CN101597517A - A kind of rich oil de-benzene process - Google Patents
A kind of rich oil de-benzene process Download PDFInfo
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- CN101597517A CN101597517A CNA2009100165357A CN200910016535A CN101597517A CN 101597517 A CN101597517 A CN 101597517A CN A2009100165357 A CNA2009100165357 A CN A2009100165357A CN 200910016535 A CN200910016535 A CN 200910016535A CN 101597517 A CN101597517 A CN 101597517A
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Abstract
The invention discloses a kind of rich oil de-benzene process, the rich oil that whole cold wash benzene workshop section sends is sent into the heating of oil gas interchanger, enter the poor oil-rich heat exchanger heating afterwards, enter the debenzolizing tower tube furnace after rich oil is heated to 160-180 ℃ and further be heated to 190-200 ℃, then send into the debenzolizing tower distillation and take off benzene; Distillation is taken off light benzene, refined heavy benzole and the naphtalene oil of benzene institute output respectively by debenzolizing tower cat head and side line extraction, become the oil-poor tower still that enters behind the rich oil de-benzene, oil-poor first part in the tower still enters the heating of debenzolizing tower tube furnace, provide heat by sending the distillation of debenzolizing tower above the debenzolizing tower tower still back to again after the heating for rich oil, flow through poor oil-rich heat exchanger, oil-poor one section water cooler and oil-poor two sections water coolers of oil-poor second section in the tower still are sent the recycle of whole cold wash benzene workshop section after being cooled to 25-30 ℃ back to.It both can satisfy the requirement of whole cold wash benzene washing oil recycle, did not have waste water again, waste gas discharges outward, and can simplify flow process, energy-conserving and environment-protective, and it is higher to take off the benzene rate.
Description
Technical field
The present invention relates to coal chemical enterprise the next rich oil of whole cold wash benzene workshop section is distilled the technology of taking off benzene, exactly a kind of rich oil de-benzene process
Background technology
At present, the whole cold wash benzene of domestic coke-oven plant gas purification workshop section all adopts tar washing oil or oil washing oil to wash benzene in the coal gas, and washing oil absorbs benzene and becomes rich oil, becomes washing oil again or claims oil-poor after benzene is taken off in the rich oil distillation.In order to guarantee the recycle of washing oil, must remove the benzene in the rich oil, make it to become can be sent to whole cold wash benzene workshop section wash the oil-poor of benzene once more.The method that existing all kinds of processing method all adopts steamed to blow removes the crude benzol in the rich oil, and is to utilize single tower flow process or double-column process to obtain a kind of benzene, two kinds of benzene or three kinds of products under the condition of normal pressure.In the production process since with steam as the distillatory thermal source, therefore, can produce a large amount of unmanageable crude benzol and divide dried uply, both expended valuable steam resource, easily cause serious environmental to pollute again, the recycling economy index of advocating with country also differs greatly.
Summary of the invention
The objective of the invention is, a kind of rich oil de-benzene process is provided, it both can satisfy the requirement of whole cold wash benzene washing oil recycle, can not utilize steamed stripping benzene again, do not have waste water in the production process, waste gas discharges outward, simplifies flow process, energy-conserving and environment-protective, and it is higher to take off the benzene rate.
The present invention is achieved through the following technical solutions for achieving the above object, and a kind of rich oil negative pressure benzene removal novel process comprises the steps:
A kind of rich oil de-benzene process, the rich oil that whole cold wash benzene workshop section sends is sent into the heat exchange of oil gas interchanger, enter the poor oil-rich heat exchanger heat exchange afterwards, the rich oil heat exchange enters the debenzolizing tower tube furnace after about 160-180 ℃ and further is heated to 190-200 ℃, then sends into debenzolizing tower and distills and take off benzene; Distillation is taken off light benzene, refined heavy benzole and the naphtalene oil of benzene institute output respectively by debenzolizing tower cat head and side line extraction, become the oil-poor debenzolizing tower tower still that enters behind the rich oil de-benzene, oil-poor first part in the tower still enters the heating of debenzolizing tower tube furnace, send debenzolizing tower and rich oil mixed heat transfer back to by debenzolizing tower tower still top again after the heating, for the distillation of rich oil provides heat, flow through successively poor oil-rich heat exchanger, oil-poor one section water cooler and oil-poor two sections water coolers of oil-poor second section in the tower still are sent the recycle of whole cold wash benzene workshop section after being cooled to 25-30 ℃ back to.
