CN201848243U - Trimethyl benzene continuous oxidation reactor - Google Patents
Trimethyl benzene continuous oxidation reactor Download PDFInfo
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- CN201848243U CN201848243U CN2010205640247U CN201020564024U CN201848243U CN 201848243 U CN201848243 U CN 201848243U CN 2010205640247 U CN2010205640247 U CN 2010205640247U CN 201020564024 U CN201020564024 U CN 201020564024U CN 201848243 U CN201848243 U CN 201848243U
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- kettle
- air inlet
- inlet pipe
- continuous oxidation
- oxidation reaction
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Abstract
The utility model relates to a trimethyl benzene continuous oxidation reactor, belonging to the technical field of production equipment in the chemical industry. The equipment comprises a tower-shaped reactor kettle body, wherein an upper section of the kettle body is provided with a stirring device, the top of the kettle body is provided with a gas phase outlet, a lower section of the kettle body is provided with a heating device, the bottom of the kettle body is provided with a discharge hole, a middle section of the kettle body is provided with a feeding pipe and an air inlet pipe which are distributed up and down, the lower section of the kettle body is provided with a kettle bottom air inlet pipe, the kettle bottom air inlet pipe is provided with a flow guide cylinder which forms an annular gap with the lower section of the kettle body, and a vent hole of the kettle bottom air inlet pipe is positioned within a range of a lower port of the flow guide cylinder. After adopting the trimethyl benzene continuous oxidation reactor, not only accumulated material blocking is avoided, but also inoxidized residual materials are more sufficiently mixed with air to be further oxidized in dynamic turbulent flow process, so as to obtain the effect of improving the yield of trimethyl benzene acid, and achieve two aims at one time.
Description
Technical field
The utility model relates to a kind of pseudocumene continuous oxidation reaction device, and the continuous oxidation technology of especially a kind of pseudocumene is produced the oxidation reaction apparatus of trimellitic acid, belongs to the chemical production equipment technical field.
Background technology
Trimellitic acid is a kind of important chemical material.Understand according to the applicant, the method that existing pseudocumene generates trimellitic acid through oxidation reaction has two kinds of batch (-type) and continous ways.
The oxidation reaction apparatus that clearance-type adopts is generally the tower bubbling style reactor.This type of reactor is introduced air from the bottom of tower, flow out from the top.Air produces oxidation reaction with reaction mass by contacting naturally.1), air and reaction mass mix inhomogeneous its defective has:, the air molecule surface touches material can produce oxidation reaction, do not reach and then form bubble and scurry from reactor head and flow out, so reaction efficiency is not high, only is suitable for low-producing small-bore tower reactor; 2), repeat charging, blowing every several hours needs, intensifications of boosting, step-down cooling, so the hardware of equipment easily produces fatigue, and lack service life, the frequency of maintenance height, and safety coefficient is not high, and environmental protection pressure is big; 3), the energy consumption height, loss of material is big, energy is difficult to recycle.
The oxidation reaction apparatus that continous way adopts is with many reactors (oxidation reactors of a plurality of clearance-types) series connection, and classification is oxidation progressively, makes pseudocumene be oxidized to trimellitic acid continuously.Its typical structure can be 200610086124.1 Chinese patent application referring to application number.This kind equipment significant disadvantages is that equipment investment is big, and technological process is long.Especially, the trimellitic acid that generates when the pseudocumene reaction mass of liquid state and air oxidation reaction crystallization easily accumulates in reactor bottom, not only hinders discharging, influences technological process, and can cause the later stage oxidation reaction not smooth, influences the yield of trimellitic acid.In addition, the connection between each reactor need increase pipeline or conveying equipment, thereby causes problems such as solid material knot wall, obstruction easily, makes to be difficult to long-time normal operation, and the operation control of many reactors is comparatively complicated, and technic index is difficult to stable control.
The utility model content
The purpose of this utility model is: at the major defect that above-mentioned prior art exists, propose a kind of pseudocumene continuous oxidation reaction device that can effectively avoid the bottom buildup to stop up, thereby guarantee that technological process is smooth and easy, and oxidation reaction is unaffected.
In order to reach above purpose, pseudocumene continuous oxidation reaction device of the present utility model comprises tower jar shape reactor kettle; The epimere of described kettle is equipped with agitating device, and the top has gaseous phase outlet; The hypomere of described kettle has heater, and the bottom has discharging opening; Described kettle stage casing has upper and lower distribution feed pipe and air inlet pipe; Described kettle hypomere has air inlet pipe at the bottom of the still, is equipped with on the air inlet pipe at the bottom of the described still and the kettle hypomere forms ring-type guide shell at interval, and the venthole of air inlet pipe is positioned at the lower port scope of described guide shell at the bottom of the described still.
