CN214486839U - Device for continuously synthesizing tetrahydrophthalic anhydride - Google Patents
Device for continuously synthesizing tetrahydrophthalic anhydride Download PDFInfo
- Publication number
- CN214486839U CN214486839U CN202120369233.4U CN202120369233U CN214486839U CN 214486839 U CN214486839 U CN 214486839U CN 202120369233 U CN202120369233 U CN 202120369233U CN 214486839 U CN214486839 U CN 214486839U
- Authority
- CN
- China
- Prior art keywords
- maleic anhydride
- tube
- reaction
- butadiene
- pipe
- 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.)
- Active
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 method and a device for continuously synthesizing tetrahydrophthalic anhydride, belonging to the technical field of organic synthesis. Comprises a butadiene material tank, a first-stage tubular microemulsion reactor, a flash evaporation kettle, a jet mixer and a maleic anhydride material tank; the butadiene material tank is connected with the inlet of the first-stage tubular microemulsion reactor through a butadiene delivery pump; the maleic anhydride material tank is connected with the inlet of the first-stage tubular microemulsion reactor through a maleic anhydride delivery pump; the outlet of the first-stage tubular microemulsion reactor is connected with the inlet of the flash evaporation kettle, and the outlet of the flash evaporation kettle is connected with the inlet of the jet mixer; the outlet of the jet mixer is connected with a maleic anhydride material tank, and the maleic anhydride material tank is connected with the inlet of the jet mixer through a maleic anhydride circulating pump. The tetrahydrophthalic anhydride product produced by the novel device has stable quality, high utilization rate, high automation degree of the device, low production cost, high product quality, reduced equipment requirement, reduced equipment cost, advanced technology and extremely competitive process.
Description
Technical Field
The utility model relates to a synthesis device of tetrahydrophthalic anhydride, which belongs to the technical field of organic synthesis.
Background
The tetrahydrophthalic anhydride is taken as a maleic anhydride derivative and is widely applied to the fields of resin curing agents, electronics, polyester high-grade coatings, green environment-friendly plasticizers, medicines, pesticides and the like. The cured product formed by the tetrahydrophthalic anhydride derivative and the epoxy resin is an ideal packaging material and is widely applied to packaging of basic electronic components such as resistors, capacitors, inductors, diodes, triodes and the like to complex devices such as semiconductor devices, integrated circuits and the like. As an important chemical intermediate, the demand of the product is increasing in China in recent years.
Tetrahydrophthalic anhydride was first prepared in 1928 by Dlels-Alder, using the polycondensation of maleic anhydride and butadiene, the tetrahydrophthalic anhydride synthesis reaction equation is shown below. The reaction is a synergistic mechanism, namely diene and dienophile are subjected to cyclic transition state, the breakage of old bonds and the formation of new bonds are carried out simultaneously, and the reaction process is completed in one step.
Tetrahydrophthalic anhydride synthesis reaction formula
In recent years, the product has been obtained not only in the laboratory but also in industrial production by this method. Recently, some patents on methods of increasing yield and reaction speed using pressure, solvent and elevated temperature have been reported. The domestic output of tetrahydrophthalic anhydride cannot meet the increasing market demand, and production enterprises adopt a parallel intermittent production line to expand production, but the intermittent production has the defects of large occupied area, low efficiency, small production capacity, complex production process, difficult automation control, difficult quality control, difficult reduction of production cost and the like. The patent 202020115716.7 adopts a semi-continuous reaction device to synthesize tetrahydrophthalic anhydride, and the patent CN205774230 adopts a multi-stage reaction kettle to continuously produce methyl tetrahydrophthalic anhydride in series. The research of Beijing university of chemical industry includes dissolving maleic anhydride in solvent, adding polymerization inhibitor, heating to slightly lower than reaction temperature, introducing butadiene, continuous reaction in tubular reactor, cooling the reaction liquid after the reaction reaches the end point, crystallizing, filtering, washing and drying to obtain tetrahydrophthalic anhydride. When 1, 3-butadiene and maleic anhydride are used for synthesizing tetrahydrophthalic anhydride, the side reaction is the self-polymerization of the 1, 3-butadiene. The active conjugated double bonds of 1, 3-butadiene make it very susceptible to polymerization reactions, resulting in butadiene dimers, rubbery autopolymers, butadiene peroxide autopolymers, and butadiene endpolymers. But the conversion rate of the reaction is low, the reaction time is long, the side reactions are more, and the product quality is poor.
