CN101343208B - Desorption technique for methylbenzene in tail gas from benzyl chloride preparation - Google Patents
Desorption technique for methylbenzene in tail gas from benzyl chloride preparation Download PDFInfo
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- CN101343208B CN101343208B CN2008101395633A CN200810139563A CN101343208B CN 101343208 B CN101343208 B CN 101343208B CN 2008101395633 A CN2008101395633 A CN 2008101395633A CN 200810139563 A CN200810139563 A CN 200810139563A CN 101343208 B CN101343208 B CN 101343208B
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- benzyl chloride
- toluene
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Abstract
The invention discloses a toluene desorption process in tail gas produced in the benzyl chloride production, which adopts benzyl chloride as a toluene absorbent to input the tail gas produced in the benzyl chloride production to an absorbing tower from the bottom part, a benzyl chloride liquid flows out through the bottom part of the absorbing tower and enters a desorbing tower after being preheated, the toluene obtained after atmospheric distillation operations in the desorbing tower is directly input to the benzyl chloride production, the benzyl chloride liquid flowing out from the bottom part of the desorbing tower undergoes multi-level cooling and is fed to the absorbing tower from the top part so as to spray and absorb the toluene in the tail gas produced in the benzyl chloride production, as well as enabling the desorption process to form the absorption and desorption cycling production. The process can effectively recover the toluene in the tail gas produced in the benzyl chloride production, and make the toluene be directly used in the benzyl chloride production, thereby reducing the product consumption of benzyl chloride production, product costs, discharge of pollutant toluene and the environmental pollution, and the process also greatly improves the product quality of byproduct hydrochloric acid.
Description
Technical field
The present invention relates to the Benzyl Chloride production technique, is desorption technique for methylbenzene in a kind of tail gas from benzyl chloride preparation.
Background technology
The production method of Benzyl Chloride adopts the batch production mode usually, that is: raw material toluene feeds intake to chlorination tank through the toluene pump delivery, with thermal oil material in the still is heated then, when treating that material seethes with excitement in the still, toluene gas begins to be back in the tower after the condenser cooling along rising in the tower.In the toluene gas uphill process, outside tower under the irradiation of illumination lamp, toluene gas and chlorine carry out substitution reaction and produce Benzyl Chloride, along with constantly carrying out of reaction, the content of Benzyl Chloride constantly raises in the still, and when treating that Benzyl Chloride content reaches 95% left and right sides, material is thick benzyl in the still, contain a certain amount of toluene gas in the hydrochloric acid tail gas that reaction generates, hydrochloric acid tail gas absorbs through falling-film absorber and generates hydrochloric acid.
Though the intermittent mode of production of above-mentioned Benzyl Chloride has more advantage,, the toluene in the hydrogen chloride tail gas that produces in the Benzyl Chloride production can not reclaim, and this has just increased product consumption and product cost; Owing to have part toluene in the byproduct hydrochloric acid, this has also influenced the quality product of hydrochloric acid simultaneously.
Summary of the invention
Purpose of the present invention provides desorption technique for methylbenzene in a kind of tail gas from benzyl chloride preparation, thereby the toluene that reaches in the hydrogen chloride tail gas that will produce in the Benzyl Chloride production separates, and toluene is directly sent in the production of Benzyl Chloride again, and then reduced production costs.
The present invention for achieving the above object, be achieved through the following technical solutions: desorption technique for methylbenzene in a kind of tail gas from benzyl chloride preparation, adopt Benzyl Chloride as the toluene absorption agent, the tail gas that produces in the Benzyl Chloride production is entered through the bottom, absorption tower, Benzyl Chloride liquid flows out through the bottom, absorption tower and enter desorption tower after preheating, directly enter in the Benzyl Chloride production by the toluene that obtains after the operation of desorption tower atmospheric distillation, cool off through multistage cooling by the effusive Benzyl Chloride liquid in desorption tower bottom, send into the top, absorption tower the toluene in the tail gas that produces in the Benzyl Chloride production is sprayed absorption, desorption technique is formed absorb desorption cycle production.