Owing to be provided with air inlet pipe at the bottom of the still, therefore can play certain effect of brushing to the autoclave body bottom deposit, inhibition is gathered, especially after being provided with guide shell, the venthole of air inlet pipe is positioned at the lower port scope of guide shell again at the bottom of the still, and the ring-type that the reaction mass that the air of input causes to fall and break by guide shell travels back across under the effect of ascending air between kettle hypomere and the guide shell falls at interval, and circulation is rolled, the result has effectively avoided the buildup clogging, has guaranteed that technological process is smooth and easy.In addition, facts have proved that the reaction speed of pseudocumene oxidation generation trimellitic acid is along with the concentration of trimellitic acid improves and slows down.After the trimellitic acid of pseudocumene oxidation reaction generation reaches certain saturated concentration (being generally 65%), further oxidation reaction will be very difficult.Even take such as stirring, rationally control conventional measures such as mixing ratio, reaction temperature and interpolation catalyst, the yield of final trimellitic acid all is difficult to improve.After adopting the utility model, not only avoided the buildup obstruction, simultaneously, in dynamic turbulent process, made that unoxidized salvage stores is more abundant to be mixed with air, further oxidized, obtained the effect that has improved the trimellitic acid yield, kill two birds with one stone.
It is that air inlet pipe is concentric ring-shaped or snail shape at the bottom of the described still, is intervally distributed with venthole up above that the utility model further improves; The lower port of described guide shell is shunk.
Like this, not only can make ascending air more effectively brush the decline reaction mass, it be raised up, and after air enters lower port, present the trend that flows to the guide shell inwall, thereby reaction mass is blown to the ring-type interval, the easier formation circulation of rolling.
Description of drawings
Below in conjunction with accompanying drawing the utility model is further described.
Fig. 1 is the structural representation of an embodiment of the utility model.
Fig. 2 is the structural representation of Fig. 1 embodiment guide shell part.
Fig. 3 is Fig. 1 embodiment heating arrangement schematic diagram.
Fig. 4 is the structural representation of Fig. 1 embodiment deflection plate part.
Fig. 5 is the vertical view of Fig. 3 deflection plate.
Fig. 6 is the vertical view of Fig. 1.
The specific embodiment
Embodiment one
The pseudocumene continuous oxidation reaction device of present embodiment such as Fig. 1 and shown in Figure 6, the reactor kettle 1 of tower jar shape are divided into upper, middle and lower three sections 1-1,1-2, the 1-3 that reduces from top to bottom, connect by the transition awl between each section.The epimere of kettle is equipped with the agitating device 4 of external vertical driven by motor, and the top has gaseous phase outlet V, and measurement, venting.The hypomere 1-3 of kettle and stage casing 1-2 have double wall formula hot oil heater 5 (its concrete structure hereinafter describes in detail in conjunction with Fig. 3), and the bottom has discharging opening D, and heat conductive oil inlet H1 and temperature-measuring port T1.
Kettle hypomere adjacent bottom place has by air inlet pipe at the bottom of the still of air intlet G3 input, and guide shell 3 is housed on air inlet pipe at the bottom of the still.Air inlet pipe is concentric ring-shaped or snail shape at the bottom of the still, is intervally distributed with venthole up above, and the venthole of air inlet pipe all is positioned at the lower port scope of guide shell 3 at the bottom of the still, and venthole can distribute comparatively equably like this.Guide shell 3 concrete structures that are positioned at air inlet pipe top at the bottom of the still of kettle hypomere form ring-type at interval with the kettle hypomere as shown in Figure 2, and its lower port is shunk.The venthole of air inlet pipe is positioned at the lower port scope of guide shell fully at the bottom of the still, therefore when air inlet, the air of input is by guide shell, the ring-type that the reaction mass that causes to fall and break travels back across under the effect of ascending air between kettle hypomere and the guide shell falls at interval, and circulation is rolled, thereby avoided the buildup clogging, further fully oxidation in dynamic turbulent process simultaneously makes the yield of final trimellitic acid improve more than 10% than prior art.
