CN102126914B - Extractive distillation process in hydrofining process of crude benzene - Google Patents
Extractive distillation process in hydrofining process of crude benzene Download PDFInfo
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- CN102126914B CN102126914B CN201110007235XA CN201110007235A CN102126914B CN 102126914 B CN102126914 B CN 102126914B CN 201110007235X A CN201110007235X A CN 201110007235XA CN 201110007235 A CN201110007235 A CN 201110007235A CN 102126914 B CN102126914 B CN 102126914B
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Abstract
The invention relates to an extractive distillation process in the hydrofining process of crude benzene. The process comprises the following steps: 1) extractant enters from the top of an extractive distillation column, hydrotreated oil enters from the middle of the extractive distillation column; and the tower top product enters a stripping tower in a gaseous phase mode; 2) the tower top product of the extractive distillation column enters the stripping tower to perform distillation purification, the non-arene product in the top of the stripping tower is discharged, the heavy phase product at the bottom of the stripping tower is sent to a liquid-liquid separating tank by a pump; and 3) in the liquid-liquid separating tank, liquid is collected to obtain a heavy phase product and a light phase product, the heavy phase product containing extractant and arene are sent back to the extractive distillation column; and the light phase product, namely non-arene is sent back to the stripping tower. By adopting the process, the heavy non-arene can be effectively prevented from being sent to the extraction section of the extractive distillation column and the quality of product can be increased; and the total height of the extractive distillation column can be reduced, the manual operation is convenient to perform and the problem that the lack of heat caused by the overhigh extractive distillation column can be avoided.
Description
Technical field
The present invention relates to the extractive distillation technique in a kind of crude benzol raw material unifining process.
Background technology
At present, in the industrial crude benzene refining process, hydrogenated oil through hydrogenation workshop section, because the low temperature hydrogenation reaction conditions is gentle, a large amount of non-aromaticss is followed among hydrogenated oil, as not removing, must be mixed in the product, to greatly affect quality product, so the separation behind the low temperature hydrogenation at first must be removed non-aromatics.Because the boiling point of non-aromatics and the boiling point of benzene are very approaching, common distillation is difficult to remove, and therefore need to take effective ways to separate.
In hydrogenated oil, separate at present the method that non-aromatics generally adopts, be divided into liquid-phase extraction method and extractive distillation method two large class techniques by processing mode; Liquid-phase extraction technique is fit to the wider raw material of variation range, and especially when non-aromatics content was very high, it had some superiority aspect energy consumption, but technical process is longer, and number of devices is various, and this has just brought construction investment large, operation, maintenance difficulty, the large series of problems that waits of extraction agent loading level.
The extractive distillation technical process is short, and number of devices is few, by using extraction agent different, tetramethylene sulfone, N-N-formyl morpholine N-etc. is arranged again.Fig. 1 is existing extractive distillation technique, its equipment comprises extraction distillation column C-101, backflash D-101, cat head water cooler E-101, reboiler E-102, pump P-102, pump P-101, the raw mix hydrogenated oil in extraction distillation column through extraction agent extractive distillation, the overhead extraction non-aromatics, rich extraction agent is sent into recovery tower through the effect of pump P-102 at the bottom of the tower.Reclaim overhead extraction aromatic hydrocarbons, poor extraction agent returns extraction tower and recycles at the bottom of the tower.
Although above-mentioned Technology all can satisfy the specification of quality to product, and technique is all very ripe, because it is more to separate required stage number, about 80 polylith column plates, and also stripping section loads littlely owing to liquid phase, and tower diameter is thinner.Cause extraction distillation column aspect height, to be unfavorable for on-the-spot employee's operation.In whole device, be higher than about 20 meters of other rectifying tower, thereby be unfavorable for on-the-spot employee's operation on the service platform of setting.Simultaneously, be easy to produce the middle heat loss owing to full tower is higher and cause the phenomenon of heat supply deficiency, thereby cause component heavier in the non-aromatics that cat head is overflowed under the effect that refluxes, to return easily the extraction section of extraction distillation column.
Summary of the invention
The purpose of this invention is to provide the extractive distillation technique in a kind of hydrofining process of crude benzene, this technique can prevent effectively that heavy non-aromatics from returning the extraction section of extraction distillation column, improves the quality of product; Reduced simultaneously the full tower height degree of extraction distillation column, made things convenient for workman's operation, avoided because the not enough problem of the heat supply that the extraction distillation column excessive height causes.
