CN213376525U - Oxidation reactor for continuous liquid phase oxidation of o-chlorotoluene - Google Patents
Oxidation reactor for continuous liquid phase oxidation of o-chlorotoluene Download PDFInfo
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- CN213376525U CN213376525U CN202021753952.8U CN202021753952U CN213376525U CN 213376525 U CN213376525 U CN 213376525U CN 202021753952 U CN202021753952 U CN 202021753952U CN 213376525 U CN213376525 U CN 213376525U
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- static mixer
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- oxidation
- chlorotoluene
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The utility model provides an oxidation reactor for continuous liquid phase oxidation of o-chlorotoluene, which comprises a static mixer, an external circulation pipe and a heat exchanger; the lower part of the cylindrical tower body is sequentially provided with a second feed inlet, a first feed inlet and an air inlet from bottom to top, the air inlet horizontally extends outwards along the tangential direction of the outer diameter of the cylindrical tower body, the static mixer is fixedly arranged in the cylindrical tower body, the outer circulating pipe is fixedly arranged on the outer side of the cylindrical tower body, the inlet at the upper end is positioned above the static mixer, the outlet at the lower end is positioned between the static mixer and the air inlet, and the heat exchanger is communicated with the outer circulating pipe; the air inlet is horizontally extended outwards along the tangential direction of the outer diameter of the cylindrical tower body, so that the entering gas forms cyclone, the high-efficiency gas-liquid mass transfer capacity and material mixing capacity can be realized, the total reaction rate is improved, the generation of byproducts is reduced, particularly the content of o-chlorobenzoic acid is improved, the content of dechlorinated substances is reduced, and the production added value is improved.
Description
Technical Field
The utility model relates to an oxidation reactor technical field especially relates to an oxidation reactor for continuous liquid phase oxidation of o chloro toluene.
Background
At present, o-chlorobenzoic acid is prepared by a batch oxidation reaction by using o-chlorotoluene as a raw material and adopting a full mixed flow reactor or a bubble column reactor. In the oxidation process, the process has the problems of low conversion rate, high oxygen content in tail gas, low yield and the like.
In an o-chlorotoluene liquid-phase air oxidation reaction device, the overall reaction rate or the content of byproducts can be increased due to the objective reason of uneven concentration of air, catalysts or intermediate reaction products caused by insufficient gas-liquid mass transfer or uneven mixing, and particularly, chlorinated aromatic hydrocarbon dechlorination can occur, so that the added value of products is reduced.
In addition, problems are also encountered with carrying out the reaction using existing bubble column reactors: the gas is dispersed into smaller bubbles after passing through the gas distributor, but the gas bubbles are re-aggregated into large bubbles during the rising process, which is disadvantageous for the mass transfer of the gas-liquid phase. The accumulation of the bubbles which are not beneficial to mass transfer can cause the overall reaction rate to be reduced, and more seriously, the oxygen content in the tail gas at the outlet of the oxidation reaction device is too high, so that explosive mixtures are easily formed with toluene, and serious potential safety hazards exist.
SUMMERY OF THE UTILITY MODEL
In view of this, the utility model provides an oxidation reactor for continuous liquid phase oxidation of o chloro toluene that gas-liquid mass transfer is abundant and the misce bene, and overall reaction rate is high, and oxygen content is lower in the tail gas, and the security is good.
