end of funnel, another part streams then enters circulation tube by the liquid section upper end that falls of circulation tube, to carry out participation reaction, improve reaction effect, through guiding device from the material that guiding device exit end flows out, solid catalyst continues to sink under the effect of self gravitation and inertial flow, gather in the bottom of precipitating phase, can discharge from the throw out outlet bottom precipitating phase, the liquid state such as hexanediamine and gaseous composition then turn to and upwards flow, iiquid residence in supernatant section with further supernatant, form the hexanediamine mixture being substantially free of catalyzer, hexanediamine output tube through being arranged on supernatant section enters subsequent treatment process after drawing, gas containing hydrogen and ethanol rises to the top of liquid, the separation carried out between hydrogen and ethanol can be drawn by pneumatic outlet through cyclonic separation section top, so that by the hydrogen after being separated and ethanol respectively through suitable purifying treatment or without purifying treatment after reuse, this three phase separation mode, device structure is simple, not only be conducive to improving precipitate and separate effect, and the disturbance avoided to greatest extent supernatant section medium, be conducive to the content reducing solid catalyst in supernatant section medium, make to be substantially devoid of solid catalyst the mixed solution sent from supernatant section.
Preferably, the diameter of the supernatant section of described tower body is greater than the diameter of the cyclonic separation section of described tower body, and the cyclonic separation section of described tower body is taper type with the position that is connected of the supernatant section of tower body.Thus by the mode of this expanding deceleration, can improve further and sink to the bottom and supernatant effect.
Preferably, the outside of described tower body is arranged with heating coil 17, and described heating coil is arranged on the precipitating phase of described tower body or is arranged on the precipitating phase of described tower body and the supernatant section of described tower body, can ensure the temperature of reaction in open stage tower body thus.
Preferably, described pneumatic outlet connects hydrogen separation of ethanol device by pipeline, described hydrogen separation of ethanol device is provided with hydrogen outlet and nol outlet, the hydrogen steam line that described hydrogen outlet is connected described compressor inlet by hydrogen reuse pipeline or accessed to described compressor inlet air feed is the recycling achieved hydrogen and ethanol thus.
Concise and to the point working process of the present utility model is: squeeze into reactant at the bottom surge pump of circulation tube, circulating hydrogen mixes with the fresh hydrogen supplemented after compressor pressurization, what then join circulation tube rises liquid section, just very naturally due to gas lift effect, reactant is circulated in such circulation tube.Carry out hydrogenation reaction simultaneously.This reaction is thermopositive reaction, passes into the water coolant of 40 DEG C to shift out reaction heat in order to maintain optimum operating temperature in the chuck of circulation tube.Material in circulation tube enters separator along tangential direction, most hydrogen is along with alcohol vapour volatile matter is from removing, part liquid return is to the inclination downtake of two circulation tubes, another part liquid then enters the intersection of supernatant and precipitation by the pipeline of a special shape, the effect due to gravity makes nickel powder be separated.Operating without any under mechanism at heavy equipment, because inside reactor structure can obtain going out a large amount of nickel containing the bottom decant of the hexanediamine reactor product shallow lake device of catalyzer hardly under optimum operating temperature, part recirculation in endless tube, another part discharges process.
The major function of tower body each several part is:
Article (1) two, the circulation tube that nearly 20m is long: namely as tubular type ebullated bed, in this gas, liquid emulsification contact well, reacts completely.
(2) top cyclonic separator (i.e. the cyclonic separation section of described tower body): circulation tube is connected with separator tangent line, liquid phase rotate and under, gas phase is drawn out of.Lower cone settling vessel: gravity settling borrowed by fine grain nickel catalyzator, therefore obtains reactant nickeliferous hardly on the top of settling vessel.
(3) at supernatant settling vessel (i.e. the supernatant section of described tower body and precipitating phase): isolate solid-state catalyzer from mixed solution, its outer wall is around heating coil, so that reactor heating when driving, the optimum operation condition of in reactor 74 DEG C is kept.
Claims (13)
1. a hexanediamine reactor, comprise tower body, characterized by further comprising circulation tube, described tower body is divided into cyclonic separation section under upper, supernatant section and precipitating phase, the cyclonic separation section of described tower body is cylindrical, top is provided with pneumatic outlet, the supernatant section of described tower body is cylindrical, the precipitating phase of described tower body conically, bottom is provided with throw out outlet, described circulation tube is divided into and rises liquid section and fall liquid section, described circulation tube rise liquid section and the bottom that falls liquid section is the bend pipe linkage section both linked together, the upper end rising liquid section of described circulation tube connects the cyclonic separation section of described tower body with tangential direction, the upper end falling liquid section of described circulation tube connects the cyclonic separation section of described tower body, the height of the link position of the upper end falling liquid section in the cyclonic separation section of described tower body of described circulation tube is lower than the height of the link position of the upper end rising liquid section in the cyclonic separation section of described tower body of described circulation tube.
2. hexanediamine reactor as claimed in claim 1, is characterized in that the bottom rising liquid section of described circulation tube is provided with hydrogen inlet, and described hydrogen inlet connects hydrogen inlet manifold, and described hydrogen inlet manifold connects the outlet of compressor.
