CN103525459B - Gasoline selective hydrogenation products separating technology - Google Patents
Gasoline selective hydrogenation products separating technology Download PDFInfo
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- CN103525459B CN103525459B CN201310472363.0A CN201310472363A CN103525459B CN 103525459 B CN103525459 B CN 103525459B CN 201310472363 A CN201310472363 A CN 201310472363A CN 103525459 B CN103525459 B CN 103525459B
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Abstract
The present invention relates to a kind of gasoline selective hydrogenation products separating technology, this technique is by the mode of hot high score separator in conjunction with cold high pressure separator, using pre-hydrogenation desulfurization product through the oily charging as gasoline Cutting Tap of the isolated hot high score of high pressure hot separator, Cutting Tap operation energy consumption is reduced; Hot high score gas is entered cold high pressure separator again after air cooler and water cooler condensation, separate cold high score oil and cold high score gas, be re-used as the charging of gasoline Cutting Tap by after cold high score oil and heavy petrol heat exchange, the heat of heavy petrol recycled, reduces Cutting Tap working load; Cold high pressure separator inside does not need to establish coalescer, reduces the equipment requirements of cold high pressure separator, and facility investment expense is reduced, and working cost reduces the present invention can recovered energy to greatest extent, decreases the input of equipment.
Description
Technical field
The present invention relates to a kind of technical field of petrochemical industry, relate in particular to a kind of gasoline selective hydrogenation products separating technology.
Background technology
In recent years, adopt Hydrofining Technology to improve gasoline product quality, the technique of producing clean gasoline is developed rapidly, and state of the art obtains great raising.But according to pertinent data introduction, the heat supplied of domestic hydro-refining unit process furnace is much larger than the heat supplied of external same device, and the heat supplied of heat exchange is less than external same device.As can be seen here, domestic hydro-refining unit, compared with external advanced means, also has certain gap, is mainly the calorific loss caused in the sepn process of product.
The separation process of hydrocracking reaction product has cold high score flow process and hot high score flow process usually.Usual total overall reaction product is called cold high score flow process through the flow process of air cooler laggard row gas-liquid separation; And total overall reaction product first carries out a gas-liquid separation at certain temperature, the oil gas flashed off carries out the flow process of secondary separation again after heat exchange and air cooling, is called hot high score flow process.
Cold high score flow process is with hot high score flow process because heat exchange is different, and energy recovery utilizes different.Under normal circumstances, the energy consumption comparing separately these two kinds of flow processs is very difficult.But no matter cold high score flow process or hot high score flow process, as long as all cannot recycle through the energy of the cooling of reactive moieties air cooler.The load of the reactive moieties air cooler relatively in these two kinds of flow processs, can obtain the energy that hot high score flow process is saved.But owing to have employed hot high score flow process, the energy reclaimed through hydraulic turbine can reduce.
Although hot high score flow process exists reduce plant energy consumption, reduce cold advantage of changing area, especially can reduce air cooler for extremely frigid zones to congeal the generation of phenomenon, and for recycle to extinction flow process, be conducive to preventing the accumulation of condensed-nuclei aromatics and the phenomenon of high-pressure air cooler occurs to block, but there is the larger shortcoming of hydrogen loss in hot high score flow process.Because hydrogen loss increases, compressor power can increase, hydrogen recovery and disengagement section energy consumption increase thereupon.
In a word, how effectively to reduce energy consumption, to greatest extent recovered energy, the input reducing equipment is the key that current hot high score flow process is able to widespread use.
Summary of the invention
The object of the invention is to the defect overcoming above-mentioned prior art, one is provided effectively to reduce energy consumption, recovered energy to greatest extent, the input of minimizing equipment effectively can reduce sulphur content, higher octane value can be ensured again simultaneously, and technique is simple, the gasoline selective hydrogenation products separating technology that cost of investment is low.