The technical scheme of the utility model is realized like this: the utility model provides an oxidation reactor for continuous liquid phase oxidation of o-chlorotoluene, which comprises a reaction tower, wherein the reaction tower comprises a cylinder type tower body, a tower top head and a tower bottom head, the tower top head and the tower bottom head are respectively and fixedly connected with the top and the bottom of the cylinder type tower body, the top of the tower top head is provided with a gas phase outlet and a pressure relief port, the bottom of the tower bottom head is provided with a liquid phase outlet, and the oxidation reactor also comprises a static mixer, an external circulation pipe and a heat exchanger; the lower part of the cylinder type tower body is sequentially provided with a second feed port, a first feed port and an air inlet from bottom to top, the air inlet horizontally extends outwards along the tangential direction of the outer diameter of the cylinder type tower body, a catalyst is input into the second feed port, ortho-chlorotoluene is input into the first feed port, and inert gas or air is input into the air inlet; the static mixer is fixedly arranged in the cylindrical tower body and is positioned above the air inlet; the outer circulating pipe is fixedly arranged on the outer side of the cylindrical tower body, two ends of the outer circulating pipe are respectively provided with an upper end inlet and a lower end outlet and are respectively communicated into the cylindrical tower body, the upper end inlet is positioned above the static mixer, and the lower end outlet is positioned between the static mixer and the air inlet; the heat exchanger is communicated with the external circulation pipe.
On the basis of the technical scheme, preferably, two groups of external circulating pipes and two groups of heat exchangers are symmetrically arranged on two sides of the cylindrical tower body.
On the basis of the above technical solution, preferably, the static mixer is provided with one to three layers, and the ratio of the height of the single-layer static mixer to the height of the drum tower body is 0.2 to 0.4.
On the basis of the technical scheme, preferably, the air inlets are provided with three to four air inlets and are circumferentially arranged on the outer wall of the cylindrical tower body.
On the basis of the technical scheme, the device preferably further comprises a control valve, and the upper end inlet and the lower end outlet are both provided with the control valve.
On the basis of the technical scheme, preferably, the shell side of the heat exchanger is symmetrically provided with a heat medium inlet and outlet.
On the basis of the technical scheme, preferably, the heat exchanger is a tube type heat exchanger, and the heat exchange area of the heat exchanger is 5-300 m2。
On the basis of the above technical scheme, preferably, the inert gas is nitrogen or helium.
The utility model discloses an oxidation reactor for continuous liquid phase oxidation of o chloro toluene has following beneficial effect for prior art:
(1) the air inlet is horizontally extended outwards along the tangential direction of the outer diameter of the cylindrical tower body, so that the entering gas forms cyclone, the high-efficiency gas-liquid mass transfer capacity and material mixing capacity can be realized, the total reaction rate is improved, the generation of byproducts is reduced, particularly the content of o-chlorobenzoic acid is improved, the content of dechlorinated substances is reduced, and the production added value is improved.
(2) Set up static mixer, its mixing action has strengthened the reaction, can guarantee that the oxygen in the air is reacted completely for oxygen content is in safety range in the tail gas, and the security of guarantee production is convenient for carry out modular installation according to the customization of material nature simultaneously, and it is convenient to maintain the change.
(3) Set up the extrinsic cycle pipe, the heat exchange medium can adopt high-temperature steam to heat up the system as the heat source when oxidation reaction begins, and the heat exchange medium can adopt soft water to produce steam when shifting out the reaction heat as the cold source during normal production, and the high-efficient reaction heat that utilizes reduces the energy consumption, external heat transfer device in addition, simple structure easily clears up the scale deposit, need not park and can overhaul, improves production efficiency.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
FIG. 1 is a front cross-sectional view of an oxidation reactor of the present invention;
fig. 2 is a sectional view of the drum tower of the present invention.
In the figure: 1. a reaction tower; 11. a drum tower; 12. sealing a head at the top of the tower; 13. sealing a head at the bottom of the tower; 14. a gas phase outlet; 15. a liquid phase outlet; 16. a pressure relief port; 17. a first feed port; 18. a second feed port; 19. an air inlet; 2. a static mixer; 3. an external circulation pipe; 31. an upper end inlet; 32. a lower end outlet; 4. a heat exchanger; 41. a heat medium inlet and outlet; 5. and (4) controlling the valve.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely below with reference to the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work all belong to the protection scope of the present invention.