3. hexanediamine reactor as claimed in claim 2, it is characterized in that described circulation tube is connected with feeder sleeve, the connecting portion of described feeder sleeve and described circulation tube is positioned at after the connecting portion of described hydrogen inlet manifold and described circulation tube.
4. hexanediamine reactor as claimed in claim 3, it is characterized in that the tube wall of described circulation tube is jacket structured, centre is cooling medium pass, described jacket structured circulation tube tube wall is connected with the heat-eliminating medium input tube and heat-eliminating medium output tube that are communicated with described cooling medium pass.
5. hexanediamine reactor as claimed in claim 4, what it is characterized in that described circulation tube rises middle part or the middle and lower part that the connecting portion of liquid section in the cyclonic separation section of described tower body is positioned at the cyclonic separation section of described tower body, described circulation tube the bottom that the connecting portion of liquid section in the cyclonic separation section of described tower body is positioned at the cyclonic separation section of described tower body falls.
6. hexanediamine reactor as claimed in claim 5, it is characterized in that the main part rising liquid section of described circulation tube is vertically arranged, the main part of falling liquid section of described circulation tube is obliquely installed.
7. hexanediamine reactor as claimed in claim 1, it is characterized in that being provided with guiding device in described tower body, the entrance end of described guiding device is positioned at the cyclonic separation section of described tower body, and the exit end of described guiding device is positioned at the supernatant section of described tower body and the position that is connected of precipitating phase.
8. hexanediamine reactor as claimed in claim 7, it is characterized in that the diameter of the supernatant section of described tower body is greater than the diameter of the cyclonic separation section of described tower body, the cyclonic separation section of described tower body is taper type with the position that is connected of the supernatant section of tower body.
9. hexanediamine reactor as claimed in claim 8, it is characterized in that the outside of described tower body is arranged with heating coil, described heating coil is arranged on the precipitating phase of described tower body or is arranged on the precipitating phase of described tower body and the supernatant section of described tower body.
10. the hexanediamine reactor as described in claim 2,3,4,5 or 6, it is characterized in that being provided with guiding device in described tower body, the entrance end of described guiding device is positioned at the cyclonic separation section of described tower body, and the exit end of described guiding device is positioned at the supernatant section of described tower body and the position that is connected of precipitating phase.
11. hexanediamine reactors as claimed in claim 10, it is characterized in that the diameter of the supernatant section of described tower body is greater than the diameter of the cyclonic separation section of described tower body, the cyclonic separation section of described tower body is taper type with the position that is connected of the supernatant section of tower body.
12. hexanediamine reactors as claimed in claim 11, is characterized in that the outside of described tower body is arranged with heating coil, and described heating coil is arranged on the precipitating phase of described tower body or is arranged on the precipitating phase of described tower body and the supernatant section of described tower body.
13. hexanediamine reactors as claimed in claim 12, it is characterized in that described pneumatic outlet connects hydrogen separation of ethanol device by pipeline, described hydrogen separation of ethanol device is provided with hydrogen outlet and nol outlet, the hydrogen steam line that described hydrogen outlet is connected described compressor inlet by hydrogen reuse pipeline or accessed to described compressor inlet air feed.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420482481.XU CN204294211U (en) | 2014-08-25 | 2014-08-25 | Hexanediamine reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420482481.XU CN204294211U (en) | 2014-08-25 | 2014-08-25 | Hexanediamine reactor |
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| Publication Number | Publication Date |
|---|---|
| CN204294211U true CN204294211U (en) | 2015-04-29 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201420482481.XU Active CN204294211U (en) | 2014-08-25 | 2014-08-25 | Hexanediamine reactor |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3181220A1 (en) * | 2015-12-16 | 2017-06-21 | Basf Se | A process for removing a heterogeneous catalyst from a reaction product and a process for producing an aromatic amine |
| CN109261085A (en) * | 2018-11-16 | 2019-01-25 | 重庆华峰化工有限公司 | Hexamethylene diamine synthesis system |
| CN109382071A (en) * | 2018-12-13 | 2019-02-26 | 上海释颉化工技术合伙企业(有限合伙) | A kind of combined type generation reactor being used to prepare hexamethylene diamine |
-
2014
- 2014-08-25 CN CN201420482481.XU patent/CN204294211U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3181220A1 (en) * | 2015-12-16 | 2017-06-21 | Basf Se | A process for removing a heterogeneous catalyst from a reaction product and a process for producing an aromatic amine |
| CN109261085A (en) * | 2018-11-16 | 2019-01-25 | 重庆华峰化工有限公司 | Hexamethylene diamine synthesis system |
| CN109261085B (en) * | 2018-11-16 | 2019-07-12 | 重庆华峰化工有限公司 | Hexamethylene diamine synthesis system |
| CN109382071A (en) * | 2018-12-13 | 2019-02-26 | 上海释颉化工技术合伙企业(有限合伙) | A kind of combined type generation reactor being used to prepare hexamethylene diamine |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |