CN103952174B - A kind of process unit reducing atmospheric and vacuum distillation unit flashing tower and atmospheric pressure kiln load - Google Patents
A kind of process unit reducing atmospheric and vacuum distillation unit flashing tower and atmospheric pressure kiln load Download PDFInfo
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- CN103952174B CN103952174B CN201410200205.4A CN201410200205A CN103952174B CN 103952174 B CN103952174 B CN 103952174B CN 201410200205 A CN201410200205 A CN 201410200205A CN 103952174 B CN103952174 B CN 103952174B
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Abstract
The present invention relates to a kind of refining of petroleum atmospheric and vacuum distillation unit, specifically a kind of process unit reducing atmospheric and vacuum distillation unit flashing tower and atmospheric pressure kiln load, comprise flashing tower, crude oil enters atmospheric flash tower flash zone after interchanger, naphtha fraction is obtained at flash distillation tower top, it is characterized in that, increase solvent oil in atmospheric flash tower middle and upper part and distillate line, its service temperature is 190-210 DEG C, solvent oil distillates line serial connection solvent oil and distillates flowrate control valve, and solvent oil distillates line from solvent oil and extracts desolventizing oil hydrogenation out or enter atmospheric distillation tower top; Described flashing tower is connected with atmospheric pressure kiln by atmospheric flashing column bottoms pump successively, and atmospheric pressure kiln is connected with atmospheric distillation tower bottom.The present invention increases solvent oil and distillates pipeline in atmospheric flash tower middle and upper part, effectively can reduce atmospheric and vacuum distillation unit flashing tower and atmospheric pressure kiln load, reduce the process cost of atmospheric and vacuum distillation unit, improves fractionation efficiency and the fractionation precision of device.
Description
Technical field
The present invention relates to a kind of refining of petroleum atmospheric and vacuum distillation unit, specifically a kind of process unit reducing atmospheric and vacuum distillation unit flashing tower and atmospheric pressure kiln load.
Background technology
Crude oil atmospheric vacuum distillation is that one makes crude oil generation vaporization its condensation be got off by heating again, makes it in separation column, carry out vapour-liquid heat and mass, by the physical change process that the weight Component seperation in crude oil comes.At present, conventional Atmospheric vacuum crude oil work flow is: crude oil passes through and product repeatedly heat exchange, temperature be raised to 150 ?about 180 DEG C enter primary tower, naphtha fraction is obtained at fore-running tower top, topped crude at the bottom of primary tower enters atmospheric pressure kiln (or entering atmospheric pressure kiln after heat exchange) heating after column bottoms pump boosting, atmospheric pressure kiln by oil property difference topped crude be heated to 350 ?380 DEG C enter atmospheric fractional tower, straight-run spirit is obtained on atmospheric fractional tower top, atmospheric fractional tower be generally provided with 3 ?4 side lines, obtain kerosene respectively, solar oil, diesel oil, the cuts such as heavy gas oil, four side lines are extracted out by product pump respectively after air lift, storage tank is sent to after heat exchange cooling, heavy oil at the bottom of atmospheric fractional tower sends into vacuum fractionation system after column bottoms pump boosting.
The deficiency of above-mentioned technical process be atmospheric pressure kiln whole topped crude to be heated to 350 ?380 DEG C, and for often pushing up the components such as gasoline, solar oil, kerosene, gasification temperature does not need so high, adds atmospheric pressure kiln and atmospheric tower thermal load, affects the treatment capacity of device.Meanwhile, the components such as gasoline, solar oil, kerosene, repeatedly at system internal recycle, have impact on fractionation efficiency and the fractionation precision of device.
Summary of the invention
Patent of the present invention is exactly the deficiency for current technical process, a kind of Processes and apparatus reducing atmospheric and vacuum distillation unit flashing tower and atmospheric pressure kiln load is provided, increase solvent oil in atmospheric flash tower middle and upper part and distillate pipeline, effectively can reduce atmospheric and vacuum distillation unit flashing tower and atmospheric pressure kiln load, reduce the process cost of atmospheric and vacuum distillation unit, improve fractionation efficiency and the fractionation precision of device.
