CN1940019A - Method for improving asphalt-removing oil output and decreasing solvent accounting simultaneously - Google Patents
Method for improving asphalt-removing oil output and decreasing solvent accounting simultaneously Download PDFInfo
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- CN1940019A CN1940019A CN 200510105436 CN200510105436A CN1940019A CN 1940019 A CN1940019 A CN 1940019A CN 200510105436 CN200510105436 CN 200510105436 CN 200510105436 A CN200510105436 A CN 200510105436A CN 1940019 A CN1940019 A CN 1940019A
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Abstract
Removal of asphalt for decreasing solvent account and improving oil recovery is carried out by entering raw material and oily solvent into extracting tower, countercurrent contacting to obtain deasphaltizing solution and asphalt solution, separating deasphaltizing solution to deasphaltizing oil and solvent, washing for asphalt solution by recovered solvent, entering oily solvent into extracting tower, separating asphalt solution containing solvent to asphalt and solvent, and washing asphalt solution containing solvent. It has less solvent and better washing effect.
Description
Technical field
The present invention relates to a kind of refining hydrocarbon ils of optionally solvent extraction of under the situation that does not have hydrogen, using, more particularly, the invention belongs to a kind of solvent deasphalting method.
Background technology
Solvent deasphalting can optionally be removed objectionable impuritiess such as bituminous matter in the residual oil and metallic compound, for subsequent technique as catalytic cracking, hydrocracking, lubricating oil processing provides the deasphalted oil of processing easily of a large amount of cleanings.Its byproduct pitch is to produce asphaltic products. or gas making raw material preferably, so solvent deasphalting is subjected to people's extensive attention in the residual oil deep processing, is one of residual oil deep processing important means.
At a certain temperature, lighter hydrocarbons solvents such as propane, butane are strong to the oil content dissolving power in the residual oil, to a little less than metallic compound in the residual oil and the bituminous matter dissolving power or do not dissolve substantially.Utilize this character metallic compound can be separated from residual oil with bituminous matter.
Solvent deasphalting normally carries out in extraction tower, the solvent that proportion is little enters in the tower from the extraction tower bottom, heavy residual oil is gone into tower from tower top, the two is countercurrent flow mutually in tower, in this process, oil content in the residual oil is by dissolution with solvents, and with being raised to the extraction tower top and entering solvent recovering system of deasphalted oil solution in form, the bituminous solution that contains a small amount of solvent is then discharged at the bottom of tower.The bituminous solution of discharging at the bottom of the tower because viscosity is very big, often is entrained with a large amount of oil contents, if these oil contents are not separated from bituminous solution, the deasphalted oil yield is reduced, and these oil contents are sneaked into and also influenced the asphaltic products. quality in the pitch.
For these oil contents are separated from bituminous solution, more domestic diasphaltene full scale plants below extraction tower bituminous solution layer and deasphalted oil solution layer interfacial, are often squeezed into a small amount of solvent.But the amount of solvents that adopts this kind method to squeeze into can not be too many, can make the interface fluctuation too much, the diasphaltene operation can't steadily be carried out, it is dark excessively that the bituminous solution layer can not be goed deep in the position of squeezing into solvent simultaneously, cross and to make bituminous solution contain multi-solvent deeply, cause the flashing tower gas line speed height of bituminous solution recovery system, and bring pitch the condensation cooling system of solvent into, condensate cooler is stopped up.Owing to these reasons, so washing effect is bad.
For these oil contents are separated from bituminous solution, US3830732 proposes, the bituminous solution that first extraction tower comes out is sent into second extraction tower, in second extraction tower, carry out extracting with the lighter hydrocarbons higher than first extraction tower solvent for use carbonatoms as solvent, this needs to increase new solvent recovering system undoubtedly.
US4101415 then proposes, and the bituminous solution that first extraction tower comes out is sent into second extraction tower, uses and first extraction tower same solvent, and is lower than first extraction tower in temperature, and solvent ratio is than washing under the big condition of first extraction tower.Because what first, second extraction tower used all is novel solvent, so solvent load is big.
So, still do not have now few and the de-asphalting method that washing effect is good of a kind of solvent load.