1-1.5% with second section in the described debenzolizing tower tower still in oil-poor oil-poor sent into regenerator column regeneration; Oil-poor and the rich oil that the oil gas that regeneration back generates is flowed out by the regenerator column cat head in the tower still of sending in the debenzolizing tower with debenzolizing tower mixes; The residual oil that generates behind the regenerating wash oil is positioned at regeneration Tata still, residual oil in the regeneration Tata still, wherein first part directly is sent to the tar car, and second section is delivered to the heating of regenerator column tube furnace, and the residual oil after the heating is sent regenerator column back to and mixed with the interior residual oil of Tata still of regenerating.
With vacuum pump debenzolizing tower and regenerator column are vacuumized, make and form negative pressure in debenzolizing tower and the regenerator column, the debenzolizing tower tower top pressure is controlled at-and 70KPa is to-20KPa, debenzolizing tower tower still pressure-80KPa is to-30KPa, regenerator column tower top pressure-80KPa is to-30KPa, and regeneration Tata still pressure-85KPa is to-35KPa.
50-55 ℃ of debenzolizing tower tower top temperature, 228-230 ℃ of debenzolizing tower tower still temperature.
245-250 ℃ of regenerator column tower top temperature, 310-320 ℃ of tower still temperature.
Positively effect of the present invention is: it can utilize the oil-poor debenzolizing tower that returns after tube furnace heats of portion of hot in the debenzolizing tower still to substitute steam takes off benzene as distillation thermal source, can save a large amount of steam resources, can not produce simultaneously a large amount of unmanageable crude benzol divide dried up, energy-conserving and environment-protective; In process of production, debenzolizing tower and regenerator column all are pumped into the closed-circuit system of negative pressure by vacuum pump, more help benzene and separate from washing oil, can improve the productive rate of light benzene, energy-saving, environment-friendly and high-efficiency.
Description of drawings
Fig. 1 is the process flow sheet of a kind of rich oil de-benzene process of the present invention.
Wherein: 1 debenzolizing tower; 2 debenzolizing tower tube furnaces; 3 regenerator columns; 4 regenerator column tube furnaces; 5 naphtalene oil grooves; 6 refined heavy benzole grooves; 7 light benzene return tanks; 8 oil gas interchanger; 9 non-condensable gas condensers; 10 is vacuum pump; 11 poor oil-rich heat exchangers; 12 oil-poor one section water cooler; 13 oil-poor two sections oil-poor inlets of water cooler A cycling hot.
Embodiment
A kind of rich oil de-benzene process step of the present invention is as follows:
The rich oil that whole cold wash benzene workshop section sends here is sent into oil gas interchanger 8, rich oil after the heat exchange enters poor oil-rich heat exchanger 11 heat exchange, the rich oil temperature enters debenzolizing tower tube furnace 2 after reaching about 160-180 ℃, sends into debenzolizing tower 1 after debenzolizing tower tube furnace 2 further is heated to 190-200 ℃ with the temperature of rich oil and distills and take off benzene; Distillation is taken off light benzene, refined heavy benzole and the naphtalene oil of benzene institute output respectively by debenzolizing tower 1 cat head and side line extraction, rich oil de-benzene becomes and enters debenzolizing tower 1 tower still after oil-poor, oil-poor first part in the tower still enters 2 heating of debenzolizing tower tube furnace, send debenzolizing tower 1 and rich oil mixed heat transfer back to by debenzolizing tower 1 tower still top again after the heating, taking off benzene for the distillation of rich oil provides heat; For returning debenzolizing tower 1 after the oil-poor heating of convenient described first part, the oil-poor inlet of cycling hot A can be set on debenzolizing tower 1 sidewall, the oil-poor inlet of cycling hot A is between the tower still and tower tray of debenzolizing tower 1, after oil-poor first part entered 2 heating of debenzolizing tower tube furnace in the described tower still, A was back in the debenzolizing tower 1 by the oil-poor inlet of cycling hot; Flow through successively poor oil-rich heat exchanger 11, oil-poor one section water cooler 12 and oil-poor two sections water coolers 13 of oil-poor second section in the tower still are sent the recycle of whole cold wash benzene workshop section after being cooled to 25-30 ℃ back to.Lean oil flow is cooled off with the rich oil heat exchange of the poor oil-rich heat exchanger 11 of flowing through in poor oil-rich heat exchanger 11 processes.