Fluid flow in a traditional microreactor generally belongs to laminar flow, and although the fluid flow has strong directionality, symmetry and high orderliness, the laminar flow also easily causes non-uniformity and insufficient mixing of liquid and gas, so that incomplete reaction is caused.
Patent 201710532951.7 discloses a microreactor for liquid-liquid multiphase reaction, comprising an inner tube and an outer sleeve which are coaxial; an annular micro-channel is formed between the inner tube and the outer sleeve; the inner pipe is formed by sequentially connecting a first guide pipe, an inner membrane pipe and a second guide pipe which have the same outer diameter; the first port of the first flow guide pipe is provided with a light phase inlet, and the second port of the first flow guide pipe is communicated with the first port of the inner membrane pipe; the second port of the inner membrane tube and the first port of the second flow guide tube are blocked, and the second port of the second flow guide tube is closed inside the outer sleeve tube; the upper side of the outer sleeve is provided with a heavy phase inlet; a plug is arranged between one end of the outer sleeve and the pipe wall of the first flow guide pipe, and a product outlet is arranged at the other end of the outer sleeve; the arrangement of the heavy phase inlet and the inner pipe ensures that the contact mode of the heavy phase fluid and the light phase fluid is cocurrent; a distance structure is arranged in the annular microchannel. The fluid 1 flowing into the annular microchannel from the inlet 1 and permeating into the annular microchannel through the membrane is mixed with the fluid 2 entering the annular microchannel from the inlet 2 and then reacts in the microchannel, and a product enters the next process through the product outlet.
Novel content
Aiming at the technical problems in the prior art, the utility model provides a device for continuously synthesizing tetrahydrophthalic anhydride, which can realize the continuous controllable synthesis of tetrahydrophthalic anhydride, has stable product quality, high automation degree of the device, low production cost and high product quality, reduces the equipment requirement and reduces the equipment cost.
Device for continuously synthesizing tetrahydrophthalic anhydride
The device for continuously synthesizing tetrahydrophthalic anhydride comprises a butadiene material tank, a first-stage tubular microemulsion reactor, a flash evaporation kettle, a jet mixer and a maleic anhydride material tank;
the butadiene material tank is connected with the inlet of the first-stage tubular microemulsion reactor through a butadiene delivery pump; the maleic anhydride material tank is connected with the inlet of the first-stage tubular microemulsion reactor through a maleic anhydride delivery pump; the outlet of the first-stage tubular microemulsion reactor is connected with the inlet of the flash evaporation kettle, and the outlet of the flash evaporation kettle is connected with the inlet of the jet mixer; the outlet of the jet mixer is connected with a maleic anhydride material tank, and the maleic anhydride material tank is connected with the inlet of the jet mixer through a maleic anhydride circulating pump.
A butadiene absorption device is arranged between the jet mixer and the maleic anhydride material tank.
Second, the technological process
Butadiene in the butadiene material tank enters the first-stage tubular microemulsion reactor through a butadiene transfer pump; maleic anhydride in the maleic anhydride material tank enters the first-stage tubular micro-emulsion reactor through the delivery pump, and butadiene and the maleic anhydride react in the first-stage tubular micro-emulsion reactor; after the reaction is finished, the reaction product enters a flash evaporation kettle to remove excessive butadiene, and the product tetrahydrophthalic anhydride enters the next working procedure; the removed butadiene enters a jet mixer (a second-stage absorption reactor) in a gas phase state, and maleic anhydride enters the jet mixer through a circulating pump to react with butadiene to absorb the butadiene; the mixed liquid of maleic anhydride after absorbing butadiene enters a maleic anhydride material tank; the mixed liquid in the maleic anhydride material tank enters the first-stage tubular microemulsion reactor through the delivery pump to continue to react with butadiene.
A butadiene absorption device can be arranged between the jet mixer and the maleic anhydride material tank, and maleic anhydride is used for absorbing butadiene which is not absorbed by the jet mixer.
