CN102199070A - Tubular furnace method pressure-reduced debenzolization and distillation process - Google Patents
Tubular furnace method pressure-reduced debenzolization and distillation process Download PDFInfo
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- CN102199070A CN102199070A CN2011100856780A CN201110085678A CN102199070A CN 102199070 A CN102199070 A CN 102199070A CN 2011100856780 A CN2011100856780 A CN 2011100856780A CN 201110085678 A CN201110085678 A CN 201110085678A CN 102199070 A CN102199070 A CN 102199070A
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Abstract
The invention discloses a tubular furnace method pressure-reduced debenzolization and distillation process. The process comprises the following steps of: carrying out heat exchange on rich oil from a benzene washing section by using an oil-gas heat exchanger and a lean oil-rich oil heat exchanger, entering the convection section of a tubular heating furnace for heating to 175-185 DEG C, then entering a debenzolization tower for debenzolization and distillation, collecting a crude benzene product from the tower top and returning lean oil at the tower bottom to a benzene washing tower, wherein the tower top pressure of the debenzolization tower is 13.3-70 kPa and the tower bottom pressure is 23.3-80 kPa; and the tower top temperature is 40-80 DEG C and the tower bottom temperature is 195-270 DEG C. Compared with traditional debenzolization processes, the pressure-reduced debenzolization and distillation process mainly has the advantages that: 1. the operation can be carried out under a negative pressure, and steam stripping can be omitted; 2. the yield of crude benzene is improved by 0.05-0.35%; 3. steam is not used; 4. since a regenerator is not used, the process structure is more compact and the occupation area is smaller; and 5. One oil-water separator is omitted, the regenerator is not used and a novel debenzolization tower is designed, thus effectively saving equipment investment cost.
Description
Technical field
The present invention relates to reclaim the novel process of crude benzol, belong to the coking engineering projects technology, be specifically related to a kind of integrated tube oven method decompression and take off benzene distillation technology.
Background technology
At present, domestic most crude benzol distil process mainly adopts the method for water at atmospheric pressure steam stripping, and utilizes single tower or double-column process to obtain a kind of benzene, two kinds of benzene or three benzaldehyde products under normal pressure.This type of de-benzene process adopts low pressure water vapor as thermal source, and the acting as of steam (1) carried the crude benzol material in debenzolizing tower and heated up in a steamer (2) for revivifier provides thermal source, makes the smooth deslagging of revivifier.This technical maturity is stable, but can produce a large amount of organic waste water in still-process, and contaminate environment has increased pressure to biochemical treatment equally.
The scholar of domestic some and engineering technical personnel have done some to existing processes and have improved the method and apparatus that Chinese patent CN101544913A disclosed a kind of negative pressure benzene removal on 30th in 09 month in 2009.Its technology forms negative pressure for using vacuum pump to debenzolizing tower and revivifier, cancellation steam stripping at the bottom of the debenzolizing tower tower and at the bottom of the regenerator column, adopt 2 tubular ovens to carry out tower respectively at the bottom of the circulation heating thermal source is provided.The debenzolizing tower rectifying section adopts filler to separate light benzene and heavy benzol, this technology has reduced the temperature of debenzolizing tower cat head, cancelled steam heating, in energy-conserving and environment-protective, made certain contribution, but this technology has increased vacuum pump and 2 tubular ovens, has increased investment and occupation area of equipment widely, is not suitable for technological transformation especially, and under the overall situation of benzene hydrogenation working ability surplus, debenzolizing tower top adopts filler to separate heavy benzol and the real waste for separating power and facility investment of light benzene.
Summary of the invention
At the deficiency of existing domestic and international rich oil de-benzene distil process, in conjunction with the present situation in crude benzol market, technical problem to be solved by this invention provides a kind of brand-new, low investment, floor space is little, flow process is short, and energy consumption is low, and benzene distillation technology is taken off in the tube oven method decompression of energy-saving and emission-reduction.
The present invention for the technical scheme that solves its technical problem and adopt is: benzene distillation technology is taken off in a kind of tube oven method decompression, its innovative point is, washing rich oil that benzene workshop section sends enters the tubular oven convection zone after through oil gas interchanger and poor oil-rich heat exchanger heat exchange and is preheated to 175-185 ℃ and enters debenzolizing tower and take off benzene distillation, cat head extraction crude benzol product, oil-poor getting back at the bottom of the tower washed the benzene tower, wherein: the debenzolizing tower tower top pressure is 13.3-70kPa, and tower bottom pressure is 23.3-80kPa; Tower top temperature is 40-80 ℃, and column bottom temperature is 195-270 ℃.
Preferably, the above-mentioned tube oven method decompression of the present invention is taken off in the benzene distillation technology, adopts the hydronic mode of tube furnace to guarantee that column bottom temperature is at 195-270 ℃ at the bottom of the tower.
Preferably, the above-mentioned tube oven method decompression of the present invention is taken off in the benzene distillation technology, and the debenzolizing tower cat head adopts vacuum pump that debenzolizing tower is vacuumized, and makes debenzolizing tower operate under negative pressure.
Preferably, the above-mentioned tube oven method decompression of the present invention is taken off in the benzene distillation technology, reduce the stage number of debenzolizing tower rectifying section significantly, the debenzolizing tower rectifying section changes 2-10 layer tower tray by 16-35 layer or filler, the heat supply mode of the setting of cancellation revivifier and water vapor profit reduction and reserving directly is provided with slag-drip opening at debenzolizing tower tower still.The present situation of existing coking industry be benzene hydrogenation for crude benzol output, the working ability surplus, the coking-light benzene of debenzolizing tower direct production and heavy benzol, quality product is not high, economic benefit is not good.Do not need original design a large amount of number of theoretical plate to separate and only produce crude benzol, therefore can effectively must reduce the tower tray number, reduce the height of debenzolizing tower, reduce investment.
The above-mentioned tube oven method decompression of the present invention is taken off in the benzene distillation technology, the two circulation heating modes of tube furnace are set at the bottom of the debenzolizing tower tower, the heat supply mode of the setting of cancellation revivifier and water vapor profit reduction and reserving, directly slag-drip opening is set at debenzolizing tower tower still, increase the height of debenzolizing tower tower still, the thermal source that the oil-poor top by the tower still of a part provides at the bottom of as tower through the tube furnace heating cycle, the effect that tower still deslagging is provided through tube furnace circulation heating is drawn in the oil-poor bottom via the tower still of a part.
With respect to existing domestic and international rich oil de-benzene process, positively effect of the present invention is: the heat supply mode of having cancelled the open steam profit reduction and reserving, adopt underpressure distillation, reduced the temperature of cat head, help the volatilization of light constituent, improve the yield 0.05 to 0.35% of crude benzol, reduced the energy consumption of 14-20%, water saving 50-90% has reduced the discharge of wastewater that the 0.9-1.5 ton contains benzene waste water/ton crude benzol, alleviated biochemical pressure, favourable with environment protection; The cancellation revivifier, keep a tube furnace to heat, make process structure compacter, floor space is littler, and reduce the stage number of debenzolizing tower and the height of reduction debenzolizing tower, reduce by a water-and-oil separator and effectively saved investment, this invention not only can apply to the transformation of existing technology well, is suitable for the design of new project equally.
Description of drawings
Accompanying drawing is a process flow sheet of the present invention.
Embodiment
Below in conjunction with the drawings and specific embodiments, further set forth the present invention.These embodiment are interpreted as only being used to the present invention is described and are not used in restriction protection scope of the present invention.After the content of having read the present invention's record, those skilled in the art can make various changes or modifications the present invention, and these equivalences change and modify and fall into claim of the present invention institute restricted portion equally.
The decompression of embodiment 1 tube oven method is taken off in the benzene distillation technology, washing rich oil (the main character index is as shown in table 1) that benzene workshop section sends enters the tubular oven convection zone after through oil gas interchanger and poor oil-rich heat exchanger heat exchange and is preheated to 175 ℃ and enters the debenzolizing tower that rectifying section has 2 layers of tower tray and take off benzene distillation, the debenzolizing tower tower top pressure is 13.3kPa, and tower bottom pressure is 23.3kPa; Tower top temperature is 45 ℃, and column bottom temperature is 195 ℃.Cat head extraction crude benzol product yield is 1.35% (to dry coal).Oil-poor getting back at the bottom of the tower washed the benzene tower.With respect to tube oven method vapour method rich oil de-benzene energy-conservation 20%.