In addition, kettle 1 has upper and lower distribution secondary feed tube.First order feed pipe is positioned at the kettle epimere, and by charging aperture A1 input, the first order air inlet pipe by air intlet G1 input is equipped with in its below.On the vertical axle of agitating device sencond stage impeller spaced apart is housed, this sencond stage impeller lays respectively at the above and below of first order feed pipe.Second level feed pipe is positioned at the kettle stage casing under the first order air inlet pipe, and by charging aperture A2 input, the second level air inlet pipe by air intlet G2 input is equipped with in its below.Upper and lower interval, the circuitous level Four deflection plate 2 that distributes are housed in the kettle stage casing between second level feed pipe and the second level air inlet pipe.The concrete structure of deflection plate 2 such as Fig. 4, shown in Figure 5, one side is the liquid storage pool 2-1 that forms with the kettle adjacent sidewalls, opposite side is vertical drainage plate 2-2, between liquid storage pool and the drainage plate sieve plate 2-3 with cellular passage, the top edge of drainage plate is higher than the sieve plate upper surface, thereby form the overflow rib, its lower limb extends in the liquid storage pool of next stage deflection plate, and forms the baffling gap with the inner edge of this liquid storage pool.Level Four deflection plate 2 is upper and lower interval, the circuitous distribution in the kettle stage casing.When reaction mass drops on the deflection plate from top to bottom, and air is flowed through from the bottom to top during the passage of deflection plate, reaction mass is blowed floating is the boiling shape, the liquid reaction material by overflow on liquid storage pool and the sieve plate after, along the liquid storage pool of drainage plate inflow next stage deflection plate, can keep the passage at kettle middle part like this is the ascending air passage, and reaction mass then needs through full of twists and turns baffling passage, thereby guaranteeing further that reaction mass fully mixes with air contacts, and improves oxidation efficiency.
Double wall formula hot oil heater concrete structure as shown in Figure 3, the hypomere 1-3 of kettle and stage casing 1-2 have overcoat separately respectively, thus the first order under being formed in heating double wall 5-1 and at last second level heating double wall 5-2.The conduction oil of first order heating double wall is entered by the H1 mouth, is exported by H2; The conduction oil of second level heating double wall is entered by the H3 mouth, is exported by H4.Like this, the temperature in the segmentation control reactor makes it reach perfect condition as required.In addition, have helical baffle in the heating double walls at different levels, thereby form the spiral upper upstream road, so that guarantee that temperature is even.
In addition, the deflection plate of the kettle stage casing the superiors of present embodiment top is provided with by adding mouthful first order catalyst make-up pipe of B1 input, and the guide shell top of kettle hypomere is provided with by adding mouthful second level catalyst make-up pipe of B2 input.Thereby can add catalyst by the reaction needed classification easily.Also be provided with refluxing opening F at the kettle epimere, the catalyst after the vaporization that heats up can be drawn after condensation process Returning reactor by gaseous phase outlet.All the other via holes also have the M1-4 manhole among the figure, N1-3 tail oxygen hole, T1-6 thermometer hole.
Facts have proved, adopt the equipment of embodiment after, material in a reactor through repeatedly fully oxidation, and classified reaction, the trimellitic acid yield can reach 95%, has following remarkable beneficial effect:
1, the guide shell that combines with air inlet pipe at the bottom of the still of inside reactor setting has not only effectively been avoided the buildup obstruction, and reaction mass is rolled in the reactor bottom circulation, fully mixes with air, has significantly improved oxidation efficiency, has prolonged the life cycle of reactor.
2, adopt the multilevel hierarchy charging, efficiently solve the problem that trimellitic acid too high levels inhibitory reaction carries out, further improve oxidation efficiency, make pseudocumene meet its multistep gradual reaction mechanism as far as possible, be converted into trimellitic acid to greatest extent.
3, adopt classification to add catalyst, satisfied different demands, be convenient to adjust the content of each stage catalyst, reach the effect of dynamic control peak optimization reaction speed at stage of reaction catalyst at different levels.
4, adopt multistage air inlet to distribute, adapt to the progressively oxidizing process that pseudocumene changes into trimellitic acid, satisfy the different demands of oxidations at different levels, can improve the conversion ratio of oxidation reaction by the oxygen demand of control step reactions at different levels to oxygen content.
5, inside reactor is provided with multistage distribution of gas agitating device, stirs by many places, make interior each section gas-liquid contact-making surface of reactor reach maximization, thereby it is more complete to make that oxidation reaction is carried out.
6, adopt multistage heating, can import the heat medium of different temperatures as required, thereby satisfy the demand that pseudocumene is oxidized to the different heats of each order reaction of trimellitic acid, effectively control and inner each the regional temperature of conditioned reaction device, avoid the material over oxidation to generate carbon dioxide and carbon monoxide, improve oxidization-hydrogenation ratio.
7, at inside reactor the multiple spot detection system is set,, the operation control optimization of W-response equipment is laid a good foundation for realizing Computerized intelligent control.