Three-tube type microemulsion reactor
The tubular microemulsion reactor comprises an outer tube, a reaction tube and an inner tube which are sequentially sleeved from outside to inside, wherein the inner tube is provided with Karman vortex street generating parts which are arranged at intervals along the length direction of the inner tube, a material A flows through the space between the reaction tube and the inner tube, a material B enters the space between the reaction tube and the inner tube through the reaction tube and is mixed with the material A, and the position where the material B enters is the position between the two Karman vortex street generating parts.
A mixing pipe penetrates through the outer pipe and is communicated with the reaction pipe, the position of the mixing pipe connected with the reaction pipe is positioned between the two karman vortex street generating parts and is close to the front karman vortex street generating part, and the material B enters the space between the reaction pipe and the inner pipe through the mixing pipe.
The mixing pipe can be a plurality of mixing pipes which are communicated with the inner cavity of the reaction pipe at intervals.
The reaction tube may include a microporous membrane tube, and tubular microporous portions communicating with an inner space of the reaction tube are formed at intervals along a longitudinal direction of the microporous membrane tube, and each of the tubular microporous portions is located between the two karman vortex street generating portions.
Each karman vortex street generating part is outwards protruded along the radial direction of the inner pipe, and the axial section of each karman vortex street generating part is in a circular arc shape with the middle part higher than the two ends.
Four, parallel high-efficiency micro-reactor
The first-stage tubular microemulsion reactor can also adopt a parallel high-efficiency microreactor which comprises a plurality of inner tubes and a plurality of reaction tubes sleeved outside the inner tubes, the reaction tubes are arranged in a reactor shell, heat exchange media flow through the inner tubes and the reactor shell respectively, a material A enters a space between each reaction tube and the corresponding inner tube through a plurality of branch tubes on a first material tube, and a material B enters a space between each reaction tube and the corresponding inner tube through a second material tube.
The reactor comprises a reactor shell, a first material pipe, a second material pipe, a material inlet cavity, a material outlet cavity, a material inlet pipe, a material outlet pipe and a material outlet cavity.
Furthermore, the inlet ends of the inner pipes are communicated through a first uniform distribution pipe, the first uniform distribution pipe is connected with a heat exchange medium inlet pipe, the outlet ends of the inner pipes are communicated through a second uniform distribution pipe, and the second uniform distribution pipe is connected with a heat exchange medium outlet pipe; the heat exchange medium inlet pipe is communicated with an inner cavity heat exchange pipe communicated with the inner cavity of the reactor shell, the inner cavity heat exchange pipe is communicated with the lower end of the reactor shell and is close to the discharging cavity, and a heat exchange pipe joint is communicated with the upper end of the reactor shell and is close to the feeding cavity.
The method for continuously synthesizing tetrahydrophthalic anhydride by using the device comprises the following steps of (1) melting or dissolving maleic anhydride in a solvent, reacting butadiene with a maleic anhydride solution in a first-stage tubular microemulsion reactor, and ensuring the conversion rate of the maleic anhydride due to excessive butadiene; (2) after the reaction is finished, the reaction product enters a flash evaporation kettle, excessive butadiene and solvent are removed, and the product tetrahydrophthalic anhydride enters the next working procedure; (3) the removed butadiene enters a second-stage absorption reactor in a gas phase state, and the butadiene is absorbed by a maleic anhydride solution through chemical reaction; (4) the mixed liquid of maleic anhydride after absorbing butadiene enters a maleic anhydride material tank; (5) the mixed liquid in the maleic anhydride material tank enters the first-stage tubular microemulsion reactor through the delivery pump to continue to react with butadiene.
The reaction temperature of the step (1) is 60-150 ℃, and the pressure is 0.1-1 MPa.
The pressure of the step (2) is 5-100 kpa;
the reaction temperature of the step (3) is 60-150 ℃.
The molar ratio of the butadiene to the maleic anhydride raw materials in the first-stage reactor is 1.5: 1, the molar ratio of the butadiene to the maleic anhydride raw materials of the whole system is 1: 1.
this neotype beneficial effect lies in:
the device can realize the continuous controllable synthesis of tetrahydrophthalic anhydride, and the tetrahydrophthalic anhydride is prepared by continuously adding maleic anhydride and 1, 3-butadiene diene in the combined device of the tubular micro-reactor and the jet mixer, so that the product quality is stable, the device has high automation degree, low production cost and high product quality, the equipment requirement is reduced, the equipment cost is reduced, and the technology is advanced.
