CN102861542A - Methylbenzene oxidation tower in 10000-tone level benzoic acid production - Google Patents
Methylbenzene oxidation tower in 10000-tone level benzoic acid production Download PDFInfo
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- CN102861542A CN102861542A CN2012103696985A CN201210369698A CN102861542A CN 102861542 A CN102861542 A CN 102861542A CN 2012103696985 A CN2012103696985 A CN 2012103696985A CN 201210369698 A CN201210369698 A CN 201210369698A CN 102861542 A CN102861542 A CN 102861542A
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Abstract
The invention relates to a methylbenzene oxidation tower in 10000-tone level benzoic acid production. The oxidation tower has a height of between 8 and 10m, and a diameter of between 4 and 5m, wherein an air inlet, a methylbenzene inlet, a vapor inlet, a vapor outlet, an oxidation liquid outlet and an oxidation cooling liquid incoming oxidation tower port are arranged on the oxidation tower body; the distance from the air inlet to the bottom of the tower is between 6 and 8m, the distance from the vapor inlet to the bottom of the tower is between 4 and 6m, the distance from the vapor outlet to the tower bottom is between 3.5 and 5.5m, the distance from the oxidation liquid inlet to the bottom of the tower is between 0.3 and 0.5m, and the distance from the oxidation cooling liquid incoming oxidation tower port is between 5 and 7m; and the methylbenzene inlet is formed on the tower top. After the independently researched and developed oxidation tower is adopted, the methylbenzene oxidation reaction is an exothermic reaction, the heat exchange operation process is performed outside the tower, so that the construction investment of a methylbenzene oxidation workshop in benzoic acid production can be saved by 50 percent, and a previously adopted water-circulating pump of 55kw/h is replaced by a water-circulating pump of 22kw/h by virtue of a technology of circulating cooling outside the tower, and electric energy is saved by 40 percent by the methylbenzene oxidation tower. The methylbenzene oxidation tower is convenient to maintain and operate.
Description
Technical field
The present invention relates to the benzoic acid product production system, a kind of Novel oxidation column that particularly proposes in the toluene oxidation process is the toluene oxidation tower during the above benzoic acid that uses of ton is produced in the actual industrial production.
Background technology
In the production process of original annual output 30000～50,000 tons of technical benzene formic acid products, the needed oxidizing tower equipment of toluene oxidation is high 18.5 meters, 1.5 meters of diameters (Fig. 4).The original toluene oxidation production process of benzoic acid product as shown in Figure 3.Toluene is squeezed in the tower, passed into air after the whole toluene in the tower being heated afterwards, toluene carries out oxidation, because the toluene oxidation reaction is exothermic reaction, needs to carry out heat exchange operation in tower.React the thick matter benzoic acid of rear generation that finishes; Behind distillation, distillation process, become the benzoic acid product.In tower, carry out heat exchange operation when using original oxidizing tower and toluene to carry out oxidation; The problem that exists is: at first because the height of equipment is larger, so the Equipment Foundations construction investment is large, and production operation inconvenience, and has the potential safety hazard of production operation, such as falling from high altitude; Secondly owing to carry out heat exchange operation in tower, when leaking appearred in heat-exchanger rig, the solidifying water in the heat-exchanger rig was mixed in just in the toluene liquid of oxidation, can not in time find under the state of high temperature and proceeded production operation serious accident will occur; And have and be not easy to the in time disadvantage of maintenance.
Summary of the invention
The objective of the invention is to practice in the toluene oxidation process of the large chemical company in east in the benzoic acid process of producing product Novel oxidation column and the production method of independent research; Realize production equipment miniaturization, simple and clearization of production procedure and greatly improve the security performance of production operation.
Technical scheme of the present invention is as follows:
Toluene oxidation tower during a kind of ton benzoic acid of the present invention is produced, 8～10 meters of oxidation tower heights, 4～5 meters of diameters; Be provided with air intlet 1, toluene import 2, steam inlet 3, steam (vapor) outlet 4, oxidation solution outlet 5 at the oxidation tower body, the oxidation cooling fluid is advanced oxidizing tower mouth 11; Air intlet 6-8 rice at the bottom of the tower, steam inlet 4-6 rice at the bottom of the tower, steam (vapor) outlet 4 3.5-5.5 rice at the bottom of the tower, oxidation solution outlet 0.3-0.5 rice at the bottom of the tower, oxidation cooling fluid advance oxidizing tower mouth 11 5-7 rice at the bottom of the tower, and toluene import 2 is arranged on cat head.