In addition to the implementation, the utility model can also have other embodiments.For example, kettle has only one-level feed pipe and air inlet pipe, perhaps more multistage feed pipe of kettle setting and air inlet pipe; Kettle has only upper and lower two sections, saves the deflection plate in stage casing; Can not establish the transition wimble structure between each of kettle section, and only be that relative position is divided into upper, middle and lower; Or the like.All employings are equal to the technical scheme of replacement or equivalent transformation formation, all drop on the protection domain of the utility model requirement.
Claims (9)
1. a pseudocumene continuous oxidation reaction device comprises tower jar shape reactor kettle; The epimere of described kettle is equipped with agitating device, and the top has gaseous phase outlet; The hypomere of described kettle has heater, and the bottom has discharging opening; Described kettle stage casing has upper and lower distribution feed pipe and air inlet pipe; It is characterized in that: described kettle hypomere has air inlet pipe at the bottom of the still, is equipped with on the air inlet pipe at the bottom of the described still and the kettle hypomere forms ring-type guide shell at interval, and the venthole of air inlet pipe is positioned at the lower port scope of described guide shell at the bottom of the described still.
2. pseudocumene continuous oxidation reaction device according to claim 1 is characterized in that: air inlet pipe is concentric ring-shaped or snail shape at the bottom of the described still, is intervally distributed with venthole up above; The lower port of described guide shell is shunk.
3. pseudocumene continuous oxidation reaction device according to claim 1 and 2 is characterized in that: described kettle is divided into three sections of the upper, middle and lower of reducing from top to bottom, connects by the transition awl between each section.
4. pseudocumene continuous oxidation reaction device according to claim 3, it is characterized in that: described kettle has upper and lower distribution secondary feed tube at least; First order feed pipe is positioned at the epimere of described kettle, and first order air inlet pipe is equipped with in its below; Second level feed pipe is positioned at the middle-end of described kettle, and second level air inlet pipe is equipped with in its below.
5. pseudocumene continuous oxidation reaction device according to claim 4 is characterized in that: be equipped with in the kettle between described second level feed pipe and the second level air inlet pipe between the upper and lower every, the circuitous deflection plate that distributes, have cellular passage on the described deflection plate; One side of described deflection plate is the liquid storage pool that forms with the kettle adjacent sidewalls, and opposite side is vertical drainage plate; It between described liquid storage pool and the drainage plate sieve plate with cellular passage; The top edge of described drainage plate is higher than the sieve plate upper surface, forms the overflow rib; The lower limb of described drainage plate extends in the liquid storage pool of next stage deflection plate, and forms the baffling gap with the inner edge of this liquid storage pool.
6. pseudocumene continuous oxidation reaction device according to claim 5, it is characterized in that: described heater is a double wall formula hot oil heater, comprise the first order heating double wall that kettle hypomere and overcoat constitute, and the second level heating double wall of kettle stage casing and overcoat formation.
7. pseudocumene continuous oxidation reaction device according to claim 6 is characterized in that: have helical baffle in the described heating double walls at different levels, form the spiral upper upstream road.
8. pseudocumene continuous oxidation reaction device according to claim 7 is characterized in that: the deflection plate top of the described kettle stage casing the superiors is provided with first order catalyst make-up pipe, and the guide shell top of described kettle hypomere is provided with second level catalyst make-up pipe.
9. pseudocumene continuous oxidation reaction device according to claim 8 is characterized in that: on the vertical axle of described agitating device sencond stage impeller spaced apart is housed, described sencond stage impeller lays respectively at the above and below of first order feed pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010205640247U CN201848243U (en) | 2010-10-15 | 2010-10-15 | Trimethyl benzene continuous oxidation reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010205640247U CN201848243U (en) | 2010-10-15 | 2010-10-15 | Trimethyl benzene continuous oxidation reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201848243U true CN201848243U (en) | 2011-06-01 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010205640247U Expired - Lifetime CN201848243U (en) | 2010-10-15 | 2010-10-15 | Trimethyl benzene continuous oxidation reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201848243U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101961632A (en) * | 2010-10-15 | 2011-02-02 | 镇江正丹化学工业有限公司(外商独资) | Trimethyl benzene continuous oxidation reactor |
-
2010
- 2010-10-15 CN CN2010205640247U patent/CN201848243U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101961632A (en) * | 2010-10-15 | 2011-02-02 | 镇江正丹化学工业有限公司(外商独资) | Trimethyl benzene continuous oxidation reactor |
| CN101961632B (en) * | 2010-10-15 | 2012-05-23 | 江苏正丹化学工业股份有限公司 | Trimethyl benzene continuous oxidation reactor |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20110601 Effective date of abandoning: 20120523 |