As shown in figure 1, combine figure 2, the utility model discloses an oxidation reactor for continuous liquid phase oxidation of adjacent chlorotoluene, including reaction tower 1, reaction tower 1 includes cylinder tower body 11, top of the tower head 12 and tower bottom head 13, and top of the tower head 12 and tower bottom head 13 are fixed connection respectively in cylinder tower body 11 top and bottom, and gas phase outlet 14 and pressure release mouth 16 have been seted up at top of the tower head 12 top, and liquid phase outlet 15 has been seted up to tower bottom head 13 bottom, still includes static mixer 2, extrinsic cycle pipe 3, heat exchanger 4 and control valve 5.
Wherein, the lower part of the cylinder tower body 11 is provided with a second feed inlet 18, a first feed inlet 17 and an air inlet 19 in turn from bottom to top, the air inlet 19 horizontally extends outwards along the tangential direction of the outer diameter of the cylinder tower body 11, a catalyst is input into the second feed inlet 18, an o-chlorotoluene is input into the first feed inlet 17, and an inert gas or air is input into the air inlet 19. Among them, preferably, the inert gas is nitrogen or helium. In practical applications, the ratio of the diameter to the height of the tubular tower 11 is preferably 0.15 to 0.65.
The static mixer 2 is fixedly arranged in the cylindrical tower body 11, and the static mixer 2 is positioned above the air inlet 19 and used for uniformly mixing the gas phase and the liquid phase. Wherein, preferably, the static mixer 2 is provided with one to three layers, and the ratio of the height of the single-layer static mixer 2 to the height of the drum tower 11 is 0.2 to 0.4.
The external circulation pipe 3 is fixedly arranged outside the cylindrical tower body 11, two ends of the external circulation pipe 3 are respectively provided with an upper end inlet 31 and a lower end outlet 32 which are respectively communicated to the inside of the cylindrical tower body 11, the upper end inlet 31 is positioned above the static mixer 2, and the lower end outlet 32 is positioned between the static mixer 2 and the air inlet 19 and is used for flowing circulation of the heat medium.
The heat exchanger 4 is communicated with the external circulation pipe 3 and is used for heat medium exchange. Further, a heat medium inlet 41 and a heat medium outlet 41 are symmetrically formed on the shell side of the heat exchanger 4. Wherein, preferably, the heat exchanger 4 is a shell and tube heat exchanger, and the heat exchange area of the heat exchanger 4 is 5-300 m2。
The upper inlet 31 and the lower outlet 32 are provided with control valves 5 for controlling the inlet and outlet of the heat medium.
Furthermore, two groups of external circulation pipes 3 and heat exchangers 4 are symmetrically arranged at two sides of the cylindrical tower body 11, so that the heat circulation efficiency and the uniformity can be improved.
Furthermore, the air inlets 19 are provided with three to four air inlets which are circumferentially arranged on the outer wall of the cylindrical tower body 11, so that cyclone is formed, and the gas-liquid mass transfer capacity and the material mixing capacity are improved.
The working principle is as follows:
first, o-chlorotoluene and a catalyst are fed from the first inlet 17 and the second inlet 18, respectively, and simultaneously, a certain air volume of inert gas is blown from the inlet 19. Wherein. The inert gas may be nitrogen or helium.
Then, low-pressure high-temperature steam is introduced from a heat medium inlet 41 of the heat exchanger 4 as a heat source, enters the drum tower body 11 through a lower end outlet 32 of the external circulation pipe 3 to heat the reaction, and returns to the heat exchanger 4 from an upper end inlet 31 to circulate.
Thirdly, when the temperature of the o-chlorotoluene in the cylindrical tower body 11 rises to be 40-50 ℃ different from the reaction temperature, the inert gas is stopped to be introduced into the air inlet 19, and air is introduced into the reaction tower 1, so that the oxidation reaction starts to occur. At the same time, the supply of steam to the heat exchanger 4 is stopped and soft water is introduced as cooling medium.
Finally, when the oxidation reaction is completed, the o-chlorobenzoic acid product is obtained from the liquid phase outlet 15.
The above description is only a preferred embodiment of the present invention, and should not be taken as limiting the invention, and any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (8)
1. The utility model provides an oxidation reactor for continuous liquid phase oxidation of o-chlorotoluene, includes reaction tower (1), reaction tower (1) includes cylinder tower body (11), top of the tower head (12) and tower bottom head (13) fixed connection respectively in cylinder tower body (11) top and bottom, gas phase outlet (14) and pressure release mouth (16) have been seted up at top of the tower head (12) top, liquid phase outlet (15) have been seted up to tower bottom head (13) bottom, its characterized in that: the device also comprises a static mixer (2), an external circulation pipe (3) and a heat exchanger (4);
a second feed port (18), a first feed port (17) and an air inlet (19) are sequentially formed in the lower portion of the cylindrical tower body (11) from bottom to top, the air inlet (19) horizontally extends outwards along the tangential direction of the outer diameter of the cylindrical tower body (11), a catalyst is input into the second feed port (18), ortho-chlorotoluene is input into the first feed port (17), and inert gas or air is input into the air inlet (19);
the static mixer (2) is fixedly arranged in the cylindrical tower body (11), and the static mixer (2) is positioned above the air inlet (19);
the outer circulating pipe (3) is fixedly arranged on the outer side of the cylindrical tower body (11), two ends of the outer circulating pipe (3) are respectively provided with an upper end inlet (31) and a lower end outlet (32) and are respectively communicated into the cylindrical tower body (11), the upper end inlet (31) is positioned above the static mixer (2), and the lower end outlet (32) is positioned between the static mixer (2) and the air inlet (19);
the heat exchanger (4) is communicated with the external circulation pipe (3).
2. An oxidation reactor for the continuous liquid phase oxidation of o-chlorotoluene according to claim 1, characterized in that: two groups of external circulation pipes (3) and heat exchangers (4) are symmetrically arranged at two sides of the cylindrical tower body (11).
3. An oxidation reactor for the continuous liquid phase oxidation of o-chlorotoluene according to claim 1, characterized in that: the static mixer (2) is provided with one to three layers, and the ratio of the height of the static mixer (2) to the height of the cylindrical tower body (11) is 0.2 to 0.4.
4. An oxidation reactor for the continuous liquid phase oxidation of o-chlorotoluene according to claim 1, characterized in that: three to four air inlets (19) are arranged and circumferentially arranged on the outer wall of the cylindrical tower body (11).
5. An oxidation reactor for the continuous liquid phase oxidation of o-chlorotoluene according to claim 1, characterized in that: the device is characterized by further comprising a control valve (5), wherein the control valve (5) is arranged on the upper end inlet (31) and the lower end outlet (32).
6. An oxidation reactor for the continuous liquid phase oxidation of o-chlorotoluene according to claim 1, characterized in that: and a heat medium inlet and outlet (41) is symmetrically formed in the shell side of the heat exchanger (4).
7. An oxidation reactor for the continuous liquid phase oxidation of o-chlorotoluene according to claim 1, characterized in that: the heat exchanger (4) is a tube type heat exchanger, and the heat exchange area of the heat exchanger (4) is 5-300 m2。
8. An oxidation reactor for the continuous liquid phase oxidation of o-chlorotoluene according to claim 1, characterized in that: the inert gas is nitrogen or helium.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021753952.8U CN213376525U (en) | 2020-08-20 | 2020-08-20 | Oxidation reactor for continuous liquid phase oxidation of o-chlorotoluene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021753952.8U CN213376525U (en) | 2020-08-20 | 2020-08-20 | Oxidation reactor for continuous liquid phase oxidation of o-chlorotoluene |
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| Publication Number | Publication Date |
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| CN213376525U true CN213376525U (en) | 2021-06-08 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202021753952.8U Active CN213376525U (en) | 2020-08-20 | 2020-08-20 | Oxidation reactor for continuous liquid phase oxidation of o-chlorotoluene |
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| CN (1) | CN213376525U (en) |
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