Desorption technique for methylbenzene in described a kind of tail gas from benzyl chloride preparation, its processing step is as follows:
1. the tail gas that produces in the Benzyl Chloride production is entered in the tower by the bottom, absorption tower, Benzyl Chloride liquid sprays through the top that water cooler is cooled to carry out after 6-10 ℃ the absorption tower, and the toluene in the tail gas that produces in the Benzyl Chloride production is absorbed;
2. the hydrogen chloride tail gas after absorbing is sent into hydrochloric acid unit after entering into and absorbing in the falling-film absorber;
3. step absorbs the pump of Benzyl Chloride liquid through the bottom, absorption tower behind the toluene in 1. and adds in the charging branch road that is sent to preheater and carry out preheating, the charging branch road temperature of preheater is 130-150 ℃, Benzyl Chloride liquid after the preheating is admitted in the desorption tower, and Benzyl Chloride liquid carries out the atmospheric distillation operation in desorption tower;
4. the toluene vapor in the desorption tower enters the toluene storage tank after the condenser condenses at desorption tower top, and wherein toluene enters in the production of Benzyl Chloride, and hydrogenchloride enters the hydrochloric acid processing unit;
5. through disengaging behind the toluene Benzyl Chloride liquid again the reboiler through the desorption tower bottom enter the pump of desorption tower bottom, the backflow branch road that pumps into the desorption tower preheater then is cooled to 80-100 ℃, enter water cooler again and further be cooled to 6-10 ℃, make Benzyl Chloride liquid enter the top, absorption tower then the toluene in the tail gas that produces in the Benzyl Chloride production is sprayed absorption.
Reboiler temperature of the present invention is 180-200 ℃.Absorption tower and desorption tower are atmospheric tower.
The advantage of technology of the present invention is: it can carry out efficient recovery with the toluene in the tail gas that produces in the Benzyl Chloride production, toluene can be directly used in the Benzyl Chloride production, thereby reduce the product consumption that Benzyl Chloride is produced, and reduced product cost, through measuring and calculating, in the Benzyl Chloride production technique, use technology of the present invention, the consumption of toluene consumes toluene by the ton Benzyl Chloride and is reduced to 755 kilograms for 775 kilograms, one ton of Benzyl Chloride of every production can reduce cost about 150 yuan, the performance of enterprises is increased by a fairly big margin, reach 100ppm through the toluene in the hydrogen chloride tail gas behind the Separation and Recovery toluene simultaneously, reduced the discharging of pollutent toluene, reduced environmental pollution, technology of the present invention has also significantly improved the quality product of byproduct hydrochloric acid etc.
Description of drawings
Accompanying drawing 1 is a process flow diagram of the present invention.
Embodiment
Embodiment
Desorption technique of the present invention is connected with tail gas unit in the Benzyl Chloride production technique, toluene through technology Separation and Recovery of the present invention is directly used in the production of Benzyl Chloride, enter absorption in the falling-film absorber 10 through the hydrogen chloride tail gas after the 1 spray absorption of absorption tower, further reduced the toluene level in the hydrogen chloride tail gas.The device that uses in the technical process of the present invention and being connected to: 1 bottom, absorption tower is connected by the pump 2 of pipeline with the bottom, absorption tower, the pump 2 of 1 bottom, absorption tower is connected with preheater 3 by pipeline, the charging branch road of preheater 3 is connected with desorption tower 5 by pipeline, desorption tower 5 tops are connected with condenser 6 by pipeline, condenser 6 is connected with toluene tank 7 by pipeline, and toluene tank 7 is connected with the hydrochloric acid processing unit with Benzyl Chloride production technique feeding unit respectively.Preheater 3 backflow branch roads are connected with water cooler 4 by pipeline, and water cooler 4 is connected with 1 top, absorption tower by pipeline, and 1 top, absorption tower is connected with falling-film absorber 10 by pipeline, and falling-film absorber 10 is connected with hydrochloric acid unit.Desorption tower 5 bottoms are connected with reboiler 8 by pipeline, and reboiler 8 is connected by the pump 9 of pipeline with the desorption tower bottom, and the pump 9 of desorption tower bottom is connected with preheater 3 backflow branch roads by pipeline.
Above-mentioned each apparatus structure of the present invention and principle of work are known technology, and used auxiliary material of absorption tower and desorption tower and reaction etc. are known technology, so do not do detailed description.