Adopt Novel oxidation column, the toluene pump by oxidizing tower toluene import 2, is squeezed into toluene liquid to pass into steam behind the oxidizing tower toluene liquid is carried out heat temperature raising.Continue to be warming up to 155 ℃-165 ℃ when when the toluene liquid temp reaches 115 ℃-130 ℃, beginning blowing air, then the steam off valve.Toluene liquid carries out exothermic oxidation reaction in oxidizing tower.Through after the oxidation in 6-7 hour, open oxidizing tower oxidation cooling liquid inlet 11, open oxidation solution cooling device outlet 10, open oxidation solution cooling device import 9, open oxidizing tower oxidation solution outlet 5; Start the oxidation solution circulating pump oxidation solution is carried out tower outer circulation cooling.
Heat exchanger has passed into cooling medium, no longer is described in detail herein.
Description of drawings
Fig. 1: oxidizing tower schematic diagram of the present invention;
Fig. 2: production technological process of the present invention;
Fig. 3: original production process flow chart;
Fig. 4: former oxidation unit figure;
1, air intlet 2, toluene import 3, steam inlet 4, steam (vapor) outlet 5, oxidation solution outlet 6, cooling water inlet 7, coolant outlet 8, cooling device 9, oxidation solution advance that cooling device mouth 10, oxidation solution go out cooling device mouth 11, the oxidation cooling fluid is advanced the oxidizing tower mouth.
The specific embodiment
Below in conjunction with accompanying drawing the present invention is elaborated:
Adopt equipment as shown in Figure 2,8～10 meters of oxidation tower heights, 4～5 meters of diameters; Be provided with air intlet 1, toluene import 2, steam inlet 3, steam (vapor) outlet 4, oxidation solution outlet 5 at the oxidation tower body, the oxidation cooling fluid is advanced oxidizing tower mouth 11; Air intlet 6-8 rice at the bottom of the tower, steam inlet 4-6 rice at the bottom of the tower, steam (vapor) outlet 4 3.5-5.5 rice at the bottom of the tower, oxidation solution outlet 0.3-0.5 rice at the bottom of the tower, oxidation cooling fluid advance oxidizing tower mouth 11 5-7 rice at the bottom of the tower, and toluene import 2 is arranged on cat head.
Main connected mode is as follows:
1. oxidizing tower toluene import 2 is connected with the toluene pump discharge;
2. oxidizing tower oxidation solution outlet 5 is connected with the oxidation solution pump inlet;
3. the oxidation solution circulating-pump outlet is connected with oxidation solution cooling device import 9;
4. oxidation solution heat exchanger exit 10 is connected with oxidizing tower oxidation cooling liquid inlet 11.
In conjunction with the Novel oxidation column applicating flow chart, with the following example embodiment and effect at our factory of the present invention are described:
Embodiment 1:
The toluene pump by oxidizing tower toluene import 2, is squeezed into toluene liquid to pass into steam behind the oxidizing tower toluene liquid is carried out heat temperature raising.Continue to be warming up to 155 ℃-160 ℃ when when the toluene liquid temp reaches 115 ℃-125 ℃, beginning blowing air, then the steam off valve.Toluene liquid carries out exothermic oxidation reaction in oxidizing tower.Through after the oxidation in 6-7 hour, open oxidizing tower oxidation cooling liquid inlet 11, open oxidation solution cooling device outlet 10, open oxidation solution cooling device import 9, (heat exchanger has passed into cooling medium, no longer is described in detail herein) opens oxidizing tower oxidation solution outlet 5; Startup oxidation solution circulating pump carries out tower outer circulation cooling to oxidation solution 160 ℃-163 ℃ oxidation solution.
Embodiment 2:
The toluene pump by oxidizing tower toluene import 2, is squeezed into toluene liquid to pass into steam behind the oxidizing tower toluene liquid is carried out heat temperature raising.Continue to be warming up to 160 ℃-165 ℃ when when the toluene liquid temp reaches 120 ℃-125 ℃, beginning blowing air, then the steam off valve.Toluene liquid carries out exothermic oxidation reaction in oxidizing tower.Through after the oxidation in 6.5-7.5 hour, open oxidizing tower oxidation cooling liquid inlet 11, open oxidation solution cooling device outlet 10, open oxidation solution cooling device import 9, (heat exchanger has passed into cooling medium, no longer is described in detail herein) opens oxidizing tower oxidation solution outlet 5; Startup oxidation solution circulating pump carries out tower outer circulation cooling to oxidation solution 163 ℃-166 ℃ oxidation solution.