Oil-poor and rich oil of the present invention all is a washing oil, promptly becomes rich oil behind the oil-poor absorption benzene, promptly becomes again oil-poor behind the rich oil de-benzene.
In order to keep the quality of circulating washing oil, the oil-poor regenerator column 3 of sending into of the 1-1.5% with second section in the described debenzolizing tower 1 tower still in oil-poor distills manipulation of regeneration; Manipulation of regeneration makes most of oil-poor oil gas that is evaporated into, and the oil gas of generation is mixed with rich oil by overflow oil-poor in the tower still that enters debenzolizing tower 1 bottom and debenzolizing tower 1 of regenerator column 3 cats head; The residual oil that regeneration generates is positioned at regenerator column 3 tower stills, residual oil in the regenerator column 3 tower stills, wherein first part directly is sent to the tar vat in tar workshop, second section is delivered to 4 heating of regenerator column tube furnace, be heated to residual oil after 320 ℃ and send regenerator column 3 back to and mixes, distill the regenerated thermals source as regenerator column 3 with residual oil in the regenerator column 3 tower stills.
For improving the production efficiency of light benzene, in process of production, vacuumize with 10 pairs of debenzolizing towers 1 of vacuum pump and regenerator column 3, make and form negative pressure in debenzolizing tower 1 and the regenerator column 3, learn through the repeated multiple times demonstration, when debenzolizing tower 1 tower top pressure be controlled at-70KPa is to-20KPa, debenzolizing tower 1 tower still pressure-80KPa is to-30KPa, regenerator column 3 tower top pressures-80KPa is to-30KPa, and regenerator column 3 tower still pressure-85KPa are during to-35KPa, and it is most effective that light benzene generates.
For ease of reclaiming light benzene, through experiment repeatedly, temperature is controlled at 50 ℃ in the time of the light benzene steam of distillation output in the debenzolizing tower 1 should being overflowed by debenzolizing tower 1 top, and will send in the oil gas interchanger 8 by the light benzene steam that debenzolizing tower 1 is overflowed and carry out heat exchange with rich oil, make the light benzene steam become 50 ℃ liquid, then light benzene liquid enters condensate cooler, phlegma advances light benzene return tank 7, after light benzene in the light benzene return tank 7 separated water outlet, a part was back to debenzolizing tower 1, and another part is as the product extraction; The side line semen collection heavy benzol and the naphtalene oil of debenzolizing tower.The light benzene steam flow both can reach the purpose of cooling again to the rich oil heating of the oil gas interchanger 8 of flowing through when oil gas interchanger 8, can save the energy effectively, simplify technical process.
For the efficient of guaranteeing rich oil de-benzene distillation and regenerator column 3 distillation regeneration washing oil reaches best, prove through repeated multiple times, temperature in debenzolizing tower 1 and the regenerator column 3 should be controlled at following scope: debenzolizing tower 1 tower top temperature 50-55 ℃, 228-230 ℃ of debenzolizing tower 1 tower still temperature, and 245-250 ℃ of regenerator column tower top temperature, 310-320 ℃ of tower still temperature.