Desorption technique of the present invention is: adopt Benzyl Chloride as the toluene absorption agent, 1 bottom enters through the absorption tower with the tail gas that produces in the Benzyl Chloride production, the outflow of 1 bottom enters desorption tower 5 to Benzyl Chloride liquid after preheating through the absorption tower, directly enter in the Benzyl Chloride production by the toluene that obtains after the operation of desorption tower 5 atmospheric distillations, cool off through multistage cooling again by the effusive Benzyl Chloride liquid in desorption tower 5 bottoms, send into 1 top, absorption tower the toluene in the tail gas that produces in the Benzyl Chloride production is sprayed absorption, desorption technique of the present invention is formed absorb desorption cycle production, isolated toluene is directly used in the Benzyl Chloride production, the tail gas that produces in the Benzyl Chloride production enters the absorption tower again, make through containing the toluene amount in the hydrogen chloride tail gas that absorbs and further reduce, improve the hydrochloric acid quality product.
Concrete processing step of the present invention is as follows:
1. the tail gas (hydrogen chloride gas) that produces in Benzyl Chloride being produced is entered in the tower by 1 bottom, absorption tower, Benzyl Chloride liquid sprays through the top that water cooler 4 is cooled to enter after 6-10 ℃ absorption tower 1, and the toluene in the tail gas that produces in the Benzyl Chloride production is absorbed;
2. the hydrogen chloride tail gas after absorbing is sent into hydrochloric acid unit after entering into and absorbing in the falling-film absorber 10;
3. step absorbs the pump 2 of Benzyl Chloride liquid through 1 bottom, absorption tower behind the toluene in 1. and adds in the charging branch road that is sent to preheater 3 and carry out preheating, the charging branch road temperature of preheater 3 is 130-150 ℃, Benzyl Chloride liquid after the preheating is admitted in the desorption tower 5, and Benzyl Chloride liquid carries out the atmospheric distillation operation in desorption tower 5;
4. the toluene vapor in the desorption tower 5 enters toluene storage tank 7 after condenser 6 condensations at desorption tower 5 tops, and wherein toluene enters in the production of Benzyl Chloride, and hydrogenchloride enters the hydrochloric acid processing unit;
5. through disengaging behind the toluene Benzyl Chloride liquid again the reboiler 8 through desorption tower 5 bottoms enter the pump 9 of desorption tower bottom, the backflow branch road that pumps into preheater 3 is cooled to 80-100 ℃, enter water cooler 4 again and further be cooled to 6-10 ℃, make Benzyl Chloride liquid enter 1 top, absorption tower then the toluene in the tail gas that produces in the Benzyl Chloride production is sprayed absorption, form circulation with this and absorb desorb.
Claims (4)
1. desorption technique for methylbenzene in the tail gas from benzyl chloride preparation, it is characterized in that: adopt Benzyl Chloride as the toluene absorption agent, the tail gas that produces in the Benzyl Chloride production is entered through the bottom, absorption tower, Benzyl Chloride liquid flows out through the bottom, absorption tower and enter desorption tower after preheating, directly enter in the Benzyl Chloride production by the toluene that obtains after the operation of desorption tower atmospheric distillation, cool off through multistage cooling by the effusive Benzyl Chloride liquid in desorption tower bottom, send into the top, absorption tower the toluene in the tail gas that produces in the Benzyl Chloride production is sprayed absorption, desorption technique is formed absorb desorption cycle production.
2. desorption technique for methylbenzene in a kind of tail gas from benzyl chloride preparation according to claim 1 is characterized in that: its processing step is as follows:
1. the tail gas that produces in Benzyl Chloride being produced is entered in the tower by absorption tower (1) bottom, and Benzyl Chloride liquid sprays through the top that water cooler (4) is cooled to enter after 6-10 ℃ absorption tower (1), and the toluene in the tail gas that produces in the Benzyl Chloride production is absorbed;
2. the hydrogen chloride tail gas after absorbing is sent into hydrochloric acid unit after entering into and absorbing in the falling-film absorber (10);
3. step absorbs the pump (2) of Benzyl Chloride liquid through absorption tower (1) bottom behind the toluene in 1. and adds in the charging branch road that is sent to preheater (3) and carry out preheating, the charging branch road temperature of preheater (3) is 130-150 ℃, Benzyl Chloride liquid after the preheating is admitted in the desorption tower (5), and Benzyl Chloride liquid carries out the atmospheric distillation operation in desorption tower (5);
4. the toluene vapor in the desorption tower (5) enters toluene storage tank (7) after condenser (6) condensation at desorption tower top, and wherein toluene enters in the production of Benzyl Chloride, and hydrogenchloride enters the hydrochloric acid processing unit;
5. through disengaging behind the toluene Benzyl Chloride liquid again the reboiler (8) through desorption tower (5) bottom enter the pump (9) of desorption tower bottom, the backflow branch road that pumps into desorption tower preheater (3) then is cooled to 80-100 ℃, enter water cooler (4) again and further be cooled to 6-10 ℃, make Benzyl Chloride liquid enter top, absorption tower (1) then the toluene in the tail gas that produces in the Benzyl Chloride production is sprayed absorption.
