CN101597517B - Rich oil de-benzene process - Google Patents
Rich oil de-benzene process Download PDFInfo
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- CN101597517B CN101597517B CN2009100165357A CN200910016535A CN101597517B CN 101597517 B CN101597517 B CN 101597517B CN 2009100165357 A CN2009100165357 A CN 2009100165357A CN 200910016535 A CN200910016535 A CN 200910016535A CN 101597517 B CN101597517 B CN 101597517B
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Abstract
The invention discloses a rich oil de-benzene process, comprising the following steps: the rich oil from the final cooling benzol scrubbing unit is sent into a gas and oil exchanger to heat, then the oil is sent into a heat exchanger between lean oil and rich-oil to heat; the rich oil is heated to 160-180 DEG C and introduced to a de-benzene pipe tower type furnace to further heat to 190-200 DEG C, then the oil is sent to a de-benzene tower to remove benzene by distillation; the light benzene, fine heavy benzene and naphthalene oil produced by distillation de-benzene are extracted respectively from the overhead and side line of the de-benzene tower; after removing benzene, the rich oil is converted to lean oil and then sent to the tower pot; the first part of the lean oil in the tower pot is sent to the de-benzene pipe tower type furnace to heat and then sent back to the de-benzene tower from the upside of the tower pot of the de-benzene tower to provide energy for the distillation of rich oil; the second part of lean oil in the tower pot flows through the heat exchanger between lean oil and rich-oil, lean oil first chiller and lean oil second chiller to cool to 25-30 DEG C, and then the lean oil is sent back to the final cooling benzol scrubbing unit to recycle. The process can meet the demand of the final cooling benzol scrubbing recycling, has no out-emission of exhaust gas and waste water, simpler procedures, environmental friendliness and higher de-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 the 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 process 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, be prone to 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 realizes that through following technical scheme a kind of rich oil negative pressure benzene removal novel process comprises the steps: for realizing above-mentioned purpose
A kind of rich oil de-benzene process; The rich oil that whole cold wash benzene workshop section sees off is sent into the heat exchange of oil gas interchanger; Get into the poor oil-rich heat exchanger heat exchange afterwards, the rich oil heat exchange gets into 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; Light benzene, refined heavy benzole and naphtalene oil that benzene institute output is taken off in distillation are respectively by debenzolizing tower cat head and side line extraction; Become oil-poor entering debenzolizing tower tower still behind the rich oil de-benzene; Oil-poor first part in the tower still gets into 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 said debenzolizing tower tower still in oil-poor oil-poor sent into regenerator column regeneration; The oil gas that regeneration back generates is flowed out oil-poor in the tower still of sending in the debenzolizing tower with debenzolizing tower to be mixed with rich oil by the regenerator column cat head; 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 regeneration Tata still.
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, and 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: the oil-poor debenzolizing tower that after tube furnace heats, returns of the portion of hot in its debenzolizing tower still capable of using substitutes 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 from washing oil, separate, and 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 condensing surfaces; 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 according to the invention is following:
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 gets into poor oil-rich heat exchanger 11 heat exchange; Get into debenzolizing tower tube furnace 2 after the rich oil temperature reaches about 160-180 ℃, send into debenzolizing tower 1 after debenzolizing tower tube furnace 2 further is heated to 190-200 ℃ with the temperature of rich oil and distill and take off benzene; Light benzene, refined heavy benzole and naphtalene oil that benzene institute output is taken off in distillation are respectively by debenzolizing tower 1 cat head and side line extraction; Rich oil de-benzene becomes oil-poor back and gets into debenzolizing tower 1 tower still; Oil-poor first part in the tower still gets into 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 got into 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 are washing oil, promptly become rich oil behind the oil-poor absorption benzene, promptly become 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 said 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-poor and rich oil that the oil gas of generation is overflowed in the tower still that gets into debenzolizing tower 1 bottom and debenzolizing tower 1 by regenerator column 3 cats head mixes; 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 regenerator column tube furnace 4 heating, is heated to residual oil after 320 ℃ and sends regenerator column 3 back to and mix with residual oil in the regenerator column 3 tower stills, distills the regenerated thermals source as regenerator column 3.
For improving the production efficiency of light benzene, in process of production, vacuumize with 10 pairs of debenzolizing towers of vacuum pump 1 and regenerator column 3; Make in debenzolizing tower 1 and the regenerator column 3 and form negative pressure, 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-85KP a are during to-35KP a, 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 should the light benzene steam of distillation output in the debenzolizing tower 1 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 gets into 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; Should debenzolizing tower 1 and regenerator column 3 interior temperature 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 (3)
1. 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; Get into poor oil-rich heat exchanger (11) heat exchange afterwards; The rich oil heat exchange gets into debenzolizing tower tube furnace (2) after 160-180 ℃ and further is heated to 190-200 ℃, then sends into debenzolizing tower (1) distillation and takes off benzene; Light benzene, refined heavy benzole and naphtalene oil that benzene institute output is taken off in distillation are respectively by debenzolizing tower (1) cat head and side line extraction; Rich oil de-benzene becomes oil-poor back and gets into debenzolizing tower (1) tower still; Oil-poor first part in the tower still gets into 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, 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; Oil-poor regenerator column (3) manipulation of regeneration of sending into of 1-1.5% with second section in said debenzolizing tower (1) the tower still in oil-poor; The oil gas that manipulation of regeneration generates is flowed out to send in the debenzolizing tower (1) by regenerator column (3) cat head and mixes with the interior oil-poor and rich oil of the tower still of debenzolizing tower (1); 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 regenerator column (3) back to and mixed with the interior residual oil of regenerator column (3) tower still; With vacuum pump (10) debenzolizing tower (1) and regenerator column (3) are vacuumized; Make and form negative pressure in debenzolizing tower (1) and the regenerator column (3); Debenzolizing tower (1) tower top pressure is controlled at-70 kPa to-20kPa; Debenzolizing tower (1) tower still pressure-80 kPa is to-30 kPa, and regenerator column (3) tower top pressure-80 kPa is to-30 kPa, and regenerator column (3) tower still pressure-85 kPa is to-35 kPa.
2. require described a kind of rich oil de-benzene process like right 1, it is characterized in that: tower top temperature 50-55 ℃ of debenzolizing tower (1), 228-230 ℃ of debenzolizing tower (1) tower still temperature.
3. require described a kind of rich oil de-benzene process like right 1, 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 |
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| 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 CN101597517A (en) | 2009-12-09 |
| CN101597517B true CN101597517B (en) | 2012-05-23 |
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Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| 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 |
| CN113150840B (en) * | 2021-04-23 | 2023-03-28 | 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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