Summary of the invention
The objective of the invention is to provide a kind of can divide the bituminous solution entrained oil washing fully to come out, deasphalted oil yield height, and also solvent load is few, does not need to increase the de-asphalting method of new solvent recovering system.
Method provided by the invention is:
Stock oil with contain Oil solvent and enter counter current contact in the extraction tower, obtain deasphalted oil solution and bituminous solution, wherein deasphalted oil solution separating is deasphalted oil and solvent, bituminous solution washs through recovered solvent, gained contains Oil solvent and returns extraction tower, solvent-laden bituminous solution is separated into pitch and solvent, and recovered solvent is used for washing solvent-laden bituminous solution from deasphalted oil solution, bituminous solution.
The solvent that the present invention is used for the diasphaltene extraction tower contains Oil solvent after for the washing bituminous solution, rather than novel solvent, therefore solvent load is few, the washing of bituminous solution is by fully sedimentation or carry out extracting in another extraction tower in static mixer, the settling vessel in pipeline, so washing effect is good, deasphalted oil yield height.
Description of drawings
Fig. 1 is the de-asphalting method schematic flow sheet that reduction solvent load provided by the invention improves oily yield simultaneously, and the washing of bituminous solution is by carrying out in static mixer, the settling vessel in pipeline.
Fig. 2 is the de-asphalting method schematic flow sheet that reduction solvent load provided by the invention improves oily yield simultaneously, and the washing of bituminous solution is to carry out in another extraction tower.
Embodiment
In the present invention, deasphalting stock oil can be that the long residuum of various crude oil is or/and vacuum residuum.
Described solvent is to be selected from C
3-C
7A kind of or its mixture in alkane or alkene, condensate oil, light naphthar, the petroleum naphtha.
In the present invention, the operational condition of diasphaltene extraction tower and raw material oil properties, used solvent and relevant to the specification of quality of product.The temperature at general extraction tower top is controlled in 60 ℃-150 ℃ the scope, in order to improve extraction efficiency, preferably keep 10 ℃-30 ℃ the temperature difference between at the bottom of extracting cat head and the tower, extractive solvent ratio is 3: 1-5: 1 (weight ratio that promptly contains Oil solvent and stock oil), the pressure of extraction tower cans be compared to the high 0.2MPa-0.5MPa of pressure of settling vessel or another extraction tower most, be generally 3.0MPa-5.0MPa, the temperature of settling vessel or another extraction tower temperature best and at the bottom of the extraction tower is identical, perhaps than its low about 5 ℃.In order to guarantee abundant sedimentation, bituminous solution should be not less than 30min in the residence time of settling vessel or another extraction tower.
Extraction tower can be the rotating disc contactor of called optical imaging, sieve-tray tower or packing tower.
Below in conjunction with accompanying drawing method provided by the present invention is further detailed.Some utility appliance such as process furnace, interchanger etc. among the figure do not mark, but this is known to those of ordinary skills.
Fig. 1 is the de-asphalting method schematic flow sheet that reduction solvent load provided by the invention improves oily yield simultaneously, and the washing of bituminous solution is by carrying out in static mixer, the settling vessel in pipeline.
The flow process of this figure is as follows: stock oil enters the top of extraction tower 1 successively through pipeline 17, pump 3, pipeline 6, contain Oil solvent then enters extraction tower 1 successively through pipeline 13, pump 4, pipeline 7 bottom from what settling vessel came out behind the washing bituminous solution, the two in extraction tower 1 mutually countercurrent flow carry out extracting.Find in the research that containing a small amount of oil content in the solvent does not influence deasphalting extraction rate was acquired, because the oil content in the residual oil all will be dissolved in the solvent sooner or later.The oil content that is come out by solvent extraction in the extraction tower 1 is with the top that is raised to extraction tower 1 of deasphalted oil solution in form, enter deasphalted oil solvent recovering system 11 through pipeline 19, isolated deasphalted oil is drawn through pipeline 15, and recovered solvent enters pump 5 through pipeline 20.Taking out surplus pitch then discharges through pipeline 9 at the bottom of tower with the form of bituminous solution.In order to wash the oil content in the bituminous solution, squeeze in the bituminous solution through pipeline 8 with pump 5 from the fresh solvent that solvent recovering system obtains, and enter settling vessel 2 through mixing tank 10, the two is two-layer through fully being divided in settling vessel 2, the upper strata is the solvent layer of oil-containing 2%-3%, lower floor is that the upper strata contains Oil solvent and squeezes into extraction tower 1 through pipeline 7 and recycle through pipeline 13, pump 4 successively through the bituminous solution layer of washing.The bituminous solution of settling vessel 2 lower floors then enters asphalt flux recovery system 12 through pipeline 14, and isolated pitch is drawn through pipeline 16, and recovered solvent enters pump 5 through pipeline 21.The fresh solvent that replenishes when going into operation or in the operation process is introduced pumps 5 through pipeline 18.