3. desorption technique for methylbenzene in a kind of tail gas from benzyl chloride preparation according to claim 2 is characterized in that: reboiler (8) temperature is 180-200 ℃.
4. desorption technique for methylbenzene in a kind of tail gas from benzyl chloride preparation according to claim 2 is characterized in that: absorption tower (1) and desorption tower (5) are atmospheric tower.
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| CN2008101395633A CN101343208B (en) | 2008-08-22 | 2008-08-22 | Desorption technique for methylbenzene in tail gas from benzyl chloride preparation |
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| CN2008101395633A CN101343208B (en) | 2008-08-22 | 2008-08-22 | Desorption technique for methylbenzene in tail gas from benzyl chloride preparation |
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| CN101343208B true CN101343208B (en) | 2011-03-16 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103910597A (en) * | 2014-03-25 | 2014-07-09 | 甘肃农业大学 | Method for purifying lycopene by using deoxycholic acid |
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| CN101972554B (en) * | 2010-10-26 | 2012-10-03 | 山东聊城中盛蓝瑞化工有限公司 | Anti-blocking rectifying tower and cleaning process thereof |
| CN103585857B (en) * | 2013-11-04 | 2015-11-18 | 聊城市鲁西化工工程设计有限责任公司 | A kind of tail gas HCl recovery system and technique |
| RU2539658C1 (en) * | 2013-12-10 | 2015-01-20 | Федеральное государственное казенное учреждение "33 Центральный научно-исследовательский испытательный институт Министерства обороны Российской Федерации" | Method of producing benzyl chloride |
| CN103922891B (en) * | 2014-05-08 | 2015-07-15 | 南京工业大学 | Energy integration method for producing benzyl chloride through series connection of two stages of reactive distillation |
| CN105174217A (en) * | 2014-06-20 | 2015-12-23 | 唐慧建 | Method for purifying chlorotoluene byproduct hydrogen chloride gas and regenerating absorbent |
| CN106310875A (en) * | 2015-07-01 | 2017-01-11 | 启东久星化工有限公司 | System for separating organic matter from mixture of hydrogen chloride and organic matter |
| CN104984634A (en) * | 2015-07-15 | 2015-10-21 | 天津大学 | Treating device for waste gas containing volatile organic matters |
| CN106606917B (en) * | 2015-10-22 | 2019-04-26 | 中国石油化工股份有限公司 | The method and apparatus of toluene oxidation treating tail gas |
| CN105566054A (en) * | 2015-12-16 | 2016-05-11 | 南京工业大学 | Method and system for recycling byproduct hydrogen chloride in aromatic chlorination production process |
| CN112675663A (en) * | 2020-11-26 | 2021-04-20 | 浙江工业大学 | Toluene tail gas treatment method |
| CN115090238B (en) * | 2022-06-28 | 2024-04-19 | 浙江迪邦化工有限公司 | System and process for continuously producing benzyl chloride |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1110270A (en) * | 1994-12-13 | 1995-10-18 | 浙江大学精细化工厂 | Method and equipment for producing benzyl fluoride |
| CN101219927A (en) * | 2008-01-07 | 2008-07-16 | 天津大学 | Continuous process and device for the separation of benzyl chloride regular packing column |
-
2008
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1110270A (en) * | 1994-12-13 | 1995-10-18 | 浙江大学精细化工厂 | Method and equipment for producing benzyl fluoride |
| CN101219927A (en) * | 2008-01-07 | 2008-07-16 | 天津大学 | Continuous process and device for the separation of benzyl chloride regular packing column |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103910597A (en) * | 2014-03-25 | 2014-07-09 | 甘肃农业大学 | Method for purifying lycopene by using deoxycholic acid |
| CN103910597B (en) * | 2014-03-25 | 2016-04-13 | 甘肃农业大学 | By the method for Deoxycholic Acid purified lycopene |
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| CN101343208A (en) | 2009-01-14 |
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