For achieving the above object, the present invention is achieved through the following technical solutions:
Extractive distillation technique in a kind of hydrofining process of crude benzene, this technique comprises the steps:
1) extraction agent enters from the extractive distillation top of tower, and hydrogenated oil enters at the extraction distillation column middle part; Overhead product enters to carry with the form of gas phase and heats up in a steamer tower, and extraction agent and aromatic hydrocarbons drain into next unit in the extraction distillation column tower reactor;
2) extraction distillation column top gaseous phase product introduction is carried and is heated up in a steamer tower and carry out rectification and purification, heats up in a steamer column overhead non-aromatics product and sends carrying, and carries the heavy phase product that heats up in a steamer at the bottom of the Tata and sends into liquid liquid separator tank through the effect of pump;
3) in liquid liquid separator tank, be divided into heavy phase product and light mutually product after the fluid accumulation, heavy phase product extraction agent and aromatic hydrocarbons return extraction distillation column; Light phase product non-aromatics is returned to carry and is heated up in a steamer tower.
The stage number of described extraction distillation column is the 60-80 piece.
The described stage number of heating up in a steamer tower of carrying is the 5-20 piece.
The equipment of realizing described technique comprises extraction distillation column, carries and heat up in a steamer tower, liquid liquid separator tank, backflash, cat head water cooler; Carry and heat up in a steamer the tower bottom and be provided with kettle-type reboiler, the extraction distillation column top exit heats up in a steamer the tower sidepiece and is connected with carrying, and carries and heats up in a steamer tower bottom connecting fluid liquid separator tank, and liquid liquid separator tank is connected with the extraction distillation column sidepiece; Carry and heat up in a steamer top of tower and connect the cat head water cooler, the other end of cat head water cooler connects backflash, and backflash heats up in a steamer top of tower and is connected with carrying.
Compared with prior art, the invention has the beneficial effects as follows:
1) prevents that heavier non-aromatics from falling back to the extraction section in the extraction distillation column, improve the quality of product.
2) because having reduced the extraction distillation column height, prevent that tower bottom heating from crossing senior general and overflowing from cat head as the benzene of bottom product.
3) compare with former technique, effectively reduce the operation height of extraction distillation column, handled easily.
Description of drawings
Fig. 1 is the schema of existing extractive distillation technique;
Among Fig. 1: C-101 extraction distillation column E-102 extraction distillation column reboiler P-102 pump D-101 backflash P-101 pump D-101 backflash
Fig. 2 is extractive distillation process flow sheet of the present invention.
Among Fig. 2: C-201 extraction distillation column C-202 carries and heats up in a steamer tower E-201 cat head water cooler D-201 backflash E-202 and carry and heat up in a steamer tower reboiler E-203 extraction distillation column reboiler D-202 liquid liquid separator tank P-201 pump P-202 pump P-203 pump
Embodiment
The invention will be further described below in conjunction with the drawings and the specific embodiments.
See Fig. 2, the extractive distillation technique in a kind of hydrofining process of crude benzene, equipment comprises extraction distillation column C-201, carries and heat up in a steamer tower C-202, liquid liquid separator tank D-202, backflash D-201, cat head water cooler E-201; Carry and heat up in a steamer tower C-202 bottom and be provided with kettle-type reboiler E-202, extraction distillation column C-201 top exit heats up in a steamer tower C-202 sidepiece and is connected with carrying, carry and heat up in a steamer tower C-202 bottom connecting fluid liquid separator tank D-202, liquid liquid separator tank D-202 is connected with extraction distillation column C-201 sidepiece; Carry and heat up in a steamer tower C-202 top and connect cat head water cooler E-201, the other end of cat head water cooler E-201 connects backflash D-201, and backflash D-201 heats up in a steamer top of tower C-202 and is connected with carrying.
Extractive distillation technique in a kind of hydrofining process of crude benzene, this technique comprises the steps:
1) extraction agent enters extraction distillation column from extraction distillation column C-201 top, and hydrogenated oil enters extraction distillation column C-201 at the extraction distillation column middle part; Overhead product enters to carry with the form of gas phase and heats up in a steamer tower C-202, and extraction agent and aromatic hydrocarbons drain into next unit in extraction distillation column C-201 tower reactor;
2) extraction distillation column C-201 top gaseous phase product mainly is non-aromatics and with a small amount of aromatic hydrocarbons and extraction agent, it enters to carry heating up in a steamer and carries out rectification and purification among the tower C-202, heat up in a steamer tower C-202 cat head non-aromatics product and send carrying, carry the heavy phase product that heats up in a steamer at the bottom of the tower C-202 tower and enter liquid liquid separator tank D-202 through the effect of pump P-202;
3) in liquid liquid separator tank D-202, be divided into heavy phase product and light mutually product after the fluid accumulation, the heavy phase product mainly contains extraction agent and aromatic hydrocarbons, and extraction agent and aromatic hydrocarbons return extraction distillation column C-201; Light phase product mainly is non-aromatics, returns to carry and heats up in a steamer tower C-202.