The tubular microemulsion reactor disclosed by the utility model adopts the structure that the karman vortex street generating part is formed on the inner pipe, the tubular microemulsion reactor has the advantages that the material A flows through the space between the reaction pipe and the inner pipe along the length direction of the reaction pipe, after passing through the karman vortex street generating part, the material A periodically drops out of double-row line vortexes which are opposite in rotation direction and are regularly arranged to form the karman vortex street, the material B at the karman vortex street generating part is dispersed through the membrane pipe and then enters the space between the reaction pipe and the inner pipe as micro liquid drops or bubbles, so that the material A forms a vortex to be mutually fused with the material B with a micro volume, the contact interface of the material A and the material B is greatly improved, the fusion reaction of the two-phase materials is sufficient, and the reaction efficiency is improved; excessive butadiene in the first-stage reactor is removed through the jet mixer to obtain a qualified tetrahydrophthalic anhydride product, and meanwhile, the removed butadiene is further mixed and reacted in the jet mixer, so that the utilization rate of raw materials and the reaction conversion rate are improved. The utility model discloses a high-efficient microreactor of parallel, for the microreactor that connects in parallel based on foretell microreactor forms, its difference lies in replacing the outer tube of foretell microreactor for the reactor casing, and outside heat exchange mainly leans on the heat transfer medium of flowing through reactor casing inner chamber like this, can realize the heat transfer when each reaction tube is outside, adopts the structure of parallel, mixes under abundant prerequisite at two kinds of materials, improves mixed reaction efficiency, and then improves production efficiency.
Drawings
FIG. 1 is a schematic structural diagram of the present invention;
FIG. 2 is a partial sectional view of the structure of a pipe-type microemulsion reactor of example 1;
FIG. 3 is a partial sectional view of the structure of a pipe-type microemulsion reactor of example 2;
FIG. 4 is a schematic structural diagram of the novel parallel high-efficiency microreactor;
FIG. 5 is a structural side view of the novel parallel high-efficiency microreactor;
FIG. 6 is a partial structural sectional view of the novel parallel high-efficiency microreactor;
FIG. 7 is another partial sectional structural view of a parallel high-efficiency microreactor according to the present invention;
1-a reactor shell, 2-an inner cavity of the reactor shell, 3-an inner tube, 4-a karman vortex street generating part, 5-a first uniform distribution tube, 6-a heat exchange medium inlet tube, 7-a second uniform distribution tube, 8-a heat exchange medium outlet tube, 9-a reaction tube, 10-a first material tube, 11-a branch tube, 12-an inner cavity heat exchange tube, 13-a heat exchange tube joint, 14-a feeding cavity, 15-a second material tube, 16-a discharging cavity, 17-a discharging tube, 18-a mixing tube, 19-an outer tube and 20-a tubular microporous part;
21-maleic anhydride material tank, 22-jet mixer, 23-maleic anhydride circulating pump, 24-flash evaporation kettle, 25-tetrahydrophthalic anhydride delivery pump, 26-first-stage tubular microemulsion reactor, 27-maleic anhydride delivery pump, 28-butadiene delivery pump and 29-butadiene material tank.
Detailed Description
The technical solution of the present invention will be further explained by the following embodiments. It should be understood by those skilled in the art that the examples are only for the purpose of facilitating the understanding of the present invention and should not be construed as specifically limiting the present invention.