The main character index of crude benzol product is as shown in table 2, and oil-poor main character index is as shown in table 3.
Embodiment 2
The tube oven method decompression is taken off in the benzene distillation technology, washing rich oil (the main character index is as shown in table 1) that benzene workshop section sends enters the tubular oven convection zone after through oil gas interchanger and poor oil-rich heat exchanger heat exchange and is preheated to 185 ℃ and enters the debenzolizing tower that rectifying section has 10 layers of tower tray and take off benzene distillation, the debenzolizing tower tower top pressure is 70kPa, and tower bottom pressure is 80kPa; Tower top temperature is 80 ℃, and column bottom temperature is 270 ℃.Cat head extraction crude benzol product, yield is 1.1% (to dry coal), oil-poor the getting back at the bottom of the tower washed the benzene tower.With respect to tube oven method vapour method rich oil de-benzene energy-conservation 14.5%.
The main character index of crude benzol product is as shown in table 2, and oil-poor main character index is as shown in table 3.
Embodiment 3
The single tower benzene that takes off of original tradition is produced crude benzol technology, 60 tons of/hour washing oil internal circulating loads, and 0.82 ton/hour of crude benzol output consumes 1.2 tons/hour of steam.Change debenzolizing tower equipment through technological transformation, the cancellation revivifier, adopt above-mentioned tube oven method decompression to take off benzene distillation technology, washing rich oil (the main character index is as shown in table 1) that benzene workshop section sends enters the tubular oven convection zone after through oil gas interchanger and poor oil-rich heat exchanger heat exchange and is preheated to 180 ℃ and enters the debenzolizing tower that rectifying section has 6 layers of tower tray and take off benzene distillation, the debenzolizing tower tower top pressure is 41.6kPa, and tower bottom pressure is 51.7kPa; Tower top temperature is 62.5 ℃, and column bottom temperature is 230 ℃.Cat head extraction crude benzol product, oil-poor the getting back at the bottom of the tower washed the benzene tower.With respect to tube oven method vapour method rich oil de-benzene energy-conservation 16.5%.
The main character index of crude benzol product is as shown in table 2, and oil-poor main character index is as shown in table 3.The crude benzol productive rate rises to 1.15% (to dry coal) by original 0.8.Original benzene that takes off is cancelled with 1.2 tons of/hour steam consumptions of steam, reduces to contain 1.2 tons of/hour quantity dischargeds of benzene waste water.Owing to adopt negative-pressure operation, whole energy consumption reduces by 11.2%.
To sum up, the present invention has cancelled the heat supply mode of open steam profit reduction and reserving, adopt underpressure distillation, reduced the temperature of cat head, help the volatilization of light constituent, improve the yield 0.05 to 0.35% of crude benzol, reduced the energy consumption of 10-20%, water saving 50-90% has reduced the discharge of wastewater that the 0.9-1.5 ton contains benzene waste water/ton crude benzol, alleviated biochemical pressure, favourable with environment protection; The cancellation revivifier, keep a tube furnace to heat, make process structure compacter, floor space is littler, and reduce the stage number of debenzolizing tower and the height of reduction debenzolizing tower, reduce by a water-and-oil separator and effectively saved investment, this invention not only can apply to the transformation of existing technology well, is suitable for the design of new project equally.
Table 1. rich oil main character index
The clumsy main character index of table 2.
The oil-poor main character index of table 3.
Claims (4)
1. benzene distillation technology is taken off in a tube oven method decompression, it is characterized in that, washing rich oil that benzene workshop section sends enters the tubular oven convection zone after through oil gas interchanger and poor oil-rich heat exchanger heat exchange and is preheated to 175-185 ℃ and enters debenzolizing tower and take off benzene distillation, cat head extraction crude benzol product, oil-poor getting back at the bottom of the tower washed the benzene tower, wherein: the debenzolizing tower tower top pressure is 13.3-70kPa, and tower bottom pressure is 23.3-80kPa; Tower top temperature is 40-80 ℃, and column bottom temperature is 195-270 ℃.
2. benzene distillation technology is taken off in tube oven method decompression according to claim 1, it is characterized in that the debenzolizing tower rectifying section has 2-10 layer tower tray.