Technical scheme taked for achieving the above object is:
A kind of gasoline selective hydrogenation products separating technology, is characterized in that comprising the following steps:
(1) first hot high score oil and hot high score gas is isolated by the pre-hydrogenation desulfurization product feeding high pressure hot separator after hydrogenation, desulphurization reaction, wherein hot high score gas is after air cooler, water cooler condensation, enter in cold high pressure separator and be separated, obtain cold high score oil and cold high score gas;
(2) hot high score oil step (1) obtained and cold high score oil are sent in gasoline Cutting Tap, tower top cuts out petroleum naphtha, tower undercutting goes out heavy petrol, after this heavy petrol and cold high score oil carry out heat exchange, mix with recycle hydrogen, after reaction heating furnace heating, enter heavy petrol hydrodesulphurisatioreactors reactors and carry out hydrodesulfurization reaction, obtain heavy petrol hydrogenating desulfurization product;
(3) the heavy petrol hydrogenating desulfurization product that step (2) obtains is entered last running cold high pressure separator after heat exchange, condensation to be separated, top separates the cold high score gas of heavy oil, and bottom separates heavy petrol;
(4) heavy petrol step (3) obtained is sent into stripping tower and is refined, and tower top separates petroleum naphtha, separates treated gasoline at the bottom of tower.
Send into recycle hydrogen coalescer after the cold high score gas mixing described step (1) and step (3) obtained, isolate recycle hydrogen and light oil, wherein recycle hydrogen mixes with new hydrogen and recycles after desulfurization.
The present invention, by the mode of high pressure hot separator in conjunction with cold high pressure separator, using pre-hydrogenation desulfurization product through the oily hot feed as gasoline Cutting Tap of the isolated hot high score of high pressure hot separator, makes Cutting Tap operation energy consumption reduce.Isolated for high pressure hot separator high heat point gas is entered cold high pressure separator again after air cooler and water cooler condensation, isolate cold high score oil and cold high score gas, are re-used as the charging of gasoline Cutting Tap after the heavy petrol heat exchange that cold high score oil and the undercutting of gasoline Cutting Tap are gone out, the heat of heavy petrol is recycled.Hot high score oil and cold high score oil content not from the charging of Cutting Tap different positions, reduction Cutting Tap working load, the petroleum naphtha that Cutting Tap is cut out and heavy petrol are closer to the requirement of clean gasoline; Cold high pressure separator inside does not need to establish coalescer, reduces the equipment requirements of cold high pressure separator, and facility investment expense is reduced, and working cost reduces; Light oil cold high score gas and heavy oil cold high score gas share same recycle hydrogen coalescer, reduce facility investment, and recycle hydrogen coalescer inside is provided with swirler simultaneously, ensure that separating effect.
Accompanying drawing explanation
Fig. 1 is process flow sheet of the present invention, and in figure, the meaning of each numbering representative is as follows:
1: from pre-hydrogenation desulfurization product; 2: petroleum naphtha; 3: recycle hydrogen; 4: refining heavy petrol; 5: light oil; 6: desulphurization circulating hydrogen; 7: rich amine solution.
1-1: high pressure hot separator; 1-2: hot high score gas air cooler; 1-3: hot high score water cooler; 1-4: cold high pressure separator; 1-5: interchanger; 1-6: gasoline Cutting Tap; 1-7: process furnace; 1-8: heavy petrol hydrodesulphurisatioreactors reactors; 1-9: interchanger; 1-10: hydrogenation products air cooler; 1-11: heavy fractioning hydrogenation product aftercooler; 1-12: last running cold high pressure separator; 1-13: stripping tower; 1-14: recycle hydrogen coalescer; 1-15: desulphurization of recycle hydrogen tower.
Embodiment
1, after catalytically cracked gasoline removal of impurities, incoming stock surge tank, through the boosting of catalytic gasoline pump, mixes laggard selectable hydrogenator, removes diolefine, then enter pre-hydrodesulphurisatioreactors reactors removal activity sulphur with recycle hydrogen.
2, the pre-hydrogenation desulfurization product 1 after desulfurization is through high pressure hot separator 1-1, carry out gas-liquid separation, the hot high score oil that bottom separates is as the charging of gasoline Cutting Tap 1-6, the hot high score gas that top separates is after air cooler 1-2, water cooler 1-3 condensation, enter cold high pressure separator 1-4, separate cold high score gas and cold high score oil.