The technology of the present invention specifically adopts following technical scheme:
A kind of process unit reducing atmospheric and vacuum distillation unit flashing tower and atmospheric pressure kiln load, comprise flashing tower, crude oil enters atmospheric flash tower flash zone after interchanger heating, naphtha fraction is obtained at flash distillation tower top, it is characterized in that, atmospheric flash tower middle and upper part increase solvent oil distillate pipeline, its service temperature be 190 ?210 DEG C, solvent oil distillates line serial connection solvent oil and distillates flowrate control valve, and solvent oil distillates line from solvent oil and extracts desolventizing oil hydrogenation out or enter atmospheric distillation tower top; Described flashing tower is connected with atmospheric pressure kiln by atmospheric flashing column bottoms pump successively, and atmospheric pressure kiln is connected with atmospheric distillation tower bottom.
Wherein, after solvent oil distillates flowrate control valve, be connected in series solvent oil interchanger, after solvent oil heat exchange, be pumped to hydrogenation unit by solvent oil.In solvent oil interchanger, solvent oil and heat medium water heat exchange, heat medium water is incorporated to full factory heat medium water pipe network, effectively can utilize the low temperature exhaust heat of solvent oil.
Another scheme of the present invention is: enter atmospheric distillation tower top by atmospheric distillation tower top feeding line after solvent oil distillates flowrate control valve, service temperature be 190 ?210 DEG C.
Further, described atmospheric pressure kiln outlet operating temperature (OUT) be 355 ?365 DEG C.
In the present invention, described solvent oil physical and chemical index is:
Compared with prior art, beneficial effect of the present invention is: after 1) atmospheric flash tower solvent oil is extracted out, reduce the load of atmospheric pressure kiln and upstream device, reduces the running cost of atmospheric and vacuum distillation unit; 2) for distillate hydrogenation device provides the raw material of high-quality; 3) low temperature exhaust heat of solvent oil is effectively utilized; 4) improve fractionation efficiency and the fractionation precision of atmospheric distillation tower and upstream device.5) effectively can improve unit capacity, improve device economic benefit.
Accompanying drawing explanation
Fig. 1 is atmospheric and vacuum distillation unit normal pressure system process figure of the present invention.
In figure, 1 ?crude oil enter device pipeline, 2 ?crude heat exchanger, 3 ?atmospheric flash towers, pipeline extracted out by heavy oil at the bottom of 4 ?flashing towers, 5 ?atmospheric flashing column bottoms pumps, 6 ?petroleum naphtha go out pipeline, 7 ?atmospheric pressure kiln, 8 ?atmospheric distillation tower underfeed line, 9 ?atmospheric distillation tower, 10 ?atmospheric distillation tower top feeding line, 11 ?solvent oil distillate line, 12 ?solvent oil distillate flowrate control valve, 13 ?solvent oil interchanger, 14 ?solvent oil pumps, 15 ?solvent oils remove hydrogenation pipeline.
Embodiment
As shown in Figure 1, crude oil enters device pipeline 1 through crude oil and enters crude heat exchanger 2 and be heated to 225 DEG C and enter atmospheric flash tower 3 flash zone, distillates pipeline 6 go out device after flash distillation tower top obtains naphtha fraction through petroleum naphtha; In atmospheric flash tower 3 middle and upper part, new solubilizing agent oil distillates line 11, service temperature be 190 ?200 DEG C, solvent oil is under solvent oil distillates the adjustment of flowrate control valve 12, flow is 5 tons/time enter solvent oil interchanger 13, after solvent oil and heat medium water heat exchange, heat medium water is incorporated to full factory heat medium water pipe network, effectively can utilize the low temperature exhaust heat of solvent oil.After solvent oil temperature is down to 40 DEG C, delivers to solvent oil after being boosted by solvent oil pump 14 and go hydrogenation pipeline 15 to enter distillate hydrogenation device, as the hydrogenating materials of high-quality.
Or solvent oil is under solvent oil distillates the adjustment of flowrate control valve 12, flow is 5 tons/time enter atmospheric distillation tower 9 top through atmospheric distillation tower top feeding line 10, service temperature is 200 DEG C, and solvent oil is at this further gasification separation.
Heavy oil at the bottom of flashing tower enters atmospheric pressure kiln 7 and heats after heavy oil extraction pipeline 4 enters atmospheric flashing column bottoms pump 5 boosting at the bottom of flashing tower, service temperature is 365 DEG C and enters atmospheric distillation tower 9 flash zone by atmospheric distillation tower underfeed line 8, and diesel oil and heavy gas oil component gasify further at atmospheric distillation tower.