3. benzene distillation technology is taken off in tube oven method decompression according to claim 1 and 2, it is characterized in that, adopts tube furnace circulation heating at the bottom of the debenzolizing tower tower.
4. benzene distillation technology is taken off in tube oven method decompression according to claim 3, it is characterized in that, the debenzolizing tower cat head adopts vacuum pump that debenzolizing tower is vacuumized.
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| CN 201110085678 CN102199070B (en) | 2011-04-06 | 2011-04-06 | Tubular furnace method pressure-reduced debenzolization and distillation process |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102796571A (en) * | 2012-07-25 | 2012-11-28 | 济钢集团国际工程技术有限公司 | System for producing light benzene by performing negative pressure debenzolization on rich oil |
| CN103697694A (en) * | 2012-09-28 | 2014-04-02 | 宝钢工程技术集团有限公司 | Negative-pressure heating dual-chamber tubular furnace for distilling crude benzene |
| CN104043259A (en) * | 2014-06-28 | 2014-09-17 | 济钢集团有限公司 | Benzene distillation device with negative-pressure control device |
| CN104327864A (en) * | 2014-11-15 | 2015-02-04 | 马钢(集团)控股有限公司 | Cooling system and cooling method of recycle gas in inlet of coke dry quenching furnace |
| CN104961620A (en) * | 2015-06-03 | 2015-10-07 | 马钢(集团)控股有限公司 | Method for treating benzene hydrogenated polymer |
| CN105154144A (en) * | 2015-08-31 | 2015-12-16 | 山东铁雄新沙能源有限公司 | Negative-pressure debenzylation device and negative-pressure debenzolization method |
| CN111349476A (en) * | 2020-03-17 | 2020-06-30 | 本钢板材股份有限公司 | Method for improving cleaning effect of crude benzene washing benzene tower |
| CN111939584A (en) * | 2020-09-04 | 2020-11-17 | 中冶焦耐(大连)工程技术有限公司 | Process and system for evaporating crude benzene in benzene hydrogenation reaction system |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101597517A (en) * | 2009-06-17 | 2009-12-09 | 济钢集团国际工程技术有限公司 | A kind of rich oil de-benzene process |
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- 2011-04-06 CN CN 201110085678 patent/CN102199070B/en not_active Expired - Fee Related
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101597517A (en) * | 2009-06-17 | 2009-12-09 | 济钢集团国际工程技术有限公司 | A kind of rich oil de-benzene process |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102796571A (en) * | 2012-07-25 | 2012-11-28 | 济钢集团国际工程技术有限公司 | System for producing light benzene by performing negative pressure debenzolization on rich oil |
| CN102796571B (en) * | 2012-07-25 | 2014-04-30 | 济钢集团国际工程技术有限公司 | System for producing light benzene by performing negative pressure debenzolization on rich oil |
| CN103697694A (en) * | 2012-09-28 | 2014-04-02 | 宝钢工程技术集团有限公司 | Negative-pressure heating dual-chamber tubular furnace for distilling crude benzene |
| CN104043259A (en) * | 2014-06-28 | 2014-09-17 | 济钢集团有限公司 | Benzene distillation device with negative-pressure control device |
| CN104327864A (en) * | 2014-11-15 | 2015-02-04 | 马钢(集团)控股有限公司 | Cooling system and cooling method of recycle gas in inlet of coke dry quenching furnace |
| CN104961620A (en) * | 2015-06-03 | 2015-10-07 | 马钢(集团)控股有限公司 | Method for treating benzene hydrogenated polymer |
| CN105154144A (en) * | 2015-08-31 | 2015-12-16 | 山东铁雄新沙能源有限公司 | Negative-pressure debenzylation device and negative-pressure debenzolization method |
| CN111349476A (en) * | 2020-03-17 | 2020-06-30 | 本钢板材股份有限公司 | Method for improving cleaning effect of crude benzene washing benzene tower |
| CN111939584A (en) * | 2020-09-04 | 2020-11-17 | 中冶焦耐(大连)工程技术有限公司 | Process and system for evaporating crude benzene in benzene hydrogenation reaction system |
| CN111939584B (en) * | 2020-09-04 | 2023-09-15 | 中冶焦耐(大连)工程技术有限公司 | Crude benzene evaporation process and system in benzene hydrogenation reaction system |
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