Claims (5)
1, a kind of rich oil de-benzene process, it is characterized in that: the rich oil that whole cold wash benzene workshop section sends here is sent into oil gas interchanger (8) heat exchange, enter poor oil-rich heat exchanger (11) heat exchange afterwards, the rich oil heat exchange enters debenzolizing tower tube furnace (2) after about 160-180 ℃ and further is heated to 190-200 ℃, then sends into debenzolizing tower (1) and distills and take off benzene; The light benzene of benzene institute output is taken off in distillation, refined heavy benzole and naphtalene oil are respectively by debenzolizing tower (1) cat head and side line extraction, rich oil de-benzene becomes and enters debenzolizing tower (1) tower still after oil-poor, oil-poor first part in the tower still enters debenzolizing tower tube furnace (2) heating, send debenzolizing tower (1) and rich oil mixed heat transfer back to by debenzolizing tower (1) tower still top again after the heating, for the distillation of rich oil provides heat, the oil-poor second section poor oil-rich heat exchanger (11) of flowing through successively in the tower still, oil-poor one section water cooler (12) and oil-poor two sections water coolers (13) are sent the recycle of whole cold wash benzene workshop section after being cooled to 25-30 ℃ back to.
2, require described a kind of rich oil de-benzene method as right 1, it is characterized in that: oil-poor regenerator column (3) manipulation of regeneration of sending into of the 1-1.5% with second section in described debenzolizing tower (1) the tower still in oil-poor; The oil gas that manipulation of regeneration generates is sent in the debenzolizing tower (1) by the outflow of regenerator column (3) cat head and the oil-poor and rich oil in the tower still of debenzolizing tower (1) mixes; The residual oil that regeneration generates is positioned at regenerator column (3) tower still, residual oil in regenerator column (3) the tower still, wherein first part directly is sent to the tar vat in tar workshop, second section is delivered to regenerator column tube furnace (4) heating, and the residual oil after the heating is sent the interior residual oil of regenerator column (3) and regenerator column (3) tower still back to and mixed.
3, require described a kind of rich oil de-benzene method as right 2, it is characterized in that: debenzolizing tower (1) and regenerator column (3) are vacuumized with vacuum pump (10), make and form negative pressure in debenzolizing tower (1) and the regenerator column (3), debenzolizing tower (1) tower top pressure is controlled at-and 70KPa is to-20KPa, debenzolizing tower (1) tower still pressure-80KPa is to-30KPa, regenerator column (3) tower top pressure-80KPa is to-30KPa, and regenerator column (3) tower still pressure-85KPa is to-35KPa.
4, require described a kind of rich oil de-benzene method as right 3, it is characterized in that: tower top temperature 50-55 ℃ of debenzolizing tower (1), 228-230 ℃ of debenzolizing tower (1) tower still temperature.
5, require described a kind of rich oil de-benzene method as right 3, it is characterized in that: 245-250 ℃ of regenerator column tower top temperature, 310-320 ℃ of tower still temperature.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100165357A CN101597517B (en) | 2009-06-17 | 2009-06-17 | Rich oil de-benzene process |
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| Application Number | Priority Date | Filing Date | Title |
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| CN2009100165357A CN101597517B (en) | 2009-06-17 | 2009-06-17 | Rich oil de-benzene process |
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| CN101597517A true CN101597517A (en) | 2009-12-09 |