Example 1
Butadiene in a butadiene material tank 29 enters the first-stage tubular microemulsion reactor 26 through a butadiene conveying pump 28; maleic anhydride in the maleic anhydride material tank 1 enters the first-stage tubular microemulsion reactor 26 through the delivery pump 27, and butadiene and maleic anhydride react in the first-stage tubular microemulsion reactor 26; the reaction temperature is 60-150 ℃, and the pressure is 0.1-1 MPa;
after the reaction is finished, the reaction product enters a flash evaporation kettle 24, excessive butadiene and solvent are removed, the pressure is 5-100kpa, and the product tetrahydrophthalic anhydride enters a product storage tank; the removed butadiene enters a jet mixer 22 (a second-stage absorption reactor) in a gas phase state, and maleic anhydride enters the jet mixer 22 through a circulating pump 23 to react with butadiene to absorb butadiene, wherein the reaction temperature is 60-150 ℃; mixed liquid obtained after butadiene is absorbed by maleic anhydride enters a maleic anhydride material tank 21; the mixed liquid in the maleic anhydride material tank 21 enters the first-stage tubular microemulsion reactor 26 through the delivery pump 27 to continue to react with butadiene.
A butadiene absorption device can be arranged between the jet mixer and the maleic anhydride material tank, and maleic anhydride is used for absorbing butadiene which is not absorbed by the jet mixer.
The process flow conditions are as described above.
The first-stage tubular microemulsion reactor comprises an outer tube 19, a reaction tube 9 and an inner tube 3 which are sequentially sleeved from outside to inside as shown in figure 2, wherein the inner tube 3 is provided with Karman vortex street generating parts 4 which are arranged at intervals along the length direction of the inner tube, and a mixing tube 18 penetrates through the outer tube 19 and is communicated with the reaction tube 9; the position where the mixing pipe 18 is connected with the reaction pipe 9 is positioned between the two karman vortex street generating parts 4 and close to the previous karman vortex street generating part 4; the material maleic anhydride flows through the space between the reaction tube 9 and the inner tube 3, and the material butadiene enters the space between the reaction tube 9 and the inner tube 3 through the mixing tube 18 and is mixed and reacted with the maleic anhydride. This neotype theory of operation and advantage lie in: maleic anhydride flows through the space between the reaction tube 9 and the inner tube 3 along the length direction of the reaction tube 9, after the maleic anhydride passes through the Karman vortex street generating part 4, double-row vortex with opposite rotating directions and regular arrangement is periodically dropped to form a Karman vortex street, butadiene at the Karman vortex street generating part enters the space between the reaction tube 9 and the inner tube 3 through the mixing tube 18, so that the maleic anhydride forms a Karman vortex street state and is fused with the butadiene, the fusion reaction of two-phase materials is sufficient, and the reaction efficiency is improved.
As a preferred embodiment of the present invention, the karman vortex street generating part 4 is convex outward in the radial direction of the inner tube 3, preferably, the karman vortex street generating part 4 is in a circular spherical shell shape or an elliptical spherical shell shape, and the axial cross section of the karman vortex street generating part 4 is in a circular arc shape with the middle part higher than the two ends. In order to improve the mixing efficiency of the two materials, the present embodiment can adopt a multi-stage mixing mode, and the mixing pipes 18 can be multiple and are communicated with the inner cavity of the reaction pipe 9 at intervals.
Example 2
The process flow conditions and other structures were the same as in example 1.
This example discloses another pipe-type microemulsion reactor, as shown in fig. 3, the reaction tube 9 is a microporous membrane tube, tubular microporous portions 20 communicating with the inner space of the reaction tube 9 are formed at intervals along the length direction of the microporous membrane tube, each tubular microporous portion 20 is located between two karman vortex street generators 4, maleic anhydride flows between the reaction tube 9 and the inner tube 3, butadiene flows between the outer tube 19 and the reaction tube 9, and butadiene enters the inside of the reaction tube 9 through the tubular microporous portions 20 and is mixed with maleic anhydride forming karman vortex street phenomenon, the heat exchange medium a flows through the inside of the inner tube 3, and the heat exchange medium B flows through the outside of the outer tube 19. The advantages of this embodiment are: the tubular micro-holes 20 act as a dispersion, further enhancing mixing; butadiene enters in the form of small drops or small bubbles and is mixed with the vortex of maleic anhydride after passing through the Karman vortex street, so that the mixing reaction is more sufficient.
Example 3
The process flow conditions were the same as in example 1.