The present embodiment for Shandong Jincheng Heavy Oil Chemical Co., Ltd.'s 1,500,000 tons/year of atmospheric and vacuum distillation unit, unit capacity is 170 tons/time, solvent oil extracted amount is 5 tons/time, solvent oil enters petrol and diesel oil mixed hydrogenation device.
Solvent oil index described in the present embodiment is as follows:
| Density g/cm 3 | Initial boiling point DEG C | Final boiling point DEG C | Sulphur content PPM | Nitrogen content PPM |
| 0.8000 | 124 | 298 | 1041 | 45 |
In the present embodiment, after solvent oil enters petrol and diesel oil mixed hydrogenation device, atmospheric pressure kiln and heating under reduced pressure stove load reduce greatly, per hourly save Sweet natural gas 100NM
3at the bottom of atmospheric flash tower tower, oil temperature rises to 225 DEG C by 223 DEG C, reduces the load of atmospheric flash tower and upstream device, improves fractionation efficiency and the fractionation precision of atmospheric flash tower and upstream device, and device amount of finish about 3% can be improved, improve the economic benefit of device.
Claims (4)
1. one kind is reduced the process unit of atmospheric and vacuum distillation unit flashing tower and atmospheric pressure kiln load, comprise flashing tower, crude oil enters atmospheric flash tower flash zone after interchanger heating, naphtha fraction is obtained at flash distillation tower top, it is characterized in that, increase solvent oil in atmospheric flash tower middle and upper part and distillate line, its service temperature is 190-210 DEG C, solvent oil distillates line serial connection solvent oil and distillates flowrate control valve, and solvent oil distillates line from solvent oil and extracts desolventizing oil hydrogenation out or enter atmospheric distillation tower top; Described flashing tower is connected with atmospheric pressure kiln by atmospheric flashing column bottoms pump successively, and atmospheric pressure kiln is connected with air distillation tower bottom;
Described solvent oil physical and chemical index is:
2. the process unit of reduction atmospheric and vacuum distillation unit flashing tower according to claim 1 and atmospheric pressure kiln load, is characterized in that, is connected in series solvent oil interchanger after solvent oil distillates flowrate control valve, is pumped to hydrogenation unit after solvent oil heat exchange by solvent oil.
3. the process unit of reduction atmospheric and vacuum distillation unit flashing tower according to claim 1 and atmospheric pressure kiln load, it is characterized in that, solvent oil connects atmospheric distillation tower top feeding line after distillating flowrate control valve, atmospheric distillation tower top feeding line enters atmospheric distillation tower top, and service temperature is 190-210 DEG C.
4. the reduction atmospheric and vacuum distillation unit flashing tower according to Claims 2 or 3 and the process unit of atmospheric pressure kiln load, is characterized in that, described atmospheric pressure kiln outlet operating temperature (OUT) is 355-365 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410200205.4A CN103952174B (en) | 2014-05-13 | 2014-05-13 | A kind of process unit reducing atmospheric and vacuum distillation unit flashing tower and atmospheric pressure kiln load |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201410200205.4A CN103952174B (en) | 2014-05-13 | 2014-05-13 | A kind of process unit reducing atmospheric and vacuum distillation unit flashing tower and atmospheric pressure kiln load |
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| CN103952174A CN103952174A (en) | 2014-07-30 |
| CN103952174B true CN103952174B (en) | 2015-10-28 |
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| CN201410200205.4A Expired - Fee Related CN103952174B (en) | 2014-05-13 | 2014-05-13 | A kind of process unit reducing atmospheric and vacuum distillation unit flashing tower and atmospheric pressure kiln load |
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Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1710027A (en) * | 2005-06-06 | 2005-12-21 | 周衍亮 | Crude oil full-fraction one-stage reduced pressure distillation process |
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2014
- 2014-05-13 CN CN201410200205.4A patent/CN103952174B/en not_active Expired - Fee Related
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1710027A (en) * | 2005-06-06 | 2005-12-21 | 周衍亮 | Crude oil full-fraction one-stage reduced pressure distillation process |
Non-Patent Citations (1)
| Title |
|---|
| 侯祥麟.原油蒸馏工艺过程.《中国炼油技术》.1991,第52-69页. * |
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