Fig. 2 is the de-asphalting method schematic flow sheet that reduction solvent load provided by the invention improves oily yield simultaneously, and the washing of bituminous solution is to carry out in another extraction tower.
The flow process of this figure is as follows: stock oil enters the top of extraction tower 1 successively through pipeline 17, pump 3, pipeline 6, contain Oil solvent then enters extraction tower 1 successively through pipeline 13, pump 4, pipeline 7 bottom from what settling vessel came out behind the washing bituminous solution, the two in extraction tower 1 mutually countercurrent flow carry out extracting.Find in the research that containing a small amount of oil content in the solvent does not influence deasphalting extraction rate was acquired, because the oil content in the residual oil all will be dissolved in the solvent sooner or later.The oil content that is come out by solvent extraction in the extraction tower 1 is with the top that is raised to extraction tower 1 of deasphalted oil solution in form, enter deasphalted oil solvent recovering system 11 through pipeline 19, isolated deasphalted oil is drawn through pipeline 15, and recovered solvent enters pump 5 through pipeline 20.Take out surplus pitch and then at the bottom of tower, enter another extraction tower 22 through pipeline 9 with the form of bituminous solution.In order to wash the oil content in the bituminous solution, the fresh solvent that obtains from solvent recovering system is squeezed into the bottom of extraction tower 22 through pipeline 8 with pump 5, the two is two-layer through fully being divided in extraction tower 22, the upper strata is the solvent layer of oil-containing 2%-3%, lower floor is that the upper strata contains Oil solvent and squeezes into extraction tower 1 through pipeline 7 and recycle through pipeline 13, pump 4 successively through the bituminous solution layer of washing.The bituminous solution of extraction tower 22 lower floors then enters asphalt flux recovery system 12 through pipeline 14, and isolated pitch is drawn through pipeline 16, and recovered solvent enters pump 5 through pipeline 21.The fresh solvent that replenishes when going into operation or in the operation process is introduced pumps 5 through pipeline 18.
In the present invention, the solvent that is used for the diasphaltene extraction tower is the Oil solvent that contains behind the washing bituminous solution, rather than novel solvent, therefore solvent load is few, the washing of bituminous solution is to be undertaken by static mixer in pipeline, and fully sedimentation in an ad hoc settling vessel, so washing effect is good, deasphalted oil yield height.
The following examples will the invention will be further described.But it is not thereby limiting the invention.
Used its character of raw material of the present invention sees Table 1, and the composition of solvent for use sees Table 2.
Table 1, feedstock property
| Density (20 ℃), g.cm -3 | 0.9289 |
| Viscosity (100 ℃), mm 2/s | 129.48 |
| Carbon residue, % | 8.5 |
The composition of table 2, solvent (mol%)
| Ethane | 0.5 |
| Propane | 68 |
| Propylene | 29 |
| Butane | 2.5 |
Experiment is per hour carried out in the middle-scale device of 10kg in a treatment capacity, the operational condition of diasphaltene extraction tower is: 75 ℃ of extracting tower top temperatures, 55 ℃ of column bottom temperatures, solvent ratio 4: 1, it is identical with common full scale plant that solvent enters the extraction tower position, on bituminous solution layer and deasphalted oil solution layer interfacial.