3, the cold high score oil that separates of the above-mentioned hot high score oil that separates using high pressure hot separator 1-1 and cold high pressure separator 1-4 is as the charging of gasoline Cutting Tap 1-6, gasoline Cutting Tap 1-6 is entered from different positions, tower top cuts out petroleum naphtha 2, tower undercutting goes out heavy petrol, after the cold high score oil that this heavy petrol and cold high pressure separator 1-4 separate carries out heat exchange (carrying out in interchanger 5), mix with recycle hydrogen 3, enter heavy petrol hydrodesulphurisatioreactors reactors 1-8 through process furnace 1-7 heating and carry out hydrodesulfurization reaction, obtain heavy petrol hydrogenating desulfurization product.
4, above-mentioned heavy petrol hydrogenating desulfurization product is after interchanger 1-9 heat exchange, hydrogenation products air cooler 1-10 and heavy fractioning hydrogenation product aftercooler 1-11 condensation, enter last running cold high pressure separator 1-12 to be separated, top separates the cold high score gas of heavy oil, and bottom separates heavy petrol.
5, heavy oil cold high score gas and the cold high score gas in process are joined and are sent into recycle hydrogen coalescer 1-14 afterwards in said process (4), separate recycle hydrogen and light oil 5.Recycle hydrogen mixes with new hydrogen after sending into desulphurization of recycle hydrogen tower 1-15 desulfurization again, and point two-way is used for selective hydrogenation and heavy fractioning hydrogenation desulphurization reaction.
6, the heavy petrol that last running cold high pressure separator 1-12 separates is sent into stripping tower 1-13 and is refined.Stripping tower top separates petroleum naphtha 2, separates treated gasoline 4 at the bottom of tower.
Claims (1)
1. a gasoline selective hydrogenation products separating technology, is characterized in that comprising the following steps:
(1) first hot high score oil and hot high score gas is isolated by the pre-hydrogenation desulfurization product feeding high pressure hot separator after hydrogenation, desulphurization reaction, wherein hot high score gas is after air cooler, water cooler condensation, enter in cold high pressure separator and be separated, obtain cold high score oil and cold high score gas;
(2) heat high wind oil step (1) obtained and cold high score oil are sent in gasoline Cutting Tap, tower top cuts out petroleum naphtha, tower undercutting goes out heavy petrol, after this heavy petrol and cold high score oil carry out heat exchange, mix with recycle hydrogen, after reaction heating furnace heating, enter heavy petrol hydrodesulphurisatioreactors reactors and carry out hydrodesulfurization reaction, obtain heavy petrol hydrogenating desulfurization product;
(3) the heavy petrol hydrogenating desulfurization product that step (2) obtains is entered last running cold high pressure separator after heat exchange, condensation to be separated, top separates the cold high score gas of heavy oil, and bottom separates heavy petrol;
(4) heavy petrol step (3) obtained is sent into stripping tower and is refined, and tower top separates petroleum naphtha, separates treated gasoline at the bottom of tower;
Send into recycle hydrogen coalescer after the cold high score gas mixing described step (1) and step (3) obtained, isolate recycle hydrogen and light oil, wherein recycle hydrogen mixes with new hydrogen and recycles after desulfurization.
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| CN201310472363.0A CN103525459B (en) | 2013-10-11 | 2013-10-11 | Gasoline selective hydrogenation products separating technology |
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| CN201310472363.0A CN103525459B (en) | 2013-10-11 | 2013-10-11 | Gasoline selective hydrogenation products separating technology |
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| CN103525459B true CN103525459B (en) | 2015-09-02 |
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| CN104403685B (en) * | 2014-09-27 | 2016-04-20 | 宁夏宝塔石化科技实业发展有限公司 | A kind of sulfuration process of gasoline selective hydrodesulfurizationmodification device |
| CN104403687B (en) * | 2014-09-27 | 2016-08-24 | 宁夏宝塔石化科技实业发展有限公司 | A kind of energy-saving method of gasoline selective hydrodesulfurizationmodification device |
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| CN1234815C (en) * | 2002-08-29 | 2006-01-04 | 中国石油化工股份有限公司 | Method of gasoline desulfurization |
| CN103087770A (en) * | 2011-10-28 | 2013-05-08 | 江苏佳誉信实业有限公司 | Clean gasoline production method through selective hydrogenation and desulfurization of catalytic gasoline |
| CN103289739A (en) * | 2012-02-29 | 2013-09-11 | 中国科学院大连化学物理研究所 | Method for modification by coupling hydrodesulfurization of FCC (Fluid Catalytic Cracking) gasoline and aromatization of liquefied petroleum gas |
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