The first-stage tubular microemulsion reactor is a parallel high-efficiency microreactor, and comprises a plurality of inner tubes 3 and a plurality of reaction tubes 9 sleeved outside the inner tubes 3 respectively, as shown in fig. 4 to 7. The reaction tubes 9 are arranged in the reactor shell 1, the cooling medium flows through the inner tubes 3 and the reactor shell 1, the maleic anhydride material enters the space between each reaction tube 9 and the corresponding inner tube 3 through the branch tubes 11 on the first material tube 10, and the butadiene material enters the space between each reaction tube 9 and the corresponding inner tube 3 through the second material tube 15.
The working principle and the advantages of the embodiment are as follows: the embodiment is a microreactor formed by tubular microemulsion reactors based on embodiments 2 and 3, and the microreactor is characterized in that the outer tube 19 of the reactor is replaced by a reactor shell 1, so that external heat exchange mainly depends on a heat exchange medium flowing through the inner cavity 2 of the reactor shell, and the simultaneous heat exchange outside each reaction tube 9 can be realized.
As a preferred embodiment of the present invention, as shown in fig. 5, in order to facilitate uniform and sufficient supply of maleic anhydride to each reaction tube 9 and to facilitate collection of mixed reactant having sufficient mixed reaction, a feeding chamber 14 and a discharging chamber 16 are respectively formed at both ends of the reactor shell 1, both ends of each reaction tube 9 are respectively communicated with the feeding chamber 14 and the discharging chamber 16, both ends of each inner tube 3 respectively penetrate through the feeding chamber 14 and the discharging chamber 16, a second material tube 15 is communicated with the feeding chamber 14, and a discharging tube 17 is communicated with the discharging chamber 16.
As a preferred embodiment of the present invention, as shown in fig. 4 and 5, in order to facilitate the uniform and sufficient supply of the cooling medium to each of the inner tubes 3 and the recovery of the heat transfer medium flowing out from each of the inner tubes 3, the inlet end of each of the inner tubes 3 is communicated through a first distribution pipe 5, the first distribution pipe 5 is connected to a heat transfer medium inlet pipe 6, the outlet end of each of the inner tubes 3 is communicated through a second distribution pipe 7, and the second distribution pipe 7 is connected to a heat transfer medium outlet pipe 8. Wherein, heat transfer medium import pipe 6 and heat transfer medium outlet pipe 8 are the annular pipe, and then improve the equipartition ability.
As a preferred embodiment of the present invention, as shown in fig. 5, the heat exchange medium inside and outside the reaction tube 9 is the same medium and is improved by the same circulation system, specifically, the heat exchange medium inlet tube 6 is communicated with an inner cavity heat exchange tube 12 communicated with the inner cavity 2 of the reactor shell, the position where the inner cavity heat exchange tube 12 is communicated with the lower end of the reactor shell 1 is close to the discharging cavity 16, and the position where the upper end of the reactor shell 1 is close to the feeding cavity 14 is communicated with a heat exchange tube connector 13. Wherein, the heat exchange medium outlet pipe 8 and the heat exchange pipe joint 13 are both connected with a heat exchange medium return pipe of the heat exchange system.
Claims (7)
1. A device for continuously synthesizing tetrahydrophthalic anhydride is characterized in that: comprises a butadiene material tank, a first-stage tubular microemulsion reactor, a flash evaporation kettle, a jet mixer and a maleic anhydride material tank;
the butadiene material tank is connected with the inlet of the first-stage tubular microemulsion reactor through a butadiene delivery pump; the maleic anhydride material tank is connected with the inlet of the first-stage tubular microemulsion reactor through a maleic anhydride delivery pump; the outlet of the first-stage tubular microemulsion reactor is connected with the inlet of the flash evaporation kettle, and the outlet of the flash evaporation kettle is connected with the inlet of the jet mixer; the outlet of the jet mixer is connected with a maleic anhydride material tank, and the maleic anhydride material tank is connected with the inlet of the jet mixer through a maleic anhydride circulating pump.
2. The apparatus of claim 1, wherein: a butadiene absorption device is arranged between the jet mixer and the maleic anhydride material tank.
3. The apparatus of claim 1, wherein: the tubular microemulsion reactor comprises an outer tube, a reaction tube and an inner tube which are sequentially sleeved from outside to inside, wherein the inner tube is provided with Karman vortex street generating parts which are arranged at intervals along the length direction of the inner tube, a material A flows through the space between the reaction tube and the inner tube, a material B enters the space between the reaction tube and the inner tube through the reaction tube and is mixed with the material A, and the position where the material B enters is the position between the two Karman vortex street generating parts.