| CN101597517B CN101597517B (en) | 2012-05-23 |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102199070A (en) * | 2011-04-06 | 2011-09-28 | 上海同特化工科技有限公司 | Tubular furnace method pressure-reduced debenzolization and distillation process |
| CN104119962A (en) * | 2013-04-26 | 2014-10-29 | 江苏沂州煤焦化有限公司 | Technology for heating rich oil by coke oven flue gas waste heat |
| CN107628923A (en) * | 2017-09-29 | 2018-01-26 | 王书虎 | A kind of negative pressure benzene removal system and method for rich oil half |
| CN107890684A (en) * | 2017-12-22 | 2018-04-10 | 中冶焦耐(大连)工程技术有限公司 | A kind of reboiler method negative pressure crude benzol Distallation systm |
| CN110330997A (en) * | 2019-07-10 | 2019-10-15 | 成渝钒钛科技有限公司 | Crude benzol recovery rate method for improving |
| CN110776962A (en) * | 2019-10-11 | 2020-02-11 | 临涣焦化股份有限公司 | Device and method for heating rich oil and removing benzene by using waste heat of coke oven ascending pipe |
| CN113150840A (en) * | 2021-04-23 | 2021-07-23 | 济南冶金化工设备有限公司 | Self-azeotropic negative pressure debenzolization process |
| CN113790626A (en) * | 2021-09-08 | 2021-12-14 | 山东博宇重工科技有限公司 | Lean oil cooling process |
| CN113999703A (en) * | 2021-10-28 | 2022-02-01 | 宣化钢铁集团有限责任公司 | System and process for efficiently eluting benzene hydrocarbon in coke oven gas |
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| US3312749A (en) * | 1963-07-24 | 1967-04-04 | Bethlehem Steel Corp | Removal of aromatic compounds from coke oven gas |
| JPS50126623A (en) * | 1974-03-19 | 1975-10-04 | ||
| CN1008276B (en) * | 1988-04-04 | 1990-06-06 | 冶金工业部鞍山焦化耐火材料设计研究院 | Single tower debenzolizing process and new model of debenzolizing tower |
| CN2429523Y (en) * | 2000-05-31 | 2001-05-09 | 孟宪洲 | Apparatus for recovering and purifying waste water and gasses from coke oven |
| CN100488924C (en) * | 2007-03-21 | 2009-05-20 | 鞍钢股份有限公司 | Crude benzene forced heat exchange process |
| CN101289633A (en) * | 2007-04-20 | 2008-10-22 | 宝山钢铁股份有限公司 | Novel regeneration process for circulation oil of crude benzol device |
| CN101270304B (en) * | 2008-05-09 | 2011-01-12 | 攀钢集团钢铁钒钛股份有限公司 | Fine purification technique for coke oven gas |
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2009
- 2009-06-17 CN CN2009100165357A patent/CN101597517B/en active Active
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102199070A (en) * | 2011-04-06 | 2011-09-28 | 上海同特化工科技有限公司 | Tubular furnace method pressure-reduced debenzolization and distillation process |
| CN102199070B (en) * | 2011-04-06 | 2013-06-12 | 上海同特化工科技有限公司 | Tubular furnace method pressure-reduced debenzolization and distillation process |
| CN104119962A (en) * | 2013-04-26 | 2014-10-29 | 江苏沂州煤焦化有限公司 | Technology for heating rich oil by coke oven flue gas waste heat |
| CN107628923A (en) * | 2017-09-29 | 2018-01-26 | 王书虎 | A kind of negative pressure benzene removal system and method for rich oil half |
| CN107890684A (en) * | 2017-12-22 | 2018-04-10 | 中冶焦耐(大连)工程技术有限公司 | A kind of reboiler method negative pressure crude benzol Distallation systm |
| CN107890684B (en) * | 2017-12-22 | 2023-06-16 | 中冶焦耐(大连)工程技术有限公司 | Reboiler method negative pressure crude benzol distillation system |
| CN110330997A (en) * | 2019-07-10 | 2019-10-15 | 成渝钒钛科技有限公司 | Crude benzol recovery rate method for improving |
| CN110776962A (en) * | 2019-10-11 | 2020-02-11 | 临涣焦化股份有限公司 | Device and method for heating rich oil and removing benzene by using waste heat of coke oven ascending pipe |
| CN113150840A (en) * | 2021-04-23 | 2021-07-23 | 济南冶金化工设备有限公司 | Self-azeotropic negative pressure debenzolization process |
| CN113790626A (en) * | 2021-09-08 | 2021-12-14 | 山东博宇重工科技有限公司 | Lean oil cooling process |
| CN113999703A (en) * | 2021-10-28 | 2022-02-01 | 宣化钢铁集团有限责任公司 | System and process for efficiently eluting benzene hydrocarbon in coke oven gas |
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| CN101597517B (en) | 2012-05-23 |
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