The stage number of described extraction distillation column is the 60-80 piece; The described stage number of heating up in a steamer tower of carrying is the 5-20 piece.
The present invention separates the stripping section of extractive distillation top of tower, heats up in a steamer tower C-202 as carrying, and separates and carry the product introduction liquid liquid separator tank D-202 that heats up in a steamer at the bottom of the tower C-202 tower.Wherein heavy phase is returned extraction distillation column in liquid liquid separator tank bottom, heats up in a steamer tower C-202 and gently return to carry from liquid liquid separator tank top.Having avoided again non-aromatics to return extraction section when effectively reducing the operation height causes heat supply excessive and cause the problem of benzene loss.
Claims (1)
1. the extractive distillation technique in the hydrofining process of crude benzene is characterized in that this technique comprises the steps:
1) extraction agent enters from the extractive distillation top of tower, and hydrogenated oil enters at the extraction distillation column middle part; Overhead product enters to carry with the form of gas phase and heats up in a steamer tower, and extraction agent and aromatic hydrocarbons drain into next unit in the extraction distillation column tower reactor;
2) extraction distillation column top gaseous phase product introduction is carried and is heated up in a steamer tower and carry out rectification and purification, heats up in a steamer column overhead non-aromatics product and sends carrying, and carries the heavy phase product that heats up in a steamer at the bottom of the Tata and sends into liquid liquid separator tank through the effect of pump;
3) in liquid liquid separator tank, be divided into heavy phase product and light mutually product after the fluid accumulation, heavy phase product extraction agent and aromatic hydrocarbons return extraction distillation column; Light phase product non-aromatics is returned to carry and is heated up in a steamer tower;
The stage number of described extraction distillation column is the 60-80 piece; The described stage number of heating up in a steamer tower of carrying is the 5-20 piece.
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| CN201110007235XA CN102126914B (en) | 2011-01-13 | 2011-01-13 | Extractive distillation process in hydrofining process of crude benzene |
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| CN201110007235XA CN102126914B (en) | 2011-01-13 | 2011-01-13 | Extractive distillation process in hydrofining process of crude benzene |
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| CN102126914B true CN102126914B (en) | 2013-03-13 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103232317A (en) * | 2013-04-05 | 2013-08-07 | 大连理工大学 | Aromatic hydrocarbon purification apparatus and process used in hydrofining of coking crude benzene |
| CN106348998A (en) * | 2016-08-30 | 2017-01-25 | 四川达兴能源股份有限公司 | Crude benzol hydrogenation refining process |
| CN114470834A (en) * | 2020-10-27 | 2022-05-13 | 湖南中岭化工有限责任公司 | Crude benzene hydrogenation extraction device |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3591490A (en) * | 1968-11-14 | 1971-07-06 | Metallgesellschaft Ag | Process of separating pure aromatic hydrocarbons from hydrocarbon mixtures |
| US3919078A (en) * | 1973-04-06 | 1975-11-11 | Inst Francais Du Petrole | Process for separating aromatic hydrocarbons by extractive distillation |
| CN1900033A (en) * | 2006-07-06 | 2007-01-24 | 湖南长岭石化科技开发有限公司 | Method for producing benzene aromatic hydrocarbon from crude benzole |
| CN202015515U (en) * | 2011-01-13 | 2011-10-26 | 中冶焦耐(大连)工程技术有限公司 | Extractive distillation equipment for crude benzol hydrofining |
-
2011
- 2011-01-13 CN CN201110007235XA patent/CN102126914B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3591490A (en) * | 1968-11-14 | 1971-07-06 | Metallgesellschaft Ag | Process of separating pure aromatic hydrocarbons from hydrocarbon mixtures |
| US3919078A (en) * | 1973-04-06 | 1975-11-11 | Inst Francais Du Petrole | Process for separating aromatic hydrocarbons by extractive distillation |
| CN1900033A (en) * | 2006-07-06 | 2007-01-24 | 湖南长岭石化科技开发有限公司 | Method for producing benzene aromatic hydrocarbon from crude benzole |
| CN202015515U (en) * | 2011-01-13 | 2011-10-26 | 中冶焦耐(大连)工程技术有限公司 | Extractive distillation equipment for crude benzol hydrofining |
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