4. The apparatus of claim 3, wherein: a mixing pipe penetrates through the outer pipe and is communicated with the reaction pipe, the position of the mixing pipe, which is connected with the reaction pipe, is positioned between the two karman vortex street generating parts and is close to the front karman vortex street generating part, and the material B enters the space between the reaction pipe and the inner pipe through the mixing pipe.
5. The apparatus of claim 4, wherein: the mixing pipe is many, and the interval communicates in the reaction tube inner chamber.
6. The apparatus of claim 3, wherein: the reaction tube comprises a microporous membrane tube, tubular microporous parts communicated with the inner space of the reaction tube are formed on the microporous membrane tube at intervals along the length direction of the microporous membrane tube, and each tubular microporous part is positioned between two karman vortex street generating parts.
7. The apparatus of claim 3, wherein: each karman vortex street generating part is outwards protruded along the radial direction of the inner pipe, and the axial section of each karman vortex street generating part is in a circular arc shape with the middle part higher than the two ends.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120369233.4U CN214486839U (en) | 2021-02-10 | 2021-02-10 | Device for continuously synthesizing tetrahydrophthalic anhydride |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120369233.4U CN214486839U (en) | 2021-02-10 | 2021-02-10 | Device for continuously synthesizing tetrahydrophthalic anhydride |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN214486839U true CN214486839U (en) | 2021-10-26 |
Family
ID=78220079
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202120369233.4U Active CN214486839U (en) | 2021-02-10 | 2021-02-10 | Device for continuously synthesizing tetrahydrophthalic anhydride |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN214486839U (en) |
-
2021
- 2021-02-10 CN CN202120369233.4U patent/CN214486839U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2017036418A1 (en) | Smart industrial micro-channel flow reactor | |
| CN112341395B (en) | Micro-reaction system and method for continuously preparing 2-methyl-4-amino-5-aminomethyl pyrimidine by using same | |
| CN211847757U (en) | Tetrahydrophthalic anhydride synthesizer | |
| CN109608353B (en) | Continuous production process and device for m-aminoacetanilide | |
| CN103521158B (en) | The method of succinonitrile is prepared in a kind of serialization | |
| CN214486841U (en) | Microreactor and parallel high-efficiency microreactor | |
| CN201692802U (en) | Device for continuously producing hexafluoro propylene oxide | |
| CN214486839U (en) | Device for continuously synthesizing tetrahydrophthalic anhydride | |
| CN213528594U (en) | Device for continuously preparing peroxide and continuously applying peroxide to oxidation reaction | |
| CN114225858A (en) | Casing structure micro-reactor and application thereof | |
| CN101962352B (en) | Method for continuously producing p-menthane hydroperoxide by p-menthane and device thereof | |
| CN112694460B (en) | Method and device for continuously synthesizing tetrahydrophthalic anhydride | |
| CN104108683B (en) | A kind of stable chlorine dioxide reactor | |
| CN1321990C (en) | Apparatus and method for monotubular multi-spiral static mixed tube style chlorohydrination of propene for production of epoxypropane | |
| CN214716657U (en) | Device for continuously synthesizing tetrahydrophthalic anhydride | |
| CN215611516U (en) | Reaction system for continuously producing hydroxylamine hydrochloride | |
| CN214636343U (en) | Caprolactam preparation equipment | |
| CN104387258B (en) | A kind of production of chloroacetic acid method and chlorination reactor | |
| CN112239450B (en) | Method for synthesizing epsilon-caprolactone | |
| CN111892479B (en) | Method and device for improving primary conversion rate of methanol in chloromethane synthesis | |
| CN112973612B (en) | System device and method for continuously synthesizing methyl tetrahydrophthalic anhydride | |
| CN210314073U (en) | Device for preparing trioxymethylene by oxidizing methylal | |
| CN203002340U (en) | Large-size ethynylation reactor | |
| CN201793511U (en) | Continuous production device for preparing p-menthane hydroperoxide from p-menthane | |
| CN213376525U (en) | Oxidation reactor for continuous liquid phase oxidation of o-chlorotoluene |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |