CN214233980U - Continuous tubular oxidation reactor for p-nitrobenzoic acid - Google Patents
Continuous tubular oxidation reactor for p-nitrobenzoic acid Download PDFInfo
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Abstract
A continuous tubular oxidation reactor for p-nitrobenzoic acid comprises a feeding section, a mixing section, a low-temperature reaction section, a high-temperature reaction section and a cooling and cooling section. The material is conveyed in the tubular reactor by means of a pressure difference. The low-temperature reaction section and the high-temperature reaction section are respectively provided with a heating medium for heating, and a temperature detection point, a flow speed detection point and a sampling port are arranged at the same time; the cooling and temperature-reducing section is respectively provided with a temperature detection point, a pressure detection point, a flow velocity detection point and a sampling port for parameter regulation and control, so that the process risk degree of the intermittent reaction process can be reduced, the continuous production can be realized, and the productivity and the yield can be obviously improved.
Description
Technical Field
The utility model relates to a p-nitrobenzoic acid continuous tubular oxidation reactor, which belongs to the field of preparing nitrobenzoic acid by oxidizing nitrotoluene.
Background
The p-nitrobenzoic acid is an intermediate for organic synthesis of medicines, dyes, veterinary drugs, photosensitive materials and the like. The method is used for producing procaine hydrochloride, procainamide hydrochloride, p-aminomethyl benzoic acid, folic acid, benzocaine, cough, cephalosporin v, p-aminobenzoyl glutamic acid and benier, and producing active brilliant red M-8B, active red purple X-2R, a light filter, a color film coupler, a metal surface rust remover, a sun-screening agent and the like.
In industrial production, p-nitrotoluene is generally used as a raw material and is prepared through oxidation reaction. There are several reasonable approaches to the oxidation process: (1) sodium dichromate oxidation; (2) an air oxidation method; (3) nitric acid oxidation. The air oxidation method has a plurality of operation procedures, the probability of bringing impurities is high, and the purity reaching the pharmaceutical grade is difficult. The development prospect of the nitric acid oxidation method is larger than that of the air oxidation method. The existing p-nitrobenzoic acid production process is to use a high-pressure reaction kettle to carry out intermittent reaction, the nitration reaction condition is harsh, the pressure is rapidly increased, the temperature is high, parameters must be strictly controlled, the safety and environmental protection risks are high, and the core problem at present is how to consider efficiency and safety.
CN111606790A discloses a process for continuously producing benzaldehyde and benzoic acid by using a jet loop reactor, but the process requires rectification, purification and other processes, the operation of the whole system is complex, the cost is high, and the conversion per pass of toluene is 40% to 50%, which needs to be improved.
CN107686449A discloses a variable diameter tubular reaction apparatus, which is composed of 3 or more than 3 reaction repeating units, and has the advantages of continuous reaction, high volume ratio, small back mixing, high selectivity of target product, and strong versatility, and can be applied to various condensation reactions and polycondensation reactions, but the reactor is not suitable for the continuous oxidation reaction process of p-nitrobenzoic acid with strong oxidation reaction, and is not suitable for the nitric acid oxidation process with harsh reaction conditions.
In the process of producing p-nitrobenzoic acid by oxidizing p-nitrotoluene, a reaction kettle is used in an intermittent method, the temperature and the pressure can be rapidly increased in the reaction process, the reaction conditions are harsh, the safety and environmental protection risks are high, and the continuous tubular oxidation reactor has obvious advantages: firstly, the oxidation reaction condition is mild, the process risk is obviously reduced, and the method is safe and reliable; secondly, segmented temperature control can be realized, and the reaction can be stopped at any time; thirdly, the required reaction volume is small, the unit volume production capacity is provided, and continuous production can be realized; fourthly, the length-diameter ratio of the tubular reactor is large, the heat transfer area is large, the reaction is more sensitive to the temperature, and the energy consumption can be saved; fifthly, the reaction selectivity is high, and the yield and the output are obviously improved.
SUMMERY OF THE UTILITY MODEL
In order to solve the existing problem, the utility model discloses a p-nitrobenzoic acid serialization tubular oxidation reactor, including mixing section, low temperature reaction section, high temperature reaction section, cooling section.
The material is conveyed in the tubular reactor by means of a pressure difference. The low-temperature reaction section and the high-temperature reaction section are respectively provided with a heating medium for heating, and a temperature detection point, a flow speed detection point and a sampling port are arranged at the same time; the cooling and cooling section is respectively provided with a temperature detection point, a pressure detection point, a flow rate detection point and a sampling port.
Slowly adding the prepared nitric acid and p-nitrotoluene into a mixing section through a feed inlet of a tubular reactor for fully mixing, then feeding the materials into a low-temperature reaction section along with the pipeline materials, feeding the materials into a high-temperature reaction section from the low-temperature reaction section step by step along with the material stroke, increasing the pressure and the temperature at the moment, sampling and analyzing, and if the materials are unqualified, reducing the feeding speed; if the product is qualified, feeding is continued, the oxidation reaction is finished, the p-nitrobenzoic acid crude product is gradually cooled through a cooling and cooling section, and then is put into a receiving tank through a discharge hole, and then is filtered, separated and dried to obtain the product p-nitrobenzoic acid.
Specifically, a p-nitrobenzoic acid serialization tubular oxidation reactor, including consecutive feed segment, mixing section, low temperature reaction section, first high temperature reaction section, second high temperature reaction section and cooling section:
(1) the feeding section 1 comprises a feeding port A101 and a feeding port B102 and is connected with the mixing section 2
The reaction materials are fed through the feeding section 1, the raw materials of nitric acid and p-nitrotoluene are fed through the two feeding ports 101 and 102, and the nitric acid and the p-nitrotoluene are conveyed to the mixing section 2 by a pump according to the process proportion; heating the materials in the mixing section 2 to 60-80 ℃ by using jacket steam; preferably, the mixing section 2 is provided with a heating medium inlet a 202 and a heating medium outlet B201 to heat the mixing section 2;
(2) the mixed material enters a low-temperature reaction section 3 after being sampled and analyzed to be qualified
The low-temperature reaction section 3 comprises an inlet sampling port A301, a temperature measuring port A302, a pressure measuring port A303, a flow rate detection port A304, an outlet sampling port B301 ', a temperature measuring port B302', a pressure measuring port B303 'and a flow rate detection port B304';
the inlet of the low-temperature reaction section 3 is provided with a sampling port A301, a temperature measuring port A302, a pressure measuring port A303 and a flow rate detecting port A304, and the inlet temperature of the low-temperature section is controlled to be 60-80 ℃.
The outlet of the low-temperature reaction section 3 is provided with a sampling port B301 ', a temperature measuring port B302', a pressure measuring port B303 'and a flow rate detecting port B304'. Controlling the outlet temperature of the low-temperature section to be 80-100 ℃; sampling and analyzing, and if the content of the paranitrobenzoic acid is lower than 5 wt%, the flow rate of the paranitrotoluene is reduced by automatic interlocking. If the content of the nitrobenzoic acid is more than or equal to 5 wt%, the nitrobenzoic acid enters the first high-temperature reaction section 4 and the second high-temperature reaction section 5 to carry out oxidation reaction.
(3) The first high-temperature reaction section 4 comprises an inlet sampling port C401, a temperature measuring port C402, a pressure measuring port C403, a flow rate detection port C404, an outlet sampling port D401 ', a temperature measuring port D402', a pressure measuring port D403 'and a flow rate detection port D404';
the second high-temperature reaction section 5 comprises an inlet sampling port G501, a temperature measuring port G502, a pressure measuring port G503, a flow rate detection port G504, an outlet sampling port H501 ', a temperature measuring port H502', a pressure measuring port H503 'and a flow rate detection port H504';
through the sampling analysis of the outlet of the low-temperature reaction section, the qualified mixed materials further enter the first high-temperature reaction section 4 and the second high-temperature reaction section 5, and oxidation reaction is carried out under the conditions that the temperature is controlled to be 100-200 ℃ and the pressure is 0.4-0.5 KPa.
The inlet of the first high-temperature reaction section 4 is provided with a sampling port C401, a temperature measuring port C402, a pressure measuring port C403 and a flow rate detection port C404; the outlet of the first high-temperature reaction section 4 is provided with a sampling port D401 ', a temperature measuring port D402', a pressure measuring port D403 'and a flow rate detection port D404';
the inlet of the second high-temperature reaction section 5 is provided with a sampling port G501, a temperature measuring port G502, a pressure measuring port G503 and a flow rate detection port G504; the outlet is provided with a sampling port H501 ', a temperature measuring port H502', a pressure measuring port H503 'and a flow rate detecting port H504';
after the oxidation reaction of the high-temperature reaction section is finished, sampling and analyzing, if the content of the nitrobenzoic acid in the sample is lower than 99.2 percent, the sample is an unqualified product, the flow rate of the p-nitrotoluene in the feeding section is reduced through automatic interlocking, and the content of the p-nitrotoluene is increased. The produced unqualified materials are cooled by the cooling section 6, collected by the receiving tank and transferred to the next batch of reaction as reaction materials.
The inlet position of the first high-temperature reaction section 4 is provided with a heat medium outlet 405, and the outlet position of the second high-temperature reaction section 5 is provided with a heat medium inlet 505' for providing a heat source for the first and second high-temperature reaction sections.
According to the requirement, a plurality of high-temperature reaction sections (more than or equal to three high-temperature reaction sections) can be arranged.
(4) The cooling and temperature-reducing section 6 comprises a sampling port E601, a temperature measuring port E602, a pressure measuring port E603, a flow rate detecting port E604, a refrigerant outlet 605 and a refrigerant inlet 605';
after the oxidation reaction is finished, gradually cooling the crude p-nitrobenzoic acid by a cooling section 6, wherein a cooling medium inlet and a cooling medium outlet are arranged in the cooling section, and a sampling port F601 ', a temperature measuring port F602', a pressure measuring port F603 'and a flow rate detection port F604' are arranged at the outlet of the cooling section 6, so as to monitor the crude condition;
a cooling medium outlet 605 and a cooling medium inlet 605' are respectively arranged at the positions, close to the inlet and the outlet, of the cooling and cooling section 6, and provide cooling media for the cooling and cooling section;
(5) the crude product enters a receiving tank through a discharge hole 606, and a p-nitrobenzoic acid product is obtained after filtration, separation and drying. The analysis shows that the yield of the p-nitrobenzoic acid product is more than 99%.
The utility model discloses to nitrobenzoic acid serialization tubular oxidation reactor adopts serialization tubular reaction, adopts fixed point control, real-time detection, has eliminated traditional batch type reation kettle effectively and has reacted when, and the reaction is violent, and reaction temperature, pressure sharply rise, the great technical problem of safe risk. Meanwhile, the reaction conversion rate and yield are obviously improved, and the yield of the nitrobenzoic acid is improved to more than 99%.
Adopt the utility model has the advantages of:
1. the continuous tubular reactor is adopted, so that the problems of high pressure and high equipment pressure and poor safety in the intermittent reaction process due to high-temperature and high-pressure reaction conditions are solved; the continuous production can improve the utilization rate of raw materials of the system and the conversion rate of target products, and is suitable for industrial production.
2. The heating process of the continuous tubular oxidation reactor is divided into the sectional type heating temperature control of the low-temperature reaction section and the high-temperature reaction section, the temperature of the oxidation reaction process is effectively controlled, the phenomenon that the safety stability in the reactor is deteriorated due to overhigh temperature is avoided, the efficiency of the oxidation reaction can be improved due to accurate temperature control, and the energy consumption is saved.
3. Meanwhile, a plurality of detection points of temperature, flow velocity and pressure are arranged, the reaction processes at a plurality of positions in the reactor are monitored in real time, the accuracy of continuous reaction is improved, other side reactions are avoided, and the quality of oxidation reaction products is improved.
4. Through sampling analysis to parameters such as temperature, pressure to formulate suitable feedback mechanism, adjust the process of segmentation heating reaction through adjusting feed rate, maneuverability is strong, can improve the security of reactor, reduces the safety risk.
5. This neotype continuous type tubular reactor has the multistage pipeline, and the coiled design can reduce area, reduces the heat loss, reduce cost and cost.
Drawings
The accompanying drawings, which are included to provide a further understanding of the disclosure and are incorporated in and constitute a part of this specification, illustrate exemplary embodiments of the disclosure and together with the description serve to explain the principles of the disclosure.
FIG. 1 is a schematic diagram of a continuous tubular oxidation reactor of example 1.
FIG. 2 is a schematic view of a feed reaction zone.
Wherein 1-a feeding section, 101-a feeding port A, 102-a feeding port B, 2-a mixing section, 201-a heating medium outlet B, 202-a heating medium inlet A, 3-a low temperature reaction section, 301-a sampling port A, 302-a temperature measuring port A, 303-a pressure measuring port A, 304-a flow rate detecting port A, 301 '-a sampling port B, 302' -a temperature measuring port B, 303 '-a pressure measuring port B, 304' -a flow rate detecting port B, 4-a first high temperature reaction section, 401-a sampling port C, 402-a temperature measuring port C, 403-a pressure measuring port C, 404-a flow rate detecting port C, 405-a heating medium outlet, 401 '-a sampling port D, 402' -a temperature measuring port D, 403 '-a pressure measuring port D, 404' -a flow rate detecting port D, 5-a second high temperature reaction section, 501-sampling port G, 502-temperature measuring port G, 503-pressure measuring port G, 504-flow rate detecting port G, 501 '-sampling port H, 502' -temperature measuring port H, 503 '-pressure measuring port H, 504' -flow rate detecting port H, 505 '-heat medium inlet, 6-cooling and cooling section, 601-sampling port E, 602-temperature measuring port E, 603-pressure measuring port E, 604-flow rate detecting port E, 601' -sampling port F, 602 '-temperature measuring port F, 603' -pressure measuring port F, 604 '-flow rate detecting port F, 605-refrigerant outlet, 605' -refrigerant inlet and 606-discharge port.
Detailed Description
The present disclosure will be described in further detail with reference to the drawings and embodiments. It is to be understood that the specific embodiments described herein are for purposes of illustration only and are not to be construed as limitations of the present disclosure. It should be further noted that, for the convenience of description, only the portions relevant to the present disclosure are shown in the drawings.
Example 1
(1) Reacting raw materials, namely nitric acid and p-nitrotoluene, enter a feeding section 1 through a feeding hole A101 and a feeding hole B102 according to a process ratio, and are conveyed to a mixing section 2; the mixture is heated to 70 ℃ in the mixing section 2 by jacket steam;
(2) the mixed materials enter a low-temperature reaction section 3, a sampling port A301, a temperature measuring port A302, a pressure measuring port A303 and a flow rate detecting port A304 are arranged at the inlet of the low-temperature reaction section 3,
a sampling port B301 ', a temperature measuring port B302', a pressure measuring port B303 'and a flow rate detecting port B304' are arranged at the outlet of the low-temperature reaction section 3;
controlling the inlet temperature of the low-temperature section to be 80 ℃ and the outlet temperature to be 100 ℃; sampling and analyzing at an outlet, wherein the content of nitrobenzoic acid is 7.8 wt% (namely more than or equal to 5 wt%), and entering a first high-temperature reaction section 4;
(3) the qualified mixed material enters a first high-temperature reaction section 4, and a sampling port C401, a temperature measuring port C402, a pressure measuring port C403 and a flow rate detection port C404 are arranged at the inlet of the first high-temperature reaction section 4; controlling the temperature of the first high-temperature reaction section 4 to be 150 ℃ and the pressure to be 0.4KPa, and carrying out oxidation reaction on the mixed materials;
the reactant further enters a second high-temperature reaction section 5, the temperature of the second high-temperature reaction section 5 is controlled to be 150 ℃, and the pressure is controlled to be 0.4KPa, and further oxidation reaction is carried out;
a sampling port H501 ', a temperature measuring port H502', a pressure measuring port H503 'and a flow rate detecting port H504' are arranged at the outlet of the second high-temperature reaction section 5;
after the oxidation reaction is completely finished, sampling and analyzing the effluent of the second high-temperature reaction section 5 to obtain the product with the nitrobenzoic acid content of 99.6 percent, which meets the requirement;
(4) the material enters a cooling and temperature-reducing section 6 to be gradually cooled, and a sampling port F601 ', a temperature measuring port F602', a pressure measuring port F603 'and a flow rate detecting port F604' are arranged at an outlet of the cooling and temperature-reducing section to monitor the condition of a crude product;
a cooling medium outlet 605 and a cooling medium inlet 605' are respectively arranged at the positions, close to the inlet and the outlet, of the cooling and cooling section 6, and provide cooling media for the cooling and cooling section;
(5) the crude product enters a receiving tank through a discharge hole 606, and a p-nitrobenzoic acid product is obtained through filtration, separation and drying; the yield of p-nitrobenzoic acid product was analyzed to be 99.3%.