After we adopt the oxidizing tower and process of independent research, because the toluene oxidation reaction is exothermic reaction, the heat exchange operation process is carried out outside tower, can save 50% of benzoic acid production toluene oxidation workshop building investment, owing to adopt tower outer circulation cooling technology to make 55 kilowatts/hour water-circulating pump of original employing, can use 22 kilowatts/hour water-circulating pump instead; Only this can saves energy 40%; Guarantee safety in production, the easy access operation.
Novel oxidation column and production procedure that the present invention proposes, be described by embodiment, person skilled obviously can be changed or suitably change and combination preparation method as herein described within not breaking away from content of the present invention, spirit and scope, realizes the technology of the present invention.Special needs to be pointed out is, the replacement that all are similar and change apparent to those skilled in the artly, they are deemed to be included in spirit of the present invention, scope and the content.
Claims (1)
1. the toluene oxidation tower during a ton benzoic acid is produced is characterized in that: 8～10 meters of oxidation tower heights, 4～5 meters of diameters; Be provided with air intlet 1, toluene import 2, steam inlet 3, steam (vapor) outlet 4, oxidation solution outlet 5 at the oxidation tower body, the oxidation cooling fluid is advanced oxidizing tower mouth 11; Air intlet 6-8 rice at the bottom of the tower, steam inlet 4-6 rice at the bottom of the tower, steam (vapor) outlet 4 3.5-5.5 rice at the bottom of the tower, oxidation solution outlet 0.3-0.5 rice at the bottom of the tower, oxidation cooling fluid advance oxidizing tower mouth 11 5-7 rice at the bottom of the tower, and toluene import 2 is arranged on cat head.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012103696985A CN102861542A (en) | 2012-09-27 | 2012-09-27 | Methylbenzene oxidation tower in 10000-tone level benzoic acid production |
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| Application Number | Priority Date | Filing Date | Title |
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| CN2012103696985A CN102861542A (en) | 2012-09-27 | 2012-09-27 | Methylbenzene oxidation tower in 10000-tone level benzoic acid production |
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| CN102861542A true CN102861542A (en) | 2013-01-09 |
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| CN2012103696985A Pending CN102861542A (en) | 2012-09-27 | 2012-09-27 | Methylbenzene oxidation tower in 10000-tone level benzoic acid production |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105669398A (en) * | 2016-01-15 | 2016-06-15 | 湖南弘润化工科技有限公司 | Device for producing benzaldehyde and method thereof |
| CN110283068A (en) * | 2019-06-05 | 2019-09-27 | 华南理工大学 | A kind of benzoic acid process units reacting thermal drivers air compressor |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1414516A (en) * | 1971-11-26 | 1975-11-19 | Inst Francais Du Petrole | Apparatus particularly designed for carrying out exothermic chemical reactions |
| CN1296937A (en) * | 2000-05-08 | 2001-05-30 | 湖南大学 | Process for preparing benzoic acid, henzaldehyde and benzyl alcohol |
| CN101284771A (en) * | 2008-05-30 | 2008-10-15 | 天津市东大化工有限公司 | Exhaust steam trap and method of use thereof |
| CN101337904A (en) * | 2008-08-15 | 2009-01-07 | 河南骏化发展股份有限公司 | Synthesis of DMF and device |
| CN101698642A (en) * | 2009-10-27 | 2010-04-28 | 天津市东大化工有限公司 | Methylbenzene raw material system in production process of benzoic acid and process flow |
-
2012
- 2012-09-27 CN CN2012103696985A patent/CN102861542A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1414516A (en) * | 1971-11-26 | 1975-11-19 | Inst Francais Du Petrole | Apparatus particularly designed for carrying out exothermic chemical reactions |
| CN1296937A (en) * | 2000-05-08 | 2001-05-30 | 湖南大学 | Process for preparing benzoic acid, henzaldehyde and benzyl alcohol |
| CN101284771A (en) * | 2008-05-30 | 2008-10-15 | 天津市东大化工有限公司 | Exhaust steam trap and method of use thereof |
| CN101337904A (en) * | 2008-08-15 | 2009-01-07 | 河南骏化发展股份有限公司 | Synthesis of DMF and device |
| CN101698642A (en) * | 2009-10-27 | 2010-04-28 | 天津市东大化工有限公司 | Methylbenzene raw material system in production process of benzoic acid and process flow |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105669398A (en) * | 2016-01-15 | 2016-06-15 | 湖南弘润化工科技有限公司 | Device for producing benzaldehyde and method thereof |
| CN110283068A (en) * | 2019-06-05 | 2019-09-27 | 华南理工大学 | A kind of benzoic acid process units reacting thermal drivers air compressor |
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Application publication date: 20130109 |