Experiment condition is identical with embodiment 1, but solvent divides two places to enter extraction tower, and one is in above bituminous solution layer and deasphalted oil solution layer interfacial, and solvent ratio is 3.5: 1, one is in below bituminous solution layer and deasphalted oil solution layer interfacial, and solvent ratio is 0.5: 1.
The operational condition of diasphaltene extraction tower is identical with embodiment 1, enter sedimentation the ad hoc settling vessel after mixing but the bituminous solution of discharging at the bottom of the tower and solvent ratio are 4: 1 fresh solvent, and the solvent that is used for the diasphaltene extraction tower is the Oil solvent that contains that washs behind the bituminous solution.
The experimental result of embodiment 1,2,3 sees Table 3, as can be known from the results of Table 3, adopts method of the present invention, though the solvent for use amount is and more identical with one section diasphaltene than two sections common diasphaltene much less, has significantly improved the deasphalted oil yield.
Table 3, diasphaltene result
| Deasphalted oil | |||
| Yield, % | Viscosity (100 ℃), mm 2/s | Carbon residue, % | |
| | 37.4 | 21.3 | 0.46 |
| | 40.5 | 21.8 | 0.52 |
| | 46.5 | 22.5 | 0.54 |
Claims (6)
1, a kind ofly reduces the de-asphalting method that solvent load improves oily yield simultaneously, it is characterized in that stock oil and contain Oil solvent entering counter current contact in the extraction tower, obtain deasphalted oil solution and bituminous solution, wherein taking off drop table oil solution is separated into and takes off drop table oil and solvent, bituminous solution washs through recovered solvent, gained contains Oil solvent and returns extraction tower, solvent-laden bituminous solution is separated into pitch and solvent, and recovered solvent is used for washing solvent-laden bituminous solution from deasphalted oil solution, bituminous solution.
2,, it is characterized in that described diasphaltene raw material is selected from vacuum residuum or/and long residuum according to the method for claim 1.
3,, it is characterized in that described solvent is a kind of or its mixture that is selected from C3-C7 alkane or alkene, condensate oil, light naphthar, the petroleum naphtha according to the method for claim 1.
4, according to the method for claim 1, the pressure that it is characterized in that extraction tower is 3.0MPa-5.0MPa, and the temperature at extraction tower top is 60 ℃-150 ℃, and the weight ratio of extractive solvent and stock oil is 3: 1-5: 1.
5, according to the method for claim 1, it is characterized in that bituminous solution carries out in settling vessel or another extraction tower through the recovered solvent washing, bituminous solution was not less than 30 minutes in the residence time of settling vessel or another extraction tower.
6,, it is characterized in that described extraction tower is rotating disc contactor, sieve-tray tower or packing tower according to the method for claim 1 or 5.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200510105436 CN1940019A (en) | 2005-09-28 | 2005-09-28 | Method for improving asphalt-removing oil output and decreasing solvent accounting simultaneously |
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| CN 200510105436 CN1940019A (en) | 2005-09-28 | 2005-09-28 | Method for improving asphalt-removing oil output and decreasing solvent accounting simultaneously |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101050383B (en) * | 2007-04-30 | 2010-06-02 | 中国石油化工股份有限公司 | Combined technique for processing heavy oil |
| CN101045872B (en) * | 2007-04-30 | 2011-02-16 | 中国石油化工股份有限公司 | Method for producing asphalt for high grade road |
| CN104449808A (en) * | 2013-09-13 | 2015-03-25 | 中国石油化工股份有限公司 | System and method for reducing ethylene unit quenching oil viscosity |
-
2005
- 2005-09-28 CN CN 200510105436 patent/CN1940019A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101050383B (en) * | 2007-04-30 | 2010-06-02 | 中国石油化工股份有限公司 | Combined technique for processing heavy oil |
| CN101045872B (en) * | 2007-04-30 | 2011-02-16 | 中国石油化工股份有限公司 | Method for producing asphalt for high grade road |
| CN104449808A (en) * | 2013-09-13 | 2015-03-25 | 中国石油化工股份有限公司 | System and method for reducing ethylene unit quenching oil viscosity |
| CN104449808B (en) * | 2013-09-13 | 2016-12-07 | 中国石油化工股份有限公司 | A kind of system and method reducing ethylene unit quench oil viscosity |
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