Example 2
(1) Conveying the reaction raw materials of nitric acid and p-nitrotoluene into a feeding section 1 through a feeding hole A101 and a feeding hole B102 by using a pump according to a process ratio, and conveying the reaction raw materials to a mixing section 2; the mixed materials are heated to 60 ℃ in the mixing section 2 through jacket steam;
(2) the mixed materials enter a low-temperature reaction section 3, a sampling port A301, a temperature measuring port A302, a pressure measuring port A303 and a flow rate detecting port A304 are arranged at the inlet of the low-temperature reaction section 3,
a sampling port B301 ', a temperature measuring port B302', a pressure measuring port B303 'and a flow rate detecting port B304' are arranged at the outlet of the low-temperature reaction section 3;
controlling the inlet temperature of the low-temperature reaction section 3 to be 80 ℃ and the outlet temperature to be 100 ℃; sampling and analyzing at an outlet, wherein the content of nitrobenzoic acid is 6.2 wt% (namely more than or equal to 5 wt%), and entering a first high-temperature reaction section 4;
(3) the qualified mixed material enters a first high-temperature reaction section 4, and a sampling port C401, a temperature measuring port C402, a pressure measuring port C403 and a flow rate detection port C404 are arranged at the inlet of the first high-temperature reaction section 4; controlling the temperature of the first high-temperature reaction section 4 to be 140 ℃ and the pressure to be 0.5KPa, and carrying out oxidation reaction on the mixed materials;
the reactant further enters a second high-temperature reaction section 5, and the temperature of the second high-temperature reaction section 5 is controlled to be 140 ℃ and the pressure is controlled to be 0.5KPa for further oxidation reaction;
a sampling port H501 ', a temperature measuring port H502', a pressure measuring port H503 'and a flow rate detecting port H504' are arranged at the outlet of the second high-temperature reaction section 5;
after the oxidation reaction is completely finished, sampling and analyzing the effluent from the second high-temperature reaction section 5 to obtain a product with the nitrobenzoic acid content of 98.1 percent, which is not in line with the requirement; the flow rate of the p-nitrotoluene at the feeding section is reduced by automatic interlocking, and the content of the p-nitrotoluene is increased;
the produced unqualified materials are cooled by a cooling section 5, and then collected by a receiving tank to be used as reaction materials to be transferred to the next batch of reaction;
secondary sampling analysis: when the content of nitrobenzoic acid is sampled and analyzed to be 99.3 percent at the outlet of the second high-temperature reaction section 5, the requirement is met;
(4) the qualified materials enter a cooling section 6 for gradual cooling, the cooling section is provided with a cooling medium inlet and a cooling medium outlet, and the outlet of the cooling section is provided with a sampling port F601 ', a temperature measuring port F602', a pressure measuring port F603 'and a flow rate detection port F604', so that the condition of crude products is monitored;
a cooling medium outlet 605 and a cooling medium inlet 605' are respectively arranged at the positions, close to the inlet and the outlet, of the cooling and cooling section 6, and provide cooling media for the cooling and cooling section;
(5) the crude product enters a receiving tank through a discharge hole 606, and a p-nitrobenzoic acid product is obtained through filtration, separation and drying; the yield of p-nitrobenzoic acid product was analyzed to be 99.1%.
It should be noted that the embodiments and features of the embodiments in the present disclosure may be combined with each other without conflict. The present disclosure will be described in detail below with reference to the accompanying drawings in conjunction with embodiments.
In the description herein, reference to the description of the terms "one embodiment/mode," "some embodiments/modes," "example," "specific example," or "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment/mode or example is included in at least one embodiment/mode or example of the application. In this specification, the schematic representations of the terms used above are not necessarily intended to be the same embodiment/mode or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments/modes or examples. Furthermore, the various embodiments/aspects or examples and features of the various embodiments/aspects or examples described in this specification can be combined and combined by one skilled in the art without conflicting therewith.
It will be understood by those skilled in the art that the foregoing embodiments are merely for clarity of illustration of the disclosure and are not intended to limit the scope of the disclosure. Other variations or modifications may occur to those skilled in the art, based on the foregoing disclosure, and are still within the scope of the present disclosure.
Claims (7)
1. The continuous tubular oxidation reactor for the p-nitrobenzoic acid is characterized by comprising a feeding section (1), a mixing section (2), a low-temperature reaction section (3), a first high-temperature reaction section (4), a second high-temperature reaction section (5) and a cooling and cooling section (6) which are sequentially connected:
1) the feeding section (1) comprises a feeding port A (101) and a feeding port B (102) and is connected with the mixing section (2);
the reaction materials are fed through a feeding section (1), the raw materials of nitric acid and p-nitrotoluene are fed through feeding ports A (101) and B (102), and the nitric acid and the p-nitrotoluene are mixed and enter a mixing section (2);
2) the mixing section (2) is connected with the low-temperature reaction section (3), and the low-temperature reaction section (3) comprises an inlet sampling port A (301), a temperature measuring port A (302), a pressure measuring port A (303), a flow rate detection port A (304), an outlet sampling port B (301 '), a temperature measuring port B (302'), a pressure measuring port B (303 ') and a flow rate detection port B (304');
the mixed materials enter a low-temperature reaction section (3) for low-temperature thermal reaction;
3) the low-temperature reaction section (3) is sequentially connected with the first high-temperature reaction section (4) and the second high-temperature reaction section (5), and the first high-temperature reaction section (4) comprises an inlet sampling port C (401), a temperature measuring port C (402), a pressure measuring port C (403), a flow rate detection port C (404), an outlet sampling port D (401 '), a temperature measuring port D (402'), a pressure measuring port D (403 '), and a flow rate detection port D (404');
the second high-temperature reaction section (5) comprises an inlet sampling port G (501), a temperature measuring port G (502), a pressure measuring port G (503), a flow rate detection port G (504), an outlet sampling port H (501 '), a temperature measuring port H (502'), a pressure measuring port H (503 ') and a flow rate detection port H (504');
qualified products at the outlet of the low-temperature reaction section (3) enter a first high-temperature reaction section (4) and a second high-temperature reaction section (5) for oxidation reaction;
4) the cooling and temperature-reducing section (6) comprises a sampling port E (601), a temperature measuring port E (602), a pressure measuring port E (603), a flow rate detecting port E (604), an outlet sampling port F (601 '), a temperature measuring port F (602'), a pressure measuring port F (603 '), and a flow rate detecting port F (604');
5) a discharge hole (606) of the cooling and cooling section (6) is connected with a receiving tank, and a target product is collected.
2. The continuous tubular oxidation reactor for p-nitrobenzoic acid according to claim 1, characterized in that the material is heated to 60 to 80 ℃ in the mixing section (2) by means of jacketed steam.
3. The continuous tubular oxidation reactor for p-nitrobenzoic acid according to claim 1, wherein the inlet temperature of the low temperature reaction section (3) is 60-80 ℃ and the outlet temperature of the low temperature reaction section (3) is 80-100 ℃.
4. The continuous tubular oxidation reactor for p-nitrobenzoic acid according to claim 1, wherein the inlet of the first high temperature reaction section (4) is provided with a heat medium outlet (405), and the outlet of the second high temperature reaction section (5) is provided with a heat medium inlet (505') to provide a heat source for the first and second high temperature reaction sections.
5. The continuous tubular oxidation reactor for p-nitrobenzoic acid according to claim 1, wherein the cooling and cooling section (6) is provided with a coolant outlet (605) and a coolant inlet (605') near the inlet and the outlet, respectively.
6. The continuous tubular oxidation reactor for p-nitrobenzoic acid according to claim 1, wherein the oxidation conditions in the first high temperature reaction section (4) and the second high temperature reaction section (5) are as follows: the temperature is 100-200 ℃, and the pressure is 0.4-0.5 KPa.
7. The continuous tubular oxidation reactor for p-nitrobenzoic acid according to claim 1 wherein the mixing section (2) is provided with a heating medium inlet a (202) and a heating medium outlet B (201) to heat the mixing section.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114225884A (en) * | 2021-12-29 | 2022-03-25 | 江苏吉华化工有限公司 | Continuous nitration reaction device |
| CN115041119A (en) * | 2022-06-08 | 2022-09-13 | 青海施丹弗化工有限责任公司 | Thiophene continuous nitration reaction device |
| CN115738985A (en) * | 2022-10-27 | 2023-03-07 | 黄山邦森新材料有限公司 | Tubular reaction system for producing ultra-low molecular weight povidone |
-
2020
- 2020-11-25 CN CN202022759658.4U patent/CN214233980U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114225884A (en) * | 2021-12-29 | 2022-03-25 | 江苏吉华化工有限公司 | Continuous nitration reaction device |
| CN115041119A (en) * | 2022-06-08 | 2022-09-13 | 青海施丹弗化工有限责任公司 | Thiophene continuous nitration reaction device |
| CN115738985A (en) * | 2022-10-27 | 2023-03-07 | 黄山邦森新材料有限公司 | Tubular reaction system for producing ultra-low